CN108721946A - Continuous demulsification method in chlorinated polyether resin production - Google Patents
Continuous demulsification method in chlorinated polyether resin production Download PDFInfo
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- CN108721946A CN108721946A CN201810474720.XA CN201810474720A CN108721946A CN 108721946 A CN108721946 A CN 108721946A CN 201810474720 A CN201810474720 A CN 201810474720A CN 108721946 A CN108721946 A CN 108721946A
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- Prior art keywords
- kettle
- complexing
- demulsification
- polyether resin
- chlorinated polyether
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/04—Breaking emulsions
- B01D17/047—Breaking emulsions with separation aids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/04—Breaking emulsions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
- B01D17/02—Separation of non-miscible liquids
- B01D17/04—Breaking emulsions
- B01D17/048—Breaking emulsions by changing the state of aggregation
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- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Processes Of Treating Macromolecular Substances (AREA)
Abstract
It is a kind of continuous demulsification method in chlorinated polyether resin production the present invention relates to breaking method technical field；It carries out in the steps below：Lotion is continuously pumped into demulsification kettle by the first step, while demulsifier is continuously pumped into demulsification kettle, and demulsifier is reacted with the lotion being continuously pumped into demulsification kettle；Second step, the slurry after completely being reacted after kettle are continuously pumped into complexing agent into complexing kettle, complexing agent is reacted with the slurry in overflow to complexing kettle from demulsification kettle overflow to complexing kettle.The present invention uses continuous demulsification production method for the first time in the production of chlorinated polyether resin, kettle, complexing kettle, the level-one of will being demulsified cure kettle and two stage cooking kettle sequentially links together, using the Flow of Goods and Materials mode of low in and high out, more existing intermittent operation, greatly reduce the labor intensity of operating personnel, the utilization rate for improving equipment greatly reduces production cycle and the production cost of chlorinated polyether resin.
Description
Technical field
It is a kind of continuous demulsification method in chlorinated polyether resin production the present invention relates to breaking method technical field.
Background technology
Mainly use demulsifier and lotion pair that breaking methods are added dropwise in chlorinated polyether resin production at present, time for adding is about
2.5 hours to 3 hours, complexing agent could be added after completion of dropwise addition into slurry, be stirred for about 30min, add sodium hydroxide water
Solution adjusts pH value, and mixing heat stabilizer is added and starts to warm up curing.Cause the production cycle of chlorinated polyether resin longer in this way, if
Standby utilization rate is low, causes the increase of enterprise's production cost.
Invention content
A kind of continuous demulsification method in being produced the present invention provides chlorinated polyether resin, overcomes the deficiency of the above-mentioned prior art,
It can effectively solve that the production cycle of chlorinated polyether resin in the production of existing chlorinated polyether resin is long, the utilization rate of equipment is low, cause production
Problem of high cost.
The technical scheme is that realized by following measures：Continuous demulsification side in a kind of production of chlorinated polyether resin
Lotion is continuously pumped into demulsification kettle by method, the first step, while demulsifier is continuously pumped into demulsification kettle, demulsifier and continuous pump
Enter the lotion being demulsified in kettle to be reacted；Second step, the slurry after reaction is from demulsification kettle overflow to complexing kettle, into complexing kettle
It is continuously pumped into complexing agent, complexing agent is reacted with the slurry in overflow to complexing kettle；Third walks, and slurry after reaction is from complexing
Kettle overflow to level-one cures in kettle, is cured in kettle to level-one and is continuously pumped into pH adjusting agent and heat stabilizer, pH adjusting agent and
Heat stabilizer cures the slurry in kettle with overflow to level-one and is reacted；4th step, the slurry after reaction overflow from level-one curing kettle
It flow in two stage cooking kettle and routinely carries out subsequent operation.
Here is the further optimization and/or improvements to foregoing invention technical solution：
The addition of above-mentioned demulsifier is the 0.1% to 0.5% of quality of the emulsion, the addition of complexing agent be quality of the emulsion 0.1% to
0.5%, the addition of pH adjusting agent is the 0.01% to 0.035% of quality of the emulsion, and the addition of heat stabilizer is quality of the emulsion
0.05% to 0.15%.
Above-mentioned pH adjusting agent is lye.
In the above-mentioned first step, the rate that lotion is continuously pumped into demulsification kettle is 6000Kg/h to 8000Kg/h.
In the above-mentioned first step, demulsifier is first filtered by demulsifier before being pumped into demulsification kettle.
In above-mentioned second step, complexing agent is first filtered by complexing agent before being pumped into complexing kettle.
The present invention uses continuous demulsification production method for the first time in the production of chlorinated polyether resin, i.e., will demulsification kettle, complexing kettle, one
Grade curing kettle and two stage cooking kettle sequentially link together, using the Flow of Goods and Materials mode of low in and high out, more existing intermittent behaviour
Make, greatly reduce the labor intensity of operating personnel, improve the utilization rate of equipment, greatly reduces the production week of chlorinated polyether resin
Phase and production cost.
Specific implementation mode
The present invention is not limited by following embodiments, can be determined according to the technique and scheme of the present invention with actual conditions specific
Embodiment.
Embodiment 1, continuous demulsification method in chlorinated polyether resin production, carries out in the steps below：The first step, lotion is continuous
It is pumped into demulsification kettle, while being continuously pumped into demulsifier into demulsification kettle, demulsifier and the lotion being continuously pumped into demulsification kettle carry out
Reaction；Second step, the slurry after first step reaction are continuously pumped into complexing into complexing kettle from demulsification kettle overflow to complexing kettle
Agent, complexing agent are reacted with the slurry in overflow to complexing kettle；Third walks, and the slurry after second step reaction is from complexing kettle overflow
It is cured in kettle to level-one, is cured in kettle to level-one and be continuously pumped into pH adjusting agent and heat stabilizer, pH adjusting agent and thermostabilization
Agent cures the slurry in kettle with overflow to level-one and is reacted；4th step, the slurry after three-step reaction overflow from level-one curing kettle
It flow in two stage cooking kettle and routinely carries out subsequent operation.
Embodiment 2, as the optimization of above-described embodiment, the addition of demulsifier is the 0.1% to 0.5% of quality of the emulsion, network
The addition of mixture is the 0.1% to 0.5% of quality of the emulsion, the addition of pH adjusting agent be quality of the emulsion 0.01% to
0.035%, the addition of heat stabilizer is the 0.05% to 0.15% of quality of the emulsion.
Embodiment 3, as the optimization of above-described embodiment, pH adjusting agent is lye.
Embodiment 4, as the optimization of above-described embodiment, in the first step, the rate that lotion is continuously pumped into demulsification kettle is
6000Kg/h to 8000Kg/h.
Embodiment 5, as the optimization of above-described embodiment, in the first step, demulsifier, first will demulsification before being pumped into demulsification kettle
Agent is filtered.
Embodiment 6, as the optimization of above-described embodiment, in second step, complexing agent, first will complexing before being pumped into complexing kettle
Agent is filtered.
Advantages of the present invention
1. the present invention uses continuous demulsification production method for the first time in the production of chlorinated polyether resin, i.e., will demulsification kettle, complexing kettle, level-one
Curing kettle and two stage cooking kettle sequentially link together, using the Flow of Goods and Materials mode of low in and high out, more existing intermittent operation,
The labor intensity for greatly reducing operating personnel improves the utilization rate of equipment, greatly reduces the production cycle of chlorinated polyether resin
And production cost；
2. demulsifier, complexing agent, pH adjusting agent and heat stabilizer were reduced to by 2.5 hours to 3 hours of existing dropwise addition mode
0.5 hour to 1 hour, the production cycle of chlorinated polyether resin reduced generally compared with the prior art.
In conclusion the present invention uses continuous demulsification production method for the first time in the production of chlorinated polyether resin, i.e., the kettle that will be demulsified,
Complexing kettle, level-one curing kettle and two stage cooking kettle sequentially link together, more existing using the Flow of Goods and Materials mode of low in and high out
Intermittent operation greatly reduces the labor intensity of operating personnel, improves the utilization rate of equipment, greatly reduces chlorinated polyether resin
Production cycle and production cost.
The above technical characteristic constitutes the embodiment of the present invention, can basis with stronger adaptability and implementation result
Actual needs increases and decreases non-essential technical characteristic, to meet the needs of different situations.
Claims (10)
1. a kind of continuous demulsification method in chlorinated polyether resin production, it is characterised in that carry out in the steps below：The first step connects lotion
It is continuous to be pumped into demulsification kettle, while demulsifier is continuously pumped into demulsification kettle, demulsifier and the lotion that is continuously pumped into demulsification kettle into
Row reaction；Second step, the slurry after reaction are continuously pumped into complexing agent, network into complexing kettle from demulsification kettle overflow to complexing kettle
Mixture is reacted with the slurry in overflow to complexing kettle；Third walks, and the slurry after reaction is cured from complexing kettle overflow to level-one
In kettle, is cured to level-one and be continuously pumped into pH adjusting agent and heat stabilizer in kettle, pH adjusting agent and heat stabilizer and overflow are extremely
Slurry in level-one curing kettle is reacted；4th step, the slurry after reaction are cured from level-one in kettle overflow to two stage cooking kettle
Routinely carry out subsequent operation.
2. continuous demulsification method in chlorinated polyether resin production according to claim 1, it is characterised in that the addition of demulsifier
It is the 0.1% to 0.5% of quality of the emulsion, the addition of complexing agent is the 0.1% to 0.5% of quality of the emulsion, the addition of pH adjusting agent
Amount is the 0.01% to 0.035% of quality of the emulsion, and the addition of heat stabilizer is the 0.05% to 0.15% of quality of the emulsion.
3. continuous demulsification method in chlorinated polyether resin production according to claim 2, it is characterised in that pH adjusting agent is alkali
Liquid.
4. continuous demulsification method in chlorinated polyether resin production according to claim 1 or 2 or 3, it is characterised in that in the first step,
The rate that lotion is continuously pumped into demulsification kettle is 6000Kg/h to 8000Kg/h.
5. continuous demulsification method in chlorinated polyether resin production according to claim 1 or 2 or 3, it is characterised in that in the first step,
Demulsifier is first filtered by demulsifier before being pumped into demulsification kettle.
6. continuous demulsification method in chlorinated polyether resin production according to claim 4, it is characterised in that in the first step, demulsifier
Before being pumped into demulsification kettle, first demulsifier is filtered.
7. continuous demulsification method in chlorinated polyether resin production according to claim 1 or 2 or 3, it is characterised in that in second step,
Complexing agent is first filtered by complexing agent before being pumped into complexing kettle.
8. continuous demulsification method in chlorinated polyether resin production according to claim 4, it is characterised in that in second step, complexing agent
Before being pumped into complexing kettle, first complexing agent is filtered.
9. continuous demulsification method in chlorinated polyether resin production according to claim 5, it is characterised in that in second step, complexing agent
Before being pumped into complexing kettle, first complexing agent is filtered.
10. continuous demulsification method in chlorinated polyether resin production according to claim 6, it is characterised in that in second step, complexing
Complexing agent is first filtered by agent before being pumped into complexing kettle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810474720.XA CN108721946A (en) | 2018-05-17 | 2018-05-17 | Continuous demulsification method in chlorinated polyether resin production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810474720.XA CN108721946A (en) | 2018-05-17 | 2018-05-17 | Continuous demulsification method in chlorinated polyether resin production |
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| CN108721946A true CN108721946A (en) | 2018-11-02 |
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| CN201810474720.XA Pending CN108721946A (en) | 2018-05-17 | 2018-05-17 | Continuous demulsification method in chlorinated polyether resin production |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539867A (en) * | 2003-04-21 | 2004-10-27 | 佛山市华昊化工有限公司电化厂 | New method-carbonating method for agglomerating MBS latex |
| CA2628148A1 (en) * | 2005-11-17 | 2007-05-31 | General Electric Company | Separatory and emulsion breaking processes |
| CN103043746A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Degreasing method of super heavy oil wastewater |
| CN206168410U (en) * | 2016-09-29 | 2017-05-17 | 万达集团股份有限公司 | Intensification feed arrangement in production of MBS resin |
-
2018
- 2018-05-17 CN CN201810474720.XA patent/CN108721946A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1539867A (en) * | 2003-04-21 | 2004-10-27 | 佛山市华昊化工有限公司电化厂 | New method-carbonating method for agglomerating MBS latex |
| CA2628148A1 (en) * | 2005-11-17 | 2007-05-31 | General Electric Company | Separatory and emulsion breaking processes |
| CN103043746A (en) * | 2011-10-17 | 2013-04-17 | 中国石油天然气股份有限公司 | Degreasing method of super heavy oil wastewater |
| CN206168410U (en) * | 2016-09-29 | 2017-05-17 | 万达集团股份有限公司 | Intensification feed arrangement in production of MBS resin |
Non-Patent Citations (2)
| Title |
|---|
| 胡学贵主编: "《高分子化学及工艺学》", 31 May 1991 * |
| 顾觉奋主编: "《分离纯化工艺原理》", 31 May 2008 * |
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