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Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto

A polymerization reactor, free radical technology, used in coatings and other directions, can solve problems such as expensive

Inactive Publication Date: 2004-03-17
BASF CORP
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Additionally, many free radically polymerizable monomers containing the desired modifying groups are more expensive than the precursors used to prepare them

Method used

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  • Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto
  • Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto
  • Process for producing polymers by free radical polymerization and condensation reaction, and apparatus and products related thereto

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0136] A reaction mixture of 5% styrene, 17.5% acrylic acid, 15% 2-ethylhexyl acrylate, 32.45% methyl methacrylate, 30% cyclohexanol and 0.05% di-tert-butyl peroxide was added continuously to the figure 1 In a similar reactor system as described in , the reactor system consisted of a 3-gallon CSTR (Continuous Stirred Tank Reactor) followed by a fixed volume tube reaction zone, each zone maintained at a constant temperature. The reaction zone liquid level and feed flow rates were adjusted to provide a residence time of 15 minutes in the main reactor. The residence time in the tube reaction zone was 30 minutes. The temperature of the main reactor was maintained at 204°C, while the temperature of the tube reaction zone was maintained at 204°C, 232°C or 246°C. The reaction product is continuously pumped to the devolatilization section from which polymer product is continuously collected and subsequently analyzed for average molecular weight (M w and M n ) and acid number, the l...

Embodiment 2

[0139] The procedure of Example 1 was repeated except that the reaction zone liquid level and feed flow rate were adjusted to provide a residence time of 30 minutes in the main reactor. The residence time in the tube reaction zone was 30 minutes. The temperature of the main reactor was maintained at 204°C, while the temperature of the tube reaction zone was maintained at 204°C or 232°C. The reaction product is continuously pumped to the devolatilization section from which polymer product is continuously collected and subsequently analyzed for average molecular weight (M w and M n ) and acid number, the latter indicating the amount of carboxyl functional groups present on the polymer chain. The results are shown in Table 2.

[0140] Tube reaction zone temperature (°C)

Embodiment 3

[0142] 5% styrene, 17.5% acrylic acid, 15% 2-ethylhexyl acrylate, 32.45% methyl methacrylate, approximately 30% cyclohexanol (see Table 3), 0.05% di-tert-butyl peroxide and varying Amount of esterification catalyst (p-toluenesulfonic acid) was added continuously to the reaction mixture with figure 1 In a similar reactor system as described in , the reactor system included a 3-gallon CSTR maintained at a constant temperature. The reaction zone liquid level and flow rate were adjusted to provide a residence time of 15 minutes in the reaction zone. The temperature of the reaction zone was maintained at 204°C. Three different amounts of p-toluenesulfonic acid were added to the reaction mixture in amounts corresponding to 0.0%, 0.1% and 0.2% by weight, respectively, of the reaction mixture. The reaction product is continuously pumped to the devolatilization section from which polymer product is continuously collected and subsequently analyzed for average molecular weight (M w an...

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PUM

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Abstract

The present invention provides a high temperature continuous polymerization and condensation process for preparing a polymeric product. The process includes continuously charging into a reaction zone: at least one radically-polymerizable monomer having a radically polymerizable group and at least one condensation reactive functionality; and at least one modifying agent having a functional group capable of reacting with the condensation reactive functionality. The reaction zone includes at least one primary reactor, but may, and preferably does, contain a secondary reactor. The process further includes maintaining an effective temperature in the primary reactor to cause polymerization of the monomer and to allow at least a portion of the condensation reactive functionality to react with the functional group of the modifying agent.

Description

[0001] REFERENCE TO RELATED APPLICATIONS: This application claims priority to Provisional Patent Application No. 60 / 092,433 (filed July 10, 1998), the disclosure of which is incorporated herein by reference. technical field [0002] The present invention relates generally to a process for the preparation of polymers, in particular to the continuous polymerization and condensation of free radically polymerizable monomers having condensation-reactive functional groups and modifiers having functional groups capable of reacting with the condensation-reactive functional groups into polymerized products method. The invention also relates to the polymer products produced by the process and to products containing the polymer products. Background technique [0003] Methods of preparing polymers are well known in the art. However, many of the methods currently used industrially to produce polymers suffer from a number of limiting factors, including high cost, severe gelation problems...

Claims

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Application Information

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IPC IPC(8): C08F2/00C08F2/02C08F4/28C08F8/00C08F20/00C08F20/04C08F265/04C08F287/00C08F291/00C08F293/00C08G63/00C08G63/78C08G85/00C09D157/00
CPCC08F2810/20C08F287/00C08F20/04C08F8/00C08F2/001C08G63/78C08F293/005C08F2800/20C08F2/00C08F291/00C08G63/00C08F265/04C08F2810/50C08F2/02C08F8/14C08F8/30C08F8/32C08F20/00C08F212/08C08F220/06C08F220/1804C08F20/06C09D133/06C08F212/12
Inventor 凯文·M·安德瑞斯约翰·D·坎贝尔理查德·希拉乔恩·A·戴伯林道格拉斯·J·迪扬河合道宏木村次雄丹尼斯·M·威尔逊
Owner BASF CORP
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