SU726112A2 - Method of control of butadiene polymerization process in solution - Google Patents

Description

(54) METHOD OF MANAGING THE MORTAR POLYMERIZATION PROCESS OF BUTADIENE

37

The interstitial parameter for one reactor, or for the corresponding previous one, increases by successive steps, determined by the size, of the intermediate parameter in the previous reactor. As an intermediate parameter, the monomer consumption (monomer concentration in the solvent) or the temperature in the corresponding reactor is used. In addition, the pressure in the first reactor is additionally adjusted depending on the temperature in it, as well as the consumption of the solvent in the battery reactor, depending on the temperature in it.

The proposed method is illustrated in the drawings, where in FIG. Figure 1 shows a block scheme that implements the control method when using as an intermediate parameter the consumption of monomer, Fig. 2 is a block diagram that implements the control method when using the temperature in the reactor as an intermediate parameter.

The monomer, solvent, and components of the catalyst podjut in located sequentially in the course; the reaction mixture 1,2 and 3 reactors.

The consumption of monomer in the reactor 1 is measured by the sensor 4 and adjusted by means of the controller 5, acting on the valve 6,

The consumption of monomer in the reactor 2 is measured by the sensor 7 and rerouted by means of the regulator 8, acting on the valve 9.

The flow rate of the solvent in the reactor 1 is measured by the sensor Yu and is controlled by the regulator 11, acting on the valve 12,

The consumption of solvent in the reactor 2 from MejnoT sensor 13 and regulate using regulator 5, I will act on the valve 15.,

The consumption of solvent in the reactor 3 is measured by the sensor 16 and controlled by means of the controller 17, acting on the valve 18.

The consumption of monomer in the reactor 3 is measured by the sensor 19 and adjusted by means of the regulator 2O, acting on the valve 21.

The melt of the aluminum component of the catalyst into the reactor 3 is measured by the sensor 22 and adjusted by means of the regulator 23, affecting the valve 24 on the loss of supply of the aluminum component of the Catalyst.

24

The consumption of the titanium component of the catalyst in the reactor 3 is measured with the aid of an atchik 25 and is regulated with the help of a reuttor 26, acting on the valve 27 of the supply line of the titanium component of the analyzer.

Polymer Flour Viscosity (or the average molecular weight of the polymer) and at the outlet of the reactor 3, the sensor 28 is adjusted by means of the regulator 29, changing the setting of the regulator 23.

The plasticity of the polymer is measured at the outlet of the reactor 3 by the sensor 30 and is controlled by means of the controller 31, changing the setting of the controller 26.

The temperature of the reaction mixture after 1, 2 and 3 reactors is measured by the corresponding sensors 32, 33 and 34.

The pressure in the reactor 1 is measured by the sensor 35, the signal from which is fed to the computing device 36.

When used in, as an intermediate parameter of monomer consumption (monomer concentration in solvent) (see Fig. 1), signals from sensors 32, 33 and 34 are fed to computing device 36. Upon reaching the maximum permissible pressure value in reactor 1 measured by sensor 35, following successively determined shchagami reduce the consumption of monomer in the reactor 1, the computing device 36 corrects the task to the controller 5. Upon reaching the allowable technological value of the signal to the controller 5 for the reactor 1 -inflammatory certain largest value decreases its schagami monomer flow to the reactor 2, correcting the reference torus controller 8. Upon reaching the allowable value of the process signal to the controller 8 similar to the reactor 1 varied reception mode 3. oeaktooa.

Upon reaching the minimum permissible pressure value in the reactor I, successively determined in steps increase the consumption of the myomer into the reactor 3; reactor 2, the adjustment of the task to the controller 8. Similarly, the transition from changing the operating mode of the reactor 2 to changing the operating mode of the reactor 1 is carried out.

With an unacceptable temperature change in the factor 1, the stabilizing pressure in reactor 1 is adjusted, the increase in temperature is compensated for by a decrease in the consumption of monomer into this reactor, and vice versa.

When used as an intermediate temperature parameter (FIG. 2), the signal from temperature sensor 32 in reactor 1 is fed to the controller

37, with which the setting of the controller 5 is adjusted. The signal from the temperature sensor 34 in 3 is supplied to the controller 39, with which the setting of the controller 20 is adjusted.

Upon reaching the maximum permissible pressure value in the reactor 1, measured by sensor 35, in successive steps of a certain size, for example, 1 C, the temperature in reactor 1 is reduced by adjusting the controller 36 to the controller 37. (or for the corresponding downstream reactor), the magnitude 1pp 1 signal to the regulator 37 is reduced by successive steps of certain magnitude, for example, by, the temperature in the reactor 2 (or in the corresponding yuschem reaktoer).

Upon reaching the minimum permissible pressure value in the reactor 1 by successive certain steps, for example, the flow rate in reactor 3 is increased, when the permissible process temperature for this reactor is reached in reactor 3 (or, the temperature in the previous reactor. The correction of the temperatures in the 2 and 3 reactors is carried out by calculating the ycrpofteTBOM 36, changing the setting of the regulator 38 and 39.

The temperature in each reactor can be further stabilized by adjusting the solvent flow rate to the corresponding reactor, changing the setting of the regulators 11 using the computing device 3Q; 14 and 17.

In the case of exceeding the maximum tetrapure, the solvent consumption increases, which increases the load on the reactors, and vice versa.

Claims (5)

1. The method of controlling the process of polymerization of butadiene according to the author. St. N 402527, characterized in that, in order to increase the productivity of the process, when the polymerization battery in the first reactor reaches the maximum allowable pressure value by successive, determined steps, decreases the intermediate parameter value in this reactor after reaching the technological value of the intermediate TiapaMeTpa for this reactor (or the corresponding subsequent reactor), by successive, determined steps, reduce the value of the intermediate 1X parameter in the subsequent along the reactor reaction mixture, upon reaching the minimum permissible pressure in the reactor, successively determined steps increase the value of the intermediate parameter in the last reactor; the size of the steps of the intermediate parameter in the previous reactor. 2. The method according to claim 1 is also distinguished by the fact that the monomer consumption (monomer concentration in the solvent) in the corresponding reactor is used as an intermediate parameter. 3. Method according to paragraphs. 1 and 2, which is also distinguished by the fact that the pressure in the first reactor is additionally corrected depending on the temperature in him 4. The method according to claim 1, characterized in t & l, that as an intermediate parameter, use the temperature in the corresponding reactor. 5. Method according to paragraphs. 1 and 4j and l with the fact that the solvent consumption in the battery reactor is additionally adjusted depending on the temperature in it :. Sources of information taken into account in the examination 1. Copyright svdedelspu USSR № 402527, cl. C O8 F 136/06, 1972. :WITH;. -. -.,. 726112