CN103145910A - Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization - Google Patents
Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization Download PDFInfo
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- CN103145910A CN103145910A CN2013101014670A CN201310101467A CN103145910A CN 103145910 A CN103145910 A CN 103145910A CN 2013101014670 A CN2013101014670 A CN 2013101014670A CN 201310101467 A CN201310101467 A CN 201310101467A CN 103145910 A CN103145910 A CN 103145910A
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Abstract
The invention belongs to the technical field of polymer preparation, relates to a preparation method of polymer, and in particular relates to a production process of polymethyl methacrylate (PMMA) through double-initiated polymerization. According to the production process, a single-kettle type reactor is combined with double initiating agents, staying time of materials in a reaction kettle is moderately prolonged, and after the materials enter a subsequent devolatilization type extruding machine, a part of initiating agents initiate reaction, so that polymerization rate is improved; and the reaction is limited in the single reaction kettle and the devolatilization type extruding machine, so that high polymerization rate and stable and controlled reaction system are guaranteed.
Description
Technical field
The present invention relates to a kind of preparation method of polymkeric substance, be specifically related to the production technique of a kind of couple of initiated polymerization PMMA, belong to the polymkeric substance preparing technical field.
Background technology
Plexiglass, the English PMMA that is called for short.PMMA has good light transmission, electrical insulating property, chemical-resistant reagent, solvent resistance, weather resistance and certain heat-resisting winter hardiness is arranged, after post-treatment, can be applicable to liquid crystal light guide plate film, LED light fixture, fiber optic materials, optical articles, automobile component, household electrical appliances parts and daily life requisite.
The method of producing PMMA has the polymerization techniques such as mass polymerization, suspension polymerization, solution polymerization, letex polymerization.Wherein, do not use solvent and water in bulk polymerisation process, compare other techniques and reduced the link of purifying, can effectively improve product purity and transmittance; Simultaneously remove again the links such as waste water, liquid waste disposal, discharging from, be conducive to environment protection.
at present, the production of PMMA continuous bulk polymerization mainly contains following two large classes: single kettle type, drop into monomer, initiator and chain-transfer agent and other auxiliary agents in still, through after certain residence time, enter follow-up devolatilization and goods stage, the defective of this method is that percent polymerization is low, generally is no more than 50%, very high for guaranteeing that quality product removes equipment requirements to monomer, the energy, plant factor are low, built-up type, comprise still-pipe or still-autoclave, in order to solve the low shortcoming of single kettle type percent polymerization, at the first reactor rear tube formula reactor or the second reactor, simultaneously add again initiator in tubular reactor or the second reactor, improve transformation efficiency with this, generally can reach 60-90%, but this method has extended circuit and the time of polyreaction, need monitoring, the factor of adjusting increases greatly, particularly along with percent polymerization improves constantly, the viscosity of whole system can constantly rise, if the significant problems such as implode appear in polyreaction one-phase in office, can have influence on the whole piece circuit, there is larger potential safety hazard when processing.
Summary of the invention
The objective of the invention is to overcome above-mentioned weak point, improve from reaction system, a kind of continuous bulk polymerization process that simply has the polymethylmethacrylate of characteristics is provided.
According to technical scheme provided by the invention, the production technique of a kind of couple of initiated polymerization PMMA, step is as follows by weight:
(1) batching: get main monomer methyl methacrylate 70-100 part, comonomer 10-30 part, the first initiator 60 * 10
-4-120 * 10
-4Part, the second initiator 15 * 10
-4-40 * 10
-4Part, chain-transfer agent 0.1-0.5 part, releasing agent 0.1-0.3 part are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 80-160 ℃ of temperature of reaction, pressure 0.8-1.2MPa, stirring reaction 1-3h under the rotating speed of 30-80r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 170-220 ℃, the condition of pressure 1.5-3MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, the by products such as monomer, chain-transfer agent and oligopolymer of deviating from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
The corresponding temperature difference is between 15-40 ℃ when the transformation period is 1h for the first initiator and the second initiator described in step (1), and the first initiator of long half time and transformation period, the second short initiator amount proportional range was 20:80-40:60.
Step (3) is described to be used through collecting respectively the monomer, solvent, the chain-transfer agent available cycles that obtain after devolatilization.
Described comonomer is a kind of in β-dimethyl-aminoethylmethacrylate, butyl methacrylate, methyl acrylate, ethyl propenoate or butyl acrylate.
Described the first initiator and the second initiator are tert-butyl peroxy acetate, Diisopropyl azodicarboxylate, peroxidized t-butyl perbenzoate, benzoyl peroxide, peroxidation-2-ethylhexyl tert-pentyl ester, 2, a kind of in 5-dimethyl-2,5 di-t-butyl peroxy hexane or ditertiary butyl peroxide.
Described chain-transfer agent is n-butyl mercaptan, isobutyl mercaptan, positive hexylmercaptan, n-dodecyl mercaptan, uncle's lauryl mercaptan; Releasing agent is n-dodecane alcohol.
The present invention has following advantage: the present invention adopts the single kettle type reactor in conjunction with dual initiator, the residence time of proper extension material in reactor, and after entering follow-up devolatilization formula forcing machine, still have the initiation reaction of part initiator, both improved percent polymerization, again reaction is limited in single reactor and devolatilization formula forcing machine, guarantees that higher percent polymerization and reaction system stablize controlled.
Embodiment
Embodiment 1
The production technique of a kind of couple of initiated polymerization PMMA, step is as follows by weight:
(1) batching: get 80 parts of main monomer methyl methacrylates, comonomer 10-30 part, the first initiator tert-butyl peroxy acetate 80 * 10
-4Part, the second initiator ditertiary butyl peroxide 20 * 10
-40.1 part of part, 0.3 part of chain-transfer agent uncle lauryl mercaptan, releasing agent n-dodecane alcohol are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 160 ℃ of temperature of reaction, pressure 0.8MPa, stirring reaction 1h under the rotating speed of 30r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 220 ℃, the condition of pressure 1.5MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, the by products such as monomer, chain-transfer agent and oligopolymer of deviating from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
Embodiment 2
The production technique of a kind of couple of initiated polymerization PMMA, step is as follows by weight:
(1) batching: get 90 parts of main monomer methyl methacrylates, 10 parts of comonomer ethyl propenoates, the first initiator peroxidized t-butyl perbenzoate 70 * 10
-4Part, the second initiator ditertiary butyl peroxide 25 * 10
-40.1 part of part, 0.3 part of chain-transfer agent uncle lauryl mercaptan, releasing agent n-dodecane alcohol are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 140 ℃ of temperature of reaction, pressure 1MPa, stirring reaction 2h under the rotating speed of 60r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 180 ℃, the condition of pressure 2MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, the by products such as monomer, chain-transfer agent and oligopolymer of deviating from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
Embodiment 3
The production technique of a kind of couple of initiated polymerization PMMA, step is as follows by weight:
(1) batching: get 80 parts of main monomer methyl methacrylates, 20 parts of comonomer ethyl propenoates, the first initiator tert-butyl peroxy acetate 20 * 10
-4Part, the second initiator dicumyl peroxide 30 * 10
-4Part, 0.1 part of chain-transfer agent uncle lauryl mercaptan, releasing agent n-dodecane alcohol 0.1-0.3 part are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 120 ℃ of temperature of reaction, pressure 0.8MPa, stirring reaction 2h under the rotating speed of 50r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 170 ℃, the condition of pressure 3MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, the by products such as monomer, chain-transfer agent and oligopolymer of deviating from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
Embodiment 4
The production technique of a kind of couple of initiated polymerization PMMA, step is as follows by weight:
(1) batching: get 80 parts of main monomer methyl methacrylates, 20 parts of comonomer methyl acrylates, the first initiator peroxidation-2-ethyl acid tert-butyl ester 75 * 10
-4Part, the second initiator peroxidized t-butyl perbenzoate 25 * 10
-40.1 part of part, 0.3 part of chain-transfer agent uncle lauryl mercaptan, releasing agent n-dodecane alcohol are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 80 ℃ of temperature of reaction, pressure 1.2MPa, stirring reaction 3h under the rotating speed of 30r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 220 ℃, the condition of pressure 1.5MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, the by products such as monomer, chain-transfer agent and oligopolymer of deviating from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
Claims (6)
1. the production technique of two initiated polymerization PMMA is characterized in that step is as follows by weight:
(1) batching: get main monomer methyl methacrylate 70-100 part, comonomer 10-30 part, the first initiator 60 * 10
-4-120 * 10
-4Part, the second initiator 15 * 10
-4-40 * 10
-4Part, chain-transfer agent 0.1-0.5 part, releasing agent 0.1-0.3 part are stirred well to it and mix, and add in polymeric kettle;
(2) polymerization: heat up in polymeric kettle, control 80-160 ℃ of temperature of reaction, pressure 0.8-1.2MPa, stirring reaction 1-3h under the rotating speed of 30-80r/min;
(3) extrude recovery: step (2) gained material enters devolatilization formula forcing machine, continues reaction under the forcing machine leading portion is warming up to 170-220 ℃, the condition of pressure 1.5-3MPa, improves transformation efficiency; At the forcing machine back segment, by the devolatilization of devolatilization mouth; 230-270 ℃ of devolatilization mouth temperature, devolatilization mouth pressure-0.09MPa--0.05Mpa, residence time 5-10m, monomer, chain-transfer agent and the oligopolymer by product deviate from from the devolatilization mouth, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to remove after the liquefaction of the by products such as oligopolymer, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; Extrude polymethylmethacrylate by forcing machine, namely get the finished product after pelletizing.
2. the production technique of two initiated polymerization PMMA as claimed in claim 1, it is characterized in that: the corresponding temperature difference is between 15-40 ℃ when the transformation period is 1h for the first initiator and the second initiator described in step (1), and the first initiator of long half time and transformation period, the second short initiator amount proportional range was 20:80-40:60.
3. the production technique of two initiated polymerization PMMA as claimed in claim 1, it is characterized in that: step (3) is described to be used through collecting respectively the monomer, solvent, the chain-transfer agent available cycles that obtain after devolatilization.
4. the production technique of two initiated polymerization PMMA as claimed in claim 1 is characterized in that: described comonomer is a kind of in β-dimethyl-aminoethylmethacrylate, butyl methacrylate, methyl acrylate, ethyl propenoate or butyl acrylate.
5. the production technique of two initiated polymerization PMMA as claimed in claim 1, it is characterized in that: described the first initiator and the second initiator are tert-butyl peroxy acetate, Diisopropyl azodicarboxylate, peroxidized t-butyl perbenzoate, benzoyl peroxide, peroxidation-2-ethylhexyl tert-pentyl ester, 2, a kind of in 5-dimethyl-2,5 di-t-butyl peroxy hexane or ditertiary butyl peroxide.
6. the production technique of two initiated polymerization PMMA as claimed in claim 1, it is characterized in that: described chain-transfer agent is n-butyl mercaptan, isobutyl mercaptan, positive hexylmercaptan, n-dodecyl mercaptan, uncle's lauryl mercaptan; Releasing agent is n-dodecane alcohol.
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| CN201310101467.0A CN103145910B (en) | 2013-03-27 | 2013-03-27 | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization |
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|---|---|---|---|
| CN201310101467.0A CN103145910B (en) | 2013-03-27 | 2013-03-27 | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926984A (en) * | 2015-07-14 | 2015-09-23 | 苏州双象光学材料有限公司 | Method for preparing high molecular weight modified polymethyl methacrylate |
| CN107413309A (en) * | 2017-05-31 | 2017-12-01 | 山东华潍膨润土有限公司 | Multifunctional and composite type adsorbent for heavy metal and preparation method thereof |
| CN110615864A (en) * | 2019-10-10 | 2019-12-27 | 万华化学集团股份有限公司 | Methyl methacrylate polymer and preparation method thereof |
| CN113461854A (en) * | 2020-03-30 | 2021-10-01 | 中石油吉林化工工程有限公司 | PMMA continuous bulk polymerization process |
| CN113999339A (en) * | 2021-12-07 | 2022-02-01 | 金聚合科技(宁波)有限公司 | Method for preparing polymethyl methacrylate |
| CN117507236A (en) * | 2023-11-29 | 2024-02-06 | 安徽新涛光电科技有限公司 | Production process and production system of methyl methacrylate polymer plate |
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| CN1102833A (en) * | 1993-11-05 | 1995-05-24 | 住友化学工业株式会社 | Process for production of methacrylate polymers |
| CN1209140A (en) * | 1995-12-14 | 1999-02-24 | 美国3M公司 | Bult radical polymerization using batch reactor |
| CN1277622A (en) * | 1998-05-19 | 2000-12-20 | 株式会社可隆 | A polymethylmethacrylate resin with an impact modifier capsulated therein and a process of preparing for the same |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104926984A (en) * | 2015-07-14 | 2015-09-23 | 苏州双象光学材料有限公司 | Method for preparing high molecular weight modified polymethyl methacrylate |
| CN107413309A (en) * | 2017-05-31 | 2017-12-01 | 山东华潍膨润土有限公司 | Multifunctional and composite type adsorbent for heavy metal and preparation method thereof |
| CN107413309B (en) * | 2017-05-31 | 2020-07-17 | 山东华潍膨润土有限公司 | Multifunctional composite heavy metal ion adsorbent and preparation method thereof |
| CN110615864A (en) * | 2019-10-10 | 2019-12-27 | 万华化学集团股份有限公司 | Methyl methacrylate polymer and preparation method thereof |
| CN113461854A (en) * | 2020-03-30 | 2021-10-01 | 中石油吉林化工工程有限公司 | PMMA continuous bulk polymerization process |
| CN113999339A (en) * | 2021-12-07 | 2022-02-01 | 金聚合科技(宁波)有限公司 | Method for preparing polymethyl methacrylate |
| CN117507236A (en) * | 2023-11-29 | 2024-02-06 | 安徽新涛光电科技有限公司 | Production process and production system of methyl methacrylate polymer plate |
| CN117507236B (en) * | 2023-11-29 | 2024-06-11 | 安徽新涛光电科技有限公司 | Production process and production system of methyl methacrylate polymer plate |
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