SU844620A1 - Method of control of polycaproamide continuous production unit - Google Patents

Description

I

This invention relates to the automation of nppiteccoB polymerization and can be used in the production of dolomoproamvdny fiber.

A known method of controlling the installation of continuous production of half-sapromide in two successively located in the first and second reactors, is -13 change. And the composition of the reaction mixture, depending on the viscosity of the reaction mixture at the outlet of the first reactor, The time spent in the second reactor depends on the viscosity of the product at the exit of the second reactor fl}.

The well-known method is characterized by the possibilities with respect to the accuracy of the stabilization of the viscosity of the iolikairoamod due to the agreement of the regimes of conduction of aerodesses to a 1G3 reactor.

The aim of the invention is to improve the accuracy of the stabilization of the viscosity of polycapamide.

2

The goal is achieved by the fact that in the known method of controlling the installation of continuous polycaproamide production in two first and second reactors in series, which consists in changing the composition of the reaction mixture depending on the size of the reaction mixture at the outlet of the first reactor, changing the residence time of the reaction mixture in the second reactor, depending on the viscosity of the product at the exit from the second reactor, the residence time of the reaction mixture in the second reactor is additionally adjusted according to from velich1shy viscosity

15 reactive mixture at the outlet of the reactor.

At the same time, the residence time of the reaction mixture in the second reactor can be stabilized by changing the flow rate.

2Q of the mixture into the second reactor.

The drawing shows a block diagram of a control system for implementing the proposed method. The polycalamide continuous production unit consists of the first 1 and second 2 sectional-type reactors connected by a melt pipe 3. The reaction mixture is fed into the reactor 1 and polymer is withdrawn from the reactor 2 indicated by arrows. The reaction mixture is continuously fed to the reactor 1 by paired inlet dispensers 4 having a common drive 5 With the help of the reducer 6, the ratio of the flow rates of the components of the reaction mixture is set and adjusted by the regulator 7. The level in the reactor 1 is measured by the level gauge 8, by supplying the reaction mixture to this reactor The op controls the regulator 9. With the aid of the spur block 10, the polymer is continuously withdrawn from reactor 1 and sent to reactor 2 along the melt line 3. By this, the intermediate viscosity of the product is continuously measured by viscometer 11. The level in solution 2 is measured by a level gauge 12, and the output viscosity of the target Product taken out of this reactor is continuously measured by the visco-winter 13. Signals from viscometer 11 and 13 are fed to the adder 14 and from it to the setpoint 15, which sets the reference to the controller 16, which controls the residence time of the polymer in the reactor 2.O With the aid of a contour level gauge a 12-regulator 16 with a setting device 15 - unit 10 stabilizes the residence time of the product in the reactor 2. With the help of KOHTjpa the level indicator 8 - regulator 9 - actuator 5 stabilizes the residence time of the product in reactor 1. At changing the composition of the mixture (the main perturbing effect) the stabilization value of the intermediate viscosity will start working by changing the composition of the reaction mixture, the viscometer 11-regulator 7-gear 6, and the contour control reactor 2 will receive a forward signal.arakterizuvoschy average value trend output viscosity (its expectation) to change the current value of intermediate viscosity. Due to this, the setting of the regulator will be equal to 8 ° L ... 16, which will allow a predetermined preset of the corrected residence time of the reaction mixture in the reactor 2, and then, when the polymer begins to exit at the exit of the reactor 2 with the output viscosity deviating from its preset value, control of the residence time in reactor 2 will be conducted through the adder 14. This will limit the amplitude of the control action (change in the number of revolutions of the pressure unit 1O), since by that time the intermediate viscosity will be often independently or fully corrected by intermediate viscosity stabilization circuit. The use of the proposed control method will improve the accuracy of stabilization of the viscosity of the site, reduce the amount of waste from the textile part of the process. Fore. Mula of the invention 1. A method for controlling the installation of a non-continuous production of polycaproam. in two successively located first and second reactors, consisting in changing the composition of the reaction mixture depending on the viscosity of the mixture — at the outlet of the first reactor, changing the residence time of the reaction—. Noah mixture in second reactor, depending on the viscosity of the product at the outlet of the second reactor, characterized in that, in order to increase accuracy. stabilizing the viscosity of polycaproamide, correcting the residence time of the reaction mixture in the second reactor, depending on the viscosity of the reaction mixture at the outlet of the first reactor. 2. The method according to claim 1, which is also characterized in that the residence time of the reaction mixture in the second reactor is stabilized by changing the flow rate of the reaction mixture in the second reactor. Sources of information that are worth considering during the examination 1. USSR copyright certificate in application No. 262373 / 23-05, cl. C O8 F 2/00, 1978.

Claims (2)

1. The way to control the installation is not—. intermittent production of polycaproamide. in two successive first and second reactors, consisting in changing the composition of the reaction mixture depending on the magnitude of the viscosity of the mixture at the outlet of the first reactor, changing the residence time of the reaction. mixture in. the second reactor, depending on the viscosity of the product at the outlet of the second reactor, characterized in that, in order to increase accuracy. stabilizing the viscosity of polycaproamide, adjust the residence time of the reaction mixture in the second reactor in the recording of the viscosity of the reaction mixture at the outlet of the first reactor. 2. The method of pop. 1, the difference is that the residence time of the reaction mixture in the second reactor is stabilized by changing the flow rate of the reaction mixture to the second reactor.