CN102295392A - Method for treating and reusing calcium chloride wastewater - Google Patents
Method for treating and reusing calcium chloride wastewater Download PDFInfo
- Publication number
- CN102295392A CN102295392A CN2011102252516A CN201110225251A CN102295392A CN 102295392 A CN102295392 A CN 102295392A CN 2011102252516 A CN2011102252516 A CN 2011102252516A CN 201110225251 A CN201110225251 A CN 201110225251A CN 102295392 A CN102295392 A CN 102295392A
- Authority
- CN
- China
- Prior art keywords
- water
- waste water
- calcium chloride
- reverse osmosis
- unit
- 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 invention which belongs to the technical field of sewage treatment concretely relates to a method for treating and reusing calcium chloride wastewater. According to the method, technologies of optimized pretreatment, biochemical treatment, water reuse through reverse osmosis, electrodialysis condensation, evaporation and recovery, and the like are utilized to achieve the zero discharge of the wastewater, and the recovery of salt and water. The method of the invention which has the advantages of small occupation area, low operation cost, and good economic and social benefits can be widely used in enterprises which generate the calcium chloride wastewater.
Description
Technical field
The invention belongs to technical field of sewage, be specifically related to a kind of water treatment and reuse method of calcium chloride waste water.
Technical background
The main source of calcium chloride waste water is representative with the waste water of the saponification reaction generation of propylene oxide, epoxy chloropropane.Mainly be in technology, need to drop in the calcium hydroxide and the hydrochloric acid that produces in the technology and produce calcium chloride waste water at last.Look into newly by technology, at present domestic method to such wastewater treatment mainly contains and directly is discharged to the municipal sewage plant and unifies processing, biological process and physics, materialization combination process etc.Other has ZL200910096097.X to introduce a kind of chlorohydrination method saponification waste-water processing and recovery method.
The waste water that produces with epoxy chloropropane is example, and epoxy chloropropane production mainly divided for two steps, and the first step is chlorohydrination, and this step needs a large amount of fresh waters; Second step was saponification reaction, and chlorohydrination method saponification waste-water mainly comes from the saponification reaction process.The large amount of sewage of discharging from saponifying process in the process of chlorohydrination production epoxide is because the higher (CaCl of salt concentration
2Massfraction is 3.5%), bring certain difficulty to processing.External epoxide sewage is generally gone down town, and city sewage work is unified to handle, and by other sewage salt is diluted when mixed flow, has alleviated the difficulty of sewage biochemical treatment.
According to the method that ZL200910096097.X introduces, have that technical process is long, the COD film pollutes, facility investment is excessive, not in conjunction with biochemical technology now, shortcoming such as can't handle to other calcium chloride waste water such as epoxy chloropropane.
Chlorohydrination is produced the waste water characteristic that produces in the technology of propylene oxide and epoxy chloropropane:
1) high pH, the pH value is up to more than 11;
2) high salt contains inorganic salts such as a large amount of calcium chloride in the waste water, only calcium chloride content is just up to more than 3.5%;
3) high COD, COD concentration is 800-5000mg/L usually;
4) high temperature, wastewater temperature is up to 70-85 ℃;
5) high suspended matter, suspended substance is up to 1000～5000mg/L;
6) easily crystallization fouling except calcium chloride, also has the inclined to one side compositions of solubleness such as calcium sulfate, silicate in the waste water, all has the problem of easy fouling basically in various treatment processs.
It is reported that one overlaps 100,000 tons/year PO production equipment, ten thousand tons of the annual about 700-1500 of waste water that discharges.In about 1,500,000 tons of the 10 tame PO of the enterprise output in the whole nation in 2010, hundred million tons of year about 1-1.7 of the waste discharge water yield.
If adopt the electroosmose process desalination, will obtain effect preferably, but will carry out pre-treatment waste water, to solve problems such as high suspended matter, easily crystallization, the pollution of COD film at least.
The complicated component of propylene oxide trade effluent, quantity discharged are also big, have brought great pollution to environment, because it has high temperature, high salt, high COD, easy problem such as local-crystalized, have caused great difficulty for the processing of waste water.The present invention has done process optimization on the basis of ZL200910096097.X, at first solve and remove suspended substance, prevent the crystalline problem, in conjunction with technology such as biochemistry, electrodialysis, reverse osmosis, evaporations, realizes the target of resource recycling and zero release.
The enhancing of and environmental consciousness serious day by day along with the domestic water shortage of resources, country also more and more payes attention to energy-saving and emission-reduction.The production technique that the used chlorohydrination of China is produced propylene oxide belongs to high water consumption industry.If in production technique or waste water reclamation utilization, do not carry out breakthrough transformation, to make the production of propylene oxide and epoxy chloropropane propose baptism, and propylene oxide and the epoxy chloropropane poly-essential starting material that are infant industry material polyamine, so be that the waste water of generation handles also that reuse has its important meaning and necessity to chlorohydrination production propylene oxide (PO).
Summary of the invention
The present invention be directed to the high pH, high temperature, high salinity, high COD of chlorohydrination method saponification waste-water, easy characteristics and the deficiencies in the prior art such as fouling, on the basis of ZL200910096097.X, done process optimization, designed and developed a kind of chlorohydrination method saponification waste-water and optimized integrated processing, salt and water recycling method.To use technological designs such as optimizing pre-treatment, biochemical treatment, reverse osmosis reuse water, electrodialysis concentrate, evaporation recovery in the method, reach substantially that wastewater zero discharge, salt and water can reclaim, floor space is little, working cost is low, economy and the good purpose of social benefit.Relative ZL200910096097.X technological line, the present invention has optimized pretreatment technology, saves air supporting, ceramic membrane filter; Save processes such as nanofiltration membrane, seawater membrane reverse osmosis pre-concentration; Increase the biochemical COD of removal process, biochemical processing process is at present just in widely used routine biochemistry method; Optimize electrodialytic technique, improve the electrodialysis cycles of concentration, reduce processing costs.
The present invention is achieved by following technical proposals:
A kind of processing of calcium chloride waste water and reuse method is characterized in that comprising the steps
(1) pH that calcium chloride waste water is regulated water quality is 11～12, salts contg is that 2.0%wt～4.0%wt, temperature are 75～85 ℃, COD
CrFor 1000mg/L～3000mg/L, suspension content are 1000mg/L～5000mg/L;
(2) through after the preliminary sedimentation in thickening pond, supernatant liquor to optimizing pretreatment unit, is optimized pre-treatment with centrifugal pumping; Add flocculation agent, bariumchloride in order, add hydrochloric acid;
Wherein the flocculation agent of Jia Ruing is a kind of in poly-ferric chloride, polymerize aluminum chloride, the bodied ferric sulfate, and consumption is 20～120 gram/ton waste water, and the settling time is 1～5 hour; As preferably, when adding flocculation agent, add coagulant aids again, wherein coagulant aids is that molecular weight is 1,200 ten thousand-3,000 ten thousand anionic polyacrylamide, consumption is 0.5～5 gram/ton waste water;
The bariumchloride addition is 0.5～20 gram/ton waste water;
The amount that adds hydrochloric acid is: for adding the amount that is equivalent to 2～50mL, 20% technical hydrochloric acid in the waste water per ton;
(3) be cooled to 40～45 ℃ with above-mentioned through pretreated waste water then, place the routine biochemistry pond, the waste water COD in the routine biochemistry pond is degraded to 60mg/L;
(4) waste water that comes out from biochemistry pool after sand filtration is filtered, enters electrodialysis unit and carries out concentration; Current density in the electrodialysis unit is 300-1000A/m
2, concentrated through circulating, the saltiness that exports dope until electrodialysis unit rises to 18.0%wt～28.0%wt, and the saltiness of fresh water is reduced to 0.1%wt～0.5%wt;
Use therein electrodialytic membranes is a homogeneous ion-exchange membrane, and film electricity the moon is 0.1～0.8 Ω/cm
2, degree of crosslinking is 70～90%;
(5) electrodialysis unit outlet dope is delivered to the evaporator tower evaporation and is reclaimed calcium chloride; Fresh water enters common reverse osmosis unit, and the product water of reverse osmosis unit and the distilled water that evaporator tower comes out are together as the water of productive use direct reuse, and the dense water of reverse osmosis unit turns back to the routine biochemistry pond.
Innovative point of the present invention and beneficial effect:
1. utilize the optimization preconditioning technique that pH, calcium sulfate, silicate, the suspension content of waste water are all declined to a great extent, thoroughly solve the high pH of such waste water, the problem of easy fouling, the pre-treatment of ZL200910096097.X technology, reduce journeys such as air supporting, ceramic membrane filter, had advantages such as pre-treatment is simple, effective, facility investment is low;
2. the conventional biochemical technology of utilization is removed the COD in the waste water.ZL200910096097.X technology owing to increased biochemical treatment, is degraded to the organism in the waste water relatively, solves the pollution problem of organism to film, and reverse osmosis and electrodialysis can be carried out smoothly after making;
3. adopted the homogeneous membrane electrodialysis to concentrate, ZL200910096097.X technology can only be concentrated to 10% to calcium chloride concentration relatively, the present invention adopts the homogeneous membrane electrodialysis of high-crosslinking-degree, low resistance, hyposmosis to concentrate, calcium chloride concentration is concentrated to more than 25%, the evaporation expense is greatly reduced, also reduced the processing cost of whole technology greatly;
4. use common reverse osmosis technology to carry out the water reuse to electrodialytic light liquid, the reverse osmosis dope biochemistry pool of returning, relative ZL200910096097.X technology, substitute the seawater membrane reverse osmosis and the nanofiltration process of former technology with common reverse osmosis, under the prerequisite that does not reduce treatment effect, facility investment and processing requirement have been reduced greatly;
5. owing to this treatment process is to develop at the various characteristics of calcium chloride waste water, can reclaim the calcium chloride solid at last, and water can recycle, reach the effect of zero release substantially, finally reach good social and economic benefit.
Embodiment
Embodiment 1
With 10 tons treatment capacity per hour spot testing is carried out in the design of each treatment unit and Installation and Debugging of whole technology at last, the calcium chloride waste water of certain propylene oxide factory is carried out pilot experiment:
1, the pH of its factory's calcium chloride waste water is 11.8, salts contg is 3.5%wt, COD
CrFor 1400mg/L, suspended substance are 1000mg/L, water temperature is 82 ℃;
2, calcium chloride waste water is sent into the thickening pond by sludge pump, carrying out milk of lime reclaims, supernatant liquor enters the optimization pretreatment unit, supernatant liquor with centrifugal pumping to optimizing pretreatment unit, optimize pre-treatment by flocculation sediment, bariumchloride precipitated sulfur acid group, add the acid neutralization and form.Wherein the settling time is 1.5 hours, and flocculation agent is a poly-ferric chloride, and consumption is 60 gram/ton waste water, and coagulant aids is that molecular weight is 1,800 ten thousand anionic polyacrylamide, and consumption is 1 gram/ton waste water.The bariumchloride addition is 2 gram/ton waste water.The hydrochloric acid addition of neutralization usefulness is 20% the technical hydrochloric acid of 10mL in the waste water per ton.After optimizing pre-treatment, the pH value of waste water reduces to 8.5, and suspension content is less than every liter of 1 gram, and the content of calcium sulfate and silicate is less than 0.01mg/L;
3, it is better relatively to optimize pretreated waste water quality, and temperature drop to 43 ℃ after cooling off enters the routine biochemistry pond.After biochemical treatment, the COD of waste water reduces to below the 60mg/L;
4, the waste water that comes out of routine biochemistry pond carries out the electrodialysis concentration after sand filtration is filtered, 2 of the membrane stacks of 200 couples of 400*800, and electrodialytic current density is 600A/m
2, concentrated through circulating, the electrodialytic membranes that uses is homogeneous ion-exchange membrane, film electricity the moon is 0.2/cm
2, degree of crosslinking is 80%, make the saltiness such as calcium chloride of dope rise to 25.0%wt, and the saltiness of fresh water is reduced to 0.2%wt.Dense water water quality: salts contg is 25%wt, COD
CrBe 50mg/L; Fresh water water quality: salts contg is 0.2%wt, COD
CrBe 50mg/L;
5, electrodialysis unit outlet dope enters the evaporator tower evaporation and reclaims calcium chloride solid and distilled water.Evaporator tower obtains Calcium dichloride dihydrate crystal and distilled water at last for imitating the multiple-effect evaporation tower, and the fresh water of reverse osmosis and the distilled water of evaporator tower are got back to the production of propylene oxide workshop jointly and carried out reuse as water of productive use.The fresh water of electrodialysis unit enters common reverse osmosis unit, and after reverse-osmosis treated, the fresh water direct reuse of reverse osmosis unit, the dense water of reverse osmosis unit are got back to biochemical treatment system and carried out biochemical treatment.
The reclamation rate of last water reaches 95%, and the calcium chloride rate of recovery is 93%, reaches the purpose of zero release substantially.
Embodiment 2:
With 5 tons treatment capacity per hour spot testing is carried out in the design of each treatment unit and Installation and Debugging of whole technology at last, the calcium chloride waste water of certain epoxy chloropropane factory is carried out pilot experiment:
1, the pH of its factory's calcium chloride waste water is 12, salts contg is 3.2%wt, COD
CrFor 1200mg/L, suspended substance are 1200mg/L, water temperature is 84 ℃;
2, calcium chloride waste water is sent into the thickening pond by sludge pump, carrying out milk of lime reclaims, supernatant liquor enters the optimization pretreatment unit, supernatant liquor with centrifugal pumping to optimizing pretreatment unit, optimize pre-treatment by flocculation sediment, bariumchloride precipitated sulfur acid group, add the acid neutralization and form.Wherein the settling time is 1.8 hours, and flocculation agent is a polymerize aluminum chloride, and consumption is 80 gram/ton waste water, and coagulant aids is that molecular weight is 1,900 ten thousand anionic polyacrylamide, and consumption is 1.5 gram/ton waste water.The bariumchloride addition is 1.5 gram/ton waste water.The hydrochloric acid addition of neutralization usefulness is 20% the technical hydrochloric acid of 12mL in the waste water per ton.After optimizing pre-treatment, the pH value of waste water reduces to 8.3, and suspension content is less than every liter of 1 gram, and the content of calcium sulfate and silicate is less than 0.01mg/L;
3, it is better relatively to optimize pretreated waste water quality, and temperature drop to 40 ℃ after cooling off enters the routine biochemistry pond.After biochemical treatment, the COD of waste water reduces to below the 60mg/L;
4, the waste water that comes out of routine biochemistry pond carries out the electrodialysis concentration after sand filtration is filtered, 1 of the membrane stack of 200 couples of 400*800, and electrodialytic current density is 500A/m
2, concentrated through circulating, the electrodialytic membranes that uses is homogeneous ion-exchange membrane, film electricity the moon is 0.2/cm
2, degree of crosslinking is 80%, make the saltiness such as calcium chloride of dope rise to 25.0%wt, and the saltiness of fresh water is reduced to 0.2%wt.Dense water water quality: salts contg is 25%wt, COD
CrBe 60mg/L; Fresh water water quality: salts contg is 0.2%wt, COD
CrBe 60mg/L;
5, the electrodialysis unit dope enters the evaporator tower evaporation and reclaims calcium chloride solid and distilled water.Evaporator tower obtains Calcium dichloride dihydrate crystal and distilled water at last for imitating the multiple-effect evaporation tower, and the fresh water of reverse osmosis and the distilled water of evaporator tower are got back to the production of propylene oxide workshop jointly and carried out reuse as water of productive use.The fresh water of electrodialysis unit enters common reverse osmosis unit, and after reverse-osmosis treated, the fresh water direct reuse of reverse osmosis unit, the dense water of reverse osmosis unit are got back to biochemical treatment system and carried out biochemical treatment.
The reclamation rate of last water reaches 96%, and the calcium chloride rate of recovery is 94%, reaches the purpose of zero release substantially.
Embodiment 3:
With 2 tons treatment capacity per hour spot testing is carried out in the design of each treatment unit and Installation and Debugging of whole technology at last, the calcium chloride waste water of certain propylene oxide factory is carried out pilot experiment:
1, the calcium chloride wastewater pH of certain factory is 11.2, salts contg is 3.0%wt, COD
CrFor 1000mg/L, suspended substance are 900mg/L, water temperature is 81 ℃;
2, calcium chloride waste water is sent into the thickening pond by sludge pump, carrying out milk of lime reclaims, supernatant liquor enters the optimization pretreatment unit, supernatant liquor with centrifugal pumping to optimizing pretreatment unit, optimize pre-treatment by flocculation sediment, bariumchloride precipitated sulfur acid group, add the acid neutralization and form.Wherein the settling time is 1.3 hours, and flocculation agent is a poly-ferric chloride, and consumption is 50 gram/ton waste water, and coagulant aids is that molecular weight is 2,000 ten thousand anionic polyacrylamide, and consumption is 0.8 gram/ton waste water.The bariumchloride addition is 1.2 gram/ton waste water.The hydrochloric acid addition of neutralization usefulness is 20% the technical hydrochloric acid of 8mL in the waste water per ton.After optimizing pre-treatment, the pH value of waste water reduces to 8.6, and suspension content is less than every liter of 1 gram, and the content of calcium sulfate and silicate is less than 0.01mg/L;
3, it is better relatively to optimize pretreated waste water quality, and temperature drop to 42 ℃ through cooling off after carries out the biochemical treatment system of routine.After biochemical treatment, the COD of waste water reduces to below the 60mg/L;
4, the waste water that comes out of routine biochemistry pond carries out the electrodialysis concentration after sand filtration is filtered, 1 of the membrane stack of 100 couples of 400*800, and electrodialytic current density is 600A/m
2, concentrated through circulating, the electrodialytic membranes that uses is homogeneous ion-exchange membrane, film electricity the moon is 0.2/cm
2, degree of crosslinking is 80%, make the saltiness such as calcium chloride of dope rise to 25.0%wt, and the saltiness of fresh water is reduced to 0.2%wt.Dense water water quality: salts contg is 25%wt, COD
CrBe 60mg/L; Fresh water water quality: salts contg is 0.2%wt, COD
CrBe 60mg/L;
5, the electrodialysis unit dope enters the evaporator tower evaporation and reclaims calcium chloride solid and distilled water.Evaporator tower obtains Calcium dichloride dihydrate crystal and distilled water at last for imitating the multiple-effect evaporation tower, and the fresh water of reverse osmosis and the distilled water of evaporator tower are got back to the production of propylene oxide workshop jointly and carried out reuse as water of productive use.The fresh water of electrodialysis unit enters common reverse osmosis unit, and after reverse-osmosis treated, the fresh water direct reuse of reverse osmosis unit, the dense water of reverse osmosis unit are got back to biochemical treatment system and carried out biochemical treatment.
The reclamation rate of last water reaches 96%, and the calcium chloride rate of recovery is 95%, reaches the purpose of zero release substantially.
Claims (2)
1. the processing of a calcium chloride waste water and reuse method is characterized in that comprising the steps:
(1) pH that calcium chloride waste water is regulated water quality is 11～12, salts contg is that 2.0%wt～4.0%wt, temperature are 75～85 ℃, COD
CrFor 1000mg/L～3000mg/L, suspension content are 1000mg/L～5000mg/L;
(2) through after the preliminary sedimentation in thickening pond, supernatant liquor to optimizing pretreatment unit, is optimized pre-treatment with centrifugal pumping; Add flocculation agent, bariumchloride in order, add hydrochloric acid;
Wherein the flocculation agent of Jia Ruing is a kind of in poly-ferric chloride, polymerize aluminum chloride, the bodied ferric sulfate, and consumption is 20～120 gram/ton waste water, and the settling time is 1～5 hour;
The bariumchloride addition is 0.5～20 gram/ton waste water;
The amount that adds hydrochloric acid is: for adding the amount that is equivalent to 2～50mL, 20% technical hydrochloric acid in the waste water per ton;
(3) be cooled to 40～45 ℃ with above-mentioned through pretreated waste water then, place the routine biochemistry pond, the waste water COD in the routine biochemistry pond is degraded to 60mg/L;
(4) waste water that comes out from biochemistry pool after sand filtration is filtered, enters electrodialysis unit and carries out concentration; Current density in the electrodialysis unit is 300-1000A/m
2, concentrated through circulating, the saltiness that exports dope until electrodialysis unit rises to 18.0%wt～28.0%wt, and the saltiness of fresh water is reduced to 0.1%wt～0.5%wt;
Use therein electrodialytic membranes is a homogeneous ion-exchange membrane, and film electricity the moon is 0.1～0.8 Ω/cm
2, degree of crosslinking is 70～90%;
(5) electrodialysis unit outlet dope is delivered to the evaporator tower evaporation and is reclaimed calcium chloride; Fresh water enters common reverse osmosis unit, and the product water of reverse osmosis unit and the distilled water that evaporator tower comes out are together as the water of productive use direct reuse, and the dense water of reverse osmosis unit turns back to the routine biochemistry pond.
2. processing according to claim 1 and reuse method, when it is characterized in that adding flocculation agent in the step (2), add coagulant aids again, wherein coagulant aids is that molecular weight is 1,200 ten thousand-3,000 ten thousand anionic polyacrylamide, and consumption is 0.5～5 gram/ton waste water.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102252516A CN102295392A (en) | 2011-08-08 | 2011-08-08 | Method for treating and reusing calcium chloride wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011102252516A CN102295392A (en) | 2011-08-08 | 2011-08-08 | Method for treating and reusing calcium chloride wastewater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102295392A true CN102295392A (en) | 2011-12-28 |
Family
ID=45356102
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011102252516A Pending CN102295392A (en) | 2011-08-08 | 2011-08-08 | Method for treating and reusing calcium chloride wastewater |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102295392A (en) |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102978418A (en) * | 2012-12-07 | 2013-03-20 | 来宾华锡冶炼有限公司 | Processing method of casting zinc dross |
| CN103255419A (en) * | 2012-02-15 | 2013-08-21 | 库特勒自动化系统(苏州)有限公司 | Recovery system and recovery method of waste system in photocell wet process |
| CN103864253A (en) * | 2014-03-13 | 2014-06-18 | 郭强 | Salt-containing wastewater treatment device and method |
| CN103880256A (en) * | 2014-04-14 | 2014-06-25 | 天津大沽化工股份有限公司 | Propylene epoxide sludge sewage treatment device |
| CN104310682A (en) * | 2014-08-16 | 2015-01-28 | 厦门世达膜科技有限公司 | A zero-discharge process for tartaric acid production wastewater |
| CN104556187A (en) * | 2014-12-24 | 2015-04-29 | 湖北石花友谊化工股份有限公司 | Preparing technology of high-purity barium chloride |
| CN105060382A (en) * | 2015-08-07 | 2015-11-18 | 滨化集团股份有限公司 | Method for treating salt-containing wastewater in production process of epoxy propane or epoxy chloropropane and apparatus for implementing method |
| CN105254141A (en) * | 2015-11-24 | 2016-01-20 | 广东先导稀材股份有限公司 | Treatment method and treatment system for high-concentration mixed salt organic wastewater |
| CN105800847A (en) * | 2014-12-30 | 2016-07-27 | 上海洗霸科技股份有限公司 | Zero-liquid-drainage treatment process for wastewater |
| CN106277484A (en) * | 2016-09-30 | 2017-01-04 | 淄博格瑞水处理工程有限公司 | A kind of high slat-containing wastewater Zero-discharge treating process producing chlorinated polyethylene generation |
| CN106630306A (en) * | 2015-10-30 | 2017-05-10 | 江苏和氏璧环保科技有限公司 | Treating and recycling method for pesticide intermediate wastewater |
| CN108658285A (en) * | 2018-04-19 | 2018-10-16 | 营创三征(营口)精细化工有限公司 | A kind of Cyanuric Chloride calcium chloride wastewater harmless treatment process |
| CN111762931A (en) * | 2020-07-17 | 2020-10-13 | 河北工业大学 | Method for efficiently concentrating saponified wastewater by chlorohydrination through integrated membrane |
| CN112624519A (en) * | 2020-12-29 | 2021-04-09 | 重庆理工大学 | Treatment method of preserved szechuan pickle wastewater |
| CN114075018A (en) * | 2021-10-20 | 2022-02-22 | 中蓝连海设计研究院有限公司 | Recycling treatment method of epoxy propane wastewater by caustic soda saponification method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101481190A (en) * | 2009-02-10 | 2009-07-15 | 杭州水处理技术研究开发中心有限公司 | Process for treating saponification wastewater by chlorohydrination |
| CN102010094A (en) * | 2009-09-07 | 2011-04-13 | 中国石油化工股份有限公司 | Method for treating high-calcium and high-salt industrial wastewater |
-
2011
- 2011-08-08 CN CN2011102252516A patent/CN102295392A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101481190A (en) * | 2009-02-10 | 2009-07-15 | 杭州水处理技术研究开发中心有限公司 | Process for treating saponification wastewater by chlorohydrination |
| CN102010094A (en) * | 2009-09-07 | 2011-04-13 | 中国石油化工股份有限公司 | Method for treating high-calcium and high-salt industrial wastewater |
Non-Patent Citations (6)
| Title |
|---|
| 《化工进展》 20091231 金可勇等 "环氧丙烷皂化废水预处理及回用方法" 182-184 1-2 第28卷, * |
| 《水处理技术》 20100531 金可勇等 "环氧丙烷皂化废水处理及回用方法" 78-79 1-2 第36卷, 第5期 * |
| 《环境污染与防治》 19980630 何光辉等 "生化处理在高盐度皂化废水中的应用" 25 1-2 第20卷, 第3期 * |
| 何光辉等: ""生化处理在高盐度皂化废水中的应用"", 《环境污染与防治》 * |
| 金可勇等: ""环氧丙烷皂化废水处理及回用方法"", 《水处理技术》 * |
| 金可勇等: ""环氧丙烷皂化废水预处理及回用方法"", 《化工进展》 * |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103255419A (en) * | 2012-02-15 | 2013-08-21 | 库特勒自动化系统(苏州)有限公司 | Recovery system and recovery method of waste system in photocell wet process |
| CN102978418A (en) * | 2012-12-07 | 2013-03-20 | 来宾华锡冶炼有限公司 | Processing method of casting zinc dross |
| CN103864253A (en) * | 2014-03-13 | 2014-06-18 | 郭强 | Salt-containing wastewater treatment device and method |
| CN103880256A (en) * | 2014-04-14 | 2014-06-25 | 天津大沽化工股份有限公司 | Propylene epoxide sludge sewage treatment device |
| CN104310682A (en) * | 2014-08-16 | 2015-01-28 | 厦门世达膜科技有限公司 | A zero-discharge process for tartaric acid production wastewater |
| CN104556187A (en) * | 2014-12-24 | 2015-04-29 | 湖北石花友谊化工股份有限公司 | Preparing technology of high-purity barium chloride |
| CN105800847A (en) * | 2014-12-30 | 2016-07-27 | 上海洗霸科技股份有限公司 | Zero-liquid-drainage treatment process for wastewater |
| CN105060382A (en) * | 2015-08-07 | 2015-11-18 | 滨化集团股份有限公司 | Method for treating salt-containing wastewater in production process of epoxy propane or epoxy chloropropane and apparatus for implementing method |
| CN106630306A (en) * | 2015-10-30 | 2017-05-10 | 江苏和氏璧环保科技有限公司 | Treating and recycling method for pesticide intermediate wastewater |
| CN105254141A (en) * | 2015-11-24 | 2016-01-20 | 广东先导稀材股份有限公司 | Treatment method and treatment system for high-concentration mixed salt organic wastewater |
| CN106277484A (en) * | 2016-09-30 | 2017-01-04 | 淄博格瑞水处理工程有限公司 | A kind of high slat-containing wastewater Zero-discharge treating process producing chlorinated polyethylene generation |
| CN108658285A (en) * | 2018-04-19 | 2018-10-16 | 营创三征(营口)精细化工有限公司 | A kind of Cyanuric Chloride calcium chloride wastewater harmless treatment process |
| CN111762931A (en) * | 2020-07-17 | 2020-10-13 | 河北工业大学 | Method for efficiently concentrating saponified wastewater by chlorohydrination through integrated membrane |
| CN112624519A (en) * | 2020-12-29 | 2021-04-09 | 重庆理工大学 | Treatment method of preserved szechuan pickle wastewater |
| CN114075018A (en) * | 2021-10-20 | 2022-02-22 | 中蓝连海设计研究院有限公司 | Recycling treatment method of epoxy propane wastewater by caustic soda saponification method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102295392A (en) | Method for treating and reusing calcium chloride wastewater | |
| CN101481190B (en) | Process for treating saponification wastewater by chlorohydrination | |
| CN108529802B (en) | Zero-discharge process for discharging high-salt-content wastewater in titanium dioxide production | |
| CN107235590B (en) | Treatment process for zero discharge and resource recycling of catalyst wastewater | |
| CN101402509B (en) | Treatment system and method for high-salt wastewater | |
| JP2018086649A (en) | Method and system for treatment of brine waste water | |
| CN103803752B (en) | Treatment method of wastewater with high salinity and high organic matters | |
| CN103265133B (en) | Recycling method of papermaking advanced treatment wastewater based on chemical decalcification | |
| CN108117207B (en) | Zero-discharge treatment process method for salt-containing wastewater | |
| CN105645439A (en) | System for preparing potassium sulfate from high-salt-content industrial wastewater and technology of system | |
| CN108117206B (en) | Zero-discharge treatment process method for salt-containing wastewater | |
| CN104445755A (en) | Method for resourceful treatment of ammonia chloride wastewaters | |
| CN104276711A (en) | Reverse osmosis membrane treatment process for recycling industrial sewage and realizing zero release | |
| CN107235600B (en) | Electroplating wastewater treatment method, treatment system and application | |
| CN107381932B (en) | Chromium-containing wastewater treatment method, treatment system and application | |
| CN104276709A (en) | Coal chemical industry concentrated brine zero discharge technique and special equipment thereof | |
| CN103771642A (en) | Recycling method for saponified ammonium-sulfate wastewater in rare soil | |
| CN106396232B (en) | Zero-discharge system and method for high-salt printing and dyeing wastewater | |
| CN110683709A (en) | Zero-discharge treatment method for fluorine-containing wastewater | |
| CN107226581B (en) | Zinc-containing wastewater treatment method, treatment system and application | |
| WO2021036406A1 (en) | Zero liquid discharge systems and processes for high-salinity wastewater treatment | |
| CN107200435B (en) | Nickel-containing wastewater treatment method, treatment system and application | |
| CN105417826A (en) | Catalyst waste water zero discharge method and device | |
| CN108117223A (en) | Brine waste zero emission processing method | |
| CN204111506U (en) | A kind of Coal Chemical Industry strong brine technique of zero discharge specific equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20111228 |