SU1419990A1 - Method of controlling continuous process of isopren polymerization - Google Patents

Description

(21) 4188446 / 23-05

(22) 02; 02.87

(46) 08/30/88. Bksh. № 32 (72) V.V.Solodky, V.A. Lavrov, V.P.Glukhov, M.S. Perfilyeva, I.V. Harmonov, V.A. Fedorov, B.A. Perlin, P.P. .Shpakov, A.V. Zak, Yu.N.Tuibarsov, E.A.Tsyganov, N.R.Gilmutdinov and S.A.Akhmetchin

(53) 678.762.3 (088.8)

(56) USSR Author's Certificate No. 530034, cl. C 08 F 2/00, 136/04, 1974.

USSR author's certificate 1139737, cl. C 08 F 136/08, 08. D 27/00, 1983.

(54) METHOD FOR MANAGING THE LEAPERING POLYMERIZATION PROCESS ISOPRENE

(57) The invention relates to the automation of synthetic rubber production technology and can be used to control the continuous polymerization process in the production of synthetic isoprene rubber. The invention allows reducing catalyst consumption and oligomer content in a by-dimension in the process of continuous polymerization of isoprene by stabilizing the monomer concentration at the reactor outlet by varying the consumption of the complex metal-organic catalyst and adjusting the Flour polymer viscosity by adjusting the reaction temperature by supplying part of the output From the first reactor, the polymerisation flow to its inlet and temperature control at the reactor inlet by varying the flow rate of said flow. 1 il.

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The invention relates to the automation of the production technology of synthetic rubber and can be used to control continuous. The polymerization process in the production of synthetic isoprene rubber.

The purpose of the invention is to reduce the catalyst consumption and the oligo umer content in the polymer.

 The drawing shows a diagram of the pea-. the use of the proposed method of control.

The scheme contains reactor 1 of polymerisation-15, cyclical pump 2, sensor 3 of the reaction mixture temperature at the inlet, reactor, sensor 4 of polymer concentration at the reactor outlet j Muki polymer viscosity sensor 5, controller 20 6 of polymer concentration at the outlet of the reactor, regulator 7 in Mooney’s polymer, regulator 8 of the temperature of the reaction mixture at the inlet of the polymerization reactor, regulating valve 9 of the complex organometallic catalyst consumption, regulating valve 10 of the polymer consumption, pipeline 11 supplying ktsionnoy mixture piping 30 water 12 feed metallo organic complex catalyst to the reactor inlet, the feed conduit 13 po- limerizata output from the first reactor to the second reactor inlet, pipeline P5 polimerizatga water supply 14 output from the first polymerization reactor, at its input.

Example. The method of controlling the continuous polymerization process 40 in the production of isoprene rubber is carried out in a battery of two reactors with a volume of 16 m. In the reactor 1 of the polymerization battery, 30 feedstock 45 of the reaction mixture (15% by weight of isoprene in isopentane) are fed through pipe 11 with the temperature measured by sensor 3. The polymer concentration at the outlet of reactor 1, measured by sensor 4, is maintained at 9.6 wt.%, for this with the aid of a regulator. 6 and regulating valve 9 to reactor G, pipeline 12 is fed with 98 l-h of a complex solution of an organometallic catalyst with a concentration of 100 gl. The polymer temperature at the inlet of reactor 1 is 44 C. To maintain the Mooney viscosity of the polymer at the reactor exit at a given level 78 units. from the outlet of the reactor 1 to its entrance through the pipeline 14 serves polymerizat in the amount of 2.5 t / h, while the temperature of the reaction mixture at the inlet to the reactor 1 after mixing with the initial reaction mixture is 1.5 C. The content of oligomers with the polymer this is 0.45 wt.% (l / 0.09 wt.% in the polymerization).

Polymer must be viscous with Mooney viscosity 68 units. Regulator toru 7 polymer Mooney viscosity set a new task - 68 units. Since the current value of the Mooney viscosity of the polymer at the outlet of the polymerization reactor 1, measured by sensor 5, is greater than the task, then from the output of regulator 7 a new task comes to controller 8 to increase the temperature of the reaction mixture at the inlet of reactor 1, The sensor 3, the regulator 8, acting on the valve 10, opens it, increasing the flow rate of the polymerizate supplied from the outlet of the reactor 1 to its inlet, until the temperature set by the regulator 7 is established. The regulator 7 stops changing the regulator reference torus 8 when viscosity according to MUNI of the polymer, measured by sensor 5, will become equal to 68 units. The temperature at the inlet of the polymerization reactor 1, measured by the sensor 3, is then 26, the flow rate of the polymerizate supplied from the outlet of the reactor 1 to its inlet, c. line 14 is 50 tons, -h. Due to the fact that the temperature at the inlet to the reactor 1, where the catalyst is fed, rises sharply, this leads to the activation of the polymerization process. The polymer concentration at the outlet of the reactor 1 is stabilized by a sensor 4, a regulator 6 and a regulating valve 9 by changing the flow rate of a complex organometallic catalyst at the same value of 9.6 wt.%, The catalyst consumption is reduced to 87, and a polymer with Mooney viscosity is obtained. 68 units, and the content of oligomers in the polymer polymer 0.45 wt.% (In the polymerizate 0.09 wt.%).

It is necessary to extrude a polymer with Mooney viscosity of 72 units. The regulator to the Mooney viscosity of Polymer 7 is set as a new task, because the current

the value of the Mooney viscosity of the polymer at the outlet of the reactor 1 is less than the value of the task, then from the output of the regulator

7A new reference to the controller arrives.

8to decrease the -temperature of the reaction mixture at the inlet of the reactor 1. The regulator 8, acting on the valve 10, reduces the flow rate of the polymerizate supplied from the outlet of the reactor 1 to its inlet, until the temperature set by the regulator

7i The regulator 7 ceases to change the setting of regulator 8 when the Mooney viscosity of the polymer measured by sensor 5 becomes 72 units. The temperature at the inlet of the reactor 1, measured by sensor 3, is equal to 16.4 ° C, a method for controlling the continuous polymerization process of isoprene carried out in a battery of reactors in the presence of a complex metal-organic catalyst by stabilizing the polymerized material supplied from the outlet of the reactor 1 to its the entrance to Livadia's pipeline-20 polymer concentration at pin 14 is equal to 20. Due to the fact that the temperature at the inlet to reactor 1, where the catalyst is fed, has decreased as compared with the previous

impact, this led to a decrease in 25 the reactor, characterized by the activity of the polymerization process, the fact that, in order to reduce consumption

during the course of the reactor, the change in catalyst consumption and the viscosity adjustment are in. Muni polymer by changing the temperature of the reaction mixture at the inlet to

The concentration of the polymer at the outlet of the reactor 1 is stabilized by a sensor 4, a regulator 6 and a regulating valve 9 by changing the flow rate of the complex organometallic catalyst at the same value of 9.6% by weight,. catalyst consumption with this enlarger catalyst and the content of oligomers in the polymer; a part of the polymerizate stream withdrawn from the lane is separated. The 30th reactor of the battery is sent to its inlet and the reactor is increased to increase the temperature of the reaction mixture at the inlet, and the expansion is decreased to decrease the temperature.

Up to 90 L H. As a result, a polymer with a Mooney viscosity is obtained. It is a polymer of polymerizate fed to a measure of 72 units. and the content of oligomers entering the reactor from its output.

in the polymer of 0.45. wt.% (in polymerization / / 0.09 wt.%).

When using the proposed method for adjusting Mooney viscosity in a wide range, the average catalyst is 93 l-h, i.e. 9.3, which corresponds to 3.1 kg per ton of rubber, and the concentration of oligomers in the polymer is 0.45% by weight.

Formula

A method of controlling the continuous process of polymerization of isoprene, carried out in a battery-reactors, in the presence of a complex metal-organic catalyst by stabilizing the polymer concentration for the polymer concentration at the reactor output by varying the catalyst consumption and adjusting the viscosity by. Muni polymer by changing the temperature of the reaction mixture at the inlet to

the catalyst and the oligomer content in the polymer, part of the polymerizate stream withdrawn from the battery’s first reactor is separated and sent to its inlet and to increase the temperature of the reaction mixture at the inlet and increase the reactor’s temperature.

h5 polymerizate entering the reactor inlet from its outlet.

-ABOUT

Claims (1)

Claim A method for controlling a continuous isoprene polymerization process carried out in a reactor battery in the presence of a complex organometallic catalyst by stabilizing the polymer concentration at the reactor outlet by changing the catalyst flow rate and adjusting the viscosity of the polymer Mooney by changing the temperature of the reaction mixture at the reactor inlet, characterized in that, In order to reduce the consumption of the catalyst and the content of oligomers in the polymer, a part of the polymerisate stream withdrawn from the Per-, first battery reactor is separated and They are fed to its inlet and, to increase the temperature of the reaction mixture at the inlet, the reactor is increased, and to reduce the temperature, the consumption of polymerizate entering the reactor from its outlet is reduced. Redktor N. Kishtulinets Compiled by A. Holland Tehred A. Kravchuk Proofreader M. Maximishinets Order 4287/23 Circulation 434 Subscription VNIIIPI of the USSR State Committee for Inventions and Discoveries 113035, Moscow, Zh-35, Raushskaya nab., 4/5 Production and printing company, Uzhhorod, ’Project, 4