United States Patent Ofitice 3,243,419 Patented Mar. 29, 1966 3,243,419 IN SITU GENERATION OF SUSPENDHNG AGENT IN THE SUSkENSION POLYMERIZATION OF STYRENE Alvin R. Ingram, Murrysville, Pa, assrgnor to Koppers Company, Inc., a corporation of Delaware N Drawing. Filed Oct. 30, 1961, Ser. No. 148,735 2 Claims. (Cl. 26093.5)
United States Patent 3,707,585 SUSPENSION POLYMERIZATION OF VINYL MON OMERS Takehiko Okamoto, Shirasawa, and Masakazn lnoue, Akihiko Kishimoto, and Tadahiro Sueyoshi, Nagoya, Japan, assignors to Toray Industries, lnc., Chuo-ku, Tokyo, Japan No Drawing. Continuation-in-part of application Ser. No. 670,380, Sept. 25, 1967. This application May 6, 1970, Ser. No. 35,284
The present invention relates to a suspension polymerization process and, more particularly, to a process for suspension polymerization of a mixture of a monovinyl monomer and a polyvinyl monomer using carboxymethyl cellulose (hereinafter referred to as "CMC") as a dispersing agent.
Liquid-liquid two phase systems are currently being exploited in a wide variety of intriguing ways in the fields of biomaterials and tissue engineering. In this review, the focus will be on selected examples of that particularly highlight the historical development or the benefits and limitations of the different polymerization strategies. It is hoped that clarification of the history and nature of liquid-liquid two-phase microgel-scaffold production methods will ignite further innovations in the production of novel macroporous biomaterials.
Bimodal coextendant suspension polymerization system
The binary suspension polymerization of a water soluble monomer and an organophilic or hydrophobic monomer having a low Tg in an integrated aqueous suspension system wherein the suspension medium for said organophilic monomer droplets comprises a hydrophilic monomer having a higher rate of reaction than the hydrophobic monomer and water in a mixture such that a solution of between about 1,000 and about 100,000 cps Brookfield viscosity is maintained in the reaction zone during polymerization of the organophilic droplets.
Condenser o 1 m3 (400 kgJhr. VC 1 reflux) Time at which stirring was stopped I 8 hours after the start of polymerization. Time at which the polymerization inhibitor was added- 3 minutes after the stoppage of stirring.–
Although this method is very similar to suspension polymerization, the two schemes differ in two important aspects; the polymerization initiator is located in the aqueous phase and the particles of polymer produced are typically in the order of 0.1 micron in diameter, some ten times smaller than the smallest encountered in suspension polymerization.
The Research on Modeling and Simulation of TFE Polymerization Process
In this process, APS is 5 g, CH3COOH is 250 mL, DDM is 100 g, and water is 400 kg. And the feed temperature of TFE is 35°C. Polymerization reactor is the main place of reaction, so its parameter setting is the most critical and important; in this paper, volume is set to 1.2 cum, the temperature is controlled between 80°C and 105°C, and the pressure is controlled between 15 atm and 17 atm. Since this reaction is a semicontinuous process, we make the reaction stop when PTFE yields reach to 150 kg.