JP3189332B2 - Polymerization reaction operation support equipment for polyolefin production - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus for supporting a polymerization reaction in the production of polyolefin. Specifically, in the presence of hydrogen using a Ziegler-based catalyst, a Philips-based catalyst, etc., in the presence of hydrogen, when polymerizing the olefin in the polymerization zone, the physical properties of the polyolefin obtained by the polymerization reaction, particularly the melt flow index MFR value, were measured. The measured values and the operating data of the reaction conditions are taken into a computer, the processing is performed to estimate the reaction state, and the MF of the polyolefin to be produced in the future reactor based on the estimated value.
An operation for producing a polyolefin having a predetermined MFR value by predicting a change in the R value, calculating an amount of change in operating conditions by comparing the predicted value with a target value, and changing the operating conditions based on the calculated amount. It relates to a support device.

[0002]

2. Description of the Related Art Hitherto, polyolefins have been molded by various molding methods and used for various purposes. Depending on these molding methods and applications, it is desired that the polyolefin has various physical properties, particularly a melt flow rate (melt flow index; referred to as “MFR” in this specification) and a density. Generally, to adjust these properties,
There are known methods for changing the type, composition, amount, etc. of the catalyst and changing the polymerization conditions.

In order to produce a polyolefin on an industrial scale, a predetermined amount of a catalyst and a cocatalyst, a predetermined amount of an olefin, a predetermined amount of hydrogen, and a solvent are placed in a polymerization zone maintained at a predetermined temperature. The feed is run under conditions such that a polyolefin having a predetermined specification, ie, a predetermined MFR and density, is continuously produced.

[0004] However, even if continuous polymerization is carried out under the conditions where the feed rates are kept constant as described above, it is difficult to keep the state in the polymerization zone constant. For this reason, it is almost impossible to produce a polyolefin having a predetermined physical property specification at a constant production amount. That is, the olefin concentration in the polymerization zone changes due to a minute change in the catalyst or a change in the activity due to the uncertain disturbance. For example, when the activity of the catalyst decreases, the olefin concentration in the zone increases, the ratio of the concentration of hydrogen and the olefin, which are molecular weight regulators, decreases, and the MFR of the polyolefin formed decreases. . Frequent minute disturbances for which the reason is not clear often occur, which changes the olefin concentration in the polymerization zone and the physical properties of the resulting polyolefin, especially the MFR
And the density and the like will fluctuate.

Conventionally, various methods for improving such a problem have been proposed. For example, there are the following methods. A method for measuring the olefin concentration and the hydrogen gas concentration in the liquid phase portion of a polymerization reactor (US Pat. No. 3,835,106)
issue). A method for monitoring the polymerization reaction system and measuring the pressure to homogenize the composition of the ethylene copolymer as the final product (U
SP 3, 691, 142). A method for monitoring the ethylene and hydrogen concentrations in the gas phase or liquid phase of a polymerization reactor, incorporating this into a control system using a computer, and controlling the ethylene and / or hydrogen supply amounts (US Pat. No. 4,469,853, 1962-25
0010).

[0006]

SUMMARY OF THE INVENTION Among the above conventional methods,
However, the method (1) has a problem that the polymerization reaction progresses until the sample is collected from the reactor and the state in the reaction system cannot be accurately grasped.

Further, the method of the present invention is characterized in that desired physical properties, particularly MF
It is not a suitable technique for producing polyethylene having R and / or density.

In the method of (1), when a minute disturbance occurs in the polymerization zone, the reaction state changes. Therefore, it is only necessary to control the ethylene and hydrogen concentrations in the gas phase or liquid phase to a predetermined amount. It is difficult to obtain a polyolefin having the same physical properties (eg, MFR).

An object of the present invention is to solve the above-mentioned conventional problems and to provide a polymerization reaction operation support device for producing a polyolefin capable of obtaining a polyolefin having a predetermined MFR value stably and reliably. .

[0010]

The apparatus for supporting the polymerization reaction for producing a polyolefin according to the present invention is characterized in that an olefin is polymerized in a polymerization zone in the presence of a catalyst and hydrogen to obtain a predetermined amount of M.
A polymerization reaction operation support device for producing a polyolefin having an FR, comprising: a process state detecting means for detecting a process state quantity representing a process state in a polymerization zone; and a M of a polyolefin product flowing out of the polymerization zone.
MFR measuring means for measuring FR, process state quantity and MF from the process state detecting means and MFR measuring means
A data storage means for taking in the R measurement values and accumulating the data in a time series; and a process state quantity and an MFR from the data storage means at a specified sampling period from a specified time in response to a start instruction. The measured values are extracted, and using the time series data, the following formulas (1) and (6)
Β-value calculating means for dynamically estimating the MFR of the polyolefin instantaneously generated in the polymerization zone by the arithmetic processing according to the equation, and calculating the β-value in the following equation (6) from the estimated value;
Using the β value calculated by the β value calculation calculating means and the current process state amount or process state change amount, the following (1)
By the calculation processing by the equation (6) and the equation (6), M
MFR prediction calculation means for predicting a change in FR value, and the MF
A process state target value calculating means for calculating a target value of the process state quantity in the overlapping zone by comparing the transition of the MFR value predicted by the R prediction calculating means with the target value of the MFR; It is characterized in that the set value of the process state quantity is changed based on the calculated process state target value.

[0011]

(Equation 2)

Code: G_L： Reactor liquid phase capacity C_P： Reactor polymer concentration F_P: Instantaneous reaction amount F_Ol： Olefin supply amount F_S： Solvent supply amount S_Ol: Amount of olefin dissolved in solvent MFR₁: Instantaneously generated MFR MFR₂： Reactor outlet MFR Y ： Power number log MFR₁ = Α₁ log (H₂/ Ol)_G + Α₂ log (Co / Ol)_G + Α₃ log (P_Ol) + Α_Four log (CE / P_Ol) + Α_Five log (T) + α₆ log (OMC / P_Ol) + Β (6) Code: (H₂/ Ol)_G: (Hydrogen / olefin) mole in gas phase
Ratio (Co / Ol)_G: In the gas phase (comonomer / olefin
) Molar ratio (P_Ol): Olefin partial pressure in gas phase (CE / P_Ol): Catalytic activity / olefin partial pressure CE = polymerization amount / catalyst feed amount T: polymerization temperature OMC: cocatalyst feed amount α₁~ Α ₆ :Empirically determined coefficients for each reaction conditionβ: Correction term to correct deviation of predicted value due to disturbance etc. In the present invention, the process state quantity is olefin, water
Supply of hydrogen, solvent, catalyst and co-catalyst,
Gas, hydrogen concentration, reaction pressure, liquid phase reaction temperature and liquid
It is operation data regarding the reaction condition of the surface height. That is, the book
The inventors have solved the above-mentioned problems of the prior art, and
The reaction state changes quickly even when the reaction state changes
Grasp, and polyolefins with the prescribed physical properties according to the state quantity
Of polyolefin that can be changed to reaction conditions to obtain olefin
As a result of intensive studies to provide a method,
Operating data and polyolefin obtained in the polymerization zone
The actual measured value of MFR of computer
Of the polyolefin instantaneously formed in the polymerization zone
MFR is dynamically and sequentially estimated, and based on the estimated value,
Of the MFR in the market, its predicted value and its target value
The target value of the reaction condition is calculated by comparison with
By changing the reaction conditions in the polymerization zone based on the standard values
Completed the present invention.
I came to.

Hereinafter, the present invention will be described in detail.

The catalyst used for producing the polyolefin according to the present invention includes a Ziegler catalyst, a Phillips catalyst and the like. An organic aluminum compound is used as a promoter. If desired, a third component such as an electron donating compound may be used.

As the solvent, inert hydrocarbon solvents such as aliphatic hydrocarbons such as hexane and heptane, aromatic hydrocarbons such as benzene, toluene and xylene, and alicyclic hydrocarbons such as cyclohexane and methylcyclohexane are used.

Examples of the olefin include α-olefins such as ethylene, propylene, butene-1, hexene-1, and 4-methylpentene-1. These olefins may be used alone or as a mixture of two or more olefins. For example, ethylene is used alone or as a mixture of ethylene and 30 mol% or less of other olefins based on ethylene.

The polymerization reaction of the olefin is carried out in the polymerization zone in the presence of an olefin, hydrogen, a catalyst and a cocatalyst, optionally a solvent,
The components and comonomers are supplied in predetermined amounts, usually 50 to 150
The reaction is carried out at a temperature of ° C., a pressure of 0.1 to 100 kg / cm ² G and a hydrogen / olefin molar ratio in the gas phase of 0.01 to 1000. Of course, the reaction conditions are appropriately selected within the above range according to the desired properties of the polyolefin.

Hereinafter, an embodiment of the driving support device of the present invention will be described in more detail with reference to the drawings. FIG. 1 is a block diagram of a polyolefin production process to which the driving support device of the present invention is applied.

In FIG. 1, a hydrogen supply line 2, an olefin supply line 3, a solvent supply line 4, a catalyst supply line 5, a promoter and a third component supply line 5 'are connected to a polymerization reactor 1, , An olefin, a solvent, a catalyst, a cocatalyst, a third component, and the like are continuously supplied in predetermined amounts according to the MFR of the polyolefin to be produced.

A liquid phase portion 1a and a gas phase portion 1b are formed in the polymerization reactor 1 by the above-mentioned feed, and the olefin is polymerized while being stirred by the stirrer 1c.

The produced polyolefin is continuously extracted from the polyolefin extraction line 6, supplied to a degassing tank or a gas separator 12, separated from unreacted gas from a pipe 12A, and then passed through a feed line 6A. The solvent is supplied to the solvent separator 13, and the solvent is separated from the pipe 13A. Next, it is supplied to the dryer (dryer) 14 via the feed line 6B, and is made into a dried polyolefin solid. This is supplied to the extruder 15 through the feed line 6C and pelletized,
Withdraw from polyolefin pellet extraction line 16.

In the present invention, the polyolefin extracted from the polymerization reactor 1, preferably, the polyolefin pellets extracted from the extraction line 16 is sampled from the sampling line 16 A at predetermined time intervals, and the sample is introduced into the MFR measuring device 17. The MFR of the polyolefin is measured. A signal based on this measured value (actually measured value) is input to the data storage unit 31 of the computer 30 (signal K ₁ ).

The above-mentioned hydrogen supply line 2, olefin supply line 3, and solvent supply line 4 have supply valves 2a, 3a, 4a for adjusting the respective supply amounts, and flow rate detectors 2b, for detecting the respective supply amounts. 3b, 4b are provided, and detection signals (K ₂ , K ₃ , K ₄ ) correlated with the flow rates from the flow rate detectors 2b, 3b, 4b are input to the data storage unit 31 of the computer 30. On the other hand, a control signal S from a control unit 36 of the computer 30 described later
The ₁ to S _4, the stroke of the catalyst supply pump 5a in order to change the olefin concentration and the hydrogen concentration to produce a polyolefin having a predetermined MFR, cocatalyst feed pump 5 '
The stroke of “a” and the opening degrees of the olefin supply valve 3a and the hydrogen supply valve 2a are controlled.

Further, a sampling line 7 is provided in the gas phase portion 1b of the polymerization reactor 1, and the gas in the gas phase portion 1b is led to an analyzer 8, for example, gas chromatography via an on-off valve 7a. The analyzer 8 measures the hydrogen concentration and the olefin concentration in the gas. A signal (K ₅ ) based on the hydrogen concentration and the olefin concentration measured by the analyzer 8 is also input to the data storage unit 31 of the computer 30.

Reference numerals 9 and 10 denote detectors for the pressure in the gas phase and the temperature in the liquid phase of the polymerization reactor 1, and detection signals (K) correlated with the pressure and temperature from the pressure detector 9 and the temperature detector 10, respectively. ₆ , K ₇ ) is also the data storage unit 31 of the computer 30.
Is input to

Reference numeral 11 denotes a supply line for supplying cooling water to the polymerization reactor 1. The supply line 11 is provided with a supply valve 11a for adjusting the supply amount and a flow rate detector 11b for detecting the supply amount. A detection signal (K ₈ ) correlated with the flow rate from 11b is input to the data storage unit 31 of the computer 30. The cooling water supply valve 11a is also the control signal S ₅ from the control unit 36 of the computer 30 to be described later, to produce a polyolefin having a predetermined MFR,
The opening is controlled to change the polymerization temperature.

Further, a solvent supply line 18 is connected to the degassing tank 12 for adjusting the slurry concentration. A supply valve 18a for adjusting the supply amount and a flow detector 18b for detecting the supply amount are provided. The detection signal (K ₉ ) correlated with the flow rate from the flow rate detector 18 b is
0 is input to the data storage unit 31.

A solvent supply line 20 is also connected to the solvent separator 13 for adjusting the slurry concentration.
A supply valve 20a for adjusting the supply amount and a flow detector 20b for detecting the supply amount are provided.
A detection signal (K ₁₀ ) correlated with the flow rate from the computer 30 is input to the data storage unit 31 of the computer 30.

The pipe 19A is a line for returning hot water to the cooling tower, and the pipe 19B is a line for circulating hot water.

As described above, in this embodiment, the process state quantity representing the process state in the polymerization reactor 1, that is, the supply amounts of the olefin, hydrogen, the solvent, the catalyst and the cocatalyst, the concentrations of the olefin and hydrogen in the gas phase, Signals K _{2 to} K _{8 obtained} by detecting operation data of reaction conditions such as pressure, reaction temperature of liquid phase part and liquid level in each process state detecting means, and MFR of polyolefin product extracted from polymerization reactor 1
Actually measured values (in the present invention, as shown in FIG. 1, a polyolefin pellet obtained through a degassing tank 12, a solvent separator 13, a drier 14, and an extruder 15 is converted into an MFR measuring device 17
It is desirable to use the MFR measured value measured in the above. ) Incorporating a signal K ₁ to the computer 30, and stores the data as the data storage unit 31 in time series data.

The computer 30 includes a data storage unit 31,
a display value calculation unit 32, an MFR prediction calculation unit 33, and a process state target value calculation unit 34;
5, a printer 37, and a reaction condition set value changing unit 38.

As described above, the driving support apparatus according to the present embodiment
Process state detecting means for transmitting detection signals K _{2 to} K ₁₀ ,
MFR measuring means for transmitting a detection signal K ₁ (MFR measuring instrument 17), the data storage unit (data storage unit 31), beta value calculating operation means (beta value calculating operation section 32), MFR prediction calculation means (MFR prediction computation unit 33), a process state target value calculating means (process state target value calculating unit 34). The operation of the driving support device will be described. When a start instruction is input from the outside (for example, input from the display 35), data of a sampling cycle specified from the specified time to the past, for example, data of the past 24 hours is obtained. 1
At each time period, data (detection signals K _{1 to} K ₁₀ ) of process state quantities and MFR measurement values are extracted from the data storage unit 31 as time-series data, and using this data, the β value calculation / The MFR of the polyolefin instantaneously generated in the polymerization zone is dynamically estimated by the arithmetic processing according to the equations (1) and (6), and β in the equation (6) is obtained from the estimated value.
Calculate the value.

Using the β value and the current process state amount or the change amount thereof, the MFR prediction operation unit 33 calculates the future (future) value of the MFR value in the future by the arithmetic processing according to the expressions (1) and (6). The transition is predicted, and the predicted value is displayed as a table or a graph, and the transition of the MFR value is printed out or displayed on a CRT screen.

Using the transition of the MFR value and the target value of the MFR, the process state target value calculation unit 34 compares the two, and changes the process state quantity until the transition of the predicted MFR value matches the target value. Then, the prediction of the transition of the MFR value is repeated by a trial and error method by the arithmetic processing according to the following equations (1) and (6) to calculate the target value of the process state quantity.

The process of the polymerization reactor 1 is performed based on the process state target value calculated by the process state target value calculator 34, for example, the hydrogen / olefin molar ratio in the gas phase, the polymerization temperature, and the cocatalyst concentration in the liquid phase. Output control signals S _{1 to} S ₅ to change the state quantity, for example, the supply amount of olefin, hydrogen, catalyst or cocatalyst, or the set value of polymerization temperature,
A polyolefin having a predetermined MFR value is produced.

Hereinafter, the MFR of the polyolefin instantaneously produced in the polymerization reactor is calculated by an arithmetic process based on a prediction model using the measured MFR value of the polyolefin produced in the polymerization reactor 1 and the operation data of the polymerization reaction conditions. The estimation method will be described in detail.

Each symbol indicates the following. G _L1 : Liquid phase capacity of polymerization reactor 1 G _L2 : Liquid phase capacity of degassing tank 12 _GL3 : Liquid phase capacity of solvent separator 13 C _P1 : Polymer concentration of polymerization reactor 1 C _P2 : Degassing tank 12 C _P3 : Polymer concentration of solvent separator 13 F _P1 : Instantaneous reaction amount of polymerization reactor 1 F _Ol1 : Olefin supply amount of polymerization reactor 1 F _S1 : Solvent supply amount of polymerization reactor 1 F _S2 : Desorption Amount of solvent supplied to gas tank 12 F _S3 : Amount of solvent supplied to solvent separator 13 S _Ol1 : Amount of olefin dissolved in solvent of polymerization reactor 1 MFR ₁ : Instantaneously generated MFR of polymerization reactor 1 MFR MFR ₂ : Polymerization reactor MFR at 1 outlet MFR ₃ : MFR at outlet of degassing tank 12 MFR ₄ : MFR at outlet of solvent separator 13 MFR ₅ : MFR at outlet of dryer 14 MFR ₆ : MFR at outlet of extruder 15 Y: Exponent L: Delay time k: Powder drop-off staff Number k = f (additive type and concentration, extruder specific energy, etc.) First, polymerization reactor 1, degassing tank 12, solvent separator 13,
M of polyolefin in dryer 14 and extruder 15
The material balance of the dynamic characteristic of FR is represented by the following prediction model equation.

(1) Polymerization reactor 1 During unsteady operation (when starting or stopping polymerization reaction, when disturbance occurs, or when changing polymerization reaction conditions, etc.)

[0039]

(Equation 3)

During normal operation (C _L1 , C _P1 , F _P1 , S
_Ol1 is constant)

[0041]

(Equation 4)

(2) Degassing tank 12 During unsteady operation

[0043]

(Equation 5)

During steady operation ( _GL2 and _CP2 are constant)

[0045]

(Equation 6)

(3) Solvent separator 13 During unsteady operation

[0047]

(Equation 7)

During normal operation

[0049]

(Equation 8)

(4) Dryer 14 MFR ₅ (t + L) = MFR ₄ (t) (4) (5) Extruder 15 MFR ₆ = k · MFR ₅ (5) Here, for example, an extruder The polyolefin pellets (granules) extracted from the sample No. 15 are sampled at predetermined time intervals, the MFR of the polyolefin is measured by the MFR measuring device 17, and the measured value MFR ₆ is used to calculate the equation (5) → the equation (4) → The MFR of the polyolefin generated instantaneously in the polymerization reactor 1 can be estimated by performing the sequential calculation based on the formula (3) → the formula (2) → the formula (1). This M
Calculating a β value from a FR estimates MFR ₁ and the following equation (6). (Each sign in the equation (6) is as described above.) Log MFR ₁ = α ₁ log (H ₂ / Ol) _G + α ₂ log (Co / Ol) _G + α ₃ log (P _Ol ) + α ₄ log (CE / P _Ol ) + α ₅ log (T) + α ₆ log (OMC / P _Ol ) + β (6) Next, the β value and the process state quantity of the polymerization reactor 1, that is,
Using the operation data of the reaction conditions or the change amount thereof, the MFR of the polyolefin to be generated in the polymerization reactor 1 in the future (future) by the arithmetic processing of the equation (6) → the equation (1)
Predict value transitions.

The predicted value of the transition of the MFR is compared with the target value of the MFR, and the process state quantity in the expression (6) is changed until the predicted value matches the target value. The prediction of the transition of the MFR value is repeated by a trial and error method by the arithmetic processing according to 1), and the target value of the process state quantity in the equation (6), in particular, the hydrogen / olefin molar ratio in the gas phase, the polymerization temperature, and the Calculate the target value of the promoter concentration.

Based on this target value, the control signals S _{1 to} S ₄ are output from the reaction condition set value changing unit 38 and the control unit 36 to supply the olefin, hydrogen, catalyst or co-catalyst in the polymerization reactor 1. Alternatively, a polyolefin having a predetermined MFR value can be produced by changing the set value of the polymerization temperature.

[0053]

As described above, in the driving support apparatus of the present invention, the above-mentioned signals input to the computer are subjected to arithmetic processing in the computer in accordance with a preset program, and the hydrogen content in the gas phase (1b in FIG. 1). Pressure, olefin partial pressure, hydrogen / olefin molar ratio, polyolefin polymerization amount in the polymerization reactor, polymer concentration, cocatalyst concentration, catalytic activity, etc., are calculated. The deviation is obtained by comparison and calculation processing with respective preset target values in order to manufacture the fuel cell, and for example, the hydrogen supply valve (2a in FIG. 1) is operated by a control signal based on the deviation to operate the above gas. The hydrogen concentration in the phase (1b) is adjusted, or the stroke of the olefin supply valve (3a) or the catalyst supply pump (5a) is operated. By controlling the olefin concentration in the phase (1b) or adjusting the hydrogen / olefin molar ratio in the gas phase to a predetermined value, the hydrogen concentration and the olefin concentration are adjusted so as to produce a polyolefin having a predetermined MFR. Control.

The required MFR can also be controlled by adjusting the cocatalyst concentration by operating the stroke of the cocatalyst supply pump (5'a) as necessary, or by changing the setting of the polymerization temperature. Can be produced.

Although the manner of changing the reaction conditions varies depending on the type of the brand of the polyolefin product, it is effective as an MFR control means for generally controlling the hydrogen / olefin molar ratio described above.

[0056]

The present invention will be described in more detail with reference to specific control examples.

Example 1 A polyolefin was produced using the apparatus shown in FIG. 1 according to the control method described above.

FIG. 2 is a diagram showing a future MFR performed by the driving support apparatus of the present invention shown in FIG.
6 is a graph showing a prediction result of the transition of the transition.

FIG. 3 shows a process state quantity (particularly, in this case, H in the gas phase portion ) for producing a polyolefin having a predetermined MFR (0.20 g / 10 min) based on the prediction result of the MFR transition shown in FIG. ₂ is a graph showing a change amount and a predicted result of a change in MFR based on the change amount.

FIG. 4 shows a predetermined MF based on these results.
It is a graph which shows transition of the actual measurement value of MFR, and the estimation value when adjustment of a process state quantity is performed at R (0.20 g / 10 minutes) .

As is apparent from FIG. 4, the estimated value of the MFR and the actually measured value are in good agreement, and the driving state support device of the present invention makes it possible to satisfactorily adjust the process state quantity.

[0062]

As described in detail above, according to the polymerization reaction operation support device for producing the polyolefin of the present invention,
An olefin is polymerized in a polymerization zone in the presence of a catalyst and hydrogen, whereby a polyolefin having a predetermined MFR can be produced reliably, stably and efficiently.

[Brief description of the drawings]

FIG. 1 is a block diagram of a polyolefin production process using a driving assistance device according to an embodiment of the present invention.

FIG. 2 is a graph showing a prediction result of a future transition of MFR, which is performed by the driving support device shown in FIG. 1 by a calculation process using a process state quantity and an actual measurement value of MFR at the present time.

FIG. 3 is a diagram showing a prediction result of a change in MFR shown in FIG. 2;
It is a graph which shows the process state quantity for manufacturing the polyolefin of predetermined | prescribed MFR, the change amount, and the prediction result of transition of MFR based on this change amount.

FIG. 4 is a graph showing measured values of MFR and transitions of the estimated values when the process state quantity is adjusted based on the results of FIGS.

[Explanation of symbols]

 REFERENCE SIGNS LIST 1 polymerization reactor 2 hydrogen supply line 3 olefin supply line 4 solvent supply line 5 catalyst supply line 6 polyolefin extraction line 7 sampling line 8 analyzer 12 degassing tank 13 solvent separator 14 dryer 15 extruder 17 MFR measuring device 30 Computer 31 Data storage unit 32 β value calculation unit 33 MFR prediction calculation unit 34 Process state target value calculation unit 36 Control unit 38 Reaction condition set value change unit

──────────────────────────────────────────────────続 き Continued on front page (58) Field surveyed (Int.Cl. ⁷ , DB name) C08F 2 / 00,2 / 01

Claims (1)

(57) [Claims] An olefin is polymerized in a polymerization zone in the presence of a catalyst and hydrogen to obtain a predetermined melt flow index (hereinafter referred to as "MFR").
Called. A polymerization reaction operation support device for producing a polyolefin having a process state detection means for detecting a process state quantity representing a process state in a polymerization zone; and measuring an MFR of a polyolefin product flowing out of the polymerization zone. MFR measurement means, data storage means for taking in the process state quantity and MFR measurement value from the process state detection means and the MFR measurement means, and accumulating the data in a time series, Then, the process state quantity and the MFR measurement value are extracted from the data storage means at the designated sampling period, and the time series data is used to calculate the process state quantity and the MFR using the following formulas (1) and (6). Instantaneous formation of polyolefin M
FR is dynamically estimated, and β in the following equation (6) is obtained from the estimated value.
Using the β value calculation means for calculating the value, the β value calculated by the β value calculation means, and the current process state amount or process state change amount (1)
By the calculation processing by the equation (6) and the equation (6), M
MFR prediction calculating means for predicting a change in FR value, and a change in MFR value and MF predicted by the MFR prediction calculating means
A process state target value calculating means for calculating a target value of the process state quantity in the polymerization zone by comparison with a target value of R; and a process state target value calculated by the process state target value calculating means. A polymerization reaction operation support device for producing a polyolefin, wherein a set value of the amount is changed. (Equation 1) Code: _{G L:} reactor liquid phase capacitance C _P: reactor polymer concentration F _P: instantaneous reaction volume F _Ol: olefin feed amount F _S: solvent feed rate S _Ol: olefin dissolved amount in the solvent MFR _1: moment generated MFR MFR ₂ : Reactor outlet MFR Y: Exponent log MFR ₁ = α ₁ log (H ₂ / Ol) _G + α ₂ log (Co / Ol) _G + α ₃ log (P _Ol ) + α ₄ log (CE / P _Ol ) + Α ₅ log (T) + α ₆ log (OMC / P _Ol ) + β (6) code: (H ₂ / O1) _G : (hydrogen / olefin) molar ratio in the gas phase (Co / O1) _G : (Comonomer / olefin) molar ratio in gas phase (P _Ol ): Partial pressure of olefin in gas phase (CE / P _Ol ): Catalytic activity / Partial pressure of olefin CE = polymerization amount / catalyst feed amount T: polymerization temperature OMC: cocatalyst feed rate alpha ₁ to? _6: coefficient determined empirically by the reaction conditions beta: due to disturbance or the like Correction term for correcting the deviation of Hakachi