The method of controlling the production of butyl rubber

 

The invention relates to the field of automation of technological processes of production of synthetic rubber and can be used in the production of butyl rubber in various technological design. To improve the quality of rubber and hardware performance manage processes copolymerization of monomers, deactivation of the catalyst, the degassing of the copolymer. At the stage of preparation of the charge support in the dynamics of the given ratio of components of the mixture, the concentration and temperature of the charge. Pre-cooled reactors copolymerization at a given speed cooling refrigerant flow in a glass and shirt reactors and carry out automatic startup of reactors for a given range of the reaction temperature of the copolymerization. The management processes are used to back microcontrollers, which are activated automatically when the exit key. More reliable control of the production as a whole. 3 C.p. f-crystals, 1 Il., table 1.

The invention relates to the field of automation of technological processes of production of synthetic rubber and can be used in the production of butyl rubber in various technologist is of the synthesis of butyl rubber, carried out in an inert solvent in the reactor with stirrer. The copolymerization of monomers (of isobutylene and isoprene) is carried out in the presence of a catalyst, with regulated costs of the charge and the catalyst, measured the temperature in the reaction zone, is determined by calculation, the Mooney viscosity of the polymer, and the parameters of the mixers that are adjusted depending on the viscosity of the polymer. Is used to manage the computer (controller), which with sensors and valves forming the loops (RF patent 2046126, IPC SS 2/06, G05D 27/00, 1993).

The disadvantage of this method of control is a limited scope, since it does not take into account the specific processes copolymerization of monomers, as well as the management processes of cooking and cooling the mixture, deactivation of the catalyst and the degassing of the polymer. No automatic start-up of reactors and reservation management system, which degrades the quality of the rubber and reduces the performance of the equipment.

The task of the invention is to extend the scope of application of the method, improvement of quality rubber and hardware performance.

The problem is solved in that the known method upravlenii catalyst, held in parallel reactors using loops, consisting of sensors-controllers-valves expenses mixture, catalyst and temperature sensors and concentration in the reactor, connected to the controller, further comprises a mixer blend with the contours of the regulation of isoprene, isobutylene, inert solvent and the concentration sensor of the charge; refrigerator with contour level control of ethylene and the temperature sensor of the charge; parallel mixers deactivator and copolymer with loops expenditure deactivator; connected in series degassers with loops expenses pair in degassers and temperature sensors connected to the controller, as well as loops expenses of ethylene in a glass and shirt reactors and backup controllers; specify the concentration and temperature of the mixture, the temperature and rate of cooling of the reactors, the reaction temperature of the copolymerization of isoprene and isobutylene, the dosage of deactivator, the temperature in the degassers and for a given concentration of the charge and according to the information of the sensor to the concentration of the charge adjusting the flow of isoprene, isobutylene and an inert solvent in cm is ity and according to the information of the temperature sensor of the charge adjusting the flow of ethylene into the fridge impact on the valve control loop of ethylene; perform start-up of reactors impact on the valves of the control circuits expenses charge to fill them; for a given temperature and rate of cooling of the reactor serves ethylene in a glass and shirt reactors impact on the valves of the control circuits expenses ethylene; for a given reaction temperature of the copolymerization of isoprene and isobutylene, and according to the information of the temperature sensors in the reactor adjust the flow of catalyst in the reactors impact on the valves of the control circuits of consumption of the catalyst; for a given dosage of deactivator correct filing deactivator in parallel mixers deactivator impact on the valves of the control circuits of the costs of deactivator; for a given temperature and according to the information of the temperature sensors in the degasifiers adjust the steam flow in sequential degassers impact on the valves of the control circuits of the costs of steam; and the copolymerization of the monomers is carried out in eight parallel reactors, deactivation of the catalyst in eight mixers deactivator and copolymer, and degassing of the copolymer in the degasification systems, consisting of two degaser, one of which is a backup. is the IKI; specified temperature in the cooling reactor is -100-102^oWhen the cooling rate is not more than 30^oC/h, and the flow of catalyst in the reactor is carried out at the desired temperature cooling reactors and adjust it to produce a given reaction temperature of the copolymerization of the monomers in the range of -65-70^oC and when the output from the main controller included in the backup microcontrollers.

Research production production of butyl rubber in an inert solvent showed that for effective management of the processes required to realize the automatic start-up of reactors copolymerization of monomers to reserve the process control system( installation of a backup computer), to take into account the speed tahaliyani reactors to reduce thermal deformation of the apparatus and reduce energy costs. In addition, it is necessary to carry out interrelated management processes of cooking and cooling the mixture, copolymerization of isobutylene and isoprene, deactivation of the catalyst and degassing of the copolymer. All this improves the quality of the rubber and increases productivity.

The essence of predlagaetvashemu production of butyl rubber (shown one technological chain manufacture of rubber).

The scheme includes processes the batch preparation and copolymerization of monomers, the deactivation of the catalyst and the degassing of the polymer consists of units 1-5, connected by pipelines. The original monomers (isobutylene and isoprene) and an inert solvent (isopentane) are added into the mixer batch 1, where the resulting mixture is sent to the refrigerator 2, where, after cooling, into the reactor 3, in which is placed a cooling glass and shirt reactor (conventionally not numbered), is used for cooling the ethylene. Then, the solution of copolymer supplied to the mixer deactivator and copolymer 4, where the deactivation of the catalyst, and then in the degasser 5 to remove unreacted monomers and solvent. In the system management apparatus 1-5 includes sensors monitoring parameters connected to the controllers and control loops 6-31, consisting of sensors-controllers-valves. The system includes a flow control inert solvent 6, 7, 30 (sensor 6, the controller 30 and the valve 7, further description of the control circuits of the controller 30 is conventionally not mentioned); - flow control of isobutylene 8, 9; - flow control isoprene 10, 11; - the control loop p is tilana) 16, 17 for cooling the mixture in the refrigerator for 2; - temperature sensor charge 18; - the gauge of concentration of the charge 19; - the temperature sensor 20 in the reactor 3;
- flow control of deactivator 21, 22;
- temperature sensor 23 in the crystallizer 5;
- flow control pair 24, 25 in the degasser 5;
the circuits controlling the flow of ethylene 26-27 in a glass and 28-29 in the jacket of the reactor 3.

For interrelated management processes used by the controller 30 (basic) and controllers 31 (backup), which are activated automatically when the exit key.

The method of controlling the production of butyl rubber was carried out as:
- set the ratio of expenses isoprene-isobutylene, isoprene-isobutylene: isopentane (blend);
- determine the temperature of the mixture, its flow rate and the initial ratio of the catalyst - batch";
- set the temperature and rate of cooling of the reactor (temperature in the reactor and the reaction temperature, copolymerizate; dosage of deactivator; the temperature in the crystallizer;
is injected into the controller 30 information from sensors 6, 8, 10, 12, 15, 16, 18, 24, 26, 28;
is determined according to the sensor 8 (the control loop 8, 9) the current consumption of isobutylene and for a given cost ratio "isoprene-isobutylene" ADJ is menut consumption isopentane (loop 6, 7), mix the components of the mixture in the mixer 1, control the concentration of the charge according to the sensor 19 and direct the mixture in the refrigerator 2, where it is pre-cooled to the specified value using the temperature sensor of the charge 18 and regulation circuit 16, 17. Perform start-up of the reactor 3, for this serves the charge using a control loop 12, 13 (the degree of filling of the reactor is determined by the flow of mixture from the reactor, the flow sensor is conventionally not shown) and for a given temperature and rate of cooling of the charge fed to the shirt and the glass reactor 3, the refrigerant (ethylene) using respectively the control circuits 26, 27 and 28, 29.

When reaching the set temperature of the reactor cooling 3 serves for a given initial costs "catalyst-charge" catalyst using a control loop 14,15 and adjust its supply to establish the desired temperature of the copolymerization reaction, which is monitored by the temperature sensor 20;
- served in the mixer deactivator and copolymer of 4 for a given dosage of deactivator (mass ratio deactivator and polymer determined by laboratory by taking into account the conversion of monomers) using cootchie 23) using the control loop 24-25;
when the output from the main controller 30 (which is connected to the inputs of the sensors and valves) include in the backup controllers 31.

Thus, maintaining the dynamics of the given ratio of components of the mixture, the concentration and temperature of the mixture, of a catalyst in the charge and the rate of cooling of the reactors, improving the accuracy of temperature regulation and reduce thermal deformation of the equipment; maintaining a given dosage of deactivator and the temperature of the degassing of the polymer increase the quality of rubber. Enabling automatic startup of reactors, reduce their simple and increase productivity, while reserving control system improve the reliability of its work. Check control method carried out in Q3 2002, LLC Togliattikauchuk and showed its effectiveness.

Below is an example of the implementation of the proposed control method and table of his performance.

Example.

Defined values:
the ratio of expenses isoprene-isobutylene" 0,025 Rel.ed.;
the ratio of expenses isoprene-isobutylene:isopentane" 0,17 Rel.ed.;
the temperature of the charge to the reactor 3 -72^oC;
- concentration mixture of 0.17 wt.%;
- consumption charge per reactor 3 12000 kg/h;the;
- the rate of cooling of the reactor 3 is not more than 30^oWith/h;
the reaction temperature of the copolymerization -65-70^o;
- dosage of deactivator 0.03 Rel.ed;
the temperature in the crystallizer 5 85-90^oC.

For control devices 1-5 use the sensors and the corresponding control loops 6-31.

1. Determined according to the sensor 7, the current consumption of isobutene in a quantity of 2000 kg/h and for a given ratio of the isoprene-isobutylene defined consumption of isoprene as 20000,025=50 kg/h, which is set by the valve 11 (the circuit 10, 11).

2. For a given ratio of the isoprene-isobutylene:isopentane defined consumption isopentane as 2000+50/0,17=9950 kg/h, which is set by the valve 7 (the circuit 6, 7). The resulting charge in the amount of 2000+50+9950=12000 kg/h control sensor of the concentration of the charge 25, because the mixture of a given composition, 17%, then guided her out of the batch mixer 1 in refrigerator 2, where the cooled it with +20 to -72^oWith using a control loop refrigerant 16, 17.

3. Submit command to submit to the reactor 3 consumption charge, using the circuit 12, 13, defined by the degree of filling (up to 5 wt.% flow from the reactor and cooled the mixture to -100^o(Yes the ethylene 26,27 and 28,29 feeding ethylene into a glass and the jacket of the reactor 3 at a ratio of costs 50/50 wt.%.

4. Defined for a given initial ratio of catalyst-charge" 0.03 Rel. unit quantity as 0,0312000=360 kg/h and submit it to the reactor 3, set the desired temperature of the copolymerization reaction -67^oTo do this, adjust the flow rate of the catalyst 16 kg/h using a control loop 14, 15.

5. For a given dosage of deactivator on the copolymer, of 0,03 Rel.%, and the number of formed polymer 1640 kg/h (with conversion of monomers to 80 wt. %) the designated flow deactivator (methanol) as 16400,03=49 kg/h, which is released by a circuit 21, 22.

6. Determined according to the sensor 23 and the temperature in the crystallizer 5, is 87^oWith, because it was within the specified range 85-90^oWith the correction on the consumption of steam is not produced (contour 24, 25).

The table shows the advantage of the proposed method of control compared to the prototype.

The implementation of the method of control is scheduled for the 4th quarter of 2002, in the production of butyl rubber in OOO "Togliattikauchuk, , Togliatti.

The expected economic effect of 2.1 million rubles per year.

Claims

1. The method of controlling the production of butyl rubber by copolymerization from the reactors using loops, consisting of sensors-controllers-valves expenses mixture, catalyst and temperature sensors in the reactor, connected to the controller, characterized in that it contains a mixer blend with the contours of the regulation of isoprene, isobutylene, inert solvent and the concentration sensor of the charge, fridge with loops level of ethylene and the temperature sensor of the charge, parallelenumerable mixers deactivator and copolymer with loops expenditure deactivator, connected in series degassers with loops expenses steam and temperature sensors connected to the controller, and the circuits controlling the flow of ethylene into a glass and shirt reactor controllers, ask the concentration and temperature of the mixture, the temperature and rate of cooling of the reactors, the reaction temperature of the copolymerization of isoprene and isobutylene, the dosage of deactivator, the temperature in the degassers, and for a given concentration of the charge and according to the information of the sensor to the concentration of the charge adjusting the flow of isoprene, isobutylene and an inert solvent in the mixer charge effects on the valves of the control circuits for these costs, for a given temperature Sheehan control loop levels of ethylene, perform start-up of reactors impact on the valves of the circuits controlling the flow of mixture to fill them, for a given temperature and rate of cooling of the reactor serves ethylene in a glass and shirt reactors impact on the valves of the control circuits of consumption of ethylene, in glass and shirt reactors for a given reaction temperature of the copolymerization of isoprene and isobutylene, and according to the information of the temperature sensors in the reactor adjust the flow of catalyst in the reactors impact on the valves of the control circuits of the cost of the catalyst, for a given dosage of deactivator correct filing deactivator in parallel mixers deactivator and copolymer impact on the valves of the control circuits of the costs of deactivator, for a given temperature degassers and according to the information of the temperature sensors in the degasifiers adjust the steam flow in sequential degassers impact on the valves of the control circuits of the steam consumption, and the copolymerization of the monomers is carried out in eight parallel reactors, deactivation of the catalyst in eight parallel mixers of deactivator and copolymer, and degassing of the copolymer in two of the I, that the degree of filling of the reactor charge is determined by the consumption of them up to 5 wt.% from the maximum of the scale sensors, the desired temperature of the cooling reactor is -100-102When the cooling rate is not more than -30S/h

3. The method according to PP.1 and 2, characterized in that the flow of catalyst in the reactor is carried out at the desired temperature cooling reactors and adjust it to produce a given reaction temperature of the copolymerization of the monomers in the range of -65-70C.

4. The method according to PP.1-3, characterized in that the output from the main controller included in the backup controllers.