JP3831289B2 - Temperature control method and apparatus for polymerization reaction process - Google Patents

Description

[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a temperature control method for a polymerization reaction process, and more particularly to a temperature control method for a process accompanied by a temperature rise due to reaction heat.
[0002]
[Prior art]
In the field of process control such as petrochemistry, control of a polymerization reaction process is one of the things that are difficult to automate. For example, in the operation of switching from the temperature rise of the reactor internal temperature to the constant temperature control, there is a great deal of dependence on the operator's intuition and experience. However, in recent years, high-mix low-volume production has been demanded, and control methods that rely on intuition and experience as before have been unable to handle them.
[0003]
In the internal temperature control of the reactor, the reaction temperature is set for each product type. In the temperature control, heat is applied from the outside of the reactor to maintain the aforementioned reaction temperature. In many cases, heat is supplied from the outside through a heat medium such as hot and cold water through a jacket around the reactor. In many cases, a so-called cascade control system is employed in which a set value of the jacket (inlet) temperature is obtained by reaction temperature feedback control and the opening of the jacket flow valve is adjusted according to this set value.
[0004]
However, heat from the outside does not quickly reach the inside of the reactor, and there are heat loss and time delay. Furthermore, reaction heat is generated in the progress of the polymerization reaction, and as a result, the temperature inside the reactor is increased. Thus, the delay in temperature control from the outside and the self-heating inside the reactor must be considered at the same time.
[0005]
To solve this problem, a method for realizing automatic control using a reaction model is described in, for example, Hanakuma, Nagasako, Sasaki: Design and application of control system in batch polymerization reactor: System / Control / Information, Vol. 35, no. 3, pp. 145-150 (1991) has been proposed. Here, stable automatic control is realized by predetermining and controlling the optimum pattern of the jacket temperature in accordance with the reaction temperature pattern.
[0006]
[Problems to be solved by the invention]
In the above prior art, the influence of the delay in heat transfer from the jacket and the temperature rise due to the heat of reaction inside the reactor are taken into consideration. However, in order to determine the jacket temperature pattern, highly accurate modeling is required for each product type. For this reason, a great deal of effort is required for model construction, and models are required for the types of products that handle them, resulting in an enormous management cost. Further, since the heat transfer coefficient of the reactor changes as the operation time elapses, the jacket temperature pattern also changes, so it is necessary to adjust it again.
[0007]
As described above, the conventional method for controlling the temperature of the polymerization reaction process has a problem that labor is large because a model used for deriving the operation pattern requires high accuracy. Furthermore, no consideration is given to aging of the process.
[0008]
An object of the present invention is to provide a temperature control method and apparatus for a polymerization reaction process that takes advantage of a temperature prediction result based on a simple model and incorporates measures against aging of the process in view of the above-described problems of the prior art. is there.
[0009]
[Means for Solving the Problems]
The present invention that achieves the above object provides a temperature control method for a polymerization reaction process in which the reaction temperature of a polymerization process in which reaction heat is generated is switched from temperature increase control to reaction temperature feedback control for constant temperature control through temperature control of a jacket. When the jacket temperature is controlled so as to reduce the difference between the heating temperature to the reactor and the jacket temperature measurement value, when the reaction temperature reaches the first determination temperature T0, the jacket temperature setting value is changed from the heating temperature to the cooling temperature. The time change of the reaction temperature is predicted based on the time differential value of the reaction temperature, the cooling temperature is corrected based on the prediction result, and the increase in the reaction temperature is maintained at the corrected cooling temperature. Further, the second determination temperature T1 is determined based on the reaction temperature and the jacket temperature, and the control is switched to the reaction temperature feedback control when the reaction temperature reaches the second determination temperature T1.
[0010]
If the reaction temperature tends to decrease due to the corrected cooling temperature, the cooling temperature is recorrected so that the reaction temperature increases.
[0011]
Further, the time change of the reaction temperature is predicted based on the time differential value, and when the increase in the reaction temperature is large, the second determination temperature is corrected to a value larger than T1, and the increase in the reaction temperature is small. In this case, it is corrected to a value smaller than T1.
[0012]
According to the present invention, when performing temperature control of the polymerization temperature process, a reaction temperature change is predicted using a simple model, the cooling temperature is appropriately corrected based on the result, and reaction temperature feedback control is input. Since the timing is appropriately determined, the temperature of the stable polymerization reaction process can be controlled.
[0013]
DETAILED DESCRIPTION OF THE INVENTION
Hereinafter, embodiments of the present invention will be described with reference to the drawings. FIG. 1 shows an overall configuration of a temperature control system of a polymerization reaction process according to an embodiment of the present invention. A polymerization reactor 10 to be controlled, a jacket 20, a reaction thermometer 30, a jacket inlet thermometer 40, a jacket circulation pump 50, a hot water valve 60, a cold water valve 70, a split range 80, and a jacket temperature controller 90 are configured. . The polymerization reactor 10 shows a general polymerization reaction, and here, a so-called exothermic process in which heat is generated with the reaction, such as a vinyl chloride polymerization reaction, is assumed.
[0014]
The elements constituting the control method include a control mode selection function 100, a reaction temperature control function 200, a reaction temperature DB 300, a startup temperature DB 400, a switch 500, and a manual input function 600.
[0015]
Each function will be described below. The control mode selection function 100 reads various set temperatures at the time of plant start-up from the start-up temperature DB 400. Further, the reactor internal temperature (T) and jacket temperature (Tj0) are read as measurement data, and the jacket temperature target value (STj) is read as a control signal.
[0016]
From these input data, a jacket temperature target value (S100) at the time of starting the plant and a feedback control input determination signal (S100A) by the reaction temperature control function 200 are output. In the present embodiment, the measured temperature of the jacket inlet 40 is shown as the jacket temperature, but the present invention is not limited to this, and any temperature may be used as long as it indicates the jacket temperature and can be installed with the measuring instrument.
[0017]
The reaction temperature control function 200 compares the reactor internal temperature (T) with the set temperature (Tref) read from the reaction temperature DB 300, and calculates an operation signal for the jacket temperature (Tjo) so that the deviation becomes small. . This is generally called reaction temperature feedback control, and is simply abbreviated as “FB control” below.
[0018]
In many cases, the “proportional integration method” is applied to the calculation of the FB control. In the proportional integration method, the operation signal (S200) is calculated by subjecting the deviation (E) between the set temperature (Tref) and the reactor internal temperature (T) to the proportional calculation and the integral calculation according to the equation (1). To do.
[0019]
S200 = K1 * E + K2 * ∫Edt (1)
Here, K1: proportional gain and K2: integral gain are parameters for adjusting the control performance of the FB control.
[0020]
FIG. 2 shows the data structure of the reaction temperature DB. The reaction temperature DB 300 associates a uniquely determined reaction temperature setting value (Tref) with a product produced in a batch polymerization reaction. In the figure, in addition to the product number, the type of raw material is also used as a factor for association. In short, the combination of the production process and the reaction temperature referred to therein is specified. When setting the set value (Tref) in the reaction temperature control function 200, in actual production, the operator may select and set from the DB or automatically set by program processing, but once production is started, the reaction In many cases, the temperature set value is almost fixed.
[0021]
FIG. 3 shows the data structure of the startup temperature DB. The startup temperature DB 400 sets temperature setting data for the control mode selection function 100 for each product and each raw material. Examples of setting items will be described below.
[0022]
The heating temperature (TH) is a jacket temperature setting value. At the start of the polymerization reaction, the reactor is heated from the outside to promote the polymerization reaction of the charged raw materials. TH is a temperature setting value at that time, and in many cases, the maximum temperature that can be supplied as a jacket heat medium is set.
[0023]
The temperature rise restriction (dTH) is a restriction provided for increasing the jacket temperature per unit time. Depending on the chemical characteristics of some products and raw materials, it is necessary to moderately increase the temperature of the heating from the outside, and this is a limitation.
[0024]
The determination temperature T0 is a determination temperature when switching from heating to cooling. In the reactor temperature control, when the reactor internal temperature (T) exceeds the determination temperature T0, the target value STj of the jacket temperature controller 90 is switched from the heating setting to the cooling setting. The cooling temperature (TC) is a jacket temperature set value, and is generally set to a value lower than the reaction temperature set value (Tref). The temperature set value is given to the TIC 90 via the switch 500 as the output S100 of the control mode selection function.
[0025]
Thereafter, when the reactor temperature control reaches the determination temperature T1, the control mode selection function 100 outputs S100A, switches the switch 500 to the reaction temperature control function 200, and performs the reaction temperature FB control. The determination temperature T1 is actually corrected from the initial set value (T10) based on the process state.
[0026]
FIG. 4 shows an example of the time change of the reaction temperature and the cooling temperature. The target value (STj), the reactor internal temperature (T), and the jacket temperature (Tj0) of the jacket temperature controller 90 are shown with respect to the reaction temperature set value (Tref). The vertical axis is temperature, and the horizontal axis is time.
[0027]
After the polymerization reaction starts, the target value (STj) is set to the heating temperature (TH). After the reactor internal temperature (T) reaches the determination temperature O (T0), (STj) is set to the cooling temperature (TC). When the reactor internal temperature (T) reaches the determination temperature (T1), FB control by the reaction temperature control function 200 is started.
[0028]
Switching between these control methods is performed by the switch 500. The switch 500 receives the output signal (S100) of the control mode selection function 100, the control mode switching signal (S100A), the output signal (S200) of the reaction temperature control function 200, and the signal from the manual input function 600, and the jacket temperature. The target value (STj) of the controller 90 is output.
[0029]
The switch 500 is connected to the output of the control mode selection function 100 at the start of the polymerization reaction. When the reactor internal temperature reaches the determination temperature (T1), it is connected to the output of the reaction temperature control function 200, and FB control is turned on. When the operator manually intervenes, the target value (STj) of the jacket temperature controller 90 can be manually operated by connecting to the output of the manual input function 600.
[0030]
FIG. 5 is a flowchart showing the control operation of this embodiment. After completion of raw material charging, polymerization reaction control is started (F10). The reactor is heated from the outside (F20), and after the reactor internal temperature satisfies the determination condition (F30), the reactor is switched to cooling (F40).
[0031]
Here, the temperature prediction 1 (F50) based on the polymerization reaction model is performed, and the cooling temperature (TC) is corrected (F60). Subsequently, cooling (F70) is executed, and temperature prediction 2 (F80) is executed. Based on this prediction result, the determination temperature (T1) is corrected (F90), and the FB input determination is made (F100). If feedback control input (F110) is possible as a result of the determination, switching to FB control by the reaction temperature control function 200 is performed, and the polymerization temperature control establishes a cascade configuration.
[0032]
The control operation from F50 to F100 described above is performed by the control mode selection function 100. FIG. 6 shows details of the control mode selection function. The control mode selection function 100 reads the reactor internal temperature (T), and outputs a temperature set value (S100) during heating and cooling operations and an FB charging determination signal (S100A). In the heating setting device 110, a heating temperature (TH) and a temperature rise restriction (dTH) are set. In the comparison 120, the determination temperature (T0) is compared with the reactor internal temperature (T), and when T0 <T is satisfied, the switch 130 is switched to the cooling setting device 140.
[0033]
The cooling setter 140 reads the reactor internal temperature (T) and outputs the cooling temperature (TC) as an output signal (S100). FIG. 7 shows a model of the cooling setter. Model 1410 predicts the behavior of reactor internal temperature (T) using a mathematical model. Specifically, regarding the change over time in the reactor internal temperature (dT / dt), considering the effect of switching from the heating operation to the cooling operation, the reactor internal temperature (T) rises slowly, or the temperature Predict whether it will cause a decline. An example of this prediction method will be described below.
[0034]
For the time variation of the reactor internal temperature (T) and external heating such as a jacket, the heat balance equation is established as (accumulation rate of sensible heat) = (exotherm rate due to reaction) + (heating rate from the surroundings). When this is expressed by a mathematical formula, the formula (2) is obtained.
VρCp (dT / dt) = Qr + UA (Tj0-T) + (Others) (2)
Here, V: reactor volume, ρ: reactant density, Cp: reactant heat capacity, Qr: exothermic rate, U: overall heat transfer coefficient, A: heat transfer area.
[0035]
Except for the exothermic rate (Qr), it is equipment data of the reactor and physical property data of the reactant, and can be preset. However, the exothermic rate (Qr) is data that is difficult to measure during the polymerization reaction control, and cannot be used directly in the prediction calculation. Therefore, the behavior of the reactor temperature (T) is predicted by the following calculation.
[0036]
First, the time change of the reactor internal temperature (T) at the time of switching from heating to cooling is obtained, and then the sensible heat accumulation rate Q0 at the time of switching is obtained by Equation (3).
Q0 = VρCp (dT0 / dt) (3)
Further, the heating rate QH from the surroundings at the time of switching is approximated by Equation (4). The heating rate QH is determined by the temperature difference between the determination temperature (T0) and the heating temperature (TH).
QH = UA (TH-T0) (4)
Further, the external heating rate QC by the cooling operation is approximated by the equation (5). Since the cooling temperature (TC) is lower than T0, QC <0.
QC = UA (TC-T0) (5)
The sensible heat accumulation rate Q ′ by switching from heating to cooling is expressed by equation (6) using equations (3) to (5). Q ′ is approximated after switching between external heating and cooling.
Q ′ = Q0−QH + QC (6)
From the above, the behavior of the reactor internal temperature after the start of cooling is expressed by the equation (7).
(DT ′ / dt) = Q ′ / VρCp (7)
That is, by determining the sign of Q ′, it can be determined whether the temperature inside the reactor rises or falls. Therefore, the model 1410 outputs the sensible heat accumulation rate Q ′, which is a predicted value, to the correction unit 1420.
[0037]
FIG. 8 is a flowchart of the correction unit that determines the cooling temperature Tc. First, temperature data is read in F800 and F810, and Q ′ and (dT ′ / dt) are obtained by the above calculation. Next, the correction unit 1420 performs the following processing on the cooling temperature (TC) based on the predicted value Q ′.
[0038]
First, it is determined whether or not the reaction temperature is lowered (F820), and the process is performed as follows. (1) If the predicted value Q ′ is positive or zero, the cooling temperature (TC) is output as it is (F850). (2) If the predicted value Q ′ is negative, the cooling temperature (TC) is corrected so that the predicted value Q ′ is positive (F830, F840).
[0039]
The TC correction method in the case (2) will be described. In the formula (6), since Q ′ only needs to be zero or more, TC may be determined so as to satisfy the following formula.
QC> QH-Q0 (8)
If the equation (8) is rearranged, the equation (9) is obtained, so that the TC may be corrected accordingly.
TC> TH- (Q0 / UA) (9)
In the above, the influence of the heat generation rate due to self-heating of the polymerization reaction is not considered. However, with respect to the predicted value Q ′, the cooling temperature is corrected so as to avoid Q ′ <0, and further, the influence of the heat generation rate (Qr) due to self-heating is added. Temperature drop can be avoided. The above is the output signal (S100) of the heating setting device 110 and the cooling setting device 140 in the control mode selection function 100.
[0040]
Next, the FB insertion determination 150 in FIG. 6 will be described. FIG. 9 shows a detailed configuration of the FB insertion determination unit. The model 1510 predicts and corrects the time change (dT / dt) of the reactor internal temperature (T). Although the model equation similar to that of the cooling setting device 140 is used, in this model 1510, it is considered that there is no influence of the heating operation, and only the influence of the cooling operation is considered.
[0041]
The model 1510 reads the reactor internal temperature (T), the jacket temperature (Tj0), and the target value (STj) of the jacket temperature controller 90. First, the time change (dT / dt) of the reactor internal temperature (T) at the time of reading is obtained, and the sensible heat accumulation rate Q10 is obtained by the equation (10) as in the case of the cooler 140.
Q10 = VρCp (dT / dt) (10)
At the same time, the jacket temperature (Tj0) and the target value (STj) are compared, and the equation (11) is calculated based on the difference.
Qj = UA (STj-Tj0) (11)
From equation (11), Qj is zero if the jacket temperature (Tj0) matches the target value (STj). On the other hand, when (Tj0) does not reach the target value, the jacket temperature controller 90 supplies further cold water, so that the jacket temperature is expected to decrease. When this effect is taken into consideration and the heat storage speed according to the equation (10) is corrected, the correction value Q1 and the corrected (dT / dt) become the equations (12) and (13), respectively.
Q1 = Q10 + Qj (12)
(DT / dt) = (dT / dt) + Qj / VρCp (13)
FIG. 10 is a flowchart for determining the determination temperature T1. After prediction (F1010) of temperature time change (dT / dt) by the model 1510, the comparison unit 1520 refers to data of the determination temperature T1 based on this (dT / dt) (F1020).
[0042]
FIG. 11 shows the T1 curve. The T1 curve plots the determination temperature corresponding to the state of the reactor internal temperature, with the horizontal axis representing the time variation (dT / dt) of the reactor internal temperature and the vertical axis representing the FB charging determination temperature (T1). In the present embodiment, a graph format is used, but it may be defined in a numeric table format. The determination temperature T1 is referred to from (dT / dt) determined by the model 1510. The characteristics of this T1 curve are based on the initial set value T10. (1) When the temperature inside the reactor is rapidly increased ((dT / dt) is large), the judgment temperature T1 is increased and the FB charging timing is delayed. (2) When the change in the reactor internal temperature is small ((dT / dt) is small), the judgment temperature T1 is lowered and the FB charging time is advanced. These are executed in the flowcharts F1030 to F1050 in FIG.
[0043]
That is, when the effect of the cooling operation is small with respect to the change in the reactor internal temperature, the temperature rises quickly. In this case, if the FB control is quickly turned on, a heating operation by feedback control is added, so that there is a possibility that the reaction temperature is greatly overshot. Therefore, the determination temperature T1 is increased and the FB charging time is delayed. On the other hand, when the influence of the cooling operation is great and the rise in the reactor internal temperature is moderate, the FB control is turned on early to quickly reach the reaction temperature (Tref).
[0044]
In the determination unit 1530 of FIG. 9, when the reactor internal temperature (T) exceeds the value described in the T1 curve based on the result of referring to T1 corresponding to the corrected (dT / dt), the FB input signal is ( S100A) is output.
[0045]
FIG. 12 shows reaction temperature change plotted with reaction temperature T1 curve. The internal temperature of the reactor at the time of cooling switching and its change over time are plotted at (0) in the T1 curve. When the influence of the cooling operation is small and (dT / dt) after correction does not change much, the determination temperature T1 for turning on the FB control is set to a temperature higher than the initial setting T10. An example of this is plotted in case (1). On the other hand, when the rise in the reactor internal temperature is sufficiently decelerated, the determination temperature is set to a temperature lower than T10. An example of this is plotted in case (2).
[0046]
FIG. 13 shows the operations of cases (1) and (2). (A) is a case of case (1). That is, when the rise in the reactor internal temperature during cooling is large, the determination temperature T1 is corrected from the initial set value T10 to a higher T1, and the heating operation immediately after the FB control is turned on is reduced.
[0047]
(B) is the case (2). That is, when the reactor internal temperature is sufficiently decelerated by cooling, the determination temperature T1 is corrected from the initial set value T10 to a lower T1, and the reaction temperature (Tref) is reached by moving the FB control forward. The time is shortened.
[0048]
Next, a description will be given in comparison with a conventional control system. FIG. 14 shows a conventional control system, and shows a case where an operator performs a heating operation and a cooling operation through a manual setting function 600. The reaction temperature control function (TIC) 250 has the same function as that of this embodiment, and the target of the jacket temperature controller 90 is set so as to reduce the deviation between the reactor internal temperature (T) and Tref set from the reaction temperature DB. Determine the value. Switch 550 switches between jacket temperature control by manual operation and cascade connection of reaction temperature control function 250.
[0049]
FIG. 15 is a characteristic diagram showing a conventional control operation. As the polymerization reaction starts, the jacket temperature is raised to the heating temperature (TH) and the reactor internal temperature (T) is raised. Based on the judgment of the operator, the jacket temperature is changed to the cooling temperature (TC), and then the reaction temperature control function 200 is cascaded to constitute a feedback control system. At this time, the switching determination from heating to cooling and the FB control input determination by cascade connection are based on the determination of the operator or reference to the set temperature. For example, mode switching is performed using the set temperatures T0 and T1 as determination temperatures. However, regardless of the rate of increase in the reactor internal temperature, the FB control is turned on when the temperature reaches T1 uniformly. Therefore, when the reactor internal temperature (T) overshoots due to the heating operation by the FB control. There is.
[0050]
On the other hand, in the case of this example, in performing the temperature control of the polymerization temperature process, the reaction temperature change is predicted using a model, the cooling temperature is appropriately corrected based on the result, and the reaction temperature feedback control is performed. Since the charging timing is determined, stable temperature control of the polymerization reaction process is possible.
[0051]
As mentioned above, although one Example of this invention was shown, the reaction temperature control function 200 is not limited to a "proportional + integral" system, For example, a model-based predictive control system is applicable.
[0052]
In the control mode selection function 100, the case where the self-heating rate (Qr) due to the polymerization reaction is not used has been described. However, for example, when a highly accurate and simple model formula can be incorporated, the term of Qr is incorporated into the model. Is easily possible. In this Qr model adjustment, it is possible to adjust in consideration of production data such as products and raw material varieties.
[0053]
In FIG. 11, the T1 curve has been described in a graph format. However, the combination table of the reactor internal temperature and the determination temperature 1 may be clearly shown, and the graph is not limited to the graph format.
[0054]
In this embodiment, the determination temperatures T0 and T1 are set from the DB, but can be set by the operator. In addition, the cooling temperature TC is corrected once after the cooling switching. However, the correction may be repeated a plurality of times, and manual correction by the operator is also possible.
[0055]
In the present invention, an exothermic process due to a polymerization reaction is an object to be controlled, but the present invention can also be applied to other reaction processes such as an endothermic process by appropriately setting an external temperature setting value.
[0056]
【The invention's effect】
According to the present invention, when performing the temperature control of the polymerization temperature process, the reaction temperature change is predicted, the cooling temperature is appropriately corrected based on the result, and the input timing of the reaction temperature feedback control is determined. The temperature of the stable polymerization reaction process can be controlled.
[Brief description of the drawings]
FIG. 1 is an overall configuration diagram of a temperature control system of a polymerization reaction process according to an embodiment of the present invention.
FIG. 2 is a schematic data configuration diagram of a reaction temperature database.
FIG. 3 is a schematic data configuration diagram of a startup temperature database.
FIG. 4 is a characteristic diagram showing changes in reaction temperature, jacket temperature, and control signals over time.
FIG. 5 is a flowchart of a polymerization reaction process temperature control method according to an embodiment of the present invention.
FIG. 6 is a configuration diagram of a control mode selection function according to an embodiment.
FIG. 7 is a functional block diagram of a cooling setting device according to an embodiment.
FIG. 8 is a flowchart of cooling setter operation according to an embodiment.
FIG. 9 is a functional block diagram of a feedback control input determination unit according to an embodiment.
FIG. 10 is a flowchart of determination temperature T1 correction according to an embodiment.
FIG. 11 is a graph of determination temperature T1.
FIG. 12 is an explanatory diagram showing a T1 curve of determination temperature and plotted reaction temperature changes.
FIG. 13 is a graph showing the change over time in reaction temperature and jacket temperature.
FIG. 14 is an overall configuration diagram of a conventional polymerization reaction process temperature control system.
FIG. 15 is a graph showing a time change of a control operation by a conventional polymerization reaction process temperature control method.
[Explanation of symbols]
DESCRIPTION OF SYMBOLS 10 ... Polymerization reactor, 20 ... Jacket, 30 ... Internal temperature thermometer, 40 ... Jacket inlet thermometer, 50 ... Jacket circulation pump, 60 ... Hot water valve, 70 ... Cold water valve, 80 ... Split range, 90 ... Jacket temperature control 100 ... Control mode selection function, 200 ... Reaction temperature control function, 300 ... Reaction temperature database, 400 ... Startup temperature database, 500 ... Switch, 600 ... Manual input function.

Claims (5)

A temperature control method for switching a reaction temperature of a polymerization process in which heat of reaction occurs from a temperature increase control to a reaction temperature feedback control for constant temperature control through temperature control of a jacket,
The temperature inside the reactor is set according to the product to be produced during the temperature rise control so as to reduce the difference between the jacket temperature setting value for heating the reactor and the jacket temperature measurement value. determination becomes a temperature T0, the switching from the heating temperature of the heating setting the jacket temperature set point cooling temperature of the cooling set, the time variation of the reactor temperature, the reactor temperature of the time due to polymerization models for products produced by predicted on the basis of the differential value, the cooling temperature is corrected by the prediction result, keeping the increase in the reactor temperature corrected cooling temperature,
Furthermore, the based on the prediction of the time change in the reactor temperature to determine the reaction temperature target value is smaller than the second determination temperature that has been set corresponding to the product to produce, the reactor temperature is the determined A temperature control method for a polymerization reaction process, wherein the control is switched to the reaction temperature feedback control when the second determination temperature T1 is reached.   2. The temperature control method for a polymerization reaction process according to claim 1, wherein when the reaction temperature tends to decrease due to the corrected cooling temperature, the cooling temperature is recorrected so that the reaction temperature increases.   In Claim 1, the time change of the reaction temperature is predicted based on the time differential value, and when the reaction temperature rises largely, T1 is corrected to a value larger than an initial setting value, and the reaction temperature rise A temperature control method for a polymerization reaction process, wherein T1 is corrected to a value smaller than the initial set value when smaller. A control method for switching the reaction temperature of a polymerization process in which heat of reaction is generated from temperature increase control to reaction temperature feedback control for constant temperature control through temperature control of a jacket,
When the jacket temperature is controlled so as to reduce the difference between the jacket temperature setting value for heating the reactor and the jacket temperature measurement value, the reaction temperature reaches a predetermined temperature T0 set corresponding to the product to be produced. , the switching the jacket temperature set value from the heating temperature of the heating set cooling temperature of the cooling setting,
The time change of the reaction temperature is predicted based on the time differential value dT / dt of the measured value, the cooling temperature is corrected based on the prediction result to keep the reaction temperature rising, and the time change of the reaction temperature based on the prediction, the reaction temperature determines a target value Tref is smaller than the determination temperature T1 of the reaction temperature is set corresponding to the product to produce, the reaction time when the reaction temperature reached the determined temperature T1 Switch to temperature feedback control,
The reaction temperature feedback control, a deviation between a target value Tref the reaction temperature measured value, calculates a jacket temperature target value so as to reduce the deviation, between the jacket temperature measurement value and the jacket temperature set point A temperature control method for a polymerization reaction process, wherein the jacket temperature is controlled so as to reduce a deviation. A temperature control device for a polymerization reaction process that switches a reaction temperature of a polymerization process in which heat of reaction is generated from a temperature rise control to a reaction temperature feedback control for constant temperature control through temperature control of a jacket,
A jacket temperature controller that controls to reduce the difference between the jacket temperature set value and the jacket temperature measurement value;
When the temperature inside the reactor reaches the first judgment temperature T0 set corresponding to the product to be produced , the jacket temperature set value is switched from the heating temperature of the heating setting to the cooling temperature of the cooling setting, and the time change of the reaction temperature Cooling setting means for predicting the temperature based on the time differential value of the reactor internal temperature , and correcting the cooling temperature based on the prediction result;
The second judgment temperature T1 set corresponding to the product to be produced is shown to indicate the time when the reaction temperature is kept at the corrected cooling temperature and the control of the reaction temperature is switched from the temperature rise control to the reaction temperature feedback control. The reaction temperature feedback is determined based on the time change of the reactor internal temperature and the jacket temperature corrected to the cooling temperature, and the reactor internal temperature reaches the determined second determination temperature T1. A temperature control apparatus for a polymerization reaction process, comprising feedback control input determining means for switching to control.

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