Method and system for calibrating the parameters of a furnace control device

Abstract

Method for calibrating the parameters of a control device for a furnace, preferably a submerged combustion furnace, for melting a mixture (1001a) of raw materials including mineral waste. The method allows for obtaining optimal values ​​for the parameters of the transfer function of the control device.It is based on: - modeling the thermal behavior of the furnace (1002) using a non-stationary heat transfer function H(s) with, as input data, the temporal variations of the temperature ΔT of the mixture (1001a) of molten raw materials; said variations being measured following the modification (3004), for a given and limited period of time, of at least one operating parameter of the furnace (1002) chosen from among the moisture content in the mixture (1001a) of raw materials, the furnace draft, the loading speed of the mixture (1001a) of raw materials, the power of the heating means (2002a-c), and / or the quantity of organic compounds or carbonaceous fuels in the mixture (1001a) of raw materials; - modeling the parameters of the transfer function C(s) of the control device (2010) applied to the modeled transfer function H(s).

Description

Title of the invention: Method and system for calibrating the parameters of a furnace control device. Technical field

[0001] The present invention relates to a method and a system for calibrating the parameters of a control device for a furnace, preferably a submerged combustion furnace, for melting a mixture of raw materials including mineral waste. It also relates to a furnace, preferably a submerged combustion furnace, that implements said method or system. Technical background

[0002] It is common practice to use a submerged combustion furnace (SCF), also called a submerged burner furnace (SBF), for melting a mixture of vitrifiable raw materials. In this type of furnace, combustion means such as oxygen / air-fuel burners are directly immersed in the mixture of vitrifiable raw materials and in the resulting molten glass bath. The direct injection, in the form of a stream, of reactants and combustion gases into the glass bath, followed by their rapid expansion and rise, accelerates melting and improves the homogeneity of the bath.

[0003] US 351 413 B, JT WAINWRIGHT 26.10.1886 describes, for example, a method of injecting air and / or fuel such as gas or petroleum into a molten glass bath in such a way that said gases circulate and heat through the bath before their combustion takes place under or near the surface of the bath. The bath is thus constantly stirred and mixed, thereby keeping it hot.

[0004] US 1 656 828 A, POWELL EDWARD R, 17.01.1928 describes a process and apparatus for manufacturing rock wool in which a mixture of raw materials is introduced into a vertical tank equipped with an adjacent inclined combustion chamber. The combustion chamber includes a burner arranged so that the combustion gases enter and melt the mixture of raw materials at the bottom of the tank. At the base of the tank, an opening allows the molten glass to flow through an air jet for blowing the molten glass into fibers.

[0005] FR 876569 A, UNION DES VERRERIES MECANIQUES, 10.11.1942 describes a submerged combustion furnace comprising a vertical tank equipped, in its lower part, with at least one submerged burner with a combustion fluid pressure of more than 0.2 atmospheres and a speed greater than 30 meters per second.

[0006] WO 2009 091 558 Al, GAS TECHNOLOGY INST [US] 29.07.2009 describes a furnace Immersed combustion comprising a double-walled fluid-circulating furnace. The furnace floor is equipped with a plurality of immersed burners whose relative spatial arrangement is optimized to improve the thermal homogeneity of the glass bath and reduce the number of unmelted pieces.

[0007] In addition to the tank adapted for melting the mixture of vitrifiable raw materials, a submerged combustion furnace may include one or more other adjacent tanks in communication with the first tank, into which the molten glass flows from the first tank to undergo various treatments such as, in particular, refining.

[0008] DE 651 687 C, GLASHUETTE ACHERN AG, 18.10.1937 describes a furnace comprising a vertical, rotating melting tank fed with raw materials through a top opening by means of a hopper. The tank includes, in the center of its lower base, oriented along the axis of revolution of the tank, a submerged burner, and is provided, around the periphery of said lower base, with openings allowing the flow of glass to a lower refining tank.

[0009] GB 1 028 481 A, SELAS CORP OF AMERICA, 04.05.1966 describes a furnace equipped with a plurality of melting tanks, each comprising, in the center of its lower base, several immersed burners. The furnace further comprises a main refining tank into which the molten glass from the melting tanks flows.

[0010] In the context of the manufacture of mineral fibers, the mixture of vitrifiable raw materials used in a submerged combustion furnace includes mineral materials that are sources of oxides, hydroxides and / or carbonates of metals, metalloids, alkalis and / or alkaline earths, the relative proportions of which are adjusted so as to obtain the desired chemical composition of the glass after melting.

[0011] Mineral materials are generally mining materials such as, for example, silica sand, bauxite, dolomite, calcium carbonates, magnesium carbonates and / or sodium carbonate. They may also be mineral co-products of other manufacturing industries.

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

[0013] A first example of recyclable mineral waste is "cullet", of which two types are distinguished: - the so-called "internal" cullet, which can include glass waste from the same manufacturing process or the same glass product production line, and generally includes cutting rejects, detected defective products, and rejected during quality control or during adjustments to product compositions; - the so-called "external" cullet which may include glass waste collected from other processes or manufacturing lines of glass products, from consumers with the aim of recycling glass products after their use, for example deconstruction waste, glass bottles, used glazing....

[0014] Generally speaking, and especially for external cullet, cullet is a mixture of glass fragments of different colors and compositions. The surface of these fragments may also be covered with organic and / or inorganic layers, resulting from various surface functionalization processes used in certain glass product applications. Finally, cullet may also include a number of foreign body fragments such as ceramics, earthenware, porcelain, terracotta, plastics, metals, electronic components, etc.

[0015] A second example of recyclable mineral waste is mineral fiber waste, whether coated or not, i.e., with or without an organic binder. This waste can originate from manufacturing industries, construction sites or other works and / or recycling channels.

[0016] A third example of recyclable mineral waste is raw materials from biomass recovery processes of plant, animal, bacterial, or fungal origin. This material can be used as fuel, but also as a means of adjusting the composition of glass and / or its redox state.

[0017] By their origin, recyclable mineral waste, particularly external waste, has varying levels of moisture and / or organic matter. When introduced into the furnace, this moisture and organic matter alter the furnace's thermal and chemical balance and cause abrupt variations in the temperature of the glass bath. The refining and redox equilibrium processes of the glass bath are also disrupted. The steady-state heating and refining regime of the furnace is thus destabilized. This can lead to reduced yields and the generation of non-conforming glass products for the intended applications, particularly for the manufacture of mineral fibers.

[0018] It is therefore common to carry out preliminary treatments of mineral waste to reduce, or even eliminate, the moisture and organic compounds they contain.

[0019] WO 0248612 A1, SAINT GOBAIN [FR] 20.06.2002 describes, for example, a process for destroying and / or inerting mineral waste, making it possible in particular to obtain a cullet that can be used for the subsequent manufacture of mineral wool. In this process, the mineral waste is introduced into a liquid and / or foamy phase maintained at a temperature of at least 800°C and previously formed in a tank equipped with a submerged burner from a mixture of partially vitrifiable materials.

[0020] WO 2006 018 582 Al, SAINT GOBAIN ISOVER [FR] 02.23.2006 describes a A process for treating mineral waste, particularly mineral fiber waste, in which pure oxygen or oxygen-enriched air is injected into a mass of material to be recycled, which is then heated by submerged burners. Through the combustion of organic compounds and the melting of the mass, a valuable cullet can be obtained for the subsequent manufacture of glass fibers.

[0021] US 4877449 ​​A, INST GAS TECHNOLOGY [US] 31.10.1989 describes a submerged combustion furnace comprising a vertical vessel equipped, in its upper part, above the glass bath, with a cooled grid onto which solid charges are deposited by means of a hopper. The combustion gases from the glass bath pass through the grid and heat the solid charges, causing them to melt and the resulting liquid to flow into the glass bath.

[0022] Alternatively, it is possible to introduce glass waste directly, i.e., without prior treatment, into the glass bath of a furnace, in particular a submerged combustion furnace intended for the manufacture of mineral fibers. Generally, a control system, such as a feedback control loop, is implemented for at least one operating, functional, or control parameter of the furnace, which compensates for disturbances to which the furnace is subjected relative to its steady state. Such an approach is made possible by the very low thermal inertia inherent in submerged combustion furnaces, especially those with a double wall and fluid circulation.

[0023] EP 2 433 911 A1, JOHNS MANVILLE [US] 28.03.2012 describes a method and device for recycling a glass wool mattress, wherein said mattress is introduced into the glass bath of a submerged combustion furnace at a uniform feed rate. A PID control device or a predictive control system allows the regulation, at the output, of several furnace operating parameters, in particular the speed of the mattress conveyors, from various input signals, such as the temperature of the glass bath, the draft and / or the flow rate of fuel and / or oxidizer in the burners.

[0024] WO 2022 / 180 345 A1, SAINT GOBAIN ISOVER [FR] 01.09.2022 describes a method for regulating a submerged combustion furnace fed with a wet mixture of mineral wool and / or biomass, wherein the feed rate of the mixture or the power of the submerged burners is regulated by means of a PID control device based on a measurement of the moisture content of said mixture. Summary of the invention Technical problem

[0025] A major drawback of processes comprising a preliminary treatment step The challenge with recyclable mineral waste is that it requires more complex facilities or treatments, and therefore more substantial material and financial investments for its implementation.

[0026] It is therefore advantageous to favor processes and systems based on the direct introduction, i.e., without prior treatment, of a mixture of raw materials including mineral waste into the furnace. The distinctive feature of these processes and systems is that they require the implementation and configuration of control systems and processes, such as feedback loops, or predictive control systems.

[0027] However, despite progress made in the automation of control systems with regard to their configuration and calibration, these remain not trivial for furnaces, particularly submerged combustion furnaces, for melting a mixture of raw materials including mineral waste.

[0028] The moisture content and organic compound content of mineral waste vary considerably depending on its origin and storage conditions. Thus, during the operating time of a furnace, particularly a submerged combustion furnace, a mixture of raw materials containing mineral waste in given proportions is highly likely to exhibit sudden and significant variations in its moisture content and organic compound content.

[0029] Furthermore, the proportion of mineral waste in the mixture is likely to vary depending on the ease or difficulty of obtaining raw materials. These variations can also contribute to sudden and significant changes in the moisture content and organic compound content of the mixture. As explained previously, such variations cause significant disturbances in the furnace's thermal and chemical balance. The furnace deviates from its steady state and can switch to unstable operating regimes.

[0030] It is also common practice to add carbon-based mineral organic fuels, generally solid, to the 1001a mixture of raw materials. These fuels provide an additional energy source for the furnace and are often sourced from energy recovery channels. The type and quantity of fuel can vary considerably depending on its origin and market availability. A typical example of fuel is coal or petroleum coke.

[0031] However, it has been observed that control systems, configured and calibrated automatically, are generally incapable of correcting or compensating, in a rapidly convergent manner and with limited setpoint overshoot amplitudes, the disturbances caused by sudden and intense variations in the humidity level and the content of organic compounds or carbonaceous fuels of the mixture of raw materials.

[0032] There therefore remains a need for a method and a system allowing reliable and efficient calibration of the control devices of a furnace, in particular with immersed combustion, allowing a rapid convergent response in the event of sudden and intense variations in the humidity level and / or the content of organic compounds or carbonaceous fuels of a mixture of raw materials including mineral waste.

[0033] Solution to the technical problem

[0034] In a first aspect of the invention, a method is provided for calibrating the parameters of a control device for a furnace, preferably a submerged combustion furnace, for melting a mixture of raw materials comprising mineral waste. - said oven includes at least one tank equipped with at least one heating means, preferably in the form of at least one immersed burner, and at least one control device configured to regulate the power of said heating means according to a setpoint temperature, T0; - said tank is suitable for melting a mixture of raw materials; - said tank includes at least one temperature measuring device; - said temperature measuring device is configured for the continuous measurement of the temperature of said molten raw material mixture, and connected to said control device; The said method includes the following steps: (a) the continuous introduction of a mixture of raw materials of a given composition into the tank; (b) continuous measurement of the temperature of the molten raw material mixture using the temperature measuring device; (c) stationary heating of the molten raw material mixture to a given temperature, Ti; (d) the modification, for a given and limited period of time, without active regulation by the control device, of at least one operating parameter of the furnace chosen from among the moisture content in the mixture of raw materials, the furnace draft, the loading speed of the mixture of raw materials, the power of the heating means, and / or the quantity of organic compounds or carbonaceous fuels in the mixture of raw materials; (e) the measurement of the temporal variations of the temperature, AT, of the mixture of molten raw materials and of the power AP of the heating means; (f) modeling, using a data processing device, the thermal behavior of the furnace using a non-heat transfer function H(s) stationary with, as input data, the temporal variations of the temperature AT of the molten raw material mixture and of at least one operating parameter modified in step (d); (g) the modelling, using a data processing device, of the parameters of the transfer function C(s) of the control device applied to the transfer function H(s) modelled in step (f).

[0035] According to other advantageous embodiments: - the non-stationary heat transfer function H(s) is modeled using a first-order response transfer function with or without dead time; - in step (d), at least two parameters, preferably three parameters, are modified sequentially or in parallel; - at step (d), the moisture content in the mixture of raw materials is modified so that the variation in the moisture content of said mixture is between 0 and 10%, and / or the kiln draft is modified so that the relative variation in said draft is between 0 and 2000kg / h; - in step (d), the quantity of organic compounds or carbonaceous fuels in the mixture of raw materials is modified so that the relative variation of said quantity of organic compounds or carbonaceous fuels is between 0 and 15% by weight, preferably between 0 and 10% by weight; - at step (d), the power of the heating means is modified so that the relative variation of said power with respect to the initial power is between 0 and 100%, preferably 0 and 50%, or even between 0 and 25%; - the control device is a Proportional-Integral-Derivative (PID) controller; - at step (g), the furnace transfer function H(s) also takes as input data a set of simulated values, I(s), of the variations in the moisture content in the raw material mixture, the furnace draft, the loading speed of the raw material mixture, the quantity of organic compounds or carbon fuels and / or the value of the setpoint temperature, T0; - the values ​​of the moisture content in the raw material mixture, the kiln draft, the kiln loading speed of the raw material mixture, and / or the quantity of organic compounds or carbonaceous fuels are simulated in the form of a random signal, such as white noise or pink noise.

[0036] The method according to the invention can be used for the calibration of a control device for a furnace, preferably a submerged combustion furnace for melting a mixture of raw materials including mineral waste.

[0037] In other words, the invention also relates to the use of a method according to the invention for calibrating a control device for a furnace, Preference for submerged combustion, for melting a mixture of raw materials including mineral waste.

[0038] In a second aspect of the invention, a system is provided for calibrating the parameters of a control device for a furnace, preferably a submerged combustion furnace, for melting a mixture of raw materials including mineral waste, - the oven includes at least one tank equipped with at least one heating means in the form of at least one immersed burner; - the tank is suitable for melting a mixture of raw materials; said system includes: - at least one temperature measuring device, said temperature measuring device being configured for the continuous measurement of the temperature of said molten raw material mixture; - at least one control device configured to regulate the power of said heating means; the parameters of the transfer equation C(s) of said control device being calibrated using a method according to the invention.

[0039] In a third aspect of the invention, a furnace, in particular with submerged combustion, is provided for melting a mixture of raw materials including mineral waste, in which a method according to the first aspect of the invention is implemented.

[0040] The furnace, preferably a submerged combustion furnace, for melting a mixture of raw materials including mineral waste, said furnace comprising: - a first tank adapted for melting a mixture of raw materials and equipped with at least one heating means in the form of at least one submerged burner, - at least one temperature measuring device configured for the continuous measurement of the temperature of said mixture of molten raw materials; - at least one control device configured to regulate the power of said heating means and to receive at least one continuous temperature measurement using said temperature measuring device; the values ​​of the parameters of the transfer function C(s) of the control device being fixed from values ​​obtained using a calibration method according to the invention.

[0041] According to other advantageous embodiments: - the furnace is such that the heating means is an oxygen / air-fuel immersed burner and the control device is further configured to regulate the power of said immersed burner by adjusting the fuel flow injected into said burner while maintaining a constant oxygen flow to fuel flow ratio;

[0042] - the oven is such that the heating means is an oxygen / air immersed burner - fuel and the control device is further configured to inject oxygen or air at a constant total flow rate of oxygen or air into said burner and into a bubbler, and at a constant oxygen or air flow rate to fuel flow rate ratio into the burner when the power of the submerged burner varies.

[0043] In a fourth aspect of the invention, an installation for the manufacture of mineral fibers is provided, comprising a submerged combustion furnace according to the fourth aspect of the invention.

[0044] Advantages of the invention

[0045] A first notable advantage of the invention is the obtaining of optimal values ​​for the parameters of the transfer function of the control device of a submerged combustion furnace. When the furnace is regulated by a control device thus calibrated, the furnace temperature converges rapidly towards the furnace setpoint temperature in the event of sudden and intense variations in the setpoint temperature, To, the moisture content in the raw material mixture 1001a, the furnace draft, the loading speed of the raw material mixture 1001a, and / or the quantity of organic compounds or carbonaceous fuels in the raw material mixture 1001a.

[0046] A second notable advantage is that it is possible to model, or even simulate, different values ​​for the parameters of the transfer function of the control device and to select those allowing optimal regulation of the oven without the need to physically implement perturbation tests on the oven to evaluate said calibration. The adjustment of the control device therefore requires less stress on the oven. Brief description of the drawings

[0047] [Fig. 1] is a schematic representation of an example of a glass or rock fiber manufacturing line.

[0048] [Fig.2] is a schematic cross-sectional representation of a submerged combustion furnace for melting a mixture of raw materials including mineral waste.

[0049] [Fig. 3] is a flowchart of a method according to the first aspect of the invention.

[0050] [Fig. 4] is a graphical representation of the evolution of the temperature of a submerged combustion furnace as a function of time after a sudden decrease in its power.

[0051] [Fig.5] is an example of a functional diagram of a servo device according to certain embodiments.

[0052] [Fig.6] is a graphical representation of an example of the time evolution of power, expressed as a variation relative to the basic power, linked to the variations temporal aspects of moisture content (upper frame) and of the quantity of organic compounds or carbonaceous fuels (lower frame).

[0053] [Fig.7] is a graphical representation of the time evolution of power (lower frame) and temperature (continuous line, upper frame) of an oven whose values ​​of the parameters of the transfer function of its control device are previously adjusted in accordance with the invention.

[0054] [Fig.8] is a graphical representation of the temporal evolution of the temperature (upper frame) and the power (middle frame) of a furnace as a function of variations in moisture content and amount of organic matter in the mixture of raw materials, and the furnace draft. Detailed description of implementation methods

[0055] With reference to [Fig. 1], a 1000 line manufacturing glass or rock fibers by the internal centrifugation method generally comprises: - silos 1001 for storing raw materials 1001a, for example mineral compounds and / or calcin; - a glass or rock melting furnace 1002 for melting raw materials 1001a; - a conveyor 1003 to transport the raw materials 1001a from the silos 1001 to the kiln 1002; - one or more fiber-making tools 1005a, 1005b, 1005c fed with glass or molten rock 1006; - an open or closed feed channel 1004 with openings located just above each fiber-making tool 1005a, 1005b, 1005c to supply them with glass or molten rock 1006.

[0056] With reference to [Fig. 2], a submerged combustion furnace 1002 generally comprises at least one refractory melting vessel 2001 equipped at its base with a series of submerged oxidizer-fuel burners 2002a-c, for example, oxygen-gas, air-fuel, or oxygen-fuel. The furnace 1002 is fed with a mixture 1001a of raw materials by a screw conveyor 1003 through an opening in its side wall. The opening may be submerged or above ground. The submerged burners 2002a-c melt the mixture 1001a and stir the pig iron 2004.

[0057] The furnace 1002 may include a second tank 2005, for example a refining tank, into which the pig iron 2004 flows via a groove 2006 provided for this purpose. The second tank 2005 may be equipped with a plurality of flame burners 2007 arranged above the surface of the pig iron 2004, with immersed or non-immersed electrodes, and a means 2008 for supplying refining, oxidizing, and / or reducing agents. The means 2008 for supplying oxidizing or reducing agents may also be arranged in the first tank 2001.

[0058] The residence of the molten iron 2004 in the second tank continues its thermal and chemical homogenization and allows its redox state to be adjusted according to specifications. At the end of this residence, the molten iron 2004 constitutes the molten glass or rock 1006 which is then conveyed to forming tools, such as fiber-forming tools 1005a-c via the channel 1004, glass granule manufacturing tools, or molding tools.

[0059] The melting tank 2001 has a temperature measuring device 2009, for example a thermocouple 2007, immersed or not, configured for continuous temperature measurement, T, of said mixture 1001a of molten raw materials, i.e. the pig iron 2004. The temperature measuring device is generally connected to a control device 2010, such as a Proportional-Integral-Derivative (PID) controller, allowing the furnace to be regulated according to a setpoint temperature, To. The setpoint temperature, To, can be a fixed value or a time profile.

[0060] The servo device 2010 is connected to the controllers (not shown) of the submerged burners and adjusts their power so that the temperature, T, of the molten iron 2004 reaches the setpoint temperature, To. In the case of oxygen-fuel burners, the burner power is adjusted by varying the oxygen and fuel flow rates and / or the ratio of these two flow rates.

[0061] The control device 2010 can further be configured to control the quantity or flow rate of oxidizing and reducing agent conveyed via the supply means 2008. This control can be exercised via a connection to the control device (not shown) of the supply means 2008. For example, if the supply means 2008 is a conveyor, the control device can vary its conveying speed according to a setpoint value provided by the control device 2010.

[0062] With reference to [Fig.2] and 3, in a first aspect of the invention, a method 3000 is provided for calibrating the parameters of a servo device 2010 of a furnace 1002, preferably with submerged combustion, for melting a mixture 1001a of raw material comprising mineral waste, - said furnace 1002 includes at least one tank 2001 equipped with at least one heating means 2002a-c, preferably in the form of at least one immersed burner, and at least one control device 2010 configured to regulate the power of said heating means 2002a-c; - said tank 2001 is adapted for the melting 2004 of a mixture 1001a of raw materials; - said tank 2001 includes at least one temperature measuring device 2009; - said temperature measuring device 2009 is configured for the continuous measurement of the temperature of said mixture 1001a of molten raw materials 2004, and connected to the audit control device 2010; The aforementioned method 3000 comprises the following steps: (a) the continuous introduction 3001 of a mixture 1001a of raw materials of given composition into the tank 2001; (b) the continuous measurement 3002 of the temperature of the mixture 1001a of molten raw materials 2004 using the temperature measuring device 2009; (c) the stationary heating 3003 of the mixture 1001a of molten raw materials 2004 according to a given temperature, T; (d) the modification 3004, for a given and limited period of time, without active regulation by the control device 2010, of at least one operating parameter of the furnace 1002 chosen from the moisture content in the mixture 1001a of raw materials, the furnace draft, the loading speed of the mixture 1001a of raw materials, the power of the heating means 2002a-c, and / or the quantity of organic compounds or carbonaceous fuels in the mixture 1001a of raw materials; (e) the measurement 3005 of the temporal variations of the temperature, AT, of the molten raw material mixture 1001a 2004; (f) the modelling 3006, using a data processing device, of the thermal behaviour of the furnace 1002 using a non-stationary heat transfer function H(s) with, as input data, the time variations of the temperature, AT, of the mixture 1001a of molten raw materials and of at least one operating parameter modified in step (d); (g) the modelling 3007, using a data processing device, of the parameters of the transfer function C(s) of the control device 2010 applied to the transfer function H(s) modelled in step (f).

[0063] The temperature measuring device 2009 can be a thermocouple or a pyrometer.

[0064] For the purposes of this invention, "carbonaceous fuels" means any type of carbon-based organic mineral fuel, preferably solid, that can be added to the mixture 1001a of raw materials. An example of a carbonaceous fuel is coal or petroleum coke.

[0065] Steps (f) and (g) of modeling are generally performed using a data processing device. An example of such a device might be one configured to automatically execute sequences of arithmetic or logical operations to perform tasks or actions. Such a device, generally called a computer, may include one or more central processing units (CPUs) and at least one control device adapted to perform these operations.

[0066] The device may also include other electronic components such as Input / output interfaces, non-volatile or volatile storage devices, and communication buses for data transfer between components within the device. One of the input / output devices may be a user interface for human-machine interaction, for example, a graphical user interface to display human-understandable information.

[0067] The data processing device may advantageously include one or more graphics processing units (GPUs) whose parallel structure makes them more efficient than central processing units in performing complex calculations.

[0068] Step (g) of modeling the thermal behavior of the furnace 1002 using a non-stationary heat transfer function H(s) allows for the creation of a numerical model of the furnace 1002. From this model, the parameters of the heat transfer function C(s) of the control device 2010 can be modeled without requiring any physical intervention on the furnace 1002 to implement this modeling. In other words, the heat transfer function H(s) provides a model of the furnace 1002 to which the control device 2010 can be applied, via its heat transfer function C(s), in order to determine, in step (g), the parameter values ​​of said device for optimal control of the furnace 1002.

[0069] Thanks to the method according to the first aspect of the invention, it is therefore possible to model, or even simulate, different values ​​for the parameters of the transfer function C(s) and to select those allowing optimal regulation of the furnace 1002 without the need to physically implement tests on the furnace 1002 to evaluate it. A significant advantage is that the furnace 1002 is considerably less stressed for the adjustment of the servo device 2010.

[0070] In step (f), the thermal behavior of the furnace 1002 is modeled using a non-stationary heat transfer function H(s).

[0071] According to one embodiment, the thermal equilibrium of the furnace 1002 can be modeled using the following equation: MCP— = 2004, t is the time, M is the mass of the furnace 1002 including the molten iron 2004 it contains, cp is the specific heat capacity of the furnace including the molten iron 2004, P(t) is the power of the heating means at time t, q is the power required to melt the mixture 1001a of raw materials according to a given loading speed, and I(t) = ô(t) + Q(t) is the instantaneous power variation linked to the temporal variations of the content, ô(t), in moisture ô and of the quantity Q(t) of organic compounds or carbonaceous fuels in the mixture 1001a of raw materials.

[0072] The power I(t) may further include the temporal variations of the furnace draw ip(t) and / or the speed v(t) of loading the mixture 1001a of raw materials. where T is the temperature of the furnace 1002 including the melting

[0073] Generally, in the case of convective heat transfer, the power q> varies proportionally to the difference between the temperature T(t) of the furnace 1002, including the molten iron 2004, at time t, and a so-called fictitious boundary layer temperature Tp. The boundary layer temperature Tp can be interpreted as a temperature representative of the temperature of the molten iron 2004 near the walls of the furnace 1002 and the mixture 1001a of unmelted raw materials. The power q> can then be estimated using the following relationship: (p = fiiTU) - 7>ù [3 and Tp are unknown constants a priori.

[0074] By setting x(t) = T(t) - To and u(t) = P(t) - PO, with To the setpoint temperature and Po the base power to reach the setpoint temperature To without perturbation, i.e. with I(t) = 0, a non-stationary heat transfer function H(s) in the Laplace domain can be: + / (*)]

[0075] with H (s) — Mcps+P ~ J ( W )

[0076] and v - P y-Mï~

[0077] In the initial state, i.e. before any disturbance of the furnace 1002, the temperature, T(t), of the furnace 1002 follows the setpoint temperature, To, i.e. T(t) = T0 for the base power, Po: R — —-

[0078] And

[0079] The quantities M, cp, Tp and [3 are generally unknown and depend on the structure of the furnace 1002, its constituent materials, the chemical nature of the pig iron 2004 and its quantity. [3 also depends on the charging speed of the raw material mixture 1001a.

[0080] In accordance with the first aspect of the invention, the thermal behavior of the furnace 1002 is modeled using the transfer function H(s), with the temporal variations of the temperature AT of the molten raw material mixture 1001a and of the operating parameter modified in step (d) as input data. The temporal variations of the temperature AT of the molten raw material mixture 1001a and of the operating parameter modified in step (d) can be interpreted as the consequences of a perturbation introduced by the modification, in step (d), of at least one operating parameter of the furnace. Exploiting this disturbance allows us to calculate the parameters of the transfer function H(s), in particular the constant y and the temperature Tp.

[0081] According to some embodiments, the non-stationary heat transfer function H(s) is modeled using a first-order response transfer function with or without dead time.

[0082] Generally, submerged combustion furnaces exhibit a certain inertia, and when one of their operating parameters is abruptly changed, in the form of a pulse, the response of said furnace 1002 is not immediate. The furnace 1002 shows a delay in responding to the disturbance.

[0083] According to an exemplary embodiment, for an impulse response in power, for example following a sudden power variation in the form of a unit step U(s)=AP / s, and a zero variation, AI= Aô + AQ = 0, in the moisture content and the quantity of organic compounds, the response can be written in the form: X(s) = =

[0084] Where AP = Pi - Po is the variation, in the form of a unit step, from the initial power Po to the power Pi different from Po. In the time domain, this function has the following expression, for t > 0:

[0085] The values ​​of the parameters y and Tp can be obtained by performing a function adjustment f(t) on the time variations of the temperature AT of the mixture 1001a of molten raw materials and of the power AP of the heating means 2002a-c.

[0086] In step (d), for a given and limited period of time, without active regulation by the control device 2010, at least one operating parameter of the furnace 1002 is modified, chosen from among the moisture content in the mixture 1001a of raw materials, the furnace draft, the loading speed of the mixture 1001a of raw materials, the power of the heating means 2002a-c, and / or the quantity of organic compounds or carbonaceous fuels in the mixture 1001a of raw materials.

[0087] The number and nature of the operating parameters to be modified depends on the composition of the raw material mixture including mineral waste and the precision required for the calibration of the control parameters.

[0088] According to certain embodiments, in step (d), at least two, or even at least three, operating parameters are modified sequentially or in parallel. Modifying at least two, or even three, parameters is generally sufficient for a representative model of the thermal behavior of a furnace. particularly with immersed combustion and, ultimately, a precise modeling of the parameters of the transfer function of the 2010 control device for effective regulation.

[0089] As discussed previously, the moisture content and the organic compound or carbonaceous fuel content of mineral waste can vary considerably depending on its origin and storage conditions. During the operating time of a submerged combustion furnace, a mixture of raw materials containing mineral waste in given proportions can exhibit sudden and significant variations in its moisture content and its organic compound or carbonaceous fuel content.

[0090] Thus, according to certain embodiments, in step (d), the moisture content in the mixture 1001a of raw materials is modified so that the variation in the moisture content of said mixture is between 0 and 10%, and / or the furnace draft is modified so that the relative variation in said draft is between 0 and 2000kg / h.

[0091] These ranges of variation in furnace draw and in moisture content of raw material mixtures including mineral waste allow for effective calibration of furnace control devices, particularly for submerged combustion furnaces.

[0092] According to certain embodiments, the furnace 1002 may include at least one means 2011 for measuring the moisture content of said 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 located on the conveyor 1003 just before loading the furnace, or further upstream, in the storage silos 1001. The moisture measurement means 2011 allows for a precise measurement of the change in moisture content of the mixture 1001a at step (d).

[0093] According to other embodiments, in step (d), the quantity of organic compounds in the mixture 1001a of raw materials is modified so that the relative variation of said quantity of organic compounds or carbon fuels is between 0 and 15% by weight, preferably between 0 and 10% by weight.

[0094] These intervals of variation in quantity of organic compounds allow a modeling of the transfer function H(s) of the furnace 1002 and, subsequently, of the transfer function C(s) of the control device 2010 which, when the latter is ultimately implemented in a device 2010 leads to a rapid convergence of the temperature of the furnace 1002 to the setpoint temperature in the event of sudden and intense variations in the content of organic compounds or carbonaceous fuels of the mixture of raw materials including mineral waste.

[0095] According to other embodiments, whether complementary or not, in step (d), the power of the heating means (2002a-c) is modified so that the relative variation of said power with respect to the initial power is between 0 and 100%, preferably 0 and 50%, or even between 0 and 25%.

[0096] By way of illustration, [Fig. 4] shows the temperature evolution (dashed line) of a submerged combustion furnace as a function of time after the introduction of 5.7 wt% coke into a mixture 1001a of raw materials followed by a sudden decrease in the furnace power from 287 kW to 173 kW. Upon the introduction of the coke, due to the energy released by its combustion, the temperature of furnace 1002, initially at T0 = 1175°C, increased to 1288°C. In [Fig. 4], time t = 0 corresponds to the moment when the power is suddenly decreased, in one unit step, from 287 kW to 173 kW. The temperature evolution is represented by the dotted symbols.

[0097] The response f(t) described above for an impulse response can be written with Po = 287kW, Pi = 173kW and To = 1175°C: / (O = ^-^^(1175-7,,)(1-^

[0098] To determine the values ​​of the parameters Tp and y, the response f(t) can be fitted to the data in [Fig. 4] using a least-squares method with Tp and y as the fitting parameters. The optimal fit, illustrated in [Fig. 4] by the solid line, gives the following values ​​for the parameters Tp and y: TP = √(Cv) = 5√(fHz)

[0099] The heat transfer function H(s) used to model the thermal behavior in this example can therefore be written as: x (1175-888) 7 5.8 x 10⁻⁴ H(s) = -—^7—“ -----î v ' 287 \ .s+5,810-4 /

[0100] And the quantity Mcp, representing the heat capacity of the furnace 1002 independent of its mass, can be calculated: Mcp~ 1.7 MJ!K

[0101] In step (g), the parameters of the transfer function C(s) of the control device 2010 are modeled by applying it to the transfer function H(s) of the furnace 1002, obtained in step (f).

[0102] Once the thermal behavior of the oven 1002 has been modeled using the transfer function H(s), it is possible to model the parameters of the transfer function C(s) of the control device 2010 applied to the transfer function H(s) of the oven.

[0103] This modeling can notably be implemented by simulation in order to determine ex-situ the optimal values ​​of the parameters of the transfer function C(s) for efficient control of the furnace 1002. Numerical calculation software programs such as Matlab or Scilab provide functions and algorithms adapted to this type of simulation.

[0104] With reference to [Fig.5], an example of modeling may consist of an iterative optimization loop in which the parameters of the transfer function C(s) of the control device are adjusted until the setpoint power P calculated by said function C(s) from a difference e between the temperature T of the furnace 1002 and a setpoint temperature To for said furnace 1002 allows the furnace 1002 to reach said setpoint temperature To when said power P increased by the power I(s) is supplied, as input data, to the transfer function H(s) of the furnace 1002.1(s) = ô(s) + Q(s) is the instantaneous power variation linked to the temporal variations of the content, ô(s), in moisture ô and of the quantity Q(s) of organic compounds or carbonaceous fuels in the mixture 1001a of raw materials.

[0105] During the execution of the iterative execution loop, the parameters of the transfer function C(s) of the control device 2010 can be adjusted manually, using an adjustment method such as the Ziegler-Nichols method, the Cohen-Coon method, the Âstrôm-Hâgglund method, or automatically using a numerical optimization method.

[0106] With the transfer function H(s) from the example in [Fig.4], the diagram in [Fig.5] can, for example, be transcribed using the following formula: X(s) -H(s) ( / / (5) + / (5) ) U(s) = C(s)e(s)

[0107] With e(t) = - x(t). Hence: X(y) = ----^^---: / (5)

[0108] According to preferred embodiments, the 2010 control device is a Proportional-Integral-Derivative (PID) controller.

[0109] The transfer function C(s) of the 2010 control device can be written in the Laplace domain: C(s) = Kp+ K~ + Kdsou Kp, Ki and Kd are respectively the proportional, integral, and derivative parameters or gains.

[0110] According to another writing, the transfer function C(s) can have the following form: C (5) = Kp[ 1 + ™ + TdS) °where ta are respectively the integration and derivative time constants and, r; = Kp / Ki = KpTi and rd =Kd / Kp = Td / Kp.

[0111] It has been observed that, in most industrial furnaces, the temperature measurements, T, of the molten raw material mixture 1001a 2004 can be affected by significant noise. In order to avoid control discrepancies, it may be advantageous to neglect the drift term of the transfer function C(s) without any noticeable impact on the control performance of the servo device.

[0112] The function C(s) can then be written: C'O) = Kp+

[0113] OuencoreC(5) = + )

[0114] The transfer function C(s) allows for the calculation, in real time, of a gain for the Correction of the setpoint of the power controllers of the 2002a-c heating system, using at least one submerged burner. The unit of the gain depends on the type of controller used. For example, in the case of a submerged burner, it may correspond to a percentage of the fuel flow rate, e.g., a volumetric flow rate of gas, injected into the burner. The flow rate value may be related to the burner power level via a linear relationship.

[0115] From the previous example, the setpoint value at the output of the 2010 control device can be written according to the following relationship: U (s) = K ,,(1 + 4s)

[0116] The input power, P, of the oven 1002 can be written as: P = P0 + Kp^ + ±^ j

[0117] The modelling of the parameters, Kp and r; of the transfer function C(s) of the control device 2010 can then consist of adjusting the values ​​which minimize the temporal variations of temperature in a simulation of the system in regulation.

[0118] This adjustment can be made manually, using an adjustment method such as the Ziegler-Nichols method, the Cohen-Coon method, the Âstrôm-Hagglund method, or automatically using a numerical optimization method.

[0119] For the example in [Fig. 4] and a fixed temperature measurement frequency α of the 2009 device greater than y, i.e., α = 1 Hz, the values ​​of the parameters Kp and r are iteratively adjusted to obtain x(t) close to zero over time. The advantage is that it is possible to evaluate the stability over time of the furnace during regulation when it is subjected to disturbances typical of glassmaking applications. Another advantage is the possibility of taking into account, during the modeling, the sampling frequency of the 2009 temperature measurement device.

[0120] According to some embodiments, 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 the variations of the moisture content in the mixture 1001a of raw materials, the furnace draft, the loading speed of the mixture 1001a of raw materials, the quantity of organic compounds or carbon fuels and / or the value of the setpoint temperature, To.

[0121] According to some preferred embodiments, the moisture content values in the 1001a mixture of raw materials, the furnace draw, the loading speed of the 1001a mixture of raw materials, and / or the quantity of organic compounds or carbonaceous fuels are simulated in the form of a random signal, such as white noise or pink noise.

[0122] According to an example of parameter modeling, Kp and r, of the transfer function C(s) of the control device for the example in [Fig. 4] and 5, with reference to [Fig. 6], the instantaneous variations, expressed as relative variations ô(t) and Q(t), of the power I(t) = ô(t) + Q(t) related to the temporal variations of the moisture content (upper frame) and the quantity Q of organic compounds or carbonaceous fuels (lower frame) are first generated in the form of pink noise. The values ​​of the parameters Kp and r are then manually adjusted iteratively to obtain a temperature close to the setpoint temperature over time.

[0123] Figure 7 shows the corresponding variations in power (lower frame) and temperature (solid line, upper frame) of furnace 1002 obtained with the adjusted values ​​of the following parameters Kp and -^: KP = 2.2 kW / ° CT / = 478 5'

[0124] Fig. 7 shows that these values ​​of parameters Kp and T allow a certain efficient screwing of the temperature T (solid line, upper frame) of the oven 1002 to the setpoint temperature To (dashed line, upper frame) over the set of instantaneous variations of the power I(s) of the [Fig.6].

[0125] In order to validate the performance of a servo device calibrated with the values ​​of the parameters Kp and thus adjusted, these were implemented in the servo device of an industrial furnace having the same transfer function H(s) as that of the example in [Fig.4] and 5. The industrial furnace, operating under real and industrial conditions, was then subjected to abrupt variations in the setpoint temperature, To, its draw, the moisture content and the quantity of organic matter or carbonaceous fuels, such as coke, contained in the mixture of raw materials.

[0126] The behavior of the furnace subjected to such variations is shown in [Fig. 8]. The upper frame shows the temporal evolution of the furnace temperature (solid line) and the setpoint temperature To (dashed line). The middle frame shows the temporal evolution of the furnace power. The lower frame shows the abrupt variations in the furnace's draft (dashed line), moisture content (solid line), and the quantity of organic matter or carbonaceous fuels (dashed line) in the raw material mixture.

[0127] The [Fig.8], upper frame, shows a rapid convergence of temperature (line continuous) of the oven at the setpoint temperature To (dotted line) regardless of the nature and simultaneity of the variations (lower frame).

[0128] A sudden change in the moisture content δ (solid line) causes a slight disturbance in power (center box), and the furnace temperature (solid line) deviates only slightly from the setpoint temperature ΔT (dashed line). Sudden changes in the furnace pull ρ (lower box, dashed line) after 5 a.m. and shortly before 3 p.m. cause sudden changes in power (center box), and the temperature (solid line), after an initial drift, converges very rapidly towards the setpoint temperature ΔT (dashed line). A sudden change in the quantity Q of organic matter or carbonaceous fuels (lower box, dashed line) around 5 p.m. leads to frequent power variations that are quickly compensated.

[0129] In addition, the control device is capable of compensating for sudden and simultaneous variations, after 07:30 and 19:00, of the setpoint temperature To (upper frame, dashed line), the draft (lower frame, dashed line) of the furnace, the moisture content (lower frame, solid line) and the quantity of organic matter or carbonaceous fuels (lower frame, dashed line).

[0130] The tests in [Fig. 8] demonstrate that the present invention enables efficient and robust calibration of a control device for a submerged combustion furnace. The control device 2010 allows for rapid compensation of sudden and intense variations in temperature, To, the setpoint (variations of 40°C in the figure), the moisture content in the raw material mixture 1001a, the furnace draft, the loading speed of the raw material mixture 1001a, and / or the quantity of organic compounds in the raw material mixture 1001a. The temperature of the furnace 1002 converges rapidly to the setpoint temperature with very limited overshoot amplitudes over time, regardless of the nature and simultaneity of the variations.

[0131] All embodiments of the first aspect of the invention are combinable.

[0132] The method according to the first aspect of the invention can advantageously be used for the calibration of a control device 2010 of a furnace 1002, preferably with submerged combustion, for the melting of a mixture 1001a of raw materials comprising mineral waste.

[0133] According to a second aspect of the invention, with reference to [Fig.2] and [Fig.3], a system is provided for calibrating the parameters of a servo device 2010 of a furnace 1002, preferably with submerged combustion, for the melting of a mixture 1001a of raw material comprising mineral waste, - the furnace 1002 includes at least one tank 2001 equipped with at least one heating means 2002a-c in the form of at least one immersed burner; - The 2001 tank is adapted for the 2004 melting of a 1001a mixture of materials first; said system includes: - at least one 2009 temperature measuring device, said 2009 temperature measuring device being configured for the continuous measurement of the temperature of said 1001a mixture of molten raw materials 2004; - at least one 2010 control device configured to regulate the power of said heating means 2002a-c; the parameters of the transfer equation C(s) of said 2010 control device being calibrated using a method according to any one of the embodiments of the first aspect of the invention.

[0134] According to a third aspect of the invention, a furnace 1002, preferably with submerged combustion, is provided for the melting 2004 of a mixture 1001a of raw materials comprising mineral waste, said furnace 1002 comprising: - a first tank 2001 adapted for the melting 2004 of a mixture of raw materials and equipped with at least one means 2002a-c of heating in the form of at least one immersed burner, - at least one 2009 temperature measuring device for the continuous measurement of the temperature of said 1001a mixture of molten raw materials 2004; - at least one control device 2010 configured to regulate the power of said heating means 2002a-c and to receive at least one continuous temperature measurement using said temperature measuring device 2009; the values ​​of the parameters of the transfer function C(s) of the control device 2010 being fixed from values ​​obtained using a calibration method according to any one of the embodiments of the first aspect of the invention.

[0135] The calibration method for determining the values ​​of the parameters of the transfer function C(s) of the 2010 servo device can be implemented using a system according to the second aspect of the invention.

[0136] As with the first aspect of the invention, the oven 1002 may include at least one means 2011 for measuring the moisture of said mixture 1001a of raw materials.

[0137] According to some embodiments, the heating means 2002a-c is an oxygen / air-fuel immersed burner and the control device 2010 is further configured to regulate the power of said immersed burner by adjusting the fuel flow injected into said burner while maintaining a constant oxygen flow to fuel flow ratio.

[0138] According to some alternative embodiments, the heating means 2002a-c is an oxygen / air-fuel submerged burner and the control device 2010 is further configured to inject oxygen or air at a constant total flow rate of oxygen or air into said burner and into a boiler, and at a flow rate ratio of oxygen or air on constant fuel flow in the burner when the power of the submerged burner varies.

[0139] In a fourth aspect of the invention, an installation for the manufacture of mineral fibers is provided, such as a glass or rock fiber manufacturing line, comprising a furnace 1002 according to any one of the embodiments of the third aspect of the invention.

[0140] The present invention, in all its aspects, can be implemented, without limitation, in many processes and manufacturing lines for glass products such as, for example, glass wool, rock wool, textile glass fibers, flat glass or hollow glass.

[0141] List of references Literature patent US 351 413 B, JT WAINWRIGHT 10 / 26 / 1886. US 1 656 828 A, POWELL EDWARD R, 01 / 17 / 1928. FR 876569 A, UNION DES VERRERIES MECANIQUES, 10.11.1942. 2009 091 558 Al, GAS TECHNOLOGY INST [US] 7 / 29 / 2009. DE 651 687 C, GLASHUETTE ACHERN AG, 18.10.1937. GB 1 028 481 A, SELAS CORP OF AMERICA, 04.05.1966. WO 0248612 Al, SAINT GOBAIN [FR] 20.06.2002. WO 2006 018 582 Al, SAINT GOBAIN ISOVER [FR] 23.02.2006. US 4877449 ​​A, INST GAS TECHNOLOGY [US] 31.10.1989. EP 2 433 911 Al, JOHNS MANVILLE [US] 3 / 28 / 2012. WO 2022 180 345 Al, SAINT GOBAIN ISO VER [FR] 01.09.2022.

Claims

Demands

1. Method (3000) for calibrating the parameters of a control device (2010) of a furnace (1002), preferably with submerged combustion, for melting a mixture (1001a) of raw materials including mineral waste, - said furnace (1002) includes at least one vessel (2001) equipped with at least one heating means (2002a-c), preferably in the form of at least one submerged burner, and at least one control device (2010) configured to regulate the power of said heating means (2002a-c) according to a setpoint temperature, To; - said tank (2001) is adapted for melting (2004) a mixture (1001a) of raw materials; - said tank (2001) includes at least one temperature measuring device (2009); - said temperature measuring device (2009) is configured for continuous temperature measurement of said mixture (1001a) of molten raw materials (2004), and connected to said servo device (2010); said method (3000) comprises the following steps: (a) the continuous introduction (3001) of a mixture (1001a) of raw materials of given composition into the tank (2001); (b) the continuous measurement (3002) of the temperature of the mixture (1001a) of molten raw materials (2004) using the temperature measuring device (2009); (c) stationary heating (3003) of the mixture (1001a) of molten raw materials (2004) according to a given temperature, T; (d) the modification (3004), for a given and limited period of time, without active regulation by the control device (2010), of at least one operating parameter of the furnace (1002) chosen from among the moisture content in the mixture (1001a) of raw materials, the furnace draft, the loading speed of the mixture (1001a) of raw materials, the power of the heating means (2002a-c), and / or the quantity of organic compounds or carbonaceous fuels in the mixture (1001a) of raw materials; (e) the measure (3005) of the temporal variations of the temperature, AT, of the mixture of raw materials (1001a) in molten form (2004) and of the power AP of the heating means (2002a-c); (f) the modelling (3006), using a data processing device, of the thermal behaviour of the furnace (1002) using a non-stationary heat transfer function H(s) with, as input data, the time variations of the temperature AT of the mixture (1001a) of molten raw materials and of at least one operating parameter modified in step (d); (g) the modelling (3007), using a data processing device, of the parameters of the transfer function C(s) of the control device (2010) applied to the transfer function H(s) modelled in step (f).

2. Method (3000) according to claim 1, wherein the non-stationary heat transfer function H(s) is modeled using a first-order response transfer function with or without dead time.

3. Method (3000) according to any one of claims 1 to 2, such that, in step (d), at least two parameters, preferably three parameters, are modified sequentially or in parallel.

4. Method (3000) according to any one of claims 1 to 3, wherein, in step (d), the moisture content in the mixture (1001a) of raw materials is modified so that the variation in the moisture content of said mixture is between 0 and 10%, and / or the kiln draft is modified so that the relative variation in said draft is between 0 and 2000 kg / h.

5. Method (3000) according to any one of claims 1 to 4, wherein, in step (d), the amount of organic compounds or carbonaceous fuels in the mixture (1001a) of raw materials is modified so that the relative variation of said amount of organic compounds or carbonaceous fuels is between 0 and 15% by weight, preferably between 0 and 10% by weight.

6. Method (3000) according to any one of claims 1 to 5, wherein, in step (d), the power of the heating means (2002a-c) is modified so that the relative variation of said power with respect to the initial power is between 0 and 100%, preferably 0 and 50%, or even between 0 and 25%.

7. Method (3000) according to any one of claims 1 to 6, wherein the control device (2010) is a Proportional-Integral-Derivative (PID) controller.

8. Method (3000) according to any one of claims 1 to 7, such that, at step (g), the transfer function H(s) of the furnace (1002) further takes, as input data, a set of simulated values, I(s), of the variations of the moisture content in the mixture (1001a) of raw materials, the furnace draft, the loading speed of the mixture (1001a) of raw materials, the quantity of organic compounds or carbon fuels and / or the value of the setpoint temperature, To.

9. Method (3000) according to claim 8, wherein the values ​​of the moisture content in the mixture (1001a) of raw materials, the furnace draft, the loading speed of the mixture (1001a) of raw materials, and / or the quantity of organic compounds or carbonaceous fuels are simulated in the form of a random signal, such as white noise or pink noise.

10. Use of a method (3000) according to any one of claims 1 to 9 for calibrating a control device (2010) for a furnace (1002), preferably with submerged combustion, for melting a mixture (1001a) of raw materials comprising mineral waste.

11. System for calibrating the parameters of a control device (2010) for a furnace (1002), preferably a submerged combustion furnace, for melting a mixture (1001a) of raw materials including mineral waste, - the furnace (1002) comprises at least one vessel (2001) equipped with at least one heating means (2002a-c) in the form of at least one submerged burner; - the vessel (2001) is adapted for melting (2004) a mixture (1001a) of raw materials; said system comprises: - at least one temperature measuring device (2009), said temperature measuring device (2009) being configured for the continuous measurement of the temperature of said mixture (1001a) of molten raw materials (2004); - at least one control device (2010) configured to regulate the power of said heating means (2002a-c);the parameters of the transfer equation C(s) of said servo device (2010) being calibrated using a method (3000) according to any one of claims 1 to 9.;

12. Furnace (1002), preferably with submerged combustion, for melting (2004) of a mixture (1001a) of raw materials including mineral waste, said furnace (1002) comprises: - a first vessel (2001) adapted for melting (2004) a mixture of raw materials and equipped with at least one heating means (2002a-c) in the form of at least one immersed burner, - at least one temperature measuring device (2009) configured for the continuous measurement of the temperature of said mixture (1001a) of molten raw materials (2004); - at least one control device (2010) configured to regulate the power of said heating means (2002a-c) and to receive at least one continuous temperature measurement using said temperature measuring device (2009); the values ​​of the parameters of the transfer function C(s) of the servo device (2010) being fixed from values ​​obtained using a calibration method (3000) according to any one of claims 1 to 9.

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

14. Oven according to any one of claim 12, wherein the heating means (2002a-c) is an oxygen / air-fuel submerged burner and the servo device (2010) is further configured to inject oxygen or air at a constant total flow rate of oxygen or air into said burner and into a boiler, and at a constant oxygen or air flow rate to fuel flow rate ratio into the burner when the power of the submerged burner varies.

15. Installation for the manufacture of mineral fibers comprising a submerged combustion furnace (1002) according to any one of claims 12 to 14.

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