A mathematical model for polymerization of isoprene with n-butyllithium in hexane

Treybig

et al. 1978

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SynopsisSytrene was polymerized in a 0.8-liter vessel which was operated as an isothermal and a nonisothermal batch reactor. Styrene and n-butyllithium conversions were determined for different reaction times. Rate equations were developed by use of the isothermal data and then used to estimate the conversions for the nonisothermal experiments. The importance of using nonisothermal data in the development of rate equations is illustrated.

“…Porter et al 23 have obtained similar results for polymerization of isoprene in hexane with n-butyllithium. was minimized by using direct search as proposed by Hooke and Jeeves.ls…”

Section: Initiation Reactionsupporting

confidence: 69%

Polymerization of styrene with n‐butyllithium in a batch reactor. A mathematical model

Tanlak

Treybig

et al. 1978

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“…Calculated distributions for micromixed, segregated, and Chen and Fan's model are illustrated in Figures 3,4,5, and 6. The kinetic model used for these calculations was proposed by Porter et al 4 for the polymerization of isoprene in hexane with butyllithium. The experimental data were reported by Ahmad.5 We have also used this procedure to calculate distributions when a!…”

Section: Mwd For Chen and Fan Modelmentioning

confidence: 99%

Segregated and two‐environment reactor models—calculation of molecular weight distributions

Anthony

1977

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SynopsisAn efficient procedure is presented for calculating molecular weight distributions for segregated reactors and two-environment reactor models.' Calculation of molecular weight distributions for segregated flow or twoenvironment mixing models by conventional methods are long and require a considerable amount of computer time. Therefore, few, if any, calculated molecular weight distributions have been presented in the literature for these mixing models.If the method of characteristics and the continuous variable assumption as presented by Zeman and Amundsonl and used by Timm et al.6 are used, the time required to calculate a distribution is greatly reduced. This calculation procedure is illustrated as follows for a stepwise polymerization with no termination. The method can, however, be readily extended to other types of polymerization mechanisms. The reaction mechanism is I + M + P 1For the batch reactor, the production of polymer chains is given by d P . dt = aM or in terms of the continuous variable assumption,where 7 is the continuous variable for the chain length and j is the discrete variable. By use of the method of characteristics, the solution for eq. (3) is P ( t ( t ) , t ) = Pl(t0)(

“…0. (6) ( 7 ) dX dt where Ci, C, , and C, (C, = Ao) are concentrations of initiator, monomer, and polymer, respectively; XI and A2 are the first and second moments of the distribution, respectively; D, and D, are number-and weight-average degrees of polymerization, respectively; A0 = C?Xi at steady state; and 0 = V/u = residence time. If the derivatives with respect to time are set equal to zero, eqs.…”

mentioning

confidence: 99%

Multiple steady‐state solutions in an isothermal perfectly mixed flow reactor

Treybig

Anthony

1977

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