JPH10296075A - Temperature control device and method for batch type reactor, and recording medium having control program recorded - Google Patents

Abstract

PROBLEM TO BE SOLVED: To obtain a reaction product of a desired quality by providing a supply temperature control means for controlling the temperature of a heat medium and control the internal temperature of a reactor by a simple method extremely accurately within a specified temperature range below a boiling point. SOLUTION: A polymerization tank 1 has a cooling water supply system for supplying a cooling water controlled to a specified temperature to a cooling jacket 5. The cooling water supply system is equipped with piping 6 for circulating the cooling water which has a temperature sensor 17 for detecting the temperature of the cooling water to be supplied into the cooling jacket 5. In addition, the cooling water piping 12 has a control valve 18 for adjusting a flow rate. An electronic control unit ECU 23 regulates the opening of the control valve 18 and thereby, controls the temperature of the cooling water to be supplied thought the piping 6 for circulating the cooling water so that the temperature of the temperature sensor 17 fitted to the piping 6 changes according to the change over time characteristics of a cooling water supply temperature.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to temperature control of a reactor in which a reaction is carried out while supplying raw materials into the reactor.

[0002]

2. Description of the Related Art Conventionally, there has been known a batch reactor in which a reaction is carried out while supplying raw materials to a reactor, and when the reaction is completed, a desired reaction product is taken out of the reactor. The temperature in the reactor is an important factor in order to obtain a reaction product of a desired quality and to carry out the reaction efficiently. In particular, when the temperature of a batch-type reactor in which a reaction is performed while supplying the above-described raw materials is controlled by heat exchange from the outside, the reaction conditions, heat transfer conditions, and heat capacity are changed by changing the amount of the contents. It is technically very difficult to achieve the desired temperature due to changes in the temperature. From such a viewpoint, it is common practice to perform so-called boiling point control for controlling the temperature in the reactor to around the boiling point of the reactant. The reason for this is that the change in temperature across the boiling point requires the transfer of heat of vaporization, so that the boiling point control has the advantage of stabilizing the temperature.

An example of such a boiling point control is described in, for example, JP-A-8-157505.

[0004]

However, the physical properties and properties of the reaction product, such as the molecular weight, depend on the reaction temperature. Therefore, the boiling point control has the advantage that temperature control is easy, but the physical properties of the product are uniquely determined, and there is a disadvantage that there is no selectivity in the physical properties or quality of the reaction product. Therefore, when it is necessary to generate a reactant having physical properties such as a specific range of molecular weight, there is a problem that it cannot be achieved by controlling the boiling point. However, when it is necessary to ensure specific quality or physical properties of the reaction product, the temperature condition must be set to a specific temperature range below the boiling point. However, to accurately control the temperature to the boiling point or lower, in the case of a batch reactor in which the reaction is performed while supplying the raw materials as described above, the reaction conditions, heat transfer conditions, heat capacity, and the like change. With technical difficulties.

[0005]

SUMMARY OF THE INVENTION The present invention has been made in view of the above circumstances, and is a relatively simple method for controlling the temperature of a batch reactor in which a reaction is performed while supplying raw materials. In addition, the object of the present invention is to obtain a reaction product of a desired quality by controlling the temperature in the reactor within a predetermined temperature range below the boiling point very accurately. The present invention is specified as follows to achieve the above object. That is, according to one feature of the present invention, in a batch reactor in which a reaction accompanied by heat of reaction is performed while supplying a raw material, a batch control in which the temperature in the reactor is controlled to a target temperature is provided. A temperature control device for a reaction type reactor, wherein a heat exchange amount calculating means for instantaneously obtaining a heat exchange amount between the inside and the outside of the reactor necessary for setting the temperature in the reactor to the target temperature, Heat medium supply means for supplying the heat medium to the outside of the reactor almost quantitatively so as to achieve the heat exchange amount calculated by the heat exchange amount calculation means, and suitable for achieving the heat exchange amount A supply temperature setting means for setting the supply temperature of the heat medium, and a supply temperature control means for controlling the temperature of the heat medium so as to achieve the supply temperature of the heat medium.

In a preferred aspect, the supply temperature control means controls a supply temperature of the heat medium by controlling a mixing ratio of heat mediums having different temperatures. Preferably, water is used as the heat medium. Further, the present invention can be suitably applied when the reaction performed in the reactor is a styrene polymerization reaction, in which case, the desired temperature is set by setting the target temperature to 40 to 80 ° C. A high quality reaction product can be obtained. The present invention is suitable for, but not limited to, the polymerization reaction of a styrene monomer. Monomers that can effectively apply the present invention to cause a polymerization reaction include α-methylstyrene and P-hydroxy. Styrene monomers such as styrene, (meth) acrylic acid, (meth)
Acrylic monomers such as methyl acrylate, ethyl (meth) acrylic terminal, butyl (meth) acrylate, and 2-ethylhexyl (meth) acrylate; vinyl monomers such as vinyl acetate and vinyl ene; isoprene and butadiene; There are olefin monomers and the like.

According to another feature of the present invention, in a batch reactor in which a reaction involving heat of reaction is carried out while supplying a raw material, the temperature in the reactor is set to a target temperature. A temperature controller for a batch-type reactor to be controlled, comprising: a reaction rate in the reactor, a material balance, and a heat balance, based on the inside of the reactor necessary to set the temperature in the reactor to the target temperature. Heat exchange amount calculation means for obtaining the heat exchange amount between the outside and the moment, and the heat medium outside the reactor so as to achieve the heat exchange amount calculated by the heat exchange amount calculation means. Heating medium supply means for supplying the heat medium supply temperature, supply temperature setting means for setting the supply temperature of the heat medium suitable for achieving the heat exchange amount, and a time change characteristic during the reaction of the set heat medium supply temperature Characteristic calculation means for determining Temperature control means for controlling the supply temperature of the heating medium so that the supply temperature of the heating medium changes according to the time-dependent characteristics of the supply temperature of the heating medium. An apparatus is provided.

[0008] According to a further feature of the present invention, in a batch reactor in which a reaction involving heat of reaction is carried out while supplying a raw material, a batch is controlled so that the temperature in the reactor becomes a target temperature. A method for controlling the temperature of a reactor, comprising: a reaction between an inside and an outside of a reactor necessary for setting a temperature in the reactor to the target temperature based on a reaction rate, a material balance, and a heat balance in the reactor. The time change characteristic of the heat exchange amount is obtained, and the heat exchange amount when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the calculated time change characteristic of the heat exchange amount is calculated. A time-dependent characteristic of the supply temperature of the heat medium that is preferable to achieve is obtained, and the supply temperature of the heat medium is changed so that the supply temperature of the heat medium varies according to the stored time-dependent characteristic of the supply temperature of the heat medium. With controlling procedure Temperature control method of a batch reactor, wherein the door is provided.

The method for controlling the temperature of a batch reactor according to the present invention can be executed by incorporating the temperature control procedure into a program using a computer and installing the program in the computer.
Therefore, according to still another feature of the present invention, there is provided a recording medium recording a temperature control program of a batch-type reactor adapted to cause a reaction involving reaction heat while supplying a raw material, Enter the target temperature in the reactor,
Input the supply conditions of the raw materials to be introduced into the reactor, input the reaction conditions of the reaction occurring in the reactor, and set the temperature between the inside and the outside of the reactor to set the temperature in the reactor to the target temperature. It is preferable to calculate the required heat exchange amount at, and to achieve the heat exchange amount when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the calculated heat exchange amount. A recording medium storing a temperature control program for calculating a supply temperature of the heat medium and outputting a temperature control signal for achieving the calculated heat medium supply temperature.

Further, from another viewpoint, the program can be configured with different contents. In this case, the temperature control of the batch-type reactor is designed so that the reaction accompanied by the heat of reaction is performed while the raw material is supplied. A recording medium on which a program is recorded, wherein a target temperature in the reactor during the reaction is inputted, a feed rate of the raw material introduced into the reactor is inputted, and a reaction condition of the reaction occurring in the reactor is inputted. Calculate the material balance in the reactor that changes every moment, calculate the heat balance in the reactor that change every moment, and set the temperature inside the reactor that changes every moment to the target temperature to obtain the target temperature. Calculate the required amount of heat exchange between the outside and the outside, the amount of heat exchange when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the calculated amount of heat exchange. Suitable to achieve The supply temperature of the heat medium is calculated, and the time-dependent change characteristic of the supply temperature of the heat medium is obtained by storing the calculation results of the supply temperature, and the supply temperature of the heat medium during the reaction is calculated according to the time change characteristic. A recording medium recording a temperature control program characterized by outputting a supply temperature control signal of a heat medium so as to change is provided.

In this case, preferably, the reaction conditions include at least a reaction rate and a reaction heat.

[0012]

DESCRIPTION OF THE PREFERRED EMBODIMENTS In the practice of the present invention, the temperature of a reactor is controlled in advance by a heating medium, preferably water, so that a target temperature is near. In this case, the raw material is supplied into the reactor at a predetermined supply rate, and the reaction is started. In the case of an exothermic reaction, heat of reaction is generated in the reaction, and the heat of reaction is removed by heat conduction through a wall surface of the reactor by heat exchange with a heat medium supplied to the outside of the reactor. The amount of heat to be removed depends on the heat of reaction, the feed rate of the raw material,
It is calculated by calculating the material balance and heat balance in the reactor from the reaction speed, reaction temperature and the like. In this case, in the batch type reactor to which the present invention is applied, since the reaction is performed while supplying the raw materials, the reaction conditions, the heat transfer conditions, the heat capacity, and the like change every moment.

Therefore, the condition for controlling the internal temperature of the reactor to be constant, that is, the amount of heat exchange between the inside and the outside of the reactor changes every moment. In the present invention, the amount of heat exchange is sequentially calculated, and the amount of heat exchange is achieved by a heat medium supplied to the outside of the reactor to control the temperature in the reactor to a predetermined temperature equal to or lower than the boiling point. Thus, a reaction product of desired quality is produced. For this reason, the feature of the present invention is that the heat exchange with the inside of the reactor is performed by keeping the supply amount of the heat medium constant and controlling only the supply temperature of the heat medium. That is, the present invention is characterized in that the temperature inside the reactor is controlled to the target temperature by controlling only the temperature conditions of the heating medium supplied to the outside of the reactor, whereby the control variable is controlled. Since one reactor is used, the temperature of the reactor can be easily and stably adjusted to a predetermined temperature equal to or lower than the boiling point.

In this case, each time the reaction is carried out, the heat exchange amount is calculated, the supply temperature of the heat medium corresponding thereto is calculated, and based on this, the heat medium is controlled while controlling the supply temperature of the heat medium. It may be supplied to the outer surface of the reactor. However, this method has an inconvenience that a calculation must be performed each time during the reaction. As another method, by determining the raw material supply amount, the time change characteristic of the heat exchange amount from the start of the raw material introduction or the start of the reaction to the end of the raw material introduction or the end of the reaction can be calculated in advance. The characteristics are obtained by calculation, the time-temperature characteristics of the supply temperature of the heat medium corresponding to the time-change characteristics are calculated and stored in advance, and the supply of the heat medium is controlled so as to obtain the characteristics. You may. Therefore, according to the present invention, since the temperature control of the reactor can be achieved by managing only the supply temperature of the heating medium, it is necessary to control the supply of the heating medium based on the temperature measurement result inside the reactor. Also in that there is no control, control becomes easier as compared with the conventional one.

[0015]

An embodiment of the present invention will be described with reference to the drawings. Referring to FIG. 1, there is shown a block diagram of a polymerization system when the present invention is used in a polymerization reaction for polymerizing a styrenic polymer. The system in this example is
A reactor, that is, a polymerization tank for supplying a styrene monomer to cause a polymerization reaction to produce polystyrene is provided. In the polymerization tank 1, a rotating shaft 2 is attached so as to hang down from the ceiling wall of the polymerization tank into the raw material mixture, and a stirrer 4 having a stirring blade 3 extending perpendicularly from the rotating shaft 2 is provided. The temperature in the polymerization tank of this example is controlled so as to maintain a target temperature of 65 ° C. throughout the reaction. For this purpose, a cooling jacket 5 is provided outside the polymerization tank so as to cover the heat affected zone of the polymerization tank. Cooling water as a heat medium circulates in the cooling jacket 5 and exchanges heat with the raw material mixture inside through the wall of the polymerization tank. The polymerization tank of this example is provided with a cooling water supply system for supplying the cooling water controlled to the predetermined temperature to the cooling jacket.

In order to circulate the cooling water set at a predetermined supply temperature to the cooling jacket 5 of the polymerization tank 1, the cooling water supply system is provided with a cooling water circulation pipe 6 and circulates the cooling water. Cooling water circulation pump 7 is installed. In the cooling water supply system of the present example, the cooling water circulation system includes a hot water tank 8 and a cold water tank 9 for storing the cooling water at two different temperatures. The hot water tank 8 stores hot water of about 70 ° C., and the cold water tank 9 stores cold water of about 10 ° C. Hot water tank 8
A hot water supply pump 11 is connected to a hot water supply pipe 10 from the tank, and a cold water supply pump 13 is connected to a cold water supply pipe 12 from the cold water tank 9.
Are respectively provided. Further, the apparatus of this example is provided with a cooler 14 for performing heat exchange with cooling water, and a re-cooling water pipe 15 to the cooler 14 is used to circulate cold water to the cooler 14. Is provided. The cooling water circulation pipe 6 has a temperature sensor 1 for detecting the temperature of the cooling water supplied into the cooling jacket 5.
7 is provided, and a control valve 18 capable of adjusting the flow rate is provided in the cold water pipe 12. Further, a cooling water return pipe 19 is connected to the cooling water circulation pipe 6, and the cooling water circulating through the cooling jacket 5 and exchanging heat by the amount flowing into the cooling water circulation pipe 6 via the control valve 18. The cooling water from the pipe 6 is returned to the cooling water tank 9.

The cooling water return pipe 19 has a three-way valve 20
The cooling water circulation pipe 6 is provided through a pipe 20.
Can be returned to the hot water tank 8. Further, the hot water supply pipe is connected to the cold water pipe 12 via another three-way valve 22, so that the supply of hot water or cold water to the cooling water circulation pipe 6 can be selected. The detection value of the temperature sensor 17 is input to an electronic control unit (ECU) 23 which is preferably configured using a computer.
Outputs a command signal to the control valve 18 based on the detected value so that the control valve 18 has a predetermined opening degree.

The ECU 23 has a preset polymerization tank 1.
Target reaction temperature (65 ° C. in this example) and feed rate of raw material (styrene monomer in this example) (300 kg / hr in this example)
), The overall heat transfer coefficient U of the polymerization tank 1, 300 in this example (Kca
l / m ² hr ℃) and temperature sensor 17, which detects the supply temperature of cooling water to the cooling jacket 5.
During operation, information such as a temperature sensor 24 for detecting the temperature in the polymerization tank 1 and a temperature sensor 25 for detecting the temperature of the cooling water at the outlet from the cooling jacket 5 is input. In accordance with a predetermined calculation program, the material balance, heat balance, heat exchange amount, and the like in the polymerization tank 1 are calculated, and the cooling water supply temperature to be supplied to the cooling jacket 5 is calculated. In this example, the time change characteristic of the cooling water supply temperature is calculated by the program from the start of the reaction to the end of the reaction. In the control of this embodiment, the ECU 23 adjusts the opening of the control valve 18 so that the temperature of the temperature sensor 17 attached to the cooling water circulation pipe 6 changes according to the time change characteristic of the cooling water supply temperature. The temperature of the cooling water supplied through the cooling water circulation pipe 6 is controlled.

As described above, the amount of water circulating through the cooling water circulation pipe 6 depends on the discharge capacity of the cooling water circulation pump 7 and is constant (7.5 m ³ / hr in this example). Hereinafter, an example of temperature control according to an embodiment of the present invention will be described with reference to FIG. The polymerization tank 1 used in the styrene polymerization operation of this example is 5.0 KL, and an organic solvent and a catalyst are charged into the polymerization tank 1 prior to polymerization.
In this example, 1,2-dichloroethane 1 was used as the organic solvent.
500 kg, 1.5 kg of tin tetrachloride as a catalyst are charged,
Further, 400 g of water is added and stirred for 30 minutes. Next, the ECU 23 is started, and first, a predetermined condition is read (step S1). These conditions include the raw material supply amount, reaction rate, overall heat transfer coefficient, target temperature, and the like. And
The ECU 23 outputs a control signal to the control valve 18 and activates the cooling water circulation pump to circulate the cooling water through the cooling jacket 5. Thereby, the cooling water is supplied to the cooling jacket 5 through the cooling water circulation pipe 6 (Step S2). At this time, the three-way valve 22 is controlled so as to pass only hot water (70 ° C.) from the hot water tank 8.
As a result, only the hot water from the hot water tank 8 passes through the cooling water circulation pipe 6 and is introduced into the cooling jacket 5. Thereby, the internal temperature of the polymerization tank 1 rises rapidly. EC
U23 is a temperature sensor 24 for detecting the temperature in the polymerization tank 1.
The temperature in the polymerization tank 1 is set to a predetermined temperature (65
° C) is reached (step S3), and when the temperature reaches the predetermined temperature, the predetermined speed (3
The supply is started at 00 kg / hr (step S4). Next, the ECU 23 calculates, from the various kinds of information read in step S1, the amount of heat exchanged which changes momentarily during the reaction, that is, the supply temperature of the cooling water when the supply amount of the cooling water is constant. Is achieved, a control signal for controlling the opening of the control valve 18 is output (steps S5, S6 and S7).

This procedure is not limited to this, but is performed as follows in this example. That is, in calculating the supply temperature of the cooling water, the ECU 23 calculates the supply temperature of the cooling water by calculating the heat balance in the cooling jacket using the polymerization rate equation, the material balance, the equation representing the polymerization heat generation rate, and the like. . r = K * Ci * Cm ² (Polymerization rate formula: first order for catalyst concentration, second order reaction for monomer concentration) where K: reaction rate constant Ci: catalyst concentration (mol / l) Cm: monomer concentration ( mol / l) Cm = v * t * (1-Xm) / V where, v: monomer dropping rate (mol / min) Xm:. monomer reaction rate V: reaction volume after t minutes (l) V ₀ : Initial value Ci = S / V where S: catalyst addition amount (mol / l) Xm / dt = r * V / (v * t) -Xm / t (1) dQ / dt = v * Hp * (−Rm) (2) where, Hp: heat of polymerization generation (kcal / kg) dQ / dt−v * Cp (65−T) = A * U * ΔT (heat transfer between inside and outside of the reactor) (3) where ΔT = (65-ti)-(65-to)) / log ((65-ti) / (65-to))
(Logarithmic mean temperature difference) ti: Cooling water supply (cooling jacket inlet) temperature to: Cooling water discharge (cooling jacket outlet) Temperature A: Heat transfer area (cooling jacket area) Cp: Heat capacity of raw material monomer (kcal / m ² · ° C) A * U * ΔT = Wc * (ti-to) (4) where U: overall heat transfer coefficient (Kcal / m ² hr ° C.) Then, equation (1) is calculated using the Runge-Kutta method. The relationship between the time and the amount of reacted monomer was determined, and the cooling water supply (cooling jacket inlet) temperature ti was calculated using (2) to (4).

FIG. 3 shows the time-dependent characteristics of the obtained cooling water supply temperature ti. Depending on the value of the overall heat transfer coefficient U, the time change characteristics are different as shown by A, B, and C, but the tendency is the same. If the overall heat transfer coefficient U is high, the heat transfer efficiency is good, so that the cooling water supply temperature can be set high. The broken line D is the time change characteristic of the calorific value of the polymerization reaction in the reactor. As shown, at the beginning of the reaction,
The cooling water supply temperature is high and drops rapidly over time. The reason for this is that, at the very beginning of the reaction, the amount of heat generated by the polymerization reaction is small and the amount to be removed outside the reactor is small. In addition, it means that the heat transfer area is relatively large with respect to the amount of the contents consisting of the inner raw material, the solvent, and the catalyst,
This means that in the initial stage of the reaction, the cooling capacity is relatively large, and it is desirable not to supply cooling water having a suddenly low temperature.

However, after that, the polymerization reaction is rapidly activated and the calorific value due to the polymerization is rapidly increased (the time range of points d1 to d2 in the figure). It is necessary to increase the cooling capacity by rapidly lowering the cooling capacity (time range around points a1 to a2, b1 to b2, c1 to c2 in the figure). Thereafter, the supply temperature of the cooling water is relatively slowly increased. During this period, the heat of the polymerization reaction is almost constant and stably changes (d2 to d3 in the figure). Then, when the supply of the raw material is stopped at the point d3, the heat of the polymerization reaction sharply decreases. Therefore, the supply temperature of the cooling water sharply increases (time range after points a3, b3, and c3). The ECU 23 controls the temperature of the cooling water supplied to the cooling jacket 5 by adjusting the opening of the control valve 18 so that the supply temperature of the cooling water changes over time as shown in FIG.

In this case, the opening degree of the control valve 18 is controlled so that the cooling water supply temperature is within a predetermined range, for example, ± 2 ° C. with respect to the target temperature (65 ° C.) (step S8). Then, when the raw material charged into the reactor reaches a predetermined target value, the supply of the raw material is stopped. FIGS. 4 and 5 show the results of actually performing the polymerization reaction according to the above control program. FIG. 4 shows that the overall heat transfer coefficient U is 2
For 80 (Kcal / m ² hr ° C), the supply temperature is controlled by controlling the opening of the control valve 18 in accordance with the time change characteristic of the cooling water supply temperature obtained in the above procedure. 17 is a plot of 17 outputs. FIG. 5 shows that the temperature in the polymerization tank 1 is measured by the temperature sensor 2.
4 is plotted. As shown in the results of FIG. 5, by controlling the opening degree of the control valve 18 in accordance with the time change characteristic of the supply temperature of the cooling water obtained by the procedure according to the present invention, the temperature in the polymerization tank 1 is set to approximately the target value of 65. It can be controlled accurately to around ° C. The properties of the resulting styrene polymer as a polymerization product were uniform and favorable. For example, according to the above control of this example, the average molecular weight of the produced styrene polymer is 10500 molecular weight distribution 2.4 and the conversion is 98.7%.
The product in the boiling point control shown in FIG.
Very high molecular weights can be obtained, while having an average molecular weight of 000. This difference in molecular weight relates to the difference in quality in the subsequent steps and is extremely important. As described above, the temperature of the inside of the polymerization tank 1 can be easily controlled to an arbitrary temperature range equal to or lower than the boiling point by the procedure of the present example, so that a product having desired properties can be obtained. Example 2 The same operation as in Example 1 was performed except that the supply temperature of the cooling water for setting the target polymerization temperature to 57 ° C. was changed as shown in FIG.

As shown in FIG.
The temperature was controlled constant. At this time, the molecular weight of the polymerization reaction product was 15,000 in weight average molecular weight and molecular weight distribution 2.
6. The reaction rate was 98.0%.

[0025]

As described above, according to the present invention, in the temperature control of a batch-type reactor in which a reaction is performed while supplying a raw material, a relatively simple configuration in which only the supply temperature of a heat medium is controlled, Reliable temperature control can be performed. In particular, in the present invention, since any environmental temperature below the boiling point corresponding to the desired physical properties of the product can be set to the target temperature, there is an effect that a good quality product can be easily obtained. Things.

[Brief description of the drawings]

FIG. 1 is a schematic configuration diagram of a styrene polymerization reaction system according to one embodiment of the present invention;

FIG. 2 is a control flowchart of U value control according to one embodiment of the present invention;

FIG. 3 is a graph showing a time change characteristic of a supply temperature of cooling water according to one embodiment of the present invention;

FIG. 4 is a graph showing an example of controlling the supply temperature of cooling water according to one embodiment of the present invention;

FIG. 5 is a graph showing a temperature change result in a polymerization tank when the supply temperature is controlled in FIG. 4;

FIG. 6 is a graph showing an example of controlling the supply temperature of cooling water according to another embodiment of the present invention;

FIG. 7 is a graph showing a temperature change in a polymerization tank in control according to another embodiment of the present invention.

[Description of sign]

 DESCRIPTION OF SYMBOLS 1 Styrene polymerization tank 4 Stirrer 5 Cooling jacket 6 Cooling water circulation pipe 7 Cooling water circulation pump 8 Hot water tank 9 Cold water tank 10 Hot water supply pipe 11 Hot water supply pump 12 Cold water supply pipe 13 Cold water supply pump 14 Cooler 15 Re-cooled water pipe 16 Cold water circulation pump 17 Temperature sensor 18 Control valve 19 Cooling water return pipe 20 Three-way valve 22 Three-way valve 23 Electronic control unit (ECU).

Claims (9)

[Claims] 1. A batch-type reactor in which a reaction involving heat of reaction is carried out while supplying a raw material, a temperature control device for the batch-type reactor for controlling the temperature in the reactor to a target temperature. A heat exchange amount calculating means for momentarily obtaining a heat exchange amount between the inside and the outside of the reactor necessary for setting the temperature in the reactor to the target temperature, and the heat exchange amount calculating means. Heating medium supply means for supplying the heat medium to the outside of the reactor almost quantitatively so as to achieve the calculated heat exchange amount, and a supply temperature of a heat medium suitable for achieving the heat exchange amount. A temperature control device for a batch reactor, comprising: a supply temperature setting means for setting; and a supply temperature control means for controlling a temperature of the heat medium so as to achieve a supply temperature of the heat medium. 2. The temperature control device according to claim 1, wherein the supply temperature control means controls a supply temperature of the heat medium by controlling a mixing ratio of heat mediums having different temperatures. . 3. The control device according to claim 1, wherein the heat medium is water. 4. The temperature control device according to claim 1, wherein the reaction performed in the reactor is a styrene polymerization reaction, and the target temperature is 40 to 80 ° C. 5. A batch-type reactor temperature control device for controlling a temperature in a batch-type reactor to a target temperature in a batch-type reactor in which a reaction involving heat of reaction is performed while supplying raw materials. In some cases, the amount of heat exchange between the inside and the outside of the reactor necessary for setting the temperature in the reactor to the target temperature is sometimes determined based on the reaction rate in the reactor, the material balance, and the heat balance. Heat exchange amount calculating means to be determined every moment; heat medium supply means for supplying the heat medium to the outside of the reactor almost quantitatively so as to achieve the heat exchange amount calculated by the heat exchange amount calculating means; Supply temperature setting means for setting a supply temperature of the heat medium suitable for achieving a heat exchange amount; characteristic calculation means for obtaining a time-change characteristic of the set heat medium supply temperature during a reaction; Change of the supply temperature of the heated heat medium Temperature control apparatus of a batch type reactor, characterized in that a supply temperature control means for controlling the supply temperature of the heat medium so that the supply temperature of the heat medium changes according to the characteristic. 6. A temperature control method for a batch-type reactor in which a reaction involving heat of reaction is performed while supplying a raw material, so that the temperature in the reactor is controlled to a target temperature. Wherein the time change of the amount of heat exchange between the inside and the outside of the reactor necessary for setting the temperature inside the reactor to the target temperature based on the reaction rate, the material balance, and the heat balance inside the reactor. The characteristics are obtained, and it is preferable to achieve the heat exchange amount when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the calculated time change characteristic of the heat exchange amount. Obtaining a time change characteristic of the supply temperature of the heat medium, controlling the supply temperature of the heat medium so that the supply temperature of the heat medium changes according to the time change characteristic of the supply temperature of the stored heat medium. A batch type counter Temperature control method of reactor. 7. A recording medium for recording a temperature control program for a batch-type reactor in which a reaction involving heat of reaction is carried out while supplying a raw material, wherein a target temperature in the reactor during the reaction is inputted. Then, input the supply conditions of the raw materials to be introduced into the reactor, input the reaction conditions of the reaction occurring in the reactor, and connect the inside and outside of the reactor with the target to set the temperature in the reactor to the target temperature. Calculating the amount of heat exchange required between, and in order to achieve the heat exchange amount when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the calculated heat exchange amount. A recording medium storing a temperature control program, wherein the temperature control program calculates a supply temperature of the heat medium, and outputs a temperature control signal for achieving the calculated heat medium supply temperature. 8. A recording medium for recording a temperature control program for a batch-type reactor in which a reaction involving reaction heat is performed while supplying raw materials, wherein a target temperature in the reactor during the reaction is inputted. Then, input the feed rate of the raw material introduced into the reactor, input the reaction conditions of the reaction occurring in the reactor, calculate the material balance in the reactor that changes every moment, and calculate the reactor that changes every moment. Calculate the heat balance in the reactor, calculate the amount of heat exchange required between the inside and the outside of the reactor in order to set the temperature in the reactor that changes every moment to the target temperature, and calculate the heat exchange Calculating the supply temperature of the heat medium suitable for achieving the heat exchange amount when the heat medium is supplied almost quantitatively to the outside of the reactor so as to achieve the amount, and calculating the supply temperature Remember each result Therefore, a temperature control program is characterized in that a time change characteristic of the supply temperature of the heat medium is obtained, and a supply temperature control signal of the heat medium is output so that the supply temperature of the heat medium during the reaction changes according to the time change characteristic. Recording medium on which is recorded. 9. The recording medium according to claim 8, wherein the reaction conditions include at least a reaction rate and a heat of reaction.