CN103145910B - Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization - Google Patents
Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization Download PDFInfo
- Publication number
- CN103145910B CN103145910B CN201310101467.0A CN201310101467A CN103145910B CN 103145910 B CN103145910 B CN 103145910B CN 201310101467 A CN201310101467 A CN 201310101467A CN 103145910 B CN103145910 B CN 103145910B
- Authority
- CN
- China
- Prior art keywords
- initiator
- devolatilization
- chain
- transfer agent
- butyl
- 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.)
- Active
Links
- 238000006116 polymerization reaction Methods 0.000 title claims abstract description 28
- 229920003229 poly(methyl methacrylate) Polymers 0.000 title claims abstract description 26
- 239000004926 polymethyl methacrylate Substances 0.000 title claims abstract description 26
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 27
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 10
- 239000000463 material Substances 0.000 claims abstract description 9
- 239000003999 initiator Substances 0.000 claims description 28
- 239000012986 chain transfer agent Substances 0.000 claims description 23
- 239000000178 monomer Substances 0.000 claims description 22
- 238000009835 boiling Methods 0.000 claims description 12
- 239000006227 byproduct Substances 0.000 claims description 12
- 230000009466 transformation Effects 0.000 claims description 11
- WNAHIZMDSQCWRP-UHFFFAOYSA-N dodecane-1-thiol Chemical compound CCCCCCCCCCCCS WNAHIZMDSQCWRP-UHFFFAOYSA-N 0.000 claims description 8
- 239000000047 product Substances 0.000 claims description 8
- VVQNEPGJFQJSBK-UHFFFAOYSA-N Methyl methacrylate Chemical compound COC(=O)C(C)=C VVQNEPGJFQJSBK-UHFFFAOYSA-N 0.000 claims description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 6
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical group CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 6
- 229940094933 n-dodecane Drugs 0.000 claims description 6
- 238000005453 pelletization Methods 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- BAPJBEWLBFYGME-UHFFFAOYSA-N Methyl acrylate Chemical compound COC(=O)C=C BAPJBEWLBFYGME-UHFFFAOYSA-N 0.000 claims description 5
- PMBXCGGQNSVESQ-UHFFFAOYSA-N 1-Hexanethiol Chemical compound CCCCCCS PMBXCGGQNSVESQ-UHFFFAOYSA-N 0.000 claims description 4
- BDFAOUQQXJIZDG-UHFFFAOYSA-N 2-methylpropane-1-thiol Chemical compound CC(C)CS BDFAOUQQXJIZDG-UHFFFAOYSA-N 0.000 claims description 4
- XYFRHHAYSXIKGH-UHFFFAOYSA-N 3-(5-methoxy-2-methoxycarbonyl-1h-indol-3-yl)prop-2-enoic acid Chemical compound C1=C(OC)C=C2C(C=CC(O)=O)=C(C(=O)OC)NC2=C1 XYFRHHAYSXIKGH-UHFFFAOYSA-N 0.000 claims description 4
- SOGAXMICEFXMKE-UHFFFAOYSA-N Butylmethacrylate Chemical compound CCCCOC(=O)C(C)=C SOGAXMICEFXMKE-UHFFFAOYSA-N 0.000 claims description 4
- JIGUQPWFLRLWPJ-UHFFFAOYSA-N Ethyl acrylate Chemical compound CCOC(=O)C=C JIGUQPWFLRLWPJ-UHFFFAOYSA-N 0.000 claims description 4
- WQAQPCDUOCURKW-UHFFFAOYSA-N butanethiol Chemical group CCCCS WQAQPCDUOCURKW-UHFFFAOYSA-N 0.000 claims description 4
- LSXWFXONGKSEMY-UHFFFAOYSA-N di-tert-butyl peroxide Chemical compound CC(C)(C)OOC(C)(C)C LSXWFXONGKSEMY-UHFFFAOYSA-N 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- GJBRNHKUVLOCEB-UHFFFAOYSA-N tert-butyl benzenecarboperoxoate Chemical compound CC(C)(C)OOC(=O)C1=CC=CC=C1 GJBRNHKUVLOCEB-UHFFFAOYSA-N 0.000 claims description 4
- -1 tert-pentyl ester Chemical class 0.000 claims description 4
- JKNCOURZONDCGV-UHFFFAOYSA-N 2-(dimethylamino)ethyl 2-methylprop-2-enoate Chemical compound CN(C)CCOC(=O)C(C)=C JKNCOURZONDCGV-UHFFFAOYSA-N 0.000 claims description 2
- 239000004342 Benzoyl peroxide Substances 0.000 claims description 2
- OMPJBNCRMGITSC-UHFFFAOYSA-N Benzoylperoxide Chemical compound C=1C=CC=CC=1C(=O)OOC(=O)C1=CC=CC=C1 OMPJBNCRMGITSC-UHFFFAOYSA-N 0.000 claims description 2
- 235000019400 benzoyl peroxide Nutrition 0.000 claims description 2
- CQEYYJKEWSMYFG-UHFFFAOYSA-N butyl acrylate Chemical compound CCCCOC(=O)C=C CQEYYJKEWSMYFG-UHFFFAOYSA-N 0.000 claims description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N hexane Substances CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 2
- PNJWIWWMYCMZRO-UHFFFAOYSA-N pent‐4‐en‐2‐one Natural products CC(=O)CC=C PNJWIWWMYCMZRO-UHFFFAOYSA-N 0.000 claims description 2
- VVWRJUBEIPHGQF-UHFFFAOYSA-N propan-2-yl n-propan-2-yloxycarbonyliminocarbamate Chemical compound CC(C)OC(=O)N=NC(=O)OC(C)C VVWRJUBEIPHGQF-UHFFFAOYSA-N 0.000 claims description 2
- 230000000977 initiatory effect Effects 0.000 abstract description 3
- 238000002360 preparation method Methods 0.000 abstract description 3
- 229920000642 polymer Polymers 0.000 abstract 2
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 14
- 239000000126 substance Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 5
- 150000003384 small molecules Chemical class 0.000 description 5
- 238000012662 bulk polymerization Methods 0.000 description 3
- XMNIXWIUMCBBBL-UHFFFAOYSA-N 2-(2-phenylpropan-2-ylperoxy)propan-2-ylbenzene Chemical compound C=1C=CC=CC=1C(C)(C)OOC(C)(C)C1=CC=CC=C1 XMNIXWIUMCBBBL-UHFFFAOYSA-N 0.000 description 1
- 229920005372 Plexiglas® Polymers 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000010528 free radical solution polymerization reaction Methods 0.000 description 1
- 239000004973 liquid crystal related substance Substances 0.000 description 1
- 239000010808 liquid waste Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000000382 optic material Substances 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 238000010557 suspension polymerization reaction Methods 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Polymerisation Methods In General (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
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 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 has certain heat-resisting winter hardiness, 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, in bulk polymerisation process, do not use solvent and water, compare other techniques and reduced the link of purifying, can effectively improve product purity and transmittance; Removed again the links such as waste water, liquid waste disposal, discharge from, be conducive to environment protection simultaneously.
At present, PMMA continuous bulk polymerization is produced and is mainly contained following two large classes: single kettle type, in still, drop into monomer, initiator and chain-transfer agent and other auxiliary agents, after certain residence time, enter follow-up devolatilization and goods stage, the defect of this method is that percent polymerization is low, is generally 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 shortcoming that single kettle type percent polymerization is low, at the first reactor rear tube formula reactor or the second reactor, in tubular reactor or the second reactor, add again initiator simultaneously, with this, improve transformation efficiency, 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 there is the significant problems such as implode in polyreaction one-phase in office, can have influence on whole piece circuit, when processing, there is larger potential safety hazard.
Summary of the invention
The object of the invention is to overcome above-mentioned weak point, from reaction system, improve, a kind of continuous bulk polymerization process simply with the polymethylmethacrylate of feature 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 temperature of reaction 80-160 ℃, 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, under forcing machine leading portion is warming up to 170-220 ℃, the condition of pressure 1.5-3MPa, continue reaction, improve transformation efficiency; At 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 the monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the by product liquefaction such as oligopolymer, remove, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product.
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.
The described monomer, solvent, the chain-transfer agent available cycles that obtain of collecting respectively after devolatilization of step (3) used.
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, 2,5-dimethyl-2, a kind of in 5 di-t-butyl peroxy hexanes or ditertiary butyl peroxide.
Described chain-transfer agent is n-butyl mercaptan, isobutyl mercaptan, positive hexylmercaptan, n-dodecyl mercaptan, tertiary lauryl mercaptan; Releasing agent is n-dodecane alcohol.
Tool of the present invention has the following advantages: the present invention adopts 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
A production technique of couple 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 the tertiary lauryl mercaptan of chain-transfer agent, 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, under forcing machine leading portion is warming up to 220 ℃, the condition of pressure 1.5MPa, continue reaction, improve transformation efficiency; At 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 the monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the by product liquefaction such as oligopolymer, remove, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product.
Embodiment 2
A production technique of couple 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 the tertiary lauryl mercaptan of chain-transfer agent, 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, under forcing machine leading portion is warming up to 180 ℃, the condition of pressure 2MPa, continue reaction, improve transformation efficiency; At 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 the monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the by product liquefaction such as oligopolymer, remove, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product.
Embodiment 3
A production technique of couple 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 the tertiary lauryl mercaptan of chain-transfer agent, 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, under forcing machine leading portion is warming up to 170 ℃, the condition of pressure 3MPa, continue reaction, improve transformation efficiency; At 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 the monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the by product liquefaction such as oligopolymer, remove, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product.
Embodiment 4
A production technique of couple 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, 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 the tertiary lauryl mercaptan of chain-transfer agent, 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, under forcing machine leading portion is warming up to 220 ℃, the condition of pressure 1.5MPa, continue reaction, improve transformation efficiency; At 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 the monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the by product liquefaction such as oligopolymer, remove, the small-molecule substance boiling point differences such as monomer, chain-transfer agent are less, unify to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product.
Claims (4)
1. a production method 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 temperature of reaction 80-160 ℃, 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, under forcing machine leading portion is warming up to 170-220 ℃, the condition of pressure 1.5-3MPa, continue reaction, improve transformation efficiency; At 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 monomer of deviating from from devolatilization mouth, chain-transfer agent and oligopolymer by product, utilize the difference of boiling point, control condensing temperature at 50-100 ℃, to after the liquefaction of oligopolymer by product, remove, the boiling point difference of monomer, chain-transfer agent is less, unifies to reclaim; By forcing machine, extrude polymethylmethacrylate, after pelletizing, obtain the finished product;
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;
Described comonomer is a kind of in β-dimethyl-aminoethylmethacrylate, butyl methacrylate, methyl acrylate, ethyl propenoate or butyl acrylate.
2. the production method of two initiated polymerization PMMA as claimed in claim 1, is characterized in that: the described monomer, solvent, the chain-transfer agent available cycles that obtain of collecting respectively after devolatilization of step (3) used.
3. the production method 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, 2,5-dimethyl-2, a kind of in 5 di-t-butyl peroxy hexanes or ditertiary butyl peroxide.
4. the production method of two initiated polymerization PMMA as claimed in claim 1, is characterized in that: described chain-transfer agent is n-butyl mercaptan, isobutyl mercaptan, positive hexylmercaptan, n-dodecyl mercaptan, tertiary lauryl mercaptan; Releasing agent is n-dodecane alcohol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310101467.0A CN103145910B (en) | 2013-03-27 | 2013-03-27 | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310101467.0A CN103145910B (en) | 2013-03-27 | 2013-03-27 | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103145910A CN103145910A (en) | 2013-06-12 |
| CN103145910B true CN103145910B (en) | 2014-09-17 |
Family
ID=48544263
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310101467.0A Active CN103145910B (en) | 2013-03-27 | 2013-03-27 | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103145910B (en) |
Families Citing this family (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 |
| 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 |
| CN110615864B (en) * | 2019-10-10 | 2021-05-14 | 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 |
| CN113999339B (en) * | 2021-12-07 | 2023-04-07 | 金聚合科技(宁波)有限公司 | Method for preparing polymethyl methacrylate |
| 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1594377A (en) * | 2004-06-24 | 2005-03-16 | 西安交通大学 | Process for rapid polymerization preparation of polymethyl methacrylate used for polymer fiber |
-
2013
- 2013-03-27 CN CN201310101467.0A patent/CN103145910B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN1594377A (en) * | 2004-06-24 | 2005-03-16 | 西安交通大学 | Process for rapid polymerization preparation of polymethyl methacrylate used for polymer fiber |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103145910A (en) | 2013-06-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103145910B (en) | Production process of polymethyl methacrylate (PMMA) through double-initiated polymerization | |
| CN103130946B (en) | The continous way production technique of polymethylmethacrylate | |
| JP3293702B2 (en) | Method for producing methyl methacrylate polymer | |
| CN101724120B (en) | Method for producing acrylate polymer | |
| CN102060961B (en) | Method for preparing high-density polyethylene-maleic anhydride graft copolymer by suspension method | |
| CN102140150B (en) | Preparation method for acrylic ester rubber | |
| CN104945556A (en) | Preparation method of methyl methacrylate-styrene copolymer | |
| CN102070745A (en) | Fluorinated acrylate copolymer-containing resin and polymerization method thereof | |
| CN103408681B (en) | A kind of method increasing substantially polyvinyl chloride production capacity | |
| JP2024037242A (en) | Method for producing recycled methyl (meth)acrylate | |
| CN111378066B (en) | Method for preparing methyl methacrylate polymer | |
| CN102070743B (en) | Method for preparing polyacrylate copolymer resin for optical conduction | |
| CN103130947B (en) | Optical-grade polymethylmethacrylacontinuous production technique | |
| CN103130945B (en) | Polymethyl methacrylate (PMMA) continuous production process for long-time operation without accumulation | |
| JP3565229B2 (en) | Method for producing methacrylic resin | |
| CN105566573A (en) | High-fluidity metallocene low-density polyethylene resin graft and preparation method thereof | |
| CN102311518B (en) | Preparation method of (methyl) acrylate polymer | |
| CN103524647B (en) | A kind of preparation method of polyvinylidene fluoride resin | |
| CN103539887A (en) | Method for continuously preparing optical-grade polymethyl methacrylate | |
| JP2004211105A (en) | Method of manufacturing methacrylic resin | |
| CN112979859A (en) | (methyl) acrylate polymer, preparation method thereof and light guide plate | |
| JP5716266B2 (en) | Method for producing methacrylic resin | |
| CN114347499A (en) | Automatic production line of high-strength and high-light-transmission acrylic rod | |
| CN100532408C (en) | Method and equipment for continuous preparation of acrylic resin by flat-push thin-layer tubular reaction and twin-screw reactive extrusion | |
| CN102850481B (en) | Preparation method of (methyl) acrylate polymer with dendritic structure |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |