CN100569809C - Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced - Google Patents
Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced Download PDFInfo
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- CN100569809C CN100569809C CNB2007100765484A CN200710076548A CN100569809C CN 100569809 C CN100569809 C CN 100569809C CN B2007100765484 A CNB2007100765484 A CN B2007100765484A CN 200710076548 A CN200710076548 A CN 200710076548A CN 100569809 C CN100569809 C CN 100569809C
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- chlorinated polypropylene
- polypropylene iii
- tetracol phenixin
- devolatilization
- screw
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- 239000004743 Polypropylene Substances 0.000 title claims abstract description 55
- 229920001155 polypropylene Polymers 0.000 title claims abstract description 55
- -1 Polypropylene Polymers 0.000 title claims abstract description 54
- 238000001035 drying Methods 0.000 title claims abstract description 21
- 239000007788 liquid Substances 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims abstract description 21
- 239000000463 material Substances 0.000 claims abstract description 9
- 238000004513 sizing Methods 0.000 claims abstract description 8
- 238000001816 cooling Methods 0.000 claims abstract description 6
- 238000005453 pelletization Methods 0.000 claims abstract description 4
- 238000009834 vaporization Methods 0.000 claims abstract description 4
- 230000008016 vaporization Effects 0.000 claims abstract description 4
- 238000005660 chlorination reaction Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 238000005516 engineering process Methods 0.000 description 11
- 239000011248 coating agent Substances 0.000 description 6
- 238000000576 coating method Methods 0.000 description 6
- 239000003795 chemical substances by application Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 239000011127 biaxially oriented polypropylene Substances 0.000 description 4
- 229920006378 biaxially oriented polypropylene Polymers 0.000 description 4
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000007385 chemical modification Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000123 paper Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 description 2
- 229920005992 thermoplastic resin Polymers 0.000 description 2
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000007900 aqueous suspension Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 150000005826 halohydrocarbons Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003836 solid-state method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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Abstract
Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced relates to the Chlorinated Polypropylene III production method.Its technical process is: 1. chlorated liquid is concentrated devolatilization tetracol phenixin under the vacuum state; 2. chlorated liquid tentatively heats; 3. preliminarily heated chlorated liquid enters high temperature in the single order screw rod machine, with the vaporization of the tetracol phenixin in the Chlorinated Polypropylene III, is extracted into condenser afterwards and reclaims under vacuum state; 4. enter second order screw rod machine, devolatilization tetracol phenixin under high temperature and vacuum state, and be recovered to condenser; 5. the Chlorinated Polypropylene III sizing material is sent into head by twin screw, and sizing material is drawn as strip; 6. to pulling into the Chlorinated Polypropylene III cooling of strip; 7. Chlorinated Polypropylene III is carried out drying; 8. enter the dicing machine pelletizing.Its outstanding advantage: particularly in single order dual-screw-stem machine, second order dual-screw-stem machine, reclaim tetracol phenixin, can reclaim tetracol phenixin to greatest extent, reduce the pollution that causes because of the tetracol phenixin volatilization to environment; Save cost; Constant product quality.
Description
Technical field
The present invention relates to the production method of Chlorinated Polypropylene III, relate in particular to the drying means in a kind of Chlorinated Polypropylene III production.
Background technology
1, Chlorinated Polypropylene III (being called for short CPP), English name: CHCORIATEDPOLYPROPYLENE, CPP is the thermoplastic resin that polypropylene (PP) forms through chemical modification, difference according to cl content, its fusing point is generally at 80 ℃～160 ℃, and decomposition temperature can be dissolved in halohydrocarbon, toluene, fourth fat equal solvent at 120 ℃～200 ℃, its wear resistance, durability, ageing resistance and acid resistance are all relatively good, have become one of important products of polypropylene chemical modification.
The main application of Chlorinated Polypropylene III: Chlorinated Polypropylene III is a thermoplastic resin, and it has stronger bounding force to polypropylene, and various materials such as polyethylene, paper, aluminium film are also had good bounding force.Therefore, widely use at aspects such as printing ink, coating, tackiness agents, main application is: 1. use in the making of compound oil ink as main resin at BOPP (two-way stretch polypropylene) film; 2. can be used as the main resin that tackiness agent is produced, for example, as the tackiness agent of BOPP film and paper with as the undercoat of BOPP film Pressuresensitive Tape; 3. Chlorinated Polypropylene III is because of its good film-forming properties and good gloss, widely uses aspect the coating of using at the polypropylene injection-molded item, and the coating of polypropylene injection-molded item for example is as coating of BOPP film etc.
Chlorinated Polypropylene III is widely used because of its excellent property, has obtained tremendous development abroad.At present China has only 10 many enterprises to be engaged in the CPP small-scale production, and of poor quality, and the trade mark is few, pollutes heavyly, and about 20,000 tons of domestic annual requirement annually needs a large amount of imports.Especially the required CCP of printing ink industry along with industry requirement class such as printing, plastic wrapping improve constantly, adds the development of senior printing ink, tackiness agent and coating, and the domestic market will continue to increase the demand of CPP.
2, Chlorinated Polypropylene III is to be made by the polypropylene chlorination reaction, and production method mainly contains three kinds of chloride solutions (is solution with the tetracol phenixin), aqueous suspension chlorination method, chlorination by solid state method.
Chloride solution is one of the most frequently used method of present industrial production Chlorinated Polypropylene III, and in China, carbon tetrachloride solution chlorination process production equipment still in the highest flight.The characteristics of chloride solution are that chlorination is even, and reaction is than being easier to control, and the product cl content generally can reach 53%～63%, can satisfy industry requirement of actual application such as coating, tackiness agent, printing ink.
Chloride solution Production Flow Chart (PP refers to polypropylene, the CTC tetracol phenixin):
3, the present traditional boulton process of domestic main application of the drying means of Chlorinated Polypropylene III.
Referring to vacuum oven formula desiccating method process flow sheet (Fig. 2).
In the vacuum type desiccating method, the chlorated liquid of polypropylene after chlorination reaction put into the chlorated liquid metering cylinder, is put into after metering in each drying tray in the vacuum oven again.At 100 ℃, the vacuum oven inner drying about vacuum tightness≤0.05MPa 2 hours is extracted the solvent tetracol phenixin in the solution out condensation and is reclaimed.The characteristics of vacuum type desiccating method are: technology is fairly simple, and is easy to operate.Weak point is that requirement equipment has good anti-corrosion, the quality product inequality, and production efficiency is low, and tail gas can not be effectively controlled during blow-on, and environmental pollution is serious.And stove formula drying is not in full closeding state in whole technological process, at metering cylinder, advance in the process of stove, blow-on, has a large amount of tetracol phenixin to evaporate in the air, can not reclaim.
Because the signing of Montreal Protocol on Substances that Deplete the Ozone Layer in the world, the volatilization of tetracol phenixin is all reduced trying every possible means in countries in the world.China environmental protection general bureau has also put into effect a large amount of volatilizations that a series of measure limits tetracol phenixin.Therefore, seeking one can reduce tetracol phenixin evaporable drying means in a large number and just seem particularly important.
Summary of the invention
The present invention is intended to the above-mentioned deficiency at prior art, release the exsiccant novel method of chlorated liquid in the Chlorinated Polypropylene III production---continuously big devolatilization amount dual-screw-stem machine drying means, can reduce the tetracol phenixin volatilization in a large number, satisfy environmental protection requirement, make numerous Chlorinated Polypropylene III manufacturing enterprises break away from an environmental protection difficult problem and quality bottleneck that the vacuum type desiccating method is brought, greatly improve production efficiency and product quality.
In order to achieve the above object, the present invention adopts following technical scheme:
Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III of the present invention is produced, its technical process is:
1., the chlorated liquid of polypropylene after chlorination concentrated, in the spissated while, devolatilization tetracol phenixin under the vacuum state, and be recovered to condenser;
2., spissated chlorated liquid is tentatively heated;
3., enter high temperature in the single order screw rod machine, under vacuum state,, be extracted into condenser afterwards and reclaim the vaporization of the tetracol phenixin in the Chlorinated Polypropylene III through 2. preliminarily heated chlorated liquid;
4., behind the devolatilization tetracol phenixin, enter second order screw rod machine, devolatilization tetracol phenixin under high temperature and vacuum state, and be recovered to condenser;
5., the Chlorinated Polypropylene III sizing material sends into head by twin screw, sizing material is drawn as strip;
6., to pulling into the Chlorinated Polypropylene III cooling of strip;
7., to carrying out drying through the overcooled Chlorinated Polypropylene III that pulls into strip;
8., enter the dicing machine pelletizing.
Continuous large-devolatilization double screw extruder drying method is compared with prior art and is had outstanding advantage in the Chlorinated Polypropylene III production of the present invention: one, in continuous big devolatilization amount dual-screw-stem machine drying, whole technological process is all finished in the enclosed vacuum system, can greatly reduce the volatilization of tetracol phenixin; Devolatilization tetracol phenixin under three vacuum states particularly reclaims tetracol phenixin before and after two, in this technology in single order dual-screw-stem machine, second order dual-screw-stem machine, can reclaim tetracol phenixin to greatest extent, reduces the pollution to environment that causes because of the tetracol phenixin volatilization; Three, can save cost by reclaiming tetracol phenixin; Four, quality product is on average stable, and the cpp solids content can reach more than 99% in theory; Five, semi-automatic technology reduces labor strength.
Figure of description
Fig. 1 is process flow sheet of the present invention (CTC among the figure refers to tetracol phenixin).
Fig. 2 is a vacuum oven formula desiccating method process flow sheet.
Embodiment
Below, introduce Chlorinated Polypropylene III of the present invention produce in the embodiment of continuous large-devolatilization double screw extruder drying method.
Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III of the present invention is produced, its technical process is:
1., the chlorated liquid of polypropylene after chlorination concentrated, in the spissated while, devolatilization tetracol phenixin under the vacuum state, and be recovered to condenser;
2., spissated chlorated liquid is tentatively heated;
3., enter high temperature in the single order dual-screw-stem machine, under vacuum state,, be extracted into condenser afterwards and reclaim the vaporization of the tetracol phenixin in the Chlorinated Polypropylene III through 2. preliminarily heated chlorated liquid;
4., behind the devolatilization tetracol phenixin, enter the second order dual-screw-stem machine, devolatilization tetracol phenixin under high temperature and vacuum state, and be recovered to condenser;
5., the Chlorinated Polypropylene III sizing material sends into its head by dual-screw-stem machine, sizing material is drawn as strip;
6., to pulling into the Chlorinated Polypropylene III cooling of strip;
7., to carrying out drying through the overcooled Chlorinated Polypropylene III that pulls into strip;
8., enter the dicing machine pelletizing.
Above-mentioned technology 1. in, polypropylene carried in the dense still through the chlorated liquid after the chlorination concentrating.
The concentration of the chlorated liquid of polypropylene after chlorination is generally 10%, above-mentioned technology 1. in, in carrying dense still, concentrate, it is dense to 25%～30% that chlorated liquid is carried.
Above-mentioned technology 2. in, spissated chlorated liquid is tentatively heated through flash pipe.
Above-mentioned technology 3. in, enter in the single order duplex bar machine through 2. preliminarily heated chlorated liquid, its temperature is controlled at 185 ℃～200 ℃ scopes.
Above-mentioned technology 4. in, the chlorated liquid of devolatilization tetracol phenixin enters in the second order dual-screw-stem machine, its temperature is controlled at 170 ℃～190 ℃ scopes.
Above-mentioned 3., the vacuum tightness in 4. is-0.1MPa～-0.08MPa.
The present invention in concrete enforcement, above-mentioned 6. in, the Chlorinated Polypropylene III cooling that pulls into strip is adopted the method for water-cooled.
Above-mentioned 7. in to carrying out drying by blower fan through the overcooled Chlorinated Polypropylene III that pulls into strip.
In the actual production; major equipment in the technology of the present invention comprises dual-screw-stem machine; comprising heating jacket; single order (going up rank) unit, second order (following rank) unit, circulation pure water case, water recirculator, water circulating pump, cooling tank, hot blast wind groove, gas blower, air knife, dicing machine and corresponding power set, they are by relevant manufacturer production.
Major equipment in the technology of the present invention also comprises two single order machine condensers, two single order machine vacuum buffer cylinders, second order machine condenser, second order vacuum buffer cylinder, flash distillation heating tube and tetracol phenixin storage tank.
Claims (1)
1, continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced, this technical process is:
1., polypropylene carried in the dense still through the chlorated liquid after the chlorination concentrating, it is dense to 25%～30% that chlorated liquid is carried, in the spissated while, devolatilization tetracol phenixin under the vacuum state, and be recovered to condenser;
2., spissated chlorated liquid is tentatively heated with flash pipe;
3., enter high temperature in the single order dual-screw-stem machine, its temperature is controlled at 185 ℃～200 ℃ scopes, with the vaporization of the tetracol phenixin in the Chlorinated Polypropylene III, is extracted into condenser afterwards and reclaims under vacuum state through 2. preliminarily heated chlorated liquid;
4., behind the devolatilization tetracol phenixin, enter the second order dual-screw-stem machine, at 170 ℃～190 ℃ of temperature devolatilization tetracol phenixin down and under the vacuum state, and be recovered to condenser;
5., the Chlorinated Polypropylene III sizing material sends into its head by dual-screw-stem machine, sizing material is drawn as strip;
6., to pulling into the Chlorinated Polypropylene III cooling of strip;
7., to carrying out drying through the overcooled Chlorinated Polypropylene III that pulls into strip;
8., enter the dicing machine pelletizing;
It is characterized in that: above-mentioned 3., the vacuum tightness in 4. for-0.1MPa～-0.08MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100765484A CN100569809C (en) | 2007-08-27 | 2007-08-27 | Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007100765484A CN100569809C (en) | 2007-08-27 | 2007-08-27 | Continuous large-devolatilization double screw extruder drying method during Chlorinated Polypropylene III is produced |
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| CN101161687A CN101161687A (en) | 2008-04-16 |
| CN100569809C true CN100569809C (en) | 2009-12-16 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104024282A (en) * | 2012-02-17 | 2014-09-03 | 东洋纺株式会社 | Polymer composition containing oxidation-modifiable chlorinated propylene and method for producing same |
| CN102702417A (en) * | 2012-06-28 | 2012-10-03 | 东莞市金成化工有限公司 | Continuous large devolatilization drying method for use in chlorinated EVA (Ethylene Vinylacetate) production |
| CN107457935B (en) * | 2016-06-06 | 2019-12-13 | 北京化工大学 | Multi-stage screw extrusion type polyolefin halogenation equipment and polyolefin halogenation method |
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Non-Patent Citations (2)
| Title |
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| 双阶式双螺杆大容量排气脱挥挤压造粒机二期工程启动. 江苏科亚化工装备有限公司.中国塑料，第11期. 0200 |
| 双阶式双螺杆大容量排气脱挥挤压造粒机二期工程启动. 江苏科亚化工装备有限公司.中国塑料，第11期. 0200 * |
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