Method and system for calibrating parameters of an automatic reactor control device.

Abstract

Disclosed is a method for calibrating the parameters of an automatic control device for a furnace, preferably an immersion combustion furnace, for melting a mixture of raw materials (1001a) containing mineral waste. This method makes it possible to obtain optimal values ​​for the parameters of the transfer function of the control device. It is based on the following: - Model the thermal behavior of the furnace (1002) using a transient heat transfer function H(s), with the time-dependent change in the temperature ΔT of the molten raw material mixture (1001a) as input data; measure the above change over a predetermined limited time period after changing (3004) at least one operating parameter of the furnace (1002), selected from the water content in the raw material mixture (1001a), the amount removed from the furnace, the feeding rate of the raw material mixture (1001a), the power of the heating means (2002a~c), and / or the amount of organic compounds or carbon-containing fuel in the raw material mixture (1001a). - Model the parameters of the control device (2010) transfer function C(s) applied to the modeled transfer function H(s).

Description

[Technical Field]

[0001] The present invention relates to a method and system for calibrating the parameters of a device that automatically controls a furnace, preferably an immersion combustion furnace, for melting a mixture of raw materials containing mineral waste. The present invention also relates to a furnace, preferably an immersion combustion furnace, that implements the above method or system. [Background technology]

[0002] To melt a mixture of vitrifiable raw materials, it is common to use an immersion combustion furnace (SCF), also known as an immersion burner furnace (SBF). In this type of furnace, the combustion means, such as an oxygen / air fuel burner combustion means, is directly immersed in the mixture of vitrifiable raw materials and in the molten glass being formed. Direct injection of reactants and gaseous combustion products into the molten glass in the form of a flow, followed by expansion and rapid ascent, promotes melting and improves the homogeneity of the molten material.

[0003] For example, U.S. Patent No. 351413 (J. Twanwright, October 26, 1886) discloses a method of injecting air and / or fuel, such as gas or oil, into a molten glass, thereby circulating and heating the molten material before the gas burns below or near the surface of the molten material. In this way, the molten material is constantly agitated and mixed, enabling it to maintain a high temperature.

[0004] U.S. Patent No. 1,656,828 (POWELL EDWARD R, January 17, 1928) discloses a method and apparatus for producing rock wool, wherein a mixture of raw materials is introduced into a vertical tank provided with an adjacent inclined combustion chamber. The combustion chamber has a burner, which is positioned so that combustion gases permeate and melt the mixture of raw materials at the bottom of the tank. An opening at the base of the tank allows the molten glass to flow by air jets and blow out fibrous molten glass.

[0005] French Patent No. 876569 (UNION DES VERRERIES MECANIQUES, November 10, 1942) discloses an immersion combustion furnace having a vertical tank, wherein the lower part of the tank has at least one immersion burner in which the pressure of the combustion fluid is greater than 0.2 atmospheres and the velocity is greater than 30 m / s.

[0006] International Publication No. 2009 / 091558 (GAS TECHNOLOGY INST[US] July 29, 2009) discloses an immersion combustion furnace having a double-walled tank with fluid circulation. The hearth is equipped with multiple immersion burners, whose relative spatial arrangement is optimized to improve thermal uniformity of the glass molten material and reduce the unmelted area.

[0007] In addition to a tank suitable for melting a mixture of vitrifiable raw materials, the immersion combustion furnace may have one or more other tanks adjacent to and in communication with the first tank. Molten glass flows into these from the first tank and undergoes various processes, particularly refining.

[0008] German Patent No. 651687 (GLASHUETTE ACHERN AG, October 18, 1937) discloses a furnace having a vertical rotating melting tank through which raw materials are supplied via a hopper opening. The tank has an immersion burner at the center of its lower base, oriented along the axis of rotation of the tank, and an opening is provided near the lower base that allows glass to flow toward a lower refining tank.

[0009] British Patent Application Publication No. 1028481 (SELAS CORP OF AMERICA, May 4, 1966) discloses a furnace comprising several molten tanks, each having numerous immersion burners within the center of its lower base. The furnace also has a main refining tank into which molten glass flows from the molten tanks.

[0010] In the context of mineral fiber production, the mixture of vitrifiable raw materials used in an immersion combustion furnace includes mineral materials that are sources of metals, metalloids, alkalis, and / or alkaline earth elements, the relative proportions of which are adjusted to obtain the desired glass chemical composition at the end of the melting process.

[0011] Mineral raw materials are generally mining raw materials, such as silica sand, bauxite, dolomite, calcium carbonate, magnesium carbonate, and / or sodium carbonate. They can also be mineral by-products from other manufacturing industries.

[0012] However, it is now common practice to replace all or part of the raw materials in a mixture with so-called recyclable mineral waste, with the aim of reducing the ecological impact of the manufacturing industry, and in particular reducing the exploitation of natural resources, energy consumption, and greenhouse gas emissions.

[0013] The first example of recyclable mineral waste is "cullet," which can be distinguished into two types: - So-called "internal" cullet, which may include glass waste from the same manufacturing process or the same glass article production line, and generally includes cutting scrap, defective articles detected and removed during quality control or article composition adjustment; - So-called "external" cullet, which may include glass waste recovered from other processes or glass article manufacturing lines, used glass articles, such as dismantling waste, glass bottles, used glazing, etc., and glass waste recovered from consumers for the purpose of recycling.

[0014] Typically, and especially in the case of external cullet, cullet is a mixture of scrap glass of different colors and compositions. The surface of this scrap may also be covered with organic and / or inorganic layers, which are the result of various processes used to functionalize the surface for specific glass article applications. Ultimately, cullet may contain a certain amount of foreign scrap, such as ceramics, pottery, porcelain, terracotta, plastics, metals, electronic components, etc.

[0015] A second example of renewable mineral waste is mineral fiber waste, which may or may not be sized, i.e., contains or does not contain organic binders. This waste may be generated from manufacturing, construction sites or other work sites and / or recycling pathways.

[0016] A third example of renewable mineral waste is raw material obtained from biomass derived from plants, animals, bacteria, or fungi. This material may be used as fuel and as a means of adjusting the composition and / or redox state of glass.

[0017] Depending on their source, renewable mineral waste, particularly external waste, can have varying levels of moisture and / or organic materials. When introduced into a furnace, this moisture and these organic materials alter the furnace's thermal and chemical equilibrium, causing abrupt changes in the temperature of the glass molten material. The processes of refining and oxidation-reduction equilibrium of the glass molten material are also disrupted. In this way, the furnace's steady-state heating and refining modes become unstable. This can lead to reduced yields and, particularly with regard to mineral fiber production, the creation of glass articles unsuitable for their intended applications.

[0018] Therefore, it is common practice to pre-treat mineral waste, thereby reducing or even removing the moisture and organic compounds it contains.

[0019] For example, International Publication No. WO 2002 / 048612 (SAINT GOBAIN [FR], June 20, 2002) discloses a method for destroying and / or inactivating mineral waste, which makes it possible, in particular, to obtain a reusable cullet for the subsequent manufacture of mineral wool. In this method, the mineral waste is introduced into a liquid and / or foamed phase which is maintained at a temperature of at least 800° C. and is preformed in a tank fitted with an immersion burner from a mixture of materials which can be partially vitrified.

[0020] International Publication No. WO 2006 / 018582 (SAINT GOBAIN ISOVER [FR], February 23, 2006) discloses a method for treating mineral waste, particularly mineral fiber waste, in which pure oxygen or oxygen-rich air is injected into a mass of recycled material which is itself subjected to heating by an immersion burner. By combustion of the organic compounds and melting of the mass, it is possible to obtain a cullet which can be recycled for the subsequent manufacture of glass fibers.

[0021] U.S. Patent No. 4,877,449 (INST GAS TECHNOLOGY [US], October 31, 1989) discloses an immersion combustion furnace having a vertical tank with a lattice cooled at the top above a glass melt, into which solid feed is deposited on this glass melt using a hopper. Combustion gases from the glass melt pass through the lattice, heating the solid feed to melt them and causing the resulting liquid to flow into the glass melt.

[0022] Alternatively, glass waste can be introduced directly, i.e., without pretreatment, into the glass melt of a furnace, particularly an immersion combustion furnace intended for the manufacture of mineral fibers. Generally, a control device, such as a feedback control loop, etc., is used for at least one operating, functional, or control parameter of the furnace, thereby compensating for disturbances received by the furnace with respect to its steady state mode. Such an approach is made possible by the very low thermal inertia inherent to immersion combustion furnaces, particularly those equipped with a double wall with fluid circulation.

[0023] European Patent Application Publication No. 2433911 (JOHNS MANVILLE [US], March 28, 2012) discloses a method and apparatus for recycling a glass wool mat, where the mat is introduced into the glass melt of an immersion combustion furnace at a uniform feeding rate. A PID controller or a predictive control system enables adjustment of a plurality of operating parameters of the furnace, particularly the speed of the mat conveyor, on the output side based on various input signals, such as the temperature of the glass melt, the withdrawal amount, and / or the flow rate of fuel and / or oxidant in the burner.

[0024] International Publication No. 2022 / 180345 (SAINT GOBAIN ISOVER [FR], September 1, 2022) discloses a method for adjusting an immersion combustion furnace supplied with a wet mixture of mineral wool and / or biomass, where the feeding rate of the mixture or the power of the immersion burner is adjusted using a PID controller based on a measured value of the moisture level in the mixture.

Prior Art Documents

Patent Documents

[0025]

Patent Document 1

Patent Document 2

Patent Document 3

Patent Document 4

Patent Document 5

Patent Document 6

Patent Document 7

Patent Document 8

Patent Document 9

[0026] The main drawback of methods involving a pretreatment process for recyclable mineral waste is that they require relatively complex equipment or treatment, and therefore, relatively substantial material and financial investments in their implementation.

[0027] Therefore, it is advantageous to employ methods and systems based on directly introducing a mixture of raw materials containing mineral waste into the furnace, i.e., without pretreatment. The peculiarity of these methods and systems lies in the fact that they require the implementation and configuration of control systems and processes, such as feedback loops or predictive control systems.

[0028] However, despite advances in the automation of control system configuration and calibration, such automation remains difficult with respect to furnaces for melting mixtures of raw materials containing mineral waste, particularly immersion combustion furnaces.

[0029] The moisture level and organic compound content of mineral waste can vary significantly depending on its source and how it is stored. Therefore, over time, in furnaces, particularly immersion furnaces, mixtures of raw materials containing mineral waste in predetermined proportions tend to experience rapid and significant changes in their moisture level and organic compound content.

[0030] Furthermore, the proportion of mineral waste in the mixture can vary depending on the ease or difficulty of sourcing the raw materials. These variations can also contribute to rapid and significant changes in the moisture level and organic compound content of the mixture. As mentioned above, these changes can cause significant disruption to the thermal and chemical equilibrium of the furnace. The furnace may deviate from its steady-state mode and enter an unstable mode.

[0031] Furthermore, it is common practice to add carbon-based organic mineral fuels, generally in solid form, to the raw material mixture 1001a. These fuels constitute an additional energy source for the furnace and often originate from energy recovery processes. The type and amount of fuel can vary considerably depending on its source and market availability. Typical fuel examples include coal or petroleum coke.

[0032] However, it has been found that automatically configured and automatically calibrated control systems are typically unable to compensate for or compensate for interference caused by rapid and abrupt changes in moisture levels and organic compound or carbon-containing fuel content in the feedstock mixture, typically in a rapidly converging manner and within limited over-amplitude settings.

[0033] Therefore, there is still a need for methods and systems that enable reliable and effective calibration of the control systems of furnaces, particularly immersion furnaces, and that allow for a rapidly converging response to rapid and significant changes in moisture levels and / or organic compound or carbon-containing fuel content in mixtures of raw materials containing mineral waste. [Means for solving the problem]

[0034] In a first embodiment of the present invention, a method is provided for calibrating the parameters of an automatic control device for a furnace, preferably an immersion combustion furnace, for melting a mixture of raw materials including mineral waste. - The furnace has at least one tank comprising at least one heating means, preferably in the form of at least one immersion burner, and at least one control device configured to adjust the power of the heating means according to a setpoint temperature T0; - The above tank is suitable for melting the raw material mixture; - The above tank has at least one temperature measuring device; - The above temperature measuring device is configured to continuously measure the temperature of the above mixture of molten raw materials and is connected to the above control device; The above method includes the following steps: (a) Continuously introducing a mixture of raw materials of a predetermined composition into a tank; (b) Continuously measuring the temperature of the molten raw material mixture using a temperature measuring device; (c) Steady heating of the molten raw material mixture to a predetermined temperature Ti; (d) Changing, for a predetermined limited time, at least one operating parameter of the furnace, selected from the water content in the raw material mixture, the furnace withdrawal rate, the rate at which the raw material mixture is fed, the power of the heating means, and / or the amount of organic compounds or carbon-containing fuel in the raw material mixture, without active adjustment by the control device; (e) Measuring the time-dependent changes in the temperature ΔT of the molten raw material mixture and the power ΔP of the heating means; (f) Using a data processing device, model the thermal behavior of the furnace using the transient heat transfer function H(s), with the temperature ΔT of the molten material mixture and the time-dependent change of at least one operating parameter modified in process (d) as input data; (g) Using a data processing device, model the parameters of the control device's transfer function C(s) which is applied to the transfer function H(s) modeled in process (f).

[0035] According to other advantageous embodiments: - Model the transient heat transfer function H(s) using the first-order response transfer function, regardless of the presence or absence of a delay time; - In step (d), at least two parameters, preferably three parameters, are changed sequentially or in parallel; - In step (d), the moisture content in the raw material mixture is changed so that the change in the moisture content of the mixture is between 0 and 10%, and / or the amount of material removed from the furnace is changed so that the relative change in the amount removed is between 0 and 2000 kg / h; - In step (d), the amount of organic compound or carbon-containing fuel in the raw material mixture is changed so that the relative change in the amount of the organic compound or carbon-containing fuel is 0 to 15% by weight, preferably 0 to 10% by weight; - In step (d), change the power of the heating means so that the relative change of the power to the initial power is 0 to 100%, preferably 0 to 50%, or even more preferably 0 to 25%; - The control device is a proportional-integral-derivative (PID) controller; - In process (g), the furnace transfer function H(s) further takes as input data a set of simulated values ​​I(s) of changes in the water content in the raw material mixture, the amount removed from the furnace, the rate at which the raw material mixture is fed, the amount of organic compounds or carbon-containing fuel, and / or the setpoint temperature T0; - The moisture content of the raw material mixture, the amount removed from the furnace, the rate at which the raw material mixture is fed in, and / or the amount of organic compounds or carbon-containing fuel are simulated as random signals, such as white noise or pink noise.

[0036] The method according to the present invention can be used to calibrate the parameters of a device that automatically controls a furnace, preferably an immersion combustion furnace, for melting a mixture of raw materials containing mineral waste.

[0037] In other words, the present invention also relates to using the method according to the present invention to calibrate the parameters of a device that automatically controls a furnace, preferably an immersion combustion furnace, for melting a mixture of raw materials containing mineral waste.

[0038] A second aspect of the present invention provides a system for calibrating the parameters of an automatically controlling furnace, preferably an immersion combustion apparatus, for melting a mixture of raw materials including mineral waste. - The furnace has at least one tank comprising at least one heating means, which is in the form of at least one immersion burner; - The tank is suitable for melting the mixture of raw materials; The above system has the following: - A temperature measuring device comprising at least one temperature measuring device configured to continuously measure the temperature of a mixture of molten raw materials; - At least one control device, the control device is configured to adjust the power of the heating means; the parameters of the transfer function C(s) of the control device are calibrated using the method according to the present invention.

[0039] In a third embodiment of the present invention, a furnace for melting a mixture of raw materials including mineral waste is provided, in particular an immersion combustion furnace, in which the method according to the first embodiment of the present invention is carried out.

[0040] A furnace for melting a mixture of raw materials including mineral waste, preferably an immersion combustion furnace, wherein the furnace has the following: - A first tank, suitable for melting a mixture of raw materials, and equipped with a heating means in the form of at least one immersion burner, - At least one temperature measuring device configured to continuously measure the temperature of the above mixture of molten raw materials, - At least one control device configured to adjust the power of the heating means and to receive at least one continuous temperature measurement using the temperature measuring device; the parameter values ​​of the transfer function C(s) of the control device are fixed from values ​​obtained using the calibration method according to the present invention.

[0041] According to other advantageous embodiments: - The furnace is configured such that the heating means is an oxygen / air fuel immersion burner, and the control device is configured to further adjust the power of the immersion burner by adjusting the fuel flow rate injected into the burner while maintaining a constant ratio of oxygen flow rate to fuel flow rate. - The furnace is configured such that the heating means is an immersion burner fueled by oxygen / air, and the control device is further configured to inject oxygen or air into the burner and bubbler according to a constant total flow rate of oxygen or air, and into the burner according to a constant ratio of the oxygen or air flow rate to the fuel flow rate, in response to changes in the power of the immersion burner.

[0042] In a fourth aspect of the present invention, equipment for producing mineral fibers is provided. This equipment includes an immersion combustion furnace according to the fourth aspect of the present invention. [Effects of the Invention]

[0043] A first notable advantage of the present invention is obtaining optimal values ​​for the parameters of the transfer function of the control device for an immersion combustion furnace. When the furnace is controlled by a control device calibrated in this manner, the furnace temperature quickly converges to the setpoint temperature in the event of rapid and significant changes in the setpoint temperature T0, the water content in the raw material mixture 1001a, the furnace withdrawal rate, the feed rate of the raw material mixture 1001a, and / or the amount of organic compounds or carbon-containing fuel in the raw material mixture 1001a.

[0044] A second significant advantage is that it is possible to model or even simulate various values ​​for the parameters of the control system's transfer function and select one that enables optimal reactor tuning without requiring physical interference tests on the reactor. Therefore, tuning the control system reduces the load on the reactor. [Brief explanation of the drawing]

[0045] [Figure 1] Figure 1 is a schematic diagram of an example of a glass or rock fiber manufacturing line. [Figure 2]Figure 2 is a schematic cross-sectional view of an immersion combustion furnace for melting a mixture of raw materials containing mineral waste. [Figure 3] Figure 3 is a flowchart of the method according to the first aspect of the present invention. [Figure 4] Figure 4 illustrates the temperature change of an immersion combustion furnace based on the elapsed time after a rapid decrease in power. [Figure 5] Figure 5 is an example of a block diagram of a control device according to a specific embodiment. [Figure 6] Figure 6 illustrates an example of the temporal change in electricity, expressed as a relative change to basic electricity, linked to the time-dependent changes in water content (upper frame) and the amount of organic compounds or carbon-containing fuels (lower frame). [Figure 7] Figure 7 illustrates the temporal changes in power (lower frame) and temperature (solid line, upper frame) of a furnace in which the transfer function parameters of the automatic control system are pre-adjusted according to the present invention. [Figure 8] Figure 8 illustrates the temporal changes in furnace temperature (top frame) and power (middle frame), as well as the amount of material removed from the furnace, based on changes in the water content and amount of organic material in the raw material mixture. [Modes for carrying out the invention]

[0046] Referring to Figure 1, a line 1000 that manufactures glass or rock fibers by internal centrifugation generally has the following: - Silo 1001 for storing raw materials 1001a (e.g., mineral compounds and / or cullet); - A glass or rock melting furnace 1002 for melting raw material 1001a; - A conveyor 1003 transports raw material 1001a from silo 1001 to melting furnace 1002; - One or more fiber forming tools 1005a, 1005b, 1005c supplied with molten glass or rock 1006; - A supply path 1004 which is open or closed, having an opening located directly above each fiber forming apparatus 1005a, 1005b, 1005c, to supply molten glass or rock 1006 thereto.

[0047] Referring to Figure 2, the immersion combustion furnace 1002 generally has at least one refractory melting tank 2001, which is fitted at its base with a group of immersion burners 2002a-c of the oxidizer-fuel type, such as oxygen-gas, air-fuel, or oxygen-fuel. A mixture of raw materials 1001a is supplied to the furnace 1002 by a screw conveyor 1003 through an opening in its side wall. The opening may be submerged or floating. The immersion burners 2002a-c melt the mixture 1001a and agitate the molten material 2004.

[0048] The furnace 1002 may have a second tank 2005, for example, a refining tank, into which the molten material 2004 flows through a throat 2006 provided for this purpose. The second tank 2005 may comprise a plurality of flame burners 2007 positioned above the surface of the molten material 2004, immersion electrodes or non-immersion electrodes, and means 2008 for supplying a refining agent, an oxidizing agent and / or a reducing agent. The means 2088 for supplying the oxidizing agent or reducing agent may be located within the first tank 2001.

[0049] The residence time of the molten material 2004 in the second tank serves to further homogenize it thermally and chemically, and to adjust its oxidation-reduction state according to the specifications. At the end of this residence period, the molten material 2004 forms molten glass or rock 1006, which is then transported via the path 1004 to the fiber forming tools 1005a-c, the glass aggregate manufacturing tools, or the molding tools.

[0050] A temperature measuring device 2009 is provided in the molten tank 2001, for example, a thermocouple 2007, which is either immersed or non-immersed, and is configured to continuously measure the temperature T of the mixture 1001a of the molten raw materials, i.e., the molten material 2004. The temperature measuring device is generally connected to a control device 2010, for example, a proportional-integral-derivative (PID) controller, which enables the control of the furnace according to a setpoint temperature T0. The setpoint temperature T0 can be a fixed value or a time profile.

[0051] The control device 2010 is connected to an immersion burner control device (not shown) and adjusts the power so that the temperature T of the molten material 2004 reaches the setpoint temperature T0. In the case of an oxygen fuel burner, the burner power is adjusted by changing the flow rates of oxygen, fuel, and / or the ratio of these two flow rates.

[0052] The control device 2010 may further be configured to control the amount or flow rate of the oxidizing agent and reducing agent supplied by the supply means 2008. This control may be performed by connecting the supply means 2008 to a control device (not shown). For example, if the supply means 2008 is a conveyor, the control device may change the conveying speed according to a set value provided by the control device 2010.

[0053] Referring to Figures 2 and 3, a first aspect of the present invention provides a method 3000 for calibrating the parameters of an automatic control device 2010 for a furnace 1002, preferably an immersion combustion furnace, for melting a mixture 1001a of raw materials containing mineral waste. - The furnace 1002 comprises at least one tank 2001, which includes at least one heating means 2002a to c, preferably in the form of at least one immersion burner, and at least one control device 2010 configured to adjust the power of the heating means 2002a to c; - The above tank 2001 is suitable for melting the raw material mixture 1001a 2004; - The above tank 2001 has at least one temperature measuring device 2009; - The above temperature measuring device 2009 is configured to continuously measure the temperature of the mixture 1001a of the molten raw material 2004 and is connected to the above control device 2010; The above method 3000 includes the following steps: (a) Continuously introducing a mixture 1001a of raw materials of a predetermined composition into tank 2001; (b) Continuously measure the temperature of the mixture 1001a of the molten raw material 2004 using the temperature measuring device 2009; (c) A predetermined temperature T i Accordingly, the mixture 1001a of the molten raw material 2004 is steadily heated 3003; (d) Without active adjustment by the control device 2010, change at least one operating parameter of the furnace 1002 selected from the moisture content in the raw material mixture 1001a, the furnace withdrawal rate, the feeding rate of the raw material mixture 1001a, the power of the heating means 2002a-c, and / or the amount of organic compounds or carbon-containing fuel in the raw material mixture 1001a over a predetermined limited time 3004; (e) Measure the time-dependent change in the temperature ΔT of the raw material mixture 1001a, which is in a molten state 2004; (f) Using a data processing device, the thermal behavior of the furnace 1002 is modeled using the transient heat transfer function H(s), with the temperature ΔT of the molten raw material mixture 1001a and the time-dependent change of at least one operating parameter modified in process (d) as input data 3006. (g) Using a data processing device, model the parameters of the transfer function C(s) of the control device 2010 that is applied to the transfer function H(s) modeled in process (f) 3007.

[0054] The temperature measuring device 2009 may be a thermocouple or a radiation thermometer.

[0055] In the context of the present invention, "carbon-containing fuel" refers to any type of carbon-based organic mineral fuel, preferably in solid form, that can be added to the raw material mixture 1001a. Examples of carbon-containing fuels include coal or petroleum coke.

[0056] The modeling steps (f) and (g) are typically performed using a data processing device. Examples of such devices include any device adapted to automatically perform a sequence of arithmetic or logical operations to perform a task or operation. Such a device, commonly called a computer, may have one or more central processing units (CPUs) and at least one control unit suitable for performing these operations.

[0057] Similarly, the device may include other electronic components, such as input / output interfaces, non-volatile or volatile memory devices, and communication buses for transferring data between components within the device. One of the input / output devices may be a user interface for human-machine interaction, such as a graphical user interface for displaying human-readable information.

[0058] The data processing unit may advantageously have one or more graphics processing units (GPUs), and this parallel configuration makes them relatively more efficient than a central processing unit in performing complex calculations.

[0059] By step (g), which models the thermal behavior of the furnace 1002 using the transient heat transfer function H(s), a digital model of the furnace 1002 can be obtained. This makes it possible to model the parameters of the transfer function C(s) of the control device 2010, and there is no need to physically intervene in the furnace 1002 to implement this model. In other words, the transfer function H(s) provides a model of the furnace 1002 that the control device 2010 can apply to via its transfer function C(s), thereby determining the parameter values ​​of the device for optimal control of the furnace 1002 in step (g).

[0060] Therefore, by the method according to the first aspect of the present invention, it is possible to select parameters that enable optimal adjustment of the furnace 1002 without the need to model or even simulate various values ​​of the parameters of the transfer function C(s) and to evaluate the adjustment by implementing physical interference tests on the furnace 1002. A notable advantage is that the load on the furnace 1002 is significantly reduced by adjusting the control device 2010.

[0061] In process (f), the thermal behavior of furnace 1002 is modeled using the transient heat transfer function H(s).

[0062] According to one embodiment, the thermal equilibrium of furnace 1002 can be modeled using the following equation:

number

[0063] Here, T is the temperature of the furnace 1002 containing the molten material 2004, t is the time, M is the mass of the furnace 1002 containing the molten material 2004, and c p δ(t) is the heat capacity per unit mass of the furnace containing the molten material 2004, P(t) is the power of the heating means at time t, φ is the power required to melt the raw material mixture 1001a at a predetermined input rate, and I(t)=δ(t)+Ω(t) is the instantaneous change in power due to the time-dependent changes in the water content δ(t) and the amount of organic or combustible carbon-containing compounds Ω(t) in the raw material mixture 1001a.

[0064] The power I(t) may further include the temporal variation of the furnace output ψ(t) and / or the feeding rate v(t) of the raw material mixture 1001a.

[0065] Generally, in the case of heat transfer such as convection, the power φ is determined by the temperature T(t) of the furnace 1002 containing the molten material 2004 at time t and the so-called virtual boundary layer temperature T p It changes in proportion to the deviation from the boundary layer temperature T. pThis can be interpreted as a temperature representative of the temperature of the molten material 2004 near the wall of furnace 1002 and the temperature of the unmolten raw material mixture 1001a. The power φ can then be estimated using the following ratio:

number

[0066] Here, β and T p This is a constant that is unknown beforehand.

[0067] Let x(t) = T(t) - T0 and u(t) = P(t) - P0, where T0 is the setpoint temperature and P0 is the basic power required to reach the setpoint temperature T0 without interference, i.e., I(t) = 0. The transient heat transfer function H(s) in the Laplace domain can be as follows:

number

[0068] Here,

number

[0069] and,

number

[0070] In the initial state, i.e., before any interference with furnace 1002, the temperature T(t) of furnace 1002 follows the setpoint temperature T0, i.e., with respect to the basic output P0, T(t) = T0:

number

[0071] and,

number

[0072] Values ​​M, c p , T p β is generally unknown and depends on the structure of the furnace 1002, its constituent materials, the chemical properties of the molten material 2004, and its quantity. β also depends on the rate at which the raw material mixture 1001a is fed in.

[0073] According to a first aspect of the present invention, the thermal behavior of the furnace 1002 is modeled using a transfer function H(s), with the time-dependent changes in the temperature ΔT of the molten raw material mixture 1001a and the operating parameters changed in process (d) as input data. The time-dependent changes in the temperature ΔT of the molten raw material mixture 1001a and the operating parameters changed in process (d) can be interpreted as the result of interference introduced by the change in at least one operating parameter of the furnace in process (d). By utilizing this interference, the parameters of the transfer function H(s), particularly the constant γ and temperature T, can be used. p It is possible to calculate this.

[0074] According to a particular embodiment, the transient heat transfer function H(s) is modeled using a first-order response transfer function, with or without a delay time.

[0075] Generally, immersion combustion furnaces have a certain inertia, and when one of their operating parameters is changed abruptly in the form of an impulse, the response of the furnace 1002 is not immediate. The furnace 1002 exhibits a delay in its response to interference.

[0076] According to one embodiment, the response to a power impulse response, for example, a rapid power change of the form of a unit step U(s) = ΔP / s, and a zero change in water content and organic compound content ΔI = Δδ + ΔΩ = 0, can be described as follows:

number

[0077] Here, ΔP = P1 - P0 represents the change from the initial power P0 to a different power P1 in the form of a unit process. In the time domain, this function is represented by the following equation for t > 0:

Number

[0078] Parameters γ and T p The values of can be obtained by adjusting the function f(t) with respect to the changes in the temperature ΔT of the molten raw material mixture 1001a and the power ΔP of the heating means 2002a - c over time.

[0079] In step (d), without active adjustment by the control device 2010 for a predetermined limited time, at least one operating parameter of the furnace 1002 is changed, which is selected from the moisture content in the raw material mixture 1001a, the furnace withdrawal amount, the input rate of the raw material mixture 1001a, the power of the heating means 2002a - c, and / or the amount of organic compounds or carbon-containing fuels in the raw material mixture 1001a.

[0080] The number and nature of the operating parameters to be changed depend on the composition of the raw material mixture containing mineral waste and the accuracy required for the calibration of the control parameters.

[0081] According to a specific embodiment, in step (d), at least two, or even three, operating parameters are changed sequentially or in parallel. Changing at least two, or even three, parameters is generally sufficient for typically modeling the thermal behavior of the furnace, especially an immersion combustion furnace, and for accurately modeling the parameters of the transfer function of the control device 2010 for ultimately effective adjustment.

[0082] As described above, the moisture level and the content of organic compounds or carbon-containing fuels in mineral waste can vary significantly depending on their source and storage method. Over the operating time of an immersion combustion furnace, a raw material mixture containing mineral waste at a predetermined ratio can exhibit rapid and significant changes in its moisture level and the content of organic compounds or carbon-containing fuels.

[0083] Therefore, according to a particular embodiment, in step (d), the moisture content in the raw material mixture 1001a is changed so that the change in the moisture content of the mixture is 0 to 10%, and / or the amount removed from the furnace is changed so that the relative change in the amount removed is 0 to 2000 kg / h.

[0084] These ranges of variation in furnace output and the moisture content of the raw material mixture, including mineral waste, allow for the effective calibration of the control system of the furnace, particularly immersion combustion furnaces.

[0085] According to a particular embodiment, the furnace 1002 may have at least one means 2011 for measuring the moisture content of the raw material mixture 1001a. This means may be any type of moisture sensor suitable for measuring the moisture content of the raw material mixture 1001a. It may be placed on the conveyor 1003 immediately before loading, or even further upstream in the storage silo 1001. The moisture measuring means 2011 enables accurate measurement of the change in the moisture content of the mixture 1001a in process (d).

[0086] In another embodiment, in step (d), the amount of organic compound in the raw material mixture 1001a is changed so that the relative change in the amount of organic compound or carbon-containing fuel is 0 to 15% by weight, preferably 0 to 10% by weight.

[0087] The range of change in the amounts of these organic compounds makes it possible to model the transfer function H(s) of the reactor 1002, and then the transfer function C(s) of the control device 2010. When these functions are finally implemented in the device 2010, the temperature of the reactor 1002 will rapidly converge to the setpoint temperature when the content of organic compounds or carbon-containing fuel in the raw material mixture containing mineral waste changes rapidly and significantly.

[0088] In other embodiments, whether complementary or not, in step (d), the power of the heating means (2002a-c) is changed such that the relative change in the power with respect to the initial power is 0-100%, preferably 0-50%, or even 0-25%.

[0089] As an example, Figure 4 shows the time-based temperature (dotted line) of an immersion combustion furnace after introducing 5.7% coke by mass into the raw material mixture 1001a, and then rapidly reducing the furnace power from 287 kW to 173 kW. Due to the energy released by the combustion of the coke, the temperature of the furnace 1002 initially rose from T0 = 1175°C to 1288°C. In Figure 4, time t=0 corresponds to the moment when the power rapidly decreased from 287 kW to 173 kW in the form of a unit process. The temperature progression is shown by the dotted line.

[0090] The aforementioned response function f(t) for the impulse response can be described as follows, using P0 = 287 kW, P1 = 173 kW, and T0 = 1175 °C:

number

[0091] Parameter T p And to determine the value of γ, the response function f(t) is given by the least squares method on the data in [Figure 4], T p And γ may be adjusted as adjustment parameters. The optimal adjustment is shown by the solid line in [Figure 4], with parameter T p And yields the following values ​​for γ:

number

number

[0092] Therefore, the transfer function H(s) that enables modeling of the thermal behavior in this example can be described as follows: TIFF2026519499000014.tif15169

[0093] Mc is a value representing the heat capacity of furnace 1002, which is independent of its mass. p This can be calculated as follows:

number

[0094] In step (g), the parameters of the transfer function C(s) of the control device 2010 are modeled by applying them to the transfer function H(s) of the furnace 1002, which is obtained in step (f).

[0095] After modeling the thermal behavior of furnace 1002 using the transfer function H(s), it becomes possible to model the parameters of the transfer function C(s) of the control device 2010 that is applied to the furnace's transfer function H(s).

[0096] This modeling may be implemented, in particular, by simulation, which determines the optimal parameters of the transfer function C(s) for the effective tuning of reactor 1002 outside of the field. Numerical computation software packages, such as Matlab® or Scilab, provide functions and algorithms suitable for this type of simulation.

[0097] Referring to Figure 5, an example of modeling may consist of an iterative optimization loop that adjusts the parameters of the control device's transfer function C(s) until the setpoint power P calculated by the function C(s) from the deviation ε between the temperature T of the furnace 1002 and the setpoint temperature T0 of the furnace 1002 allows the furnace 1002 to reach the setpoint temperature T0 when the power P increases by power I(s) and is given as input data to the transfer function H(s) of the furnace 1002. I(s) = δ(s) + Ω(s) is the instantaneous power change related to the time-dependent changes in the water content δ(s) and the amount Ω(s) of organic compounds or carbon-containing fuel in the raw material mixture 1001a.

[0098] During the execution of the iterative execution loop, the parameters of the transfer function C(s) of the control device 2010 may be manually adjusted using adjustment methods such as the Ziegler-Nichols method, the Cohen-Kuhn method, or the Ostrom-Hägglund method, or they may be automatically adjusted using numerical optimization methods.

[0099] Using the transfer function H(s) from the example in [Figure 4], the figure in [Figure 5] can be rewritten, for example, using the following equation:

number

number

[0100] Let ε(t) = -x(t). Therefore: TIFF2026519499000018.tif12169

[0101] In a preferred embodiment, the control device 2010 is a proportional-integral-derivative (PID) tuner.

[0102] The transfer function C(s) of the control device 2010 can be described in the Laplace domain as follows:

number

[0103] Here, Kp, Ki, and Kd are the parameters or gains of the proportional, integral, and derivative functions, respectively.

[0104] According to another notation, the transfer function C(s) can take the following form:

number

[0105] Here, τ i and τ d These are the integral time constant and the differential time constant, respectively, and τ i=Kp / Ki=KpTi, and τ d =Kd / Kp=Td / Kp

[0106] In most industrial furnaces, the temperature measurement T of the molten raw material mixture 1001a has been found to be subject to significant noise. To avoid adjustment deviations, it may be advantageous to ignore the derivative term of the transfer function C(s) without significantly affecting the adjustment capability of the control device.

[0107] In that case, the function C(s) can be written as follows:

number

[0108] Or it could be described as follows:

number

[0109] The transfer function C(s) allows for the real-time calculation of the gain for correcting the setpoint of the power regulator of heating means 2002a-c, which are at least one immersion burner configuration. The unit of the gain depends on the type of regulator used. For example, in the case of an immersion burner, it may correspond to a percentage of the fuel flow rate, e.g., gas volume flow rate, injected into the burner. The flow rate value can be associated with the burner power level according to a linear relationship.

[0110] Based on the example above, the setpoint value at the output of the control device 2010 can be described as follows:

number

[0111] The setpoint power P at the inlet to furnace 1002 can be described as follows:

number

[0112] Parameters Kp and τ of the transfer function C(s) of control device 2010 i The modeling can consist of adjusting values ​​that minimize the time-dependent change in temperature in the simulation of the system being tuned.

[0113] This adjustment may be performed manually using adjustment methods such as the Ziegler-Nichols method, the Cohen-Kuhn method, or the Ostrom-Hägglund method, or it may be performed automatically using numerical optimization methods.

[0114] In the example shown in [Figure 4], when the measurement frequency α of the temperature measuring device 2009 is set higher than γ, i.e., when α = 1 Hz, the parameters Kp and τ i This requires iterative adjustment so that x(t) approaches zero over time. The advantage is that it is possible to evaluate the time-dependent stability of the furnace during control, even when interferences considered normal for applications in the glass industry are added. Another advantage is that the sampling frequency of the temperature measurement device 2009 can be taken into account during modeling.

[0115] According to a particular embodiment, in step (g), the transfer function H(s) of the furnace 1002 further takes as input data a set of simulated values ​​I(s) of changes in the water content of the raw material mixture 1001a, the amount removed from the furnace, the rate at which the raw material mixture 1001a is fed, the amount of carbon-containing organic compound or fuel, and / or the value of the setpoint temperature T0.

[0116] According to a particular embodiment, the water content in the raw material mixture 1001a, the amount removed from the furnace, the rate at which the raw material mixture 1001a is fed in, and / or the amount of organic compounds or carbon-containing fuel are simulated as random signals, such as white noise or pink noise.

[0117] According to the modeling example of the parameters Kp and τi of the transfer function C(s) of the control device in the examples of [Figure 4] and [Figure 5], referring to [Figure 6], the instantaneous change of power I(t) = δ(t) + Ω(t) related to the time-dependent change of water content (upper frame) and the amount of organic compounds or carbon-containing fuel Ω (lower frame) is first generated in the form of pink noise, as relative changes δ(t) and Ω(t). Then, the parameters Kp and τ i The value is repeatedly adjusted manually to obtain a temperature close to the setpoint temperature over time.

[0118] Figure 7 shows the corresponding changes in the power (lower frame) and temperature (solid line, upper frame) of furnace 1002, which correspond to the parameters Kp and τ. i This is obtained by adjusting the following values:

number

number

[0119] [Figure 7] shows these parameters Kp and τ i The value of [ ] across the entire set of instantaneous changes in power I(s) in [Figure 6] indicates that it enables effective automatic control of the temperature T (solid line, upper frame) of the furnace 1002 to the setpoint temperature T0 (dashed line, upper frame).

[0120] The parameters Kp and τ are adjusted in this manner. i To verify the performance of the control devices calibrated with the specified value, these were implemented in a device that automatically controls an industrial furnace having the same transfer function H(s), as shown in the examples in Figures 4 and 5. The industrial furnace, operating under actual industrial conditions, was subjected to rapid changes in the setpoint temperature T0, its output volume, moisture content, and the amount of organic matter or carbon-containing fuel, such as coke, contained in the raw material mixture.

[0121] Figure 8 shows the behavior of the furnace under these changes. The upper frame shows the temporal changes in furnace temperature (upper frame, solid line) and setpoint temperature T0 (dotted line). The middle frame shows the temporal changes in furnace power. The lower frame shows rapid changes in the amount of material extracted from the furnace (dashed line), moisture content (solid line), and organic material or carbon-containing fuel (dotted line) from the raw material mixture.

[0122] The upper frame of [Figure 8] shows that the furnace temperature (solid line) rapidly converges to the setpoint temperature T0 (dotted line), regardless of the nature and simultaneity of the changes (lower frame).

[0123] A rapid change in moisture content δ (solid line) causes a slight disturbance to the power (center frame), and the furnace temperature (solid line) deviates slightly from the setpoint temperature T0 (dotted line). A rapid change in the furnace extraction amount ψ (bottom frame, dashed line) after 5 hours and just before 15 hours causes a rapid change in power (center frame), and the temperature (solid line) converges very quickly toward the setpoint temperature T0 (dotted line) after the initial deviation. At approximately 17 hours, the amount of organic material or carbon-containing fuel Ω (bottom frame, dotted line) changed rapidly, causing frequent changes in power, but this is quickly compensated for.

[0124] Furthermore, the control device can compensate for rapid and simultaneous changes in the setpoint temperature T0 (upper frame, dotted line), furnace extraction volume (lower frame, dashed line), moisture content (lower frame, solid line), and amount of organic material or carbon-containing fuel (lower frame, dotted line) after 7:30 a.m. and 7:00 p.m.

[0125] The test shown in [Figure 8] demonstrates that the present invention enables effective and robust calibration of a device for automatically controlling an immersion combustion furnace. The control device 2010 allows for rapid and abrupt compensation for rapid and violent changes in the setpoint temperature T0 (a 40°C change in the figure), the water content in the raw material mixture 1001a, the furnace withdrawal rate, the feed rate of the raw material mixture 1001a, and / or the amount of organic compounds in the raw material mixture 1001a. The temperature of the furnace 1002 rapidly converges to the setpoint temperature, while keeping the amplitude of overshoot over time extremely limited, regardless of the nature and simultaneity of the changes.

[0126] All embodiments of the first aspect of the present invention can be combined.

[0127] The method according to the first aspect of the present invention can be advantageously used to calibrate a device 2010 that automatically controls a furnace 1002, preferably an immersion combustion furnace, for melting a mixture 1001a of raw materials containing mineral waste.

[0128] A second aspect of the present invention, with reference to Figures 2 and 3, provides a method for calibrating the parameters of an automatic control device 2010 for a furnace 1002, preferably an immersion combustion furnace, for melting a mixture 1001a of raw materials containing mineral waste. - The furnace 1002 has at least one tank 2001 comprising at least one heating means 2002a-c, which is in the form of at least one immersion burner; - Tank 2001 is suitable for melting the raw material mixture 1001a; The above system has the following: - A temperature measuring device 2009, wherein at least one temperature measuring device 2009 is configured to continuously measure the temperature of the mixture 1001a of the molten raw material 2004; - At least one control device 2010 configured to adjust the power of the heating means 2002a to c; the parameters of the transfer equation C(s) of the control device 2010 are calibrated using a method according to any embodiment of the first aspect of the present invention.

[0129] According to a third aspect of the present invention, a furnace 1002, preferably an immersion combustion furnace, is provided for melting a mixture 1001a of raw materials containing mineral waste, wherein the furnace 1002 has the following: - A first tank 2001, suitable for melting a mixture of raw materials 2004, and comprising at least one heating means 2002a-c, which is in the form of at least one immersion burner. - At least one temperature measuring device 2009 for continuously measuring the temperature of the above mixture 1001a of the molten raw material 2004. - At least one control device 2010 configured to adjust the power of the heating means 2002a to c and to receive at least one continuous temperature measurement using the temperature measuring device 2009; the parameter values ​​of the transfer function C(s) of the control device 2010 are fixed from values ​​obtained using a calibration method according to any embodiment of the first aspect of the present invention.

[0130] A calibration method that enables the determination of parameter values ​​for the transfer function C(s) of the control device 2010 can be implemented using a system according to a second aspect of the present invention.

[0131] Similar to the first aspect of the present invention, the furnace 1002 may have at least one means 2011 for measuring the moisture content of the raw material mixture 1001a.

[0132] According to a particular embodiment, the heating means 2002a to c are oxygen / air fuel immersion burners, and the control device 2010 is further configured to adjust the power of the immersion burner by adjusting the fuel flow rate injected into the burner while maintaining a constant ratio of oxygen flow rate to fuel flow rate.

[0133] According to a particular embodiment, the heating means 2002a to c are oxygen / air fuel immersion burners, and the control device 2010 is further configured to inject oxygen or air into the burner and bubbler according to a constant total flow rate of oxygen or air, and into the burner according to a constant ratio of the oxygen or air flow rate to the fuel flow rate in response to changes in the power of the immersion burner.

[0134] In a fourth embodiment of the present invention, equipment for manufacturing mineral fibers, such as glass fibers or rock fibers, is provided, which includes a furnace 1002 according to any embodiment of the third aspect of the present invention.

[0135] In all its embodiments, and without limitation, the present invention can be implemented in numerous processes and manufacturing lines relating to glass articles, such as glass wool, rock wool, woven glass fibers, flat glass, or hollow glass.

[0136] Reference list: Patent documents: U.S. Patent No. 351413, J. Twanwright, October 26, 1886. U.S. Patent No. 1,656,828, Powell Edward R, January 17, 1928. French Patent No. 876569, UNION DES VERRERIES MECANAIQUES, November 10, 1942. International Publication No. 2009 / 091558, GAS TECHNOLOGY INST [US] July 29, 2009. German Patent No. 651687, GLASHUETTE ACHERN AG, October 18, 1937. British Patent Application Publication No. 1028481, SELAS CORP OF AMERICA, May 4, 1966. International Publication No. 2002 / 048612, SAINT GOBAIN [FR], June 20, 2002. International Publication No. 2006 / 018582, SAINT GOBAIN ISOVER[FR] February 23, 2006. U.S. Patent No. 4,877449, INST GAS TECHNOLOGY [US], October 31, 1989. European Patent Application No. 2433911, JOHNS MANVILLE [US] March 28, 2012. International Publication No. 2022 / 180345, SAINT GOBAIN ISOVER[FR] September 1, 2022.

Claims

1. A method (3000) for calibrating the parameters of a device (2010) that automatically controls a furnace (1002), preferably an immersion combustion furnace, for melting a mixture of raw materials (1001a) containing mineral waste, - The furnace (1002) comprises at least one heating means (2002a to c), preferably in the form of at least one immersion burner, at least one tank (2001), and a set point temperature T ０ The system has at least one control device (2010) configured to adjust the power of the heating means (2002a-c) accordingly; - The tank (2001) is suitable for melting (2004) the raw material mixture (1001a), - The tank (2001) has at least one temperature measuring device (2009), - The temperature measuring device (2009) is configured to continuously measure the temperature of the mixture (1001a) of the molten raw material (2004) and is connected to the control device (2010); The above method (3000) includes the following steps: (a) Continuously introducing a mixture of raw materials of a predetermined composition (1001a) into the tank (2001) (3001); (b) Continuously measuring the temperature of the mixture (1001a) of the molten raw material (2004) using the temperature measuring device (2009) (3002); (c) The mixture of molten raw materials (1001a) is heated to a predetermined temperature T ｉ To maintain steady heating according to (3003); (d) For a predetermined limited time, without active adjustment by the control device (2010), change at least one operating parameter of the furnace (1002), which is selected from the water content in the raw material mixture (1001a), the amount of material removed from the furnace, the rate at which the raw material mixture (1001a) is fed in, the power of the heating means (2002a-c), and / or the amount of organic compounds or carbon-containing fuel in the raw material mixture (1001a) (3004); (e) Measuring the time-dependent change in the temperature ΔT of the mixture (1001a) of the raw materials in a molten state (2004) and the power ΔP of the heating means (2002a-c) (3005); (f) Using a data processing device, the thermal behavior of the furnace (1002) is modeled using a transient heat transfer function H(s), with the temperature ΔT of the molten raw material mixture (1001a) and the time-dependent changes of at least one operating parameter changed in process (d) as input data (3006). (g) Using a data processing device, model the parameters of the transfer function C(s) of the control device (2010) that is applied to the transfer function H(s) modeled in process (f) (3007), Method (3000), including the above.

2. The method according to claim 1 (3000), wherein the transient heat transfer function H(s) is modeled using a first-order response transfer function, regardless of the presence or absence of a delay time.

3. The method according to claim 1 or 2 (3000), wherein in step (d), at least two parameters, preferably three parameters, are changed sequentially or in parallel.

4. The method according to any one of claims 1 to 3 (3000), wherein in step (d), the water content in the raw material mixture (1001a) is changed so that the change in the water content of the mixture is 0 to 10%, and / or the extraction amount from the furnace is changed so that the relative change in the extraction amount is 0 to 2000 kg / h.

5. The method according to any one of claims 1 to 4 (3000), wherein in step (d), the amount of the organic compound or carbon-containing material in the raw material mixture (1001a) is changed so that the relative change in the amount of the organic compound or carbon-containing fuel is 0 to 15% by weight, preferably 0 to 10% by weight.

6. The method according to any one of claims 1 to 5 (3000), wherein in step (d), the power of the heating means (2002a to c) is changed so that the relative change of the power with respect to the initial power is 0 to 100%, preferably 0 to 50%, and more preferably 0 to 25%.

7. The method according to any one of claims 1 to 6 (3000), wherein the control device (2010) is a proportional-integral-derivative (PID) controller.

8. In step (g), the transfer function H(s) of the furnace (1002) is further defined as input data including the water content in the raw material mixture (1001a), the amount removed from the furnace, the rate at which the raw material mixture (1001a) is fed in, the amount of carbon-containing organic compound or fuel, and / or the setpoint temperature T. ０ The method according to any one of claims 1 to 7 (3000), wherein the set I(s) is a set of simulated values ​​of the change in the value of .

9. The method according to claim 8 (3000), wherein the moisture content of the raw material mixture (1001a), the amount removed from the furnace, the feeding rate of the raw material mixture (1001a), and / or the amount of the organic compound or carbon-containing fuel are simulated as a random signal, such as white noise or pink noise.

10. A use of the method (3000) according to any one of claims 1 to 9, for calibrating a device (2010) that automatically controls a furnace (1002), preferably an immersion combustion furnace, for melting a mixture of raw materials (1001a) containing mineral waste.

11. A system for calibrating the parameters of a device (2010) that automatically controls a furnace (1002), preferably an immersion combustion furnace, for melting a mixture of raw materials (1001a) containing mineral waste, - The furnace (1002) has at least one tank (2001) comprising at least one heating means (2002a to c) which is in the form of at least one immersion burner; - The tank (2001) is suitable for melting (2004) the raw material mixture (1001a); The aforementioned system is as follows: - A temperature measuring device (2009) comprising at least one temperature measuring device (2009) configured to continuously measure the temperature of the mixture (1001a) of the molten raw material (2004); - At least one control device (2010) configured to adjust the power of the heating means (2002a-c); A system having a control device (2010) wherein the parameters of the transfer equation C(s) of the control device (2010) are calibrated using the method (3000) according to any one of claims 1 to 9.

12. A furnace (1002), preferably an immersion combustion furnace, for melting (2004) a mixture of raw materials (1001a) containing mineral waste, wherein the furnace (1002) is as follows: - A first tank (2001) suitable for melting a mixture of raw materials (2004) and comprising at least one heating means (2002a-c) in the form of at least one immersion burner, - At least one temperature measuring device (2009) for continuously measuring the temperature of the mixture (1001a) of the molten raw material (2004), - At least one control device (2010) configured to adjust the power of the heating means (2002a-c) and to receive at least one continuous temperature measurement using the temperature measuring device (2009); It has, A furnace (1002) in which the parameter values ​​of the transfer function C(s) of the control device (2010) are fixed from values ​​obtained using the calibration method (3000) described in any one of claims 1 to 9.

13. The furnace (1002) according to claim 12, wherein the heating means (2002a-c) is an oxygen / air fuel immersion burner, and the control device is further configured to adjust the power of the immersion burner by adjusting the fuel flow rate injected into the burner while maintaining a constant ratio of the oxygen flow rate to the fuel flow rate.

14. The furnace according to claim 12, wherein the heating means (2002a-c) is an oxygen / air fuel immersion burner, and the control device (2010) is further configured to inject oxygen or air into the burner and bubbler according to a constant total flow rate of oxygen or air, and into the burner according to a constant ratio of the oxygen or air flow rate to the fuel flow rate in accordance with changes in the power of the immersion burner.

15. Equipment for manufacturing mineral fibers, comprising an immersion combustion furnace (1002) according to any one of claims 12 to 14.

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