JP6544271B2 - Temperature distribution control method and control device of vertical dry distillation furnace - Google Patents

Description

  The present invention relates to a temperature distribution control method and control device for a vertical carbon-distillation furnace.

  Coke production equipment that produces molded coke represented by ferrocoke is charged with undried carbon from the top of a vertical carbonization furnace, and the coal is subjected to preheating treatment, carbonization treatment, and cooling treatment. The molded coke is discharged from the lower part of the mold dry distillation furnace (see Patent Document 1). In such a coke production facility, the temperature history of the formed coal in the preheating treatment, the carbonization treatment, and the cooling treatment greatly affects the quality of the formed coke. Therefore, in the coke production facility, it is important to control the temperature distribution in the height direction of the vertical distillation-distillation furnace to an appropriate state.

  Specifically, in order to produce high-quality molded coke, it is desirable to hold the formed coal in a high temperature region (for example, 900 ° C. or more) for about 3 hours in order to perform sufficient dry distillation treatment on the formed coal. There are also restrictions on the temperature rise rate in the softening and melting region (for example, 300 to 500 ° C.) and the thermal stress concentration region (for example, around 600 ° C.). Furthermore, it is desirable from the viewpoint of quality variation reduction to make the temperature distribution as uniform as possible in the widthwise direction of the vertical distillation furnace.

JP, 2014-178049, A

  In the coke manufacturing facility described above, a plurality of tuyeres called a high temperature tuyere, a low temperature tuyere, an extraction tuyere, and a cooling tuyere are provided in order from the top of the furnace on the side wall of the vertical dry distillation furnace. And as an operation quantity for controlling temperature distribution of a vertical dry distillation furnace to a desired state, there are a flow rate and temperature of tuyere.

  However, since a plurality of tuyeres are juxtaposed in the vertical direction of the vertical distillation-distillation furnace, the operation influence of the tuyere flow rate and temperature propagates in the vertical direction, and there is a problem that the operation influence interferes with each other.

  The present invention has been made in view of the above circumstances, and provides a temperature distribution control method and control device of a vertical dry distillation furnace capable of suppressing interference of operation influence between a plurality of tuyeres in the vertical dry distillation furnace. With the goal.

  The temperature distribution control method of the vertical dry distillation furnace according to the present invention is estimated by the estimation step of estimating the current temperature distribution in the vertical dry distillation furnace using a physical model of the countercurrent heat exchange process, and the above estimation step It is assumed that the current temperature distribution is taken as an initial value, and the operating conditions of the vertical distillation-distillation furnace at the time of estimating the current temperature distribution remain constant from then on using the physical model. Predicting the temperature distribution in the future, calculating the degree of influence of the control variable on the respective manipulated variables of the plurality of tuyeres arranged in vertical and horizontal directions of the vertical dry distillation furnace, and calculating the degree of influence In order to calculate the manipulated variable for compensating the deviation between the target temperature distribution and the future temperature distribution predicted by the prediction step using the degree of influence calculated by the degree of influence calculation step, Characterized in that it comprises a manipulated variable determining step of determining a respective operation amount of from bottom to top stepwise the tuyere in the vertical direction.

  In the temperature distribution control method of a vertical dry distillation furnace according to the present invention, in the above invention, the operation amount determination step calculates a deviation between the target temperature distribution and the future temperature distribution, and the deviation calculation step It is preferable to include a calculation step of calculating the operation amount that minimizes the deviation using the deviation calculated by the step and the degree of influence calculated by the influence degree calculation step.

  In the temperature distribution control method of a vertical dry distillation furnace according to the present invention, in the above-mentioned invention, the deviation calculation step calculates an error between the current temperature distribution estimated in the estimation step and the actual measurement value, and uses the error It is preferable to include the step of calculating the deviation between the target temperature distribution and the future temperature distribution.

  In the temperature distribution control method of a vertical dry distillation furnace according to the present invention, in the above invention, a low temperature tuyere, a high temperature feather, provided in order from the furnace top to the furnace bottom in the vertical direction of the vertical dry distillation furnace as the tuyere Among the mouth, the extraction tuyere, and the cooling tuyere, the method further includes an equal amount control step of controlling the gas flow rate of the extraction tuyere and the gas flow rate of the cooling tuyere equally. A first determination step of determining the operation amount of the extraction tuyere and the cooling tuyere, a second determination step of determining the operation amount of the high-temperature tuyere, and the operation amount of the lower part by the second determination step It is preferable to include a third determination step of determining the operation amount of the low temperature tuyere using the determined operation amount of the high temperature tuyere.

  The temperature distribution control device of the vertical dry distillation furnace according to the present invention uses the physical model of the countercurrent heat exchange process, and is provided in the vertical dry distillation furnace in which a plurality of tuyeres are vertically and horizontally arranged in parallel. The operating condition of the vertical dry distillation furnace at the time of estimating the current temperature distribution with the current temperature distribution estimated by the estimating means as the initial value and estimating the current temperature distribution of the Predicting means for predicting future temperature distribution after a predetermined time using the physical model assuming that it is constant, and influence degree calculating means for calculating the degree of influence of control variables on each operation amount of the plurality of tuyeres And using the degree of influence calculated by the degree of influence calculation means to calculate the manipulated variable for compensating the deviation between the target temperature distribution and the future temperature distribution predicted by the prediction means. Vertically below Characterized in that it comprises a manipulated variable determining means for determining the respective amount of operation of stepwise the tuyeres to the upper, the.

  In the temperature distribution control device of a vertical dry distillation furnace according to the present invention, in the above invention, the operation amount determination means calculates a deviation between the target temperature distribution and the future temperature distribution; and the deviation calculation means It is preferable to have a calculation unit that calculates the operation amount that minimizes the deviation using the deviation calculated by the above and the degree of influence calculated by the influence degree calculation unit.

  In the temperature distribution control device of a vertical dry distillation furnace according to the present invention, in the above invention, the deviation calculating means calculates an error between the current temperature distribution estimated by the estimating means and the actual measurement value, and uses the error Preferably, the deviation between the target temperature distribution and the future temperature distribution is calculated.

  In the temperature distribution control device of a vertical dry distillation furnace according to the present invention, in the above invention, the tuyere is a low temperature tuyere, a high temperature, provided in order from the furnace top to the furnace bottom side in the vertical direction of the vertical dry distillation furnace. The apparatus further comprises equivalent control means including a tuyere, an extraction tuyere, and a cooling tuyere to control the gas flow rate of the extraction tuyere equal to the gas flow rate of the cooling tuyere, the operation amount determining means A first determining means for determining an operation amount of the extraction tuyere and the cooling tuyere, a second determining means for determining an operation amount of the high temperature tuyere, and an operation amount of the lower part by the second determining means It is preferable to have the 3rd determination means which determines the operation amount of the said low temperature tuyere using the operation amount of the said high temperature tuyere determined as these.

  According to the present invention, even in the case where a plurality of tuyeres are juxtaposed in the horizontal direction and the vertical direction of the vertical distillation distillation furnace, each operation amount is determined in consideration of the operation influence between the plurality of tuyeres Therefore, interference of the operation influence can be suppressed. Thereby, the temperature distribution of the vertical distillation-distillation furnace can be controlled to a desired state.

FIG. 1 is a view showing the coke production facility of the embodiment. FIG. 2 is a view showing the positions of the respective tuyeres of the vertical carbon-distillation furnace. FIG. 3 is a block diagram showing a temperature distribution control device of the embodiment. FIG. 4 is a flowchart showing the entire flow of the temperature distribution control method. FIG. 5 is a flowchart showing an example of the physical model calculation flow. FIG. 6 is a view showing a control zone of a vertical carbon-distillation furnace. FIG. 7 is a diagram showing the degree of influence on each control variable at the time of low temperature tuyere flow rate operation. FIG. 8 is a diagram showing the degree of influence on each control variable at the time of high temperature tuyere flow rate operation. FIG. 9 is a diagram showing the cooling tuyere flow rate and the influence on each control variable at the time of the extraction tuyere flow rate operation. FIG. 10 is a diagram for explaining the calculation flow of action optimization. FIG. 11A is a diagram showing the simulation result of the control amount at the time of disturbance occurrence regarding the solid specific heat. FIG. 11 (b) is a diagram showing simulation results of the manipulated variable at the time of occurrence of disturbance regarding solid specific heat.

  Hereinafter, the temperature distribution control method and control device of the vertical dry distillation furnace in the embodiment of the present invention will be specifically described.

[1. Configuration of Coke Production Facility]
FIG. 1 is a view showing the coke production facility of the embodiment. As shown in FIG. 1, the coke production facility 1 of the present embodiment is provided with a vertical carbon-distillation furnace 2 for producing a molded coke by dry-distilling a molded coal as a main component.

  The inside of the vertical dry distillation furnace 2 is separated in the height direction into a low temperature dry distillation zone, a high temperature dry distillation zone and a cooling zone, and the formed carbon is dry distilled by the low temperature dry distillation zone and the high temperature dry distillation zone, and the dry distillation is performed in the cooling zone Cool the coke. A low temperature tuyere 3a, a high temperature tuyere 3b, an extraction tuyere 3c, and a cooling tuyere 3d are provided on the side wall of the vertical dry distillation furnace 2 in order from the furnace top to the furnace bottom side.

  The low temperature tuyere 3a is provided between the low temperature dry distillation zone and the high temperature dry distillation zone. By blowing a low temperature gas from the low temperature tuyere 3a into the vertical dry distillation furnace 2, a low temperature dry distillation zone and a high temperature dry distillation zone are separated. The high temperature tuyere 3b is provided between the high temperature dry distillation zone and the cooling zone. By blowing a high temperature gas from the high temperature tuyere 3b, the high temperature dry distillation zone and the cooling zone are separated. The extraction tuyere 3c is provided in the cooling zone. The cooling tuyere 3 d is provided on the bottom side of the vertical carbon-distillation furnace 2. A cooling zone is created in the vertical dry distillation furnace 2 by the cooling gas blown into the vertical dry distillation furnace 2 from the cooling air inlet 3d, and a part of the gas in the cooling zone is dry vertical distillation from the extraction air inlet 3c. It is extracted outside the furnace 2.

  In addition, at the furnace top of the vertical dry distillation furnace 2, a furnace gas discharge port 4 for discharging the gas in the furnace is provided. The exhaust gas piping connected to the in-furnace gas outlet 4 includes a spray tower 5 as a first gas cooling device, a gas cooler 6 as a second gas cooling device, and dust in the in-furnace gas (mainly tar mist) An electric precipitator 7 is connected to remove the The furnace gas via the spray tower 5, the gas cooler 6, and the electrostatic precipitator 7 is recovered as a generated gas and is used as a fuel after purification and desulfurization. Furthermore, a part of the recovered generated gas is recycled to the low temperature gas, the high temperature gas, and the cooling gas blown into the vertical dry distillation furnace 2. The liquid component in the gas in the furnace is recovered by the spray tower 5 and the gas cooler 6, separated into an aquarium and tar, and stored in the tank for aquarium water 8a and the tank for tar 8b.

  Furthermore, a part of the recovered generated gas is recycled to the low temperature gas, the high temperature gas, and the cooling gas blown into the vertical dry distillation furnace 2. The generated gas (high temperature gas) heated by the high temperature gas heating furnace 9 is introduced to the high temperature tuyere 3 b and blown into the vertical dry distillation furnace 2 from the high temperature tuyere 3 b. Further, the generated gas heated by the low temperature gas heating furnace 10 is guided to the low temperature tuyere 3 a through the ejector 11 and blown into the vertical dry distillation furnace 2 from the low temperature tuyere 3 a. At that time, the ejector 11 is driven by the gas flowing from the low temperature gas heating furnace 10 to the low temperature tuyere 3a, and the gas used for the coke cooling is sucked in the cooling zone. That is, together with the generated gas heated by the low temperature gas heating furnace 10, the gas sucked from the cooling zone by the ejector 11 is blown as a low temperature gas from the low temperature tuyere 3a into the vertical dry distillation furnace 2. In addition, a part of the generated gas recovered from the furnace top is led to the cooling vane 3d without heating, and blown into the vertical dry distillation furnace 2 from the cooling vane 3d as a cooling gas.

  In the vicinity of the furnace top of the vertical carbon-distillation furnace 2, a loading port 12 for molded coal is provided, and at the furnace bottom of the vertical carbon-distillation furnace 2, a discharge port 13 for cutting out molded coke is provided. Charcoal degassed in the vertical dry distillation furnace 2 is charged from the inlet 12 and filled in the cylindrical dry distillation furnace 2, and corked coke cut out from the discharge port 13 is cut out at a constant speed. As a result, the coal briquettes stay in the vertical dry distillation furnace 2 for a predetermined time.

  FIG. 2 is a view showing the positions of the respective tuyeres 3 a to 3 d of the vertical distillation-type distillation furnace 2. The vertical dry distillation furnace 2 has a substantially rectangular parallelepiped structure having a predetermined height, and is disposed so that the longitudinal direction is horizontal, and the furnace width direction is the depth direction. The respective tuyeres 3a to 3d are provided at different positions in the height direction of the vertical distillation-type distillation furnace 2, and a plurality of them are provided side by side in the longitudinal direction. In the example shown in FIG. 2, six tuyeres 3a to 3d are arranged in the longitudinal direction.

[2. Control device]
FIG. 3 is a block diagram showing the temperature distribution control device 100 according to the embodiment. The temperature distribution control device 100 includes an information processing device 101, an input device 102, and an output device 103. The information processing apparatus 101 is configured by a known information processing apparatus such as a personal computer, and includes a RAM 111, a ROM 112, and a CPU 113. The RAM 111 temporarily stores control programs and control data regarding processing executed by the CPU 113, and functions as a working area of the CPU 113.

  The ROM 112 stores an estimation program 112 a and a control program 112 b for realizing the temperature distribution control method of the present embodiment, and various control data. The CPU 113 controls the overall operation of the information processing apparatus 101 in accordance with the estimation program 112 a and the control program 112 b stored in the ROM 112. For example, the information processing apparatus 101 estimates the temperature distribution of the entire interior of the vertical distillation-distillation furnace 2 using the temperature information (measured value) at a specific position of the vertical distillation-distillation furnace 2 supplied from the coke production facility 1 . Moreover, each tuyere flow rate of the coke manufacturing equipment 1 is determined using the estimated temperature distribution. In addition, the temperature information (measured value) at the specific position of the vertical dry distillation furnace 2 is detected by a temperature sensor provided in the vertical dry distillation furnace 2.

  The input device 102 is configured of an input device such as a keyboard, a mouse pointer, and a ten key, and is operated when various information is input to the information processing apparatus 101. The output device 103 is constituted by a display device or the like, and outputs various processing information of the information processing apparatus 101.

  In the present embodiment, a temperature distribution control method is executed by the temperature distribution control device 100 so as to realize a target temperature distribution of the vertical distillation-distillation furnace 2.

[3. Temperature distribution control method]
In the temperature distribution control method of the present embodiment, the target temperature distribution can be obtained by considering the operation influence between a plurality of tuyeres in the vertical direction (height direction) and the horizontal direction (longitudinal direction) of the vertical distillation-type distillation furnace 2 Realize the history.

  FIG. 4 is a flowchart showing the entire flow of the temperature distribution control method. As shown in FIG. 4, the information processing apparatus 101 first fetches operation result data (step S1). As the operation result data, the gas flow rate of each tuyere 3a to 3d, the gas blowing temperature, the cutting speed of the discharge port 13, and the like can be mentioned.

  Next, the information processing apparatus 101 calculates a physical model taking into consideration the dry distillation reaction inside the vertical distillation-distillation furnace 2 and the heat exchange between gas and solid to obtain the current temperature distribution (step S2), and the physical model Predict the temperature distribution in the future (step S3), calculate the amount of change of the control variable at the time of unit operation of each operation amount (step S4), and using the calculation result in step S4, Optimization calculation of each operation amount is performed so as to compensate for the deviation between the target temperature distribution (target value) and the future predicted temperature (predicted value) (step S5). The compensation is to calculate so as to minimize the deviation, and in step S5, the calculation of the optimal action (optimal operation amount) for approaching the history of the target temperature distribution is performed. Step S2 is executed by the estimation program 112a of the information processing apparatus 101. Steps S4 to S5 are executed by the control program 112b of the information processing apparatus 101.

  Thereafter, the information processing apparatus 101 outputs the calculation result of step S5 as a recommended operation amount (step S6). The information processing apparatus 101 performs this series of calculations for each control cycle, and achieves and maintains the target temperature distribution in the vertical distillation-distillation furnace 2.

The temperature distribution control method of the present embodiment is characterized by the step S2 to step S5 (four steps) of FIG. 4 described above, so in the following description, these will be described as the first step to the fourth step.
First step: Estimation of current temperature distribution by physical model Second step: Prediction of future temperature distribution by physical model Third step: Degree of influence (sensitivity) on control variable when each manipulated variable is manipulated by unit amount Calculation Fourth Step: Action Optimization Calculation

  Moreover, in realizing the history of the target temperature distribution, as a variable to be controlled (hereinafter referred to as “control variable”), the gas temperature at the furnace top of the vertical distillation-type distillation furnace 2 (hereinafter referred to as “furnace top temperature”), The time taken for the coal to stay in a high temperature area near the high temperature tuyere 3b (hereinafter referred to as "high temperature holding time") and the discharge solid temperature (hereinafter referred to as "discharge temperature") are three. Furthermore, four variables of low temperature tuyere flow rate, high temperature tuyere flow rate, extraction tuyere flow rate, and cooling tuyere flow rate are used as variables (hereinafter referred to as “operational variables”) that are actively operated in performing the control. However, as described later, since it is desirable to operate the extraction tuyere flow rate and the cooling tuyere flow rate by equal amounts, there are only three substantial operation variables. The control variables and the manipulated variables will be described in detail in the description of the third and fourth steps.

[3-1. Estimation of current temperature distribution (first step)]
In the first step, a physical model of the countercurrent heat exchange process in the packed bed is used to estimate the current temperature distribution. Here, specific examples of mathematical formulas constituting the physical model and the physical model calculation will be described.

[3-1-1. Physical model]
In the physical model (non-stationary model), the gas flow rate of each tuyere 3a to 3d, the gas injection temperature, and the speed at which the discharge port 13 is cut out are taken into consideration as operation conditions that affect the temperature distribution. In addition, as a physical model, it is a model that takes into consideration the mass balance, momentum balance, and heat balance.

  The mass balance is a physical model in which a part of the solid is gasified as shown in the following expressions (1) and (2). However, since the amount of gas derived from solid is very small relative to the amount of gas blown, the right side of Formula (1) approximates 0.

Here, the horizontal direction of the vertical distillation-distillation furnace 2 is defined as the x direction, the vertical direction as the y direction, and the depth direction as the z direction. [Rho _g is the gas density in Equation ^{(1) [kg / m 3} ], u g is the horizontal component of the gas velocity [m / s], _{v g} vertical component of the gas velocity [m / s], _{w g} Is the depth component [m / s] of the gas velocity, and R is the reaction velocity [kg / m ³ · s]. In equation (2), _{s s} represents the solid density [kg / m ³ ], and v _s represents the vertical component [m / s] of the solid velocity.

  As momentum balance, as shown in the following equation (3), Ergun's equation generally used for fluid flow in the packed bed was solved for momentum balance of gas. In addition, about the momentum balance of a solid, it was assumed that only the above equation (2) was used because it was assumed that the solid only dropped vertically.

Here, P in equation (3) represents pressure [Pa], ε represents porosity [−], d _p represents particle diameter [m], and μ _g represents gas viscosity [Pa · s]. Further, _{u g} is the gas velocity _{[m / s], u g} = (u g, v g, w g) represented by a vector as.

  As the temperature balance, as shown in the following formulas (4) and (5), the heat exchange between the gas and the solid, the heat exchange between the gas and the atmosphere around the facility, and the heat of reaction are considered.

Here, C _g in equation (4) is the gas specific heat [kJ / kg · K], T _g is the gas temperature [K], and α is the heat exchange coefficient between gas and solid [kJ / m ³ · s · K], _{T s} is the solid temperature [K], h is the heat exchange coefficient between the gas and the atmosphere ^{[kJ / m 3 · s ·} K], T out facilities ambient temperature [K], ΔH _R reaction Heat [kJ / kg], η ₁ represents the reaction heat distribution coefficient. Formula _{C s} is the solid specific heat in (5) [kJ / kg · K], η 2 represents the reaction heat distribution coefficient. Furthermore, u _s is the solid velocity [m / s], and can be represented by a vector as u _s = (0, v _s , 0).

  The result of discretizing the equations (1) to (5) by an appropriate method (for example, heat transfer and computer simulation) can be expressed by the following equation (6). In addition, when calculating Formula (6), the discretization by perfect implicit solution was performed.

Here, T _g (k) in equation (6) is a vector quantity representing the temperature distribution of the gas at time step k, and T _s (k) is a vector quantity representing the temperature part distribution of the solid at time step k is there. The number of elements of the vector corresponds to the number of meshes of discretization. The number of meshes in the present embodiment is 40 in the vertical direction, 16 in the horizontal direction, and 8 in the depth direction. Moreover, u (k) in Formula (6) represents the gas flow rate and gas temperature from each tuyere which are operation amount.

[3-1-2. Calculation flowchart]
FIG. 5 is a flowchart showing an example of the physical model calculation flow. The information processing apparatus 101 executes the calculation flow shown in FIG. 5 in order to solve Equations (1) to (6) of the physical model. The information processing apparatus 101 updates the current temperature distribution for each control period using the physical model calculation.

  As shown in FIG. 5, the information processing apparatus 101 starts updating the temperature distribution by inputting necessary information such as the temperature distribution at time k (step S2a). Thereafter, the information processing apparatus 101 performs reaction calculation (step S2b), raw material falling velocity calculation (step S2c), gas flow calculation (step S2d), physical property value calculation such as solid specific heat (step S2e) Perform heat exchange coefficient calculation (step S2f), perform reaction heat calculation (step S2g), calculate influence coefficients from adjacent cells in each cell (step S2h), and calculate the temperature distribution at time k + 1 Calculate (step S2i).

Specifically, in the reaction calculation in step S2b, reaction rates R in the equations (1) and (2) are calculated. The reaction calculation is performed by the known method described in the steel manual 3rd edition (steel making, steel making). Formula (2) is calculated in the raw material descent rate calculation of step S2c. Equations (1) and (3) are calculated in the gas flow calculation in step S2d. In addition, calculation of physical property values such as solid specific heat in step S2e and heat exchange coefficient calculation in step S2f are described in the Japan Society for the Promotion of Science, Japan Iron and Steel Institute ed .: “Numbers for steel heat calculation” (1966.4.10) Newspaper company] according to the well-known method described. In the heat of reaction calculation in step S2g, the heat of reaction ΔH _R in formulas (4) and (5) is calculated. In the calculation of the influence coefficient from the adjacent cell in each cell in step S2h, the coefficient representing the thermal effect in each cell (mesh) obtained by dividing the vertical distillation distillation furnace 2 is calculated.

  Thereafter, the information processing apparatus 101 determines whether or not the processing of step S2b to step S2i has been repeated ten times (step S2j). When the process of step S2b-step S2i is not repeated 10 times (step S2 j: No), it returns to step S2 b and loops the process mentioned above. That is, the information processing apparatus 101 calculates the temperature distribution at time k + 1 by solving the equations (1) to (6) by convergence calculation. When the processing of step S2b to step S2i is repeated ten times (step S2j: Yes), the information processing apparatus 101 outputs the temperature distribution at time k + 1 (step S2k), and the subflow of the update of the temperature distribution ends. Note that repeating the process of steps S2b to S2i ten times is an example, and the number of times is not particularly limited. Also, although it is better for the number of iterations of the implicit method to be larger, for example, the number can be determined in relation to the convergence time. Alternatively, an appropriate convergence condition may be determined, and in the case where the convergence condition is satisfied, the above-described processing of step S2b to step S2i may be configured to stop the calculation repeatedly.

[3-2. Prediction of Future Temperature Distribution (Second Step)]
In the second step, using the above-described physical model, the temperature distribution after the next eight hours when the current input conditions (the tuyere flow rate, the tuyere temperature, the production amount, etc.) are maintained is predicted and calculated. Note that eight hours is an example. That is, how many hours to predict in the future can be determined as appropriate based on the characteristics of the process and the operating conditions.

In the future prediction, T _g (k) and T _s (k), which are the current temperature distributions of the first step, are set as initial temperature distributions (initial values). Then, assuming that the current product cutting speed, flow rate of each tuyere, and temperature will remain constant, the temperature distribution after 8 hours is predicted. That is, the information processing apparatus 101 assumes that the operating conditions of the vertical distillation-distillation furnace 2 at the time of estimating the current temperature distribution will remain constant in the future, and the temperature distribution after a predetermined time in the future using the above physical model Is provided with a prediction unit that predicts For example, when the time step of the physical model is 30 minutes, physical model calculation is performed 16 times to update the temperature distribution. In the following description, the temperature distribution (future temperature distribution) predicted on the assumption that the manipulated variable is held at the present value in the future will be referred to as "free response".

[3-3. Calculation of degree of influence from each operation variable to control variable (third step)]
In the third step, the degree of influence on the predicted temperature in the future when the action of changing each tuyere flow rate by the unit flow rate is taken is calculated. That is, the response calculation (sensitivity analysis) of the control variable with respect to each operation amount of the plurality of tuyeres 3a to 3d arranged in the vertical direction and the horizontal direction of the vertical dry distillation furnace 2 is performed.

In the following description, MV represents an operation variable, MV ₁ represents a low temperature tuyere flow, MV ₂ represents a high temperature tuyere flow, and MV ₃ represents a flow rate of the extraction tuyere and the cooling tuyere. Further, CV represents a control variable, CV ₁ represents a furnace top temperature, CV ₂ represents a high temperature holding time, and CV ₃ represents a discharge temperature. The subscript i (i = 1, 2, 3) means a zone. This zone is a control zone that represents the horizontal area of the vertical distillation-type distillation furnace 2 as shown in FIG. In addition, ΔCV represents the change amount (control amount) of the control variable, and ΔMV represents the change amount (operation amount) of the manipulated variable. The description of FIG. 6 will be described later.

[3-3-1. Sensitivity analysis of low temperature tuyere flow (MV ₁ )]
The sensitivity analysis of the low temperature tuyere flow MV ₁ will be described. Here, the control variables CV ₁ , CV ₂ and CV ₃ when the low temperature tuyere flow MV ₁ is raised by 100 Nm ³ / hr are predicted and calculated. In the second step free response calculation, calculation was performed under the assumption that the current tuyere flow rate and temperature remain constant in the future, but in this calculation of the degree of influence, the low temperature tuyere flow rate MV ₁ The predicted transition of each control variable CV ₁ , CV ₂ , CV ₃ is calculated by fixing it to the present value +100 Nm ³ / hr. Then, the free response is subtracted from the predicted transition of each control variable. Thus, it is possible to separate the influence of the control variables by manipulating the cold tuyere flow MV ₁ by a unit flow rate. The degree of influence (sensitivity) on each control variable after 8 hours obtained by this calculation method is shown in FIG. The unit flow rate of 100 Nm ³ / hr is an example, and the unit flow rate is not limited to this and may be set to an appropriate value.

As shown in FIG. 7, when the low temperature tuyere flow MV ₁ is operated, only the furnace top temperature CV ₁ appears to be affected, and the other control variables, ie, the high temperature holding time CV ₂ and the discharge temperature CV ₃ are small Because I ignore it. The sensitivity analysis results for the low temperature tuyere flow MV ₁ can be expressed as the following equation (7).

_{Here, ΔCV 1, i (i =} 1,2,3) represents the variation of the furnace top temperature CV ₁ in each zone i. In the equation (7), t ₁ , t ₂ and t ₃ are degrees of influence on the furnace top temperature CV ₁ of each zone i when operating the low temperature tuyere flow MV ₁ . Furthermore, T is a sensitivity analysis matrix that represents the degree of influence on the furnace top temperature CV ₁ during operation of the low temperature tuyere flow MV ₁ .

[3-3-2. Sensitivity analysis of high temperature tuyere flow (MV ₂ )]
The sensitivity analysis of the high temperature tuyere flow MV ₂ will be described. Here, the degree of influence on each control variable CV ₁ , CV ₂ and CV ₃ when the high temperature tuyere flow MV ₂ is raised by 100 Nm ³ / hr is predicted and calculated.

In the coke production facility 1 of the present embodiment, the plurality of high temperature tuyeres 3b arranged in the horizontal direction can be adjusted independently in three control zones as shown in FIG. FIG. 6 is a view showing a control zone of the vertical carbon-distillation furnace 2. For high temperature tuyere flow MV _2, calculates the degree of influence on the three control zone control variables for each. Also in the following description, the “zone” represents a control block (control zone as a horizontal direction area) in which the high temperature tuyere 3b can be operated independently.

As a representative example, the degree of influence when only the high temperature tuyere 3b of the central zone (zone 2) is operated is shown in FIG. As shown in FIG. 8, the furnace top temperature CV ₁ has appeared equally affected horizontally entire area. This is because the amount of gas at the high temperature tuyere 3 b is smoothed at the top of the vertical distillation-type distillation furnace 2. Regarding the high-temperature holding time CV _2, tends to increase only vertical region directly below the tuyere of operating the hot tuyere flow MV ₂ was observed. This is because the solid heated by the high temperature gas vertically descends in the vertical distillation-distillation furnace 2. Discharge temperature CV ₃ is neglected because the effect is small. The same sensitivity analysis is performed for the other zones (zone 1 and zone 3). The sensitivity analysis results for the high temperature tuyere flow MV ₂ can be expressed as the following equation (8) and equation (9).

Here, ΔCV _{2, i} (i = 1 _{, 2,} 3) represents the amount of change of the high-temperature holding time CV ₂ in each zone i. K _{i, j} (j = 1,2,3) in the equation (8) is the effect on the high temperature holding time CV ₂ of the j th zone when the high temperature tuyere flow MV ₂ of the i th zone is manipulated Represents a degree. G _{i, j} in equation (9) represents the degree of influence of the j-th zone on the furnace top temperature CV ₁ when the high-temperature tuyere flow MV ₂ in the i-th zone is manipulated.

3-3-3. Sensitivity Analysis of Flow Rate (MV ₃ ) of Cooling Tuyere and Extraction Tuyere]
The sensitivity analysis of the flow rate of the extraction tuyere and the cooling tuyere (hereinafter referred to as “extraction tuyere / cooling tuyere flow”) MV ₃ will be described. The results when the extraction tuyere / cooling tuyere flow MV ₃ is manipulated in equal amounts are shown in FIG. FIG. 9 is a diagram showing the cooling tuyere flow rate and the influence on each control variable at the time of the extraction tuyere flow rate operation. As shown in FIG. 9, by its equal volume operation, the result that only the discharge temperature CV ₃ is reduced is obtained. Here, it is important to operate both the extraction tuyere flow rate and the cooling tuyere flow rate with equal amounts. By keeping the flow rate of the cooling gas flowing above the extraction nozzle 3c in the vertical direction of the vertical dry distillation furnace 2 constant, the high temperature holding time CV ₂ and the furnace top temperature CV ₁ are not affected, and the discharge temperature CV _{This is because 3} can be controlled. Therefore, the information processing apparatus 101 includes a control unit that controls the flow rates of the extraction tuyere 3c and the cooling tuyere 3d to be equal. Taking this into consideration, the sensitivity analysis results for the extraction tuyere / cooling tuyere flow MV ₃ can be expressed as the following equation (10).

Here, ΔCV _{3, i} represents the amount of change of the discharge temperature CV ₃ in each zone i. R ₁ , r ₂ and r ₃ in the equation (10) are degrees of influence on the discharge temperature CV ₃ of each zone i when the extraction tuyere / cooling tuyere flow MV ₃ is operated. Furthermore, R is a sensitivity analysis matrix that represents the degree of influence on the discharge temperature CV ₃ at the time of operation of the extraction tuyere / cooling tuyere flow MV ₃ .

[3-4. Action optimization calculation (4th step)]
In the fourth step, an action optimization calculation is performed using the prediction calculation result (free response) in the second step and the sensitivity analysis result in the third step. In the calculation flow of the action optimization, in consideration of the operation influence of each tuyere 3a to 3d, the operation amount ΔMV is determined stepwise from the lower part to the upper part in the vertical direction of the vertical distillation-type distillation furnace 2. When considering the operation influence, since each tuyere 3a to 3d is parallelized in the vertical direction and the horizontal direction of the vertical distillation-distillation furnace 2, the operation influence in the horizontal direction is considered. The fourth step is to perform the action optimization calculation in the order of the following steps 1 to 3.
Step 1: Determination of the manipulated variable ΔMV ₃ of the extraction tuyere / cooling tuyere flow Step 2: Determination of the manipulated variable ΔMV ₂ of the high temperature tuyere flow Step 3: Determination of the manipulated variable ΔMV ₁ of the low temperature tuyere flow

FIG. 10 is a diagram for explaining the calculation flow of action optimization. First, for the discharge temperature CV ₃ , the control variable (high temperature holding time CV ₂ , furnace top temperature CV) of the upper part is provided by feeding back the discharge temperature CV ₃ to the extraction tuyere / cooling tuyere flow MV ₃ (step 1) ₁ ) It can be controlled independently. Sonouede, for high-temperature holding time CV _2, the high-temperature holding time CV ₂ is fed back to the high temperature tuyere flow MV ₂ for each zone (Step 2). And, for the furnace top temperature CV _1, while canceling the influence of the furnace top temperature CV ₁ by manipulating the lower portion of the hot tuyere flow MV _2, cold tuyere so as to keep the furnace top temperature CV ₁ constant The flow rate MV ₁ is operated (step 3). Thus, the control logic can be constructed in consideration of the interference of the operation influence of each tuyere flow rate. In the present embodiment, since the plurality of tuyeres 3a to 3d are arranged in parallel not only in the vertical direction but also in the horizontal direction, the control logic described above is influenced by the operation of each tuyere flow rate in the horizontal direction as well as the vertical direction. Interference is considered. Hereinafter, each step of the action optimization calculation will be described in detail.

[3-4-1. Determination of the manipulated variable (ΔMV ₃ ) of the extraction tuyere / cooling tuyere flow rate (step 1)]
Step 1 is to feed back the exhaust temperature CV _3, to determine the extracted tuyeres and cooling tuyere flow operation amount .DELTA.MV ₃ of.

First, the deviation based on the predicted value of the discharge temperature CV ₃ in each zone i is determined. The predicted value of the discharge temperature CV ₃ is a predictive calculation result in the second step (the free response). The actual measurement value of the discharge temperature CV ₃ can be obtained. Therefore, when calculating the deviation of the discharge temperature CV ₃ , first, as shown in the following equation (11), the current measurement value of the discharge temperature CV ₃ , An error d from the calculated value by the physical model in the first step is calculated. The coke production facility 1 is configured to be able to detect the current discharge temperature CV ₃ by the temperature sensor provided in the vertical distillation-type distillation furnace 2.

Then, the deviation of the exhaust temperature CV ₃ can be obtained by the following equation (12). As shown in Equation (12), by adding the error d minutes to a prediction calculation result is free response at the second step, a deviation of the exhaust temperature CV _3.

  Here, in the equation (12), δCV means the deviation of the control amount from the target value. Also, the subscript ref means a target value, and free means a free response (predicted value).

Next, the feedback to the deviation _{δCV 3, i (i = 1,2,3} ) , and extracted tuyere and cooling tuyeres flow of an operation amount .DELTA.MV ₃ obtained by equation (12). Then, the operation amount ΔMV ₃ of the extraction tuyere / cooling tuyere flow rate at which the deviation δCV _{3, i} is minimized is calculated. For example, a method by least squares as shown in the following equation (13) can be considered. R in Equation (13) is a sensitivity analysis matrix obtained by Equation (10). ^RT in Equation (13) represents the transpose of the matrix R.

[3-4-2. Determination of manipulated variable (ΔMV ₂ ) of high temperature tuyere flow rate (step 2)]
In step 2, the high temperature holding time CV ₂ is fed back for each zone to determine the manipulated value ΔMV _{2, i} of the high temperature tuyere flow rate of each zone i.

First, a deviation based on the predicted value of the high-temperature holding time CV ₂ for each zone i. The predicted value of the high-temperature holding time CV _{2, i} is the predicted calculation result (free response) in the second step. Then, the deviation can be obtained by the following equation (14). Incidentally, because it can not obtain the actual values for the high-temperature holding time CV _2, measured as described above in Equation (11) - based on the error between the estimate, the correction of the control deviation is not performed.

Next, the deviation δCV _{2, i} (i = 1,2,3) obtained by the equation (14) is fed back to the manipulated value of high temperature tuyere flow ΔMV _2,1 , ΔMV _2,2 , ΔMV _2,3 . Then, the operation amounts ΔMV _2,1 , ΔMV _2,2 , ΔMV _2,3 of the high temperature tuyerge flow rate at which the deviation δCV _{2, i} is minimized are calculated. For example, a method of least squares as shown in the following equation (15) can be considered. K in Equation (15) is a sensitivity analysis matrix obtained by Equation (8). K ^T in equation (15) represents the transpose of the matrix K.

As shown in the equation (15), it is possible to determine the operation amount ΔMV _{2, i} (i = 1,2,3) of the high temperature tuyere flow rate such that the deviation δCV _{2, i} is minimized. In addition, since the operation amount ΔMV ₃ of the extraction tuyere / cooling tuyere flow determined in step 1 is controlled independently of the upper part of the extraction tuyere 3 c of the vertical distillation-type distillation furnace 2, the operation of the high temperature tuyere flow With regard to the amount ΔMV _{2, i} , the operation amount ΔMV ₃ of the extraction tuyere / cooling tuyere flow rate is not taken into consideration.

[3-4-3. Determination of manipulated variable (ΔMV ₁ ) of low temperature tuyere flow (step 3)]
In Step 3, by feeding back the furnace top temperature CV _1, and taking into account the effect on the furnace top temperature CV ₁ by manipulating the hot tuyere flow MV _2, to determine the manipulated variable .DELTA.MV ₁ cold tuyere flow.

First, a deviation based on the predicted value of the furnace top temperature CV ₁ in each zone i. The predicted value of the furnace top temperature CV _{1, i} is the predicted calculation result (free response) in the second step. Since the furnace top temperature CV ₁ is a measured value can be obtained, in calculating the deviation of the furnace top temperature CV _1, as shown in Equation (16) below, the current measured value of the furnace top temperature CV ₁ And the error d between the value calculated by the physical model in the first step. In coke production facility 1 is configured to detect the current of the furnace top temperature CV ₁ by a temperature sensor provided in the vertical carbonization furnace 2.

Then, the deviation of the furnace top temperature CV ₁ can be obtained by the following equation (17). As shown in equation (17), by adding the error d minute free response is predictive calculation result in the second step, a deviation of the furnace top temperature CV _1.

Then, the deviation _{δCV 1, i (i = 1,2,3} ) obtained by equation (17), is fed back to the low-temperature tuyere operation amount .DELTA.MV _1. Then, the low temperature tuyere manipulation amount ΔMV ₁ that minimizes the deviation δ CV _{1, i} is calculated. For example, a method of least squares as shown in the following equation (18) can be considered.

Here It should be noted that, after subtracting the effect of the furnace top temperature CV ₁ by the operation of the high-temperature tuyere flow MV ₂ of Step 2 as described above, is to operate a low-temperature tuyere flow MV _1. That is, with regard to the low temperature tuyere manipulation amount ΔMV ₁ , excess or deficiency of the manipulation amount will occur unless the influence of the high temperature tuyere flow manipulation amount ΔMV _{2, i} is considered. If this is taken into consideration and expressed as an equation, it is as the following equation (18). T in equation (18) is a sensitivity analysis matrix obtained by equation (7). T ^T in equation (18) represents the transpose of matrix T. Further, G in the equation (18) is a sensitivity analysis matrix obtained by the equation (9).

In this step 3, as shown on the right side of equation (18), the low temperature tuyere considering the influence of the operation amount ΔMV _{2, i} (i = 1,2,3) of the high temperature tuyere flow determined in step 2 It can be seen that the operation amount ΔMV ₁ is determined.

By the action optimization calculation including the calculation of step 1 to step 3 as described above, ΔMV ₁ , ΔMV _{2, i} , ΔMV ₃ which are the optimum operation amounts of the respective tuyeres 3a to 3d can be determined. When calculating the optimum manipulated variables ΔMV ₁ , ΔMV _{2, i} and ΔMV ₃ , interference of the operation influence by the plurality of juxtaposed parallel and plural vertical and horizontal directions of the vertical distillation distillation furnace 2 can be suppressed It will be calculated. The information processing apparatus 101 performs a series of action optimization calculations including steps 1 to 3 described above for each control cycle.

[4. simulation]
Next, assuming the disturbance in the actual coke production facility 1, the control logic of the embodiment described above outputs the operation amount ΔMV that cancels the change in temperature distribution caused by the disturbance, and as a result, each control amount ΔCV is the target value Confirm on the simulation that it is maintained. Here, the response of the control system was simulated on the assumption that, as the disturbance, the formed carbon charged into the vertical dry distillation furnace 2 from the inlet 12 is changed and the specific heat of the raw material rises. The simulation result is shown in FIG.

FIG. 11A shows a simulation result of the control amount ΔCV at the time of occurrence of a disturbance related to solid specific heat. FIG. 11 (b) is a diagram showing a simulation result of the manipulated variable ΔMV at the time of occurrence of a disturbance related to solid specific heat. FIGS. 11 (a) and 11 (b) show the simulation results of zone 2 only, and one time step is 20 minutes. Further, FIG. 11A shows the furnace top temperature CV _{1 in the} upper stage, the high temperature holding time CV _{2 in} the middle stage, and the discharge temperature CV _{3 in the} lower stage. FIG. 11B shows the low temperature tuyere flow MV _{1 in the} upper stage, the high temperature tuyere flow MV _{2 in the} middle stage, and the cooling tuyere flow MV ₃ in the lower stage.

When the control was turned on at T = 50, as shown in FIG. 11A, the furnace top temperature CV ₁ , the high temperature holding time CV ₂ , and the discharge temperature CV ₃ all converged to the target values. In this case, as shown in FIG. 11B, each operation amount ΔMV starts to change so that each control variable becomes a target value from time T = 50.

Also, when the specific heat rises at T = 120 (disturbance), as shown in FIG. 11 (b), the low temperature tuyere flow MV ₁ , the high temperature tuyere flow MV ₂ , and the extraction tuyere · The cooling tuyere flow MV ₃ has all risen, and changes the manipulated variables ΔMV ₁ , ΔMV ₂ , ₁ , ΔMV ₂ , ₂ , ΔMV ₂ , ₃ , ΔMV _{3 according} to the increase (UP) in the heat capacity of the raw material doing. As can be seen from the simulation results, according to the temperature distribution control method and apparatus of the present embodiment, each control amount ΔCV ₁ , ΔCV ₂ , ΔCV ₃ can also be controlled to the target value. Thus, the validity of this control logic has been confirmed on the simulation.

As described above, in the temperature distribution control method and control device of the present embodiment, not only the influence of the operation of the tuyere flow rate and temperature is propagated in the vertical direction of the vertical distillation-type distillation furnace 2, but Propagation in the horizontal direction of the mold dry distillation furnace 2 is considered. Thereby, when a plurality of tuyeres are juxtaposed in the horizontal direction and the vertical direction of the vertical distillation-distillation furnace 2, each operation amount ΔMV ₁ , ΔMV _{2, i} , ΔMV is taken into consideration in consideration of the operation influence between the plurality of tuyeres. _{Since 3} is determined, interference of the operation influence can be minimized. Therefore, the temperature distribution of the vertical dry distillation furnace 2 can be controlled to a desired state.

  In addition, this invention is not limited to embodiment mentioned above, It can change suitably in the range which does not deviate from the objective of this invention.

  For example, in the embodiment described above, an example in which six tuyeres 3a to 3d are horizontally arranged as shown in FIG. 2 has been described, but in the present invention, each tuyere 3a to 3d is horizontal The number is not particularly limited as long as it is provided in plurality. That is, the number of zones representing the horizontal direction area of the vertical distillation-distillation furnace 2 is not limited to three, and the number of zones can be appropriately set in accordance with the number of tuyeres 3a to 3d.

  The present invention is also applicable to the entire process involving countercurrent heat exchange in the packed bed including the vertical distillation-distillation furnace 2.

DESCRIPTION OF SYMBOLS 1 coke manufacturing equipment 2 vertical dry distillation furnace 3a low temperature tuyere 3b high temperature tuyere 3c extraction tuyere 3d cooling tuyere 4 gas outlet in the furnace 5 spray tower 6 gas cooler 7 electric precipitator 8a water storage tank 8b tar tank 9 High temperature gas heating furnace 10 Low temperature gas heating furnace 11 Ejector 12 Loading port 13 Exhaust port 100 Temperature distribution control device 101 Information processing device 112 ROM
112a estimation program 112b control program 113 CPU

Claims (8)

Input the gas flow rate of each tuyere of the vertical dry distillation furnace, the gas injection temperature, and the speed at which the outlet is cut out , taking into consideration the mass balance, momentum balance, and heat balance inside the vertical dry distillation furnace. the physical model to output the temperature distribution in the vertical carbonization furnace, the gas flow rate of each tuyere of the vertical dry distillation furnace, by inputting a current value of cutting speed of the gas blowing temperature, and an outlet an estimation step in which a plurality of tuyeres to estimate the current temperature distribution of the parallelized by the vertical carbonization furnace provided in the vertical and horizontal directions,
The current temperature distribution estimated by the estimation step is used as an initial value, and the gas flow rate of each tuyere, the gas injection temperature, and the extraction speed of the outlet are constant from now on when the current temperature distribution is estimated. Predicting the future temperature distribution after a predetermined time using the physical model, assuming that
Calculating a degree of influence which is a ratio of a change amount of a control variable to a unit flow rate when the gas flow rate of each tuyere is operated by a unit flow rate for the plurality of tuyeres;
In calculating the manipulated value of the gas flow rate at the tuyere so that the deviation between the target temperature distribution of the vertical dry distillation furnace and the future temperature distribution predicted by the prediction step is minimized, An operation amount determining step of determining each operation amount of the gas flow rate of the tuyere step by step from the lower part to the upper part in the vertical direction of the vertical dry distillation furnace using the influence and the deviation which are the ratio ; Including
The tuyere includes a low temperature tuyere, a high temperature tuyere, an extraction tuyere, and a cooling tuyere provided in order from the top of the furnace to the bottom of the vertical direction of the vertical dry distillation furnace,
The bottom of the vertical carbon-distillation furnace is provided with the discharge port for cutting out shaped coke,
The control variable is a variable that performs control to achieve a target temperature distribution, such as a furnace top temperature which is a gas temperature at the furnace top of the vertical distillation-type distillation furnace, and a high temperature area in which the formed coal is near the high temperature tuyere Including the high temperature holding time which is the time to stay, and the discharge solid temperature,
The step of calculating the degree of influence calculates the ratio indicating the degree of influence on the control variable in each of a plurality of control zones representing the horizontal direction area of the vertical distillation-distillation furnace with respect to the gas flow rate of the high temperature tuyere A temperature distribution control method of a vertical distillation-type distillation furnace characterized by including. The influence calculation step is
Calculates the furnace the influence of the temperature at the top of the control zone at the time of operating the gas flow rate of said cold tuyere,
It calculates the degree of influence on the high-temperature retention time for operating the gas flow rate of the hot tuyere for each of the plurality of control zones,
Calculating the degree of influence on the discharged solid temperature of each control zone when operating the gas flow rate of the extraction tuyere and the cooling tuyere;
It said manipulated variable determining step calculates the deviation from the target value of the control amount of the control variable, the deviation and the influence and, each tuyere with which is a ratio calculated by the influence degree calculation step The temperature distribution control method of the vertical distillation-type distillation furnace according to claim 1, wherein the operation amount of the gas flow rate is determined. The operation amount determination step calculates an error between the current temperature distribution estimated by the estimation step and the actual measurement value, and calculates a deviation between the target temperature distribution and the future temperature distribution using the error. The temperature distribution control method of the vertical dry distillation furnace according to claim 1 or 2 characterized by including. The method further includes an equal amount control step of controlling the gas flow rate of the extraction tuyere and the gas flow rate of the cooling tuyere to be equal.
The influence degree calculation step calculates the influence degree to the furnace top temperature of each control zone when operating the gas flow rate of the high temperature tuyere,
The operation amount determining step is
A first determination step of determining an operation amount of a gas flow rate of the extraction tuyere and the cooling tuyere;
A second determining step of determining an operation amount of the gas flow rate of the high temperature tuyere;
An error between the predicted value of the furnace top temperature predicted by the prediction step and the actual value is calculated, and a deviation between a value obtained by adding this error to the prediction value and a target value of the furnace top temperature is calculated. Based on the deviation, the gas flow rate of the high temperature tuyere calculated in the influence degree calculation step is calculated as the change amount of the gas flow rate when operating the gas flow rate of the high temperature tuyere to the operation amount determined in the second determination step. The value obtained by multiplying the degree of influence on the furnace top temperature of each control zone when operating is subtracted to calculate the operation amount of the gas flow rate of the low temperature tuyere, and the low temperature tuyere where the deviation is minimized The temperature distribution control method of the vertical dry distillation furnace according to any one of claims 1 to 3, comprising: a third determination step of determining an operation amount of the gas flow rate of Input the gas flow rate of each tuyere of the vertical dry distillation furnace, the gas injection temperature, and the speed at which the outlet is cut out , taking into consideration the mass balance, momentum balance, and heat balance inside the vertical dry distillation furnace. the physical model to output the temperature distribution in the vertical carbonization furnace, the gas flow rate of each tuyere of the vertical dry distillation furnace, by inputting a current value of cutting speed of the gas blowing temperature, and an outlet , an estimation unit in which a plurality of tuyeres to estimate the current temperature distribution of the parallelized by the vertical carbonization furnace provided in the vertical and horizontal directions,
The current temperature distribution estimated by the estimation means is used as an initial value, and the gas flow rate of each tuyere, the gas injection temperature, and the extraction speed of the outlet are constant from now on when estimating the current temperature distribution A prediction means for predicting a future temperature distribution after a predetermined time using the physical model, assuming that
An influence degree calculation means for calculating an influence degree which is a ratio of a change amount of a control variable when the gas flow rate of each tuyere is operated by a unit flow rate for the plurality of tuyeres and the unit flow rate ;
In calculating the manipulated value of the gas flow rate of the tuyere so that the deviation between the target temperature distribution of the vertical dry distillation furnace and the future temperature distribution predicted by the prediction means becomes minimum, Operation amount determining means for determining each operation amount of the gas flow rate of the tuyere step by step from the lower part to the upper part in the vertical direction of the vertical distillation-distillation furnace using the influence and the deviation which are the ratio ; Equipped with
The tuyere includes a low temperature tuyere, a high temperature tuyere, an extraction tuyere, and a cooling tuyere provided in order from the top of the furnace to the bottom of the vertical direction of the vertical dry distillation furnace,
The bottom of the vertical carbon-distillation furnace is provided with the discharge port for cutting out shaped coke,
The control variable is a variable that performs control to achieve a target temperature distribution, such as a furnace top temperature which is a gas temperature at the furnace top of the vertical distillation-type distillation furnace, and a high temperature area in which the formed coal is near the high temperature tuyere Including the high temperature holding time which is the time to stay, and the discharge solid temperature,
The influence degree calculation means calculates, for the gas flow rate of the high temperature tuyere, a ratio representing the degree of influence on the control variable in each of a plurality of control zones representing a horizontal direction area of the vertical distillation-type distillation furnace. Temperature distribution control device for vertical carbonization-type distillation furnace characterized by The influence degree calculation means
Calculates the furnace the influence of the temperature at the top of the control zone at the time of operating the gas flow rate of said cold tuyere,
It calculates the degree of influence on the high-temperature retention time for operating the gas flow rate of the hot tuyere for each of the plurality of control zones,
Calculating the degree of influence on the discharged solid temperature of each control zone when operating the gas flow rate of the extraction tuyere and the cooling tuyere;
It said manipulated variable determining means calculates a deviation from the target value of the control amount of the control variable, the deviation and the influence and, each tuyere with which is a ratio calculated by the influence degree calculation means The temperature distribution control device of the vertical distillation-type distillation furnace according to claim 5, characterized in that the operation amount of the gas flow rate of is determined. The operation amount determining means calculates an error between the current temperature distribution estimated by the estimating means and the actual measurement value, and calculates an error between the target temperature distribution and the future temperature distribution using the error. The temperature distribution control device of the vertical carbon-distillation furnace according to claim 5 or 6 characterized by the above-mentioned. The system further comprises equivalent control means for controlling the gas flow rate of the extraction tuyere and the gas flow rate of the cooling tuyere equally.
The influence degree calculation means calculates the influence degree on the furnace top temperature of each control zone when operating the gas flow rate of the high temperature tuyere;
The operation amount determining means is
First determining means for determining an operation amount of a gas flow rate of the extraction tuyere and the cooling tuyere;
Second determining means for determining an operation amount of the gas flow rate of the high temperature tuyere;
The error between the predicted value of the furnace top temperature predicted by the prediction means and the actual measurement value is calculated, and the deviation between the value obtained by adding this error to the prediction value and the target value of the furnace top temperature is calculated From the deviation, the gas flow rate of the high temperature tuyere calculated by the influence degree calculation means to the variation of the gas flow rate when operating the gas flow rate of the high temperature tuyere to the operation amount determined by the second determination means The value obtained by multiplying the degree of influence on the furnace top temperature of each control zone when operating is subtracted to calculate the operation amount of the gas flow rate of the low temperature tuyere, and the low temperature tuyere where the deviation is minimized The temperature distribution control device of the vertical distillation-type distillation furnace according to any one of claims 5 to 7, further comprising: third determination means for determining an operation amount of the gas flow rate .

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