CN105923873A - Treatment method of exhausted salty water produced through isocyanate ester production system - Google Patents
Treatment method of exhausted salty water produced through isocyanate ester production system Download PDFInfo
- Publication number
- CN105923873A CN105923873A CN201610356358.7A CN201610356358A CN105923873A CN 105923873 A CN105923873 A CN 105923873A CN 201610356358 A CN201610356358 A CN 201610356358A CN 105923873 A CN105923873 A CN 105923873A
- Authority
- CN
- China
- Prior art keywords
- salt
- production system
- brine
- carbimide
- chlor
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Water Treatment By Sorption (AREA)
Abstract
The invention discloses a treatment method of exhausted salty water produced through an isocyanate ester production system. The method comprises the following steps that 1, the exhausted salty water produced from isocyanate ester is subjected to concentration, crystallization and separation; 2, a mother solution separated from separation equipment and a washing solution discharged from a washing tank are sent to a condensing steam turbine-generator unit electricity, water and salt cogeneration system for continuous concentration and crystallization, and the treated mother solution and washing solution can meet the usable standards; 3, the mother solution of which crystallized salt is dissolved out through a crystallizer is partially or all sent into an activated carbon tower, organic matter contained in salty water is adsorbed with activated carbon, and the mother solution subjected to adsorption returns to the condensing steam turbine-generator unit electricity, water and salt cogeneration system for continuous concentration and crystallization. The treatment method of the exhausted salty water produced through the isocyanate ester production system is simple in technological process, convenient to operate and good in effect of removing organic impurities; the treatment method can be used individually and can be used by combining the prior art, and the effect is better.
Description
Technical field
The present invention relates to chemical field, the process side of the effluent brine that specifically a kind of carbimide (MDI) production system produces
Method.
Background technology
Carbimide (MDI) production process can produce concentration about 16%-20% and containing gas chromatography impurity such as aniline
NaCl effluent brine, domestic only have a company can by proprietary technology crack organic molecule, then by oxidation, blow down,
Recycling is realized after activated carbon adsorption, other company all outer rows, cause the waste of environmental pollution and resource, and
Even if domestic the said firm can realize recycling the effluent brine produced in carbimide (MDI) production process, but by
Brine strength after processing relatively low and cannot be all of.The present invention is to utilize " condensing-type generating set electricity, water, salt connection
Product technology ", by concentrating, crystallize the effluent brine discharged in carbimide (MDI) production process, and contain after crystallization
The solid salt of organic impurities processes, and makes up to recycling.
Summary of the invention
It is an object of the invention to provide the processing method of the effluent brine that a kind of carbimide production system produces, above-mentioned to solve
The problem proposed in background technology.
For achieving the above object, the present invention provides following technical scheme:
The processing method of the effluent brine that a kind of carbimide production system produces, comprises the following steps:
(1) effluent brine from carbimide production system enters condensing-type generating set electricity, water, salt co-generation system are carried out
Concentrating, supersaturated brine separates out crystal salt in crystallizer, by adopting salt pump extraction and delivering to separation equipment and separate, and separation
In the solid salt delivery stock tank gone out, a small amount of dechlorination light salt brine from chlor-alkali production system it is made into thick salt slurry, thick salt
Slurry is sent in sink, with from chlor-alkali production system, appropriate dechlorination light salt brine counter current contacting, washs solid salt surface
Organic substance, the salt after washing the most again separated by separation equipment after for chlor-alkali production system or other user；
(2) cleaning mixture that the isolated mother solution of separation equipment and sink are discharged send condensing steam turbine generator group electricity, water,
Salt co-generation system continues to concentrate and crystallization；
(3) crystallizer separates out the mother liquor fraction after crystal salt or is all sent into activated carbon tower, with institute in activated carbon adsorption saline
The Organic substance contained, the mother solution after absorption returns condensing-type generating set electricity, water, salt co-generation system continuation condensing crystallizing.
As the present invention further scheme: the effluent brine first produced carbimide concentrates, crystallization, then to crystal salt
Process, make up to spendable standard, simultaneously with the organic impurities in activated carbon adsorption strong brine.
As the present invention further scheme: salt-pepper noise device both can use stand alone type, it is possible to be combined (ratio with heat exchanger package
Such as any types such as levin evaporators)
As the present invention further scheme: described wash crystallization salt can be by any any concentration without organic impurities
Saline, tap water or pure water.
As the present invention further scheme: described wash crystallization salt uses the dechlorination light salt brine in chlor-alkali production system.
As the present invention further scheme: described activated carbon selects the activity having stronger absorbability to aniline Organic substance
Charcoal.
As the present invention further scheme: described separation equipment is centrifuge or pressure filter
As the present invention further scheme: isolated solid crystal salt evolution salt bath in step (1), by from chlorine
The dechlorination light salt brine of alkali production system is dissolved into saturated refined brine, returns chlor-alkali production system for producing chlor-alkali and does raw material
Compared with prior art, the invention has the beneficial effects as follows: technological process is simple, easy to operate, organics removal impurity
Effect is preferable；The present invention can be used alone, it is possible to is applied in combination with prior art, and its effect is more preferable.
Accompanying drawing explanation
Fig. 1 is the flow chart of the processing method of the effluent brine that carbimide production system produces.
Detailed description of the invention
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clearly and completely
Describe, it is clear that described embodiment is only a part of embodiment of the present invention rather than whole embodiments.Based on this
Embodiment in invention, the every other reality that those of ordinary skill in the art are obtained under not making creative work premise
Execute example, broadly fall into the scope of protection of the invention.
Refer to Fig. 1, in the embodiment of the present invention, the processing method of the effluent brine that a kind of carbimide production system produces, bag
Include following steps:
(1) effluent brine from carbimide (MDI) production system enters condensing-type generating set electricity, water, salt coproduction system
System concentrates, and supersaturated brine separates out crystal salt in crystallizer, by adopting salt pump extraction and delivering to centrifuge and separate,
In isolated solid salt delivery stock tank, a small amount of dechlorination light salt brine from chlor-alkali production system it is made into thick salt slurry, dense
Thick salt slurry is sent in sink, with from chlor-alkali production system, appropriate dechlorination light salt brine counter current contacting, washs solid salt
The Organic substance on surface, the salt after washing is separated by centrifuge the most again, isolated solid crystal salt evolution salt bath, by from
The dechlorination light salt brine of chlor-alkali production system is dissolved into saturated refined brine, returns chlor-alkali production system for producing chlor-alkali and does raw material；
(2) cleaning mixture that the isolated mother solution of centrifuge and sink are discharged send condensing steam turbine generator group electricity, water, salt
Co-generation system continues to concentrate and crystallization；
(3) crystallizer separates out the mother liquor fraction after crystal salt or is all sent into activated carbon tower, with institute in activated carbon adsorption saline
The Organic substance contained, the mother solution after absorption returns condensing-type generating set electricity, water, salt co-generation system continuation condensing crystallizing.
Wash crystallization salt can be with the saline of any any concentration without organic impurities, or tap water or pure water.Generally produce
Carbimide (MDI) needs supporting chlor-alkali production system, the therefore dechlorination light salt brine of wash crystallization salt preferred chlor-alkali system.
Activated carbon variety should select the activated carbon having stronger absorbability to Organic substances such as aniline.
Effluent brine of the present invention concentrates, crystallization technique preferentially uses " condensing-type generating set electricity, water, salt co-production technology ", also
Other Technology can be used to make effluent brine concentrate, crystallize, but " condensing-type generating set electricity, water, salt co-production technology " energy
Source utilization rate is far above other technique.
Salt-pepper noise device both can use stand alone type, it is possible to use crystallizer and heat exchanger package are combined (such as levin evaporator
Etc. any type)
The separation of crystal salt slurry can be selected for centrifuge, it is possible to selects other any applicable separation equipment, such as: pressure filter.
The present invention compared with prior art has a following characteristics:
(1) technological process is simple, and easy to operate, organics removal impurity effect is preferable.
(2) present invention can be used alone, it is possible to is applied in combination with prior art, and its effect is more preferable.
It is obvious to a person skilled in the art that the invention is not restricted to the details of above-mentioned one exemplary embodiment, and do not carrying on the back
In the case of the spirit or essential attributes of the present invention, it is possible to realize the present invention in other specific forms.Therefore, no matter from
From the point of view of which point, all should regard embodiment as exemplary, and be nonrestrictive, the scope of the present invention is by appended power
Profit requires rather than described above limits, it is intended that all by fall in the implication of equivalency and scope of claim
Change is included in the present invention.Should not be considered as limiting involved claim by any reference in claim.
Although moreover, it will be appreciated that this specification is been described by according to embodiment, but the most each embodiment only comprises
One independent technical scheme, this narrating mode of description is only the most for clarity sake, and those skilled in the art should be by
Description is as an entirety, and the technical scheme in each embodiment can also be through appropriately combined, and forming those skilled in the art can
With other embodiments understood.
Claims (7)
1. the processing method of the effluent brine of a carbimide production system generation, it is characterised in that comprise the following steps:
(1) effluent brine from carbimide production system enters condensing-type generating set electricity, water, salt co-generation system concentrates, supersaturated brine separates out crystal salt in crystallizer, by adopting salt pump extraction and delivering to separation equipment and separate, in isolated solid salt delivery stock tank, it is made into thick salt slurry by a small amount of dechlorination light salt brine from chlor-alkali production system, thick salt slurry is sent in sink, with from chlor-alkali production system, appropriate dechlorination light salt brine counter current contacting, the Organic substance on washing solid salt surface, salt after washing is separated by separation equipment the most again, the solid salt separated is made saturated refined brine and is sent chlor-alkali production system to use；
(2) cleaning mixture that the isolated mother solution of separation equipment and sink are discharged send condensing steam turbine generator group electricity, water, salt co-generation system to continue to concentrate and crystallization；
(3) crystallizer separates out the mother liquor fraction after crystal salt or is all sent into activated carbon tower, and with Organic substance contained in activated carbon adsorption saline, the mother solution after absorption returns condensing-type generating set electricity, water, salt co-generation system continuation condensing crystallizing.
The processing method of the effluent brine that carbimide production system the most according to claim 1 produces, it is characterized in that, the effluent brine first produced carbimide concentrates, crystallization, then crystal salt is processed, make up to spendable standard, simultaneously with the organic impurities in activated carbon adsorption strong brine.
The processing method of the effluent brine that carbimide production system the most according to claim 1 produces, it is characterised in that described wash crystallization salt can be with any saline of any concentration, tap water or pure water without organic impurities.
The processing method of the effluent brine that carbimide production system the most according to claim 3 produces, it is characterised in that described wash crystallization salt uses the dechlorination light salt brine in chlor-alkali production system.
The processing method of the effluent brine that carbimide production system the most according to claim 1 produces, it is characterised in that described activated carbon selects the activated carbon having stronger absorbability to aniline Organic substance.
The processing method of the effluent brine that carbimide production system the most according to claim 1 produces, it is characterised in that described separation equipment is centrifuge or pressure filter and other any separable equipment.
The processing method of the effluent brine that carbimide production system the most according to claim 1 produces, it is characterized in that, isolated solid crystal salt evolution salt bath in step (1), it is dissolved into saturated refined brine by the dechlorination light salt brine from chlor-alkali production system, return chlor-alkali production system and do raw material for producing chlor-alkali, it is possible to by solid salt directly for other user.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610356358.7A CN105923873B (en) | 2016-05-26 | 2016-05-26 | A kind of processing method for the effluent brine that carbimide production system generates |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610356358.7A CN105923873B (en) | 2016-05-26 | 2016-05-26 | A kind of processing method for the effluent brine that carbimide production system generates |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105923873A true CN105923873A (en) | 2016-09-07 |
| CN105923873B CN105923873B (en) | 2018-12-18 |
Family
ID=56841270
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610356358.7A Expired - Fee Related CN105923873B (en) | 2016-05-26 | 2016-05-26 | A kind of processing method for the effluent brine that carbimide production system generates |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105923873B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110560454A (en) * | 2019-09-02 | 2019-12-13 | 南京格洛特环境工程股份有限公司 | Recycling treatment process for low-boiling-point waste salt |
| CN113620317A (en) * | 2021-06-24 | 2021-11-09 | 安徽佳先功能助剂股份有限公司 | Treatment process of dibenzoyl methane production waste |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665302A (en) * | 2009-09-17 | 2010-03-10 | 宁波万华聚氨酯有限公司 | Processing method of effluent brine produced in MDI production process |
| CN101784480A (en) * | 2007-08-23 | 2010-07-21 | 陶氏环球技术公司 | brine purification |
| CN102923736A (en) * | 2012-10-22 | 2013-02-13 | 戈尔工业品贸易（上海）有限公司 | Processing method for refining industrial brine |
| CN103787434A (en) * | 2013-12-19 | 2014-05-14 | 潘庆光 | Power-water-salt coproduction process for condensing steam turbine generator unit |
-
2016
- 2016-05-26 CN CN201610356358.7A patent/CN105923873B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101784480A (en) * | 2007-08-23 | 2010-07-21 | 陶氏环球技术公司 | brine purification |
| CN101665302A (en) * | 2009-09-17 | 2010-03-10 | 宁波万华聚氨酯有限公司 | Processing method of effluent brine produced in MDI production process |
| CN102923736A (en) * | 2012-10-22 | 2013-02-13 | 戈尔工业品贸易（上海）有限公司 | Processing method for refining industrial brine |
| CN103787434A (en) * | 2013-12-19 | 2014-05-14 | 潘庆光 | Power-water-salt coproduction process for condensing steam turbine generator unit |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110560454A (en) * | 2019-09-02 | 2019-12-13 | 南京格洛特环境工程股份有限公司 | Recycling treatment process for low-boiling-point waste salt |
| CN110560454B (en) * | 2019-09-02 | 2022-03-08 | 南京格洛特环境工程股份有限公司 | Recycling treatment process for low-boiling-point waste salt |
| CN113620317A (en) * | 2021-06-24 | 2021-11-09 | 安徽佳先功能助剂股份有限公司 | Treatment process of dibenzoyl methane production waste |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105923873B (en) | 2018-12-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4083781A (en) | Desalination process system and by-product recovery | |
| US7361276B2 (en) | Apparatus and method for osmotic membrane distillation | |
| US4141825A (en) | Desalination process system and by-product recovery | |
| He et al. | Application of alternative energy integration technology in seawater desalination | |
| TWI801782B (en) | Device and method for electrolyzing water to produce high-purity hydrogen and/or oxygen | |
| CN106011917A (en) | Production method of high-purity lithium hydroxide | |
| CN107265734B (en) | Reverse osmosis concentrated seawater treatment system and method | |
| CN102241647B (en) | Preparation technology of propylene oxide | |
| WO2014006741A1 (en) | Method and device for treating saline wastewater | |
| JP5611261B2 (en) | K and Mg recovery method and apparatus | |
| CN107032464B (en) | A kind of gas hydrate accelerant and its application in saline-water reclamation and carbon dioxide capture | |
| CN102689936A (en) | Method for processing wastewater from production of epoxy chloropropane by using glycerol as material | |
| CN105923873A (en) | Treatment method of exhausted salty water produced through isocyanate ester production system | |
| CN202208652U (en) | Salt water treating system | |
| CN206538490U (en) | A kind of cleaning of sea water desalinization strong brine puies forward magnesium system | |
| CN113277665A (en) | Method and device for treating high-concentration high-salinity wastewater through electrolytic evaporation | |
| CN108017039A (en) | Monochlorodifluoromethane by-product HCL produces the preparation method and device of high purity hydrochloric acid | |
| KR101206582B1 (en) | Apparatus and Method of Boron Removing for Sea Water Desalination | |
| CN102816055A (en) | Novel process of treatment of waste mother solution for itaconic acid fermentation through seawater desalination and membrane separation | |
| CN109468656B (en) | Cation diaphragm electrolytic cell series device for removing carbon before electrolysis and application thereof | |
| CN104130218A (en) | Circulating process for producing propylene oxide by using chlorohydrination method | |
| CN111484177A (en) | Method for removing sulfate ions by high-temperature membrane method | |
| CN109896683A (en) | The cycling and reutilization treatment process of time acid producing waste water | |
| CN104086356A (en) | Device and process for separating difluoromethane and hydrogen chloride by dry method | |
| CN111151140B (en) | Method for concentrating chlor-alkali anode dilute brine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20181218 |