Thermal treatment of mineral material, especially clays, for the cement industry, in particular for the production of artificial pozzolans

Abstract

The present invention relates to a method for producing thermally treated clays in a calciner (10), wherein the pollutants escaping during the heating of the clay are thermally converted in the calciner (10).

Description

[0001] Thermal treatment of mineral material, especially clays, for the cement industry, especially for the production of artificial pozzolans

[0002] The invention relates to a process for the thermal treatment of mineral material, in particular clays, and a plant therefor, wherein the material properties are simultaneously used to reduce the air pollutants generated during production.

[0003] Clays and clay-like materials are often used today to produce artificial pozzolans, for example, which are then used in cement production. One reason for this is that CO2 escapes from the raw material during the production of cement clinker, for example from limestone. Therefore, switching to a different starting material, currently clay, for example, is an important step to reduce CO2 emissions and avoid climate-damaging emissions.

[0004] One disadvantage of clays is that they contain a number of substances with varying compositions. One substance that often escapes from the clay during thermal treatment of the material during preheating is ammonia. Since ammonia should not (and must not) be released into the atmosphere, an exhaust gas treatment system is installed downstream of the preheater. This system treats the exhaust gas coming from the preheater and removes pollutants such as ammonia and / or nitrogen oxides from the exhaust gas. This type of exhaust gas treatment is state of the art today and can usually be found in virtually every industrial plant that processes materials at higher temperatures.

[0005] Another pollutant that often escapes when clays are heated are hydrocarbons and hydrocarbon-containing compounds, here and in the following for simplification (and neglecting other heteroatoms) summarized under Cx H y which must also be removed from the exhaust gas.

[0006] DE 10 2011 014 498 A1 discloses a process for producing a clinker substitute. US Pat. No. 9,458,059 B2 discloses a manufacturing process for synthetic pozzolans.

[0007] US 2102 / 145042 A1 discloses a process for calcining and producing artificial pozzolans.

[0008] WO 2015 / 082 075 A1 discloses a process for producing a pozzolanic or latent-hydraulic cement clinker substitute, which involves preheating and drying the starting material.

[0009] DE 20 01 171 A1 discloses an additive for hydraulically hardening inorganic binders.

[0010] EP 0 148 090 A2 discloses a dry process for the production of cement clinker using precalcination.

[0011] The object of the invention is to provide a process which enables the thermal treatment of mineral material, in particular clays, in the most energy-saving and thus environmentally friendly way possible.

[0012] This object is achieved by the method having the features specified in claim 1. Advantageous further developments emerge from the subclaims, the following description, and the drawings.

[0013] The process according to the invention is used to produce thermally treated mineral material, in particular clays, for example and in particular for the production of artificial pozzolans for use in the cement industry. Production takes place in a calciner. When clays are heated, pollutants arise that should not be released into the environment. These include, for example and in particular, ammonia NH3 and hydrocarbons as well as hydrocarbon-containing compounds. These pollutants are usually removed by energy-intensive conversion in an exhaust gas treatment system downstream of the production facility. However, this process is energy-intensive and thus leads to further, avoidable CO2 emissions. Therefore, the pollutants released during heating of the clay are thermally converted in the calciner. In particular, the calciner maintains the correct temperature for the decomposition of the pollutants.There is also an additional, very positive effect. Clay typically releases ammonia. During the combustion process, which is required to generate the temperature in the calciner, nitrogen oxides are produced. The nitrogen oxides from the combustion process synproportion with the ammonia from the clay to form nitrogen and water. This creates a dual benefit, and even eliminates the need for the usual, energy-intensive downstream exhaust gas treatment.

[0014] According to the invention, at least a portion of the mineral material, in particular the clay, is introduced directly into the calciner without preheating. This initially seems counterintuitive, since, unlike the prior art, it eliminates energy recovery in the preheater. However, considering the entire process, including flue gas purification, it is surprising that omitting preheating is more than compensated for by the energy saved during the flue gas purification. And if downstream flue gas purification is nevertheless carried out, the reduction rates required there are significantly lower. In addition, the flue gas enters at a higher temperature, so that the energy requirement for this process is also reduced.

[0015] Another key aspect of the invention is that the pollutants released from clay, particularly ammonia and carbon compounds, have a high calorific value and are thus directly converted during the heat-consuming calcination process, releasing the energy at the highest and best usable energy level. It has been found that, for certain clays, the amount of these thermally usable pollutants can be so high that even an additional fuel supply is unnecessary, but in most cases, the fuel supply can at least be reduced. Thus, the direct and unpreheated supply of the mineral material not only does not remove thermal energy from the process, but ultimately actually increases it.Without preheating in the sense of the invention means heating in which heating occurs close to the treatment temperature and thus may be associated with the release of pollutants. However, clays in particular must be dried before use. For this purpose, the starting material is heated, but not above a temperature window of 70 °C to 120 °C (the maximum temperature varies depending on the drying method and the starting material used). However, within this temperature window, the emissions of pollutants according to the invention do not occur, or at least not to a significant extent, so that drying alone is not critical with regard to these emissions. Without preheating therefore preferably means, in the sense of the invention, with a temperature of at most 120 °C.

[0016] In a further embodiment of the invention, a mineral material is selected which releases ammonia and / or organic carbon compounds when heated.

[0017] In a further embodiment of the invention, at least a portion of the mineral material, in particular the clay, is introduced into a part of the preheater adjacent to the calciner, preheated in the preheater, and from there transferred to the calciner. For example, the preheater is a cascade of two to six co-current heat exchangers with cyclone separators; in this case, the mineral material, in particular the clay, is introduced into the warmest co-current heat exchanger adjacent to the calciner. This embodiment is preferred when the calciner is operated at a comparatively high temperature, for example and in particular between 800°C and 1200°C. In this case, the temperature in this first part of the preheater is sufficiently high that the mineral material, in particular the clay, can be reliably decomposed upon heating.This allows a balance to be achieved between heat recovery and effective pollutant minimization.

[0018] In another embodiment, a second mineral raw material is fed into the preheater, with the second mineral raw material being selected to emit no or only very low amounts of pollutants upon heating. Typical examples are limestone, slag, granulated blast furnace slag, waste cement brick, or sand, which are used together with artificial pozzolans in mixtures in the cement industry, for example. This allows heat recovery with the less critical reactants while simultaneously avoiding complex exhaust gas purification.

[0019] In another embodiment, a second portion of the mineral material is fed into the preheater. The second portion is selected so that the resulting emissions remain within the legal requirements, thus avoiding exhaust gas aftertreatment.

[0020] In a further embodiment of the invention, at least a portion of the mineral material, in particular the clay, is introduced into a preheater, preheated there, and from there transferred to the calciner. Therefore, the pollutants escape from the mineral material, in particular the clay, in the preheater and are thus present in the gas stream emerging from the preheater. Therefore, at least part of the gas emerging from the preheater is fed into the calciner. For this purpose, the gas stream emerging from the preheater can, for example, be fed into a combustion chamber connected to the calciner. As a result, the pollutants enter the calciner, just as they would if the mineral material, in particular the clay, were introduced directly, and they have the same positive effect, particularly on the nitrogen oxides produced during the combustion required to generate the temperature.

[0021] In a further embodiment of the invention, the gas coming from the preheater is fed into the calciner via a material cooler. A combustion chamber can also be arranged between the material cooler and the calciner. This recirculates the heat released by the product from the calciner back into the process.

[0022] In a further embodiment of the invention, the gas coming from the preheater is fed to a dust removal device, which can be designed, for example, as a fabric filter, ceramic filter, or electrostatic precipitator, before being fed into a combustion chamber. This separates the dust content in the gas coming from the preheater and can be returned to the plant at a suitable location, for example, the calciner or preheater. This prevents the dust content from heating to an undesirably high temperature in the combustion chamber and thus becoming thermally deactivated.

[0023] In a further embodiment of the invention, at least one reactant is added to the gas coming from the preheater before the gas is fed to the calciner. The reactant can be used, for example, to convert sulfur compounds, in particular to sulfate. Sulfate is a desirable additive in the cement industry, so sulfur impurities can be profitably utilized in this way.

[0024] In a further embodiment of the invention, the calciner is operated at a temperature between 600 °C and 1400 °C, preferably between 600 °C and 1200 °C, more preferably between 750 °C and 1050 °C, particularly preferably between 800 °C and 1000 °C.

[0025] In a further embodiment of the invention, a fuel is supplied to the calciner. The fuel is selected from the group comprising solid fuels, in particular coal dust, natural gas, biogas, hydrogen, ammonia, synthesis gas, and liquid fuels, in particular oil. These fuels are highly energetic and allow for good firing.

[0026] In a further embodiment of the invention, sulfur-containing compounds from the mineral material, especially clay, are oxidized to sulfate in the calciner. Sulfates are common additives in cement, so this method allows the sulfur to be bound in a valuable way, adding value to the finished product. At the same time, environmentally harmful emissions are avoided.

[0027] In a further aspect, the invention relates to a device for the thermal treatment of mineral material, in particular clay. The device has a calciner. Furthermore, the device has a reactant feed. It is essential that the reactant feed introduces mineral material, in particular clay, directly into the calciner without preheating. This means that the first heating of the mineral material, in particular the clay, only takes place in the calciner. This in turn causes the pollutants, in particular ammonia, hydrocarbons and hydrocarbon compounds, to be released precisely in the calciner at the high temperature of the calciner. Hydrocarbons and hydrocarbon-containing compounds are burned directly, and ammonia is converted with the nitrogen oxides formed at these high temperatures to nitrogen and water. In this way, a direct conversion of the pollutants takes place in the calciner.This eliminates the need for preheating the reactant and thus for recovering energy from the exhaust gas. This seems counterintuitive, as it would impair efficiency. However, it has been shown that this eliminates the need for complex exhaust gas purification, which also requires a high level of energy.

[0028] In a further embodiment of the invention, the calciner is directly connected to a waste gas treatment system or a flue, thus without an intermediate preheater. In this embodiment, the material stream is fed into the calciner completely and without preheating. In addition, if additional treatment is necessary, the waste gas stream can already be heated to the temperature of the calciner's gas outlet, eliminating the need for the typically necessary reheating of the waste gas.

[0029] In a further aspect, the invention relates to a device for the thermal treatment of mineral material, in particular clays, wherein the device comprises a calciner and a preheater. This corresponds to the conventional design. According to the invention, a gas flow divider is arranged in the gas flow leaving the preheater. The gas flow divider serves to divide the gas flow into a recirculation gas flow and an exhaust air flow. The gas flow divider is connected to a return line. The return line serves to receive the recirculation gas flow. The return line is connected to the calciner or a combustion chamber or a material cooler. This utilizes two effects. Firstly, in the preheater, as before, the energy can be at least partially returned to the process by preheating the material to be thermally treated.On the other hand, the gas divider transfers at least a portion of the pollutants to the calciner, where they can be processed. Since complete recirculation would lead to an enrichment of, for example, the CO2 from the combustion process, a portion of the gas stream must also be released into the environment as exhaust air.

[0030] In a further embodiment of the invention, the return line has a dust removal device.

[0031] In a further embodiment of the invention, the dust removal device is connected to a dust return line. The dust return line has two ends. One end is connected to the dust removal device, the other end is connected to the calciner or preheater. This also includes an indirect connection, for example, the connection between the calciner and the preheater or a material feed device to the preheater or calciner. This allows the dust to be fed into the product without overheating and thus without deactivation, for example, in the combustion chamber.

[0032] In a further embodiment of the invention, the reactant feed comprises a reactant stream divider. The reactant stream divider is connected to a first partial reactant stream line and a second partial reactant stream line. The first partial reactant stream line is connected to the calciner and the second partial reactant stream line is connected to the preheater. This allows a hybrid of the two aforementioned devices to be used to carry out the process according to the invention. The first partial reactant stream is thus fed directly to the calciner, resulting in optimal pollutant minimization. At the same time, part of the thermal energy can be fed back into the process via the second partial reactant stream and the preheater. In addition, the device comprises a second reactant feed, wherein the second reactant feed is designed for the supply of a second mineral raw material.The secondary feed is connected to the preheater. A second mineral raw material can be fed to the preheater via the secondary feed, further improving the recovery of thermal energy from the preheater's exhaust gas. The second mineral raw material is, for example, limestone or sand, which releases no or very few pollutants during preheating and can therefore be easily used to recover thermal energy in the preheater.

[0033] In a further embodiment of the invention, the device has at least one first temperature sensor. The temperature sensor is arranged in the calciner or between the calciner and the preheater. The device further has at least one auxiliary combustion device. The auxiliary combustion device serves in particular to compensate for temperature fluctuations and is therefore usually operated with a fuel that is easy to meter and has a constant calorific value, for example gas or pulverized coal. The auxiliary combustion device is arranged on the combustion chamber, between the combustion chamber and the calciner, or in the calciner. The device has a first control device. The first control device is connected to the first temperature sensor and the auxiliary combustion device. The first control device is designed to control the auxiliary combustion device depending on the temperature detected by the first temperature sensor.

[0034] In a further embodiment of the invention, the device comprises at least a first NO x -Analyzer. For example and in particular, the NO X - Analyzer the NO x concentration using infrared spectroscopy in an extractive measurement. The NO x The analyzer is arranged in the calciner or between the calciner and the preheater or in the preheater or after the preheater. The device has at least one reactant flow divider and / or at least one second reactant feed and / or a gas flow divider. The device has a first control device or a second control device. The first control device or the second control device is connected to the first NO x-Analyzer and / or at least one first temperature sensor and the reactant flow divider and / or the gas flow divider. The first control device or the second control device is for controlling the reactant flow divider and / or the gas flow divider depending on the NO x -Analyzer detected NO x-Concentration taking into account the prevailing temperatures. This enables current adaptation to a fluctuating composition of the starting material and thus to a fluctuating release of pollutants in the process in a simple manner. In a further embodiment of the invention, the device has at least one first organic analyzer. An organic analyzer can, for example, be a flame ionization detector for detecting the concentration of hydrocarbons and hydrocarbon-containing compounds. The organic analyzer is arranged in the calciner or between the calciner and preheater or in the preheater or downstream of the preheater. The device has at least one reactant flow divider and / or at least one second reactant feed and / or a gas flow divider. The device has a first control device or a second control device.The first control device or the second control device is connected to the first organic analyzer and / or at least one first temperature sensor and the reactant flow divider and / or the gas flow divider. The first control device or the second control device is designed to control the reactant flow divider and / or the gas flow divider depending on the organic concentration detected by the first organic analyzer, taking into account the prevailing temperatures. This allows for easy, up-to-date adaptation to a fluctuating composition of the starting material and thus to a fluctuating release of pollutants in the process.

[0035] In a further embodiment of the invention, the device has at least one first NH3 analyzer. The NH3 analyzer is arranged in the calciner or between the calciner and the preheater or in the preheater or downstream of the preheater. The device has at least one reactant flow divider and / or one gas flow divider. The device has a first control device or a second control device. The first control device or the second control device is connected to the first NH3 analyzer and / or the temperature sensor and to the reactant flow divider and / or the gas flow divider. The first control device or the second control device is designed to control the reactant flow divider and / or the gas flow divider as a function of the NH3 concentration detected by the first NH3 analyzer and / or the temperature level detected by the temperature sensor.

[0036] The aforementioned devices are particularly preferably designed to carry out the method according to the invention, or the method according to the invention can particularly preferably be carried out on one of the aforementioned devices.

[0037] The method according to the invention is explained in more detail below with reference to embodiments shown in the drawings.

[0038] Fig. 1 first embodiment

[0039] Fig. 2 second embodiment

[0040] Fig. 3 third embodiment

[0041] Fig. 4 fourth embodiment

[0042] Fig. 1 shows the direct feed 30 of the reactant into the calciner 10. The device does not have a preheater. The gas leaving the calciner 10 is discharged directly as exhaust air; reactant preheating and heat recovery in the preheater do not occur. The product leaving the calciner 10 is cooled in a material cooler 20 and leaves the device via the product stream 40. Gas, for example air, is fed via the gas feed 50 to the material cooler 20 and from there preheated to the calciner 10. The calciner 10 has a combustion device that is either arranged in the calciner 10 or upstream of the calciner 10. The nitrogen oxides produced during combustion there are reacted with the ammonia originating from the clay, so that no or only tolerable emissions are generated.Likewise, hydrocarbons and hydrocarbon-containing compounds originating from the clay are reliably combusted in sufficient quantities. The lack of heat recovery in a preheater is offset by the fact that no additional energy is required for exhaust gas purification.

[0043] Fig. 2 shows a second, alternative embodiment. Here, the reactant feed 30 to preheater 70 takes place as usual, by transferring the heat from the gas coming from calciner 10 to the reactant. However, this results in the release of ammonia and / or hydrocarbons and hydrocarbon-containing compounds. To reduce these, the gas stream after preheater 70 is passed through a gas flow divider 80. A partial stream is discharged as exhaust air 80, another partial stream is combined with the gas feed 50 and fed to the material cooler and thus via material cooler 20 to calciner 10. In calciner 10, the nitrogen oxides produced by combustion are then converted again by ammonia released from the clay, and hydrocarbons and hydrocarbon-containing compounds are also burned.The preheated material is transferred from the preheater 70 into the calciner 10 and, after the thermal treatment in the calciner 10, into the material cooler 20 and leaves the device as product stream 40.

[0044] The third embodiment shown in Fig. 3 represents a hybrid of the first embodiment and the second embodiment. The reactant feed 30 leads to a reactant stream divider 90. Here, the reactant stream is divided, and a first partial reactant stream line 31 carries an unpreheated partial reactant stream directly into the calciner 10, and a second partial reactant stream line 32 carries a partial reactant stream into the preheater 70. As a result, a portion is first heated in the calciner 10, so that the substances released here, in particular ammonia as well as hydrocarbons and hydrocarbon-containing compounds, can be converted directly in the calciner 10. The other partial stream can recover part of the heat of the gas stream from the calciner 10 in the preheater 70. This also allows the undesired substances to escape during heating in the preheater 70.These are partially returned to the calciner through the separation in the gas flow divider 80, where they can be rendered harmless. This third embodiment has the advantage that adjustments can be made using two setting options (reactant flow divider 90 and gas flow divider 80). This can be useful, for example, to compensate for fluctuating emissions caused by differences in the clay. The preheated material is fed from the preheater 70 into the calciner 10, where it is combined with the first partial product stream. After thermal treatment in the calciner 10, the material is transferred to the material cooler 20 and leaves the device as product stream 40.

[0045] Fig. 4 shows a fourth embodiment, which differs from the third embodiment in particular in that this fourth embodiment has a control device 100 connected to three temperature sensors 110, wherein one temperature sensor 110 is arranged in the calciner 10, one temperature sensor between the calciner 10 and the preheater 70, and another temperature sensor 110 is arranged in the calciner. Of course, additional temperature sensors 110 may also be present. In addition, the device has a NO x -Analyzer 120, which measures the NO x -content in the exhaust gas of the preheater 70, as well as an NHs analyzer 122, which corresponds to the NHs content in the exhaust gas of the preheater 70. The control device 100 can, in particular, depending on the NO x -Analyzer 120 detected NO x-Concentration and the NHs concentration detected by the NHs analyzer 122, the reactant flow divider 90 and / or the gas flow divider 80 can be controlled. This allows, for example, more reactant to be introduced directly into the calciner 10 if the NO x concentration increases or more reactant is introduced into the preheater 70 in order to reduce NO X - concentrations to recover more energy. Likewise, at high NO X - concentrations the proportion of recirculation in the gas flow divider can be increased.

[0046] Additionally, the fourth embodiment shows a separate combustion chamber 130, in which, for example and in particular, substitute fuels, such as biomass, can be burned. In this case, the calciner 10 preferably has an auxiliary combustion device (not shown here), which is preferably also controlled by the control device 100. Temperature fluctuations resulting from fluctuations in the calorific value of the substitute fuel can be detected via the temperature sensors 110 and compensated accordingly via the auxiliary combustion device.

[0047] Reference symbol

[0048] 10 Calciners

[0049] 20 material coolers

[0050] 30 Educt feed

[0051] 31 first partial duct power line

[0052] 32 first partial duct power line

[0053] 40 Product stream

[0054] 50 Gas supply

[0055] 60 exhaust air

[0056] 70 preheaters

[0057] 80 Gas flow divider 90 Educt flow division

[0058] 100 control device

[0059] 110 Temperature sensor

[0060] 120 NOx analyzer 122 NHs analyzer

[0061] 130 combustion chamber

Claims

Patent claims 1. A process for producing thermally treated mineral material, in particular clay, in a calciner (10), wherein the pollutants released during heating of the mineral material, in particular clay, are thermally converted in the calciner (10), characterized in that at least a portion of the mineral material, in particular clay, is introduced directly and without preheating into the calciner (10).

2. The method according to claim 1, characterized in that at least one second mineral raw material is selected, wherein the at least one second mineral raw material is selected from the group comprising limestone, slag, granulated blast furnace slag, old cement block and sand.

3. Method according to one of the preceding claims, characterized in that at least a part of the mineral material, in particular the clay, is introduced into a preheater (70) and preheated in the preheater (70) and transferred from there into the calciner (10), wherein the gas coming from the preheater (70) is at least partially fed into the calciner (10).

4. Process according to claim 3, characterized in that the gas coming from the preheater (70) is passed into the calciner (10) via a material cooler (20).

5. Process according to one of claims 3 to 4, characterized in that at least one reactant is supplied to the gas coming from the preheater (70) before the gas is supplied to the calciner (10).

6. Method according to one of the preceding claims, characterized in that a fuel is supplied to the calciner (10), wherein the fuel is selected from the group comprising solid fuel, in particular coal dust, natural gas, biogas, hydrogen, ammonia, synthesis gas, liquid fuel, in particular oil. Device for the thermal treatment of mineral material, in particular clays, wherein the device comprises a calciner (10), wherein the device comprises a reactant feed (30), characterized in that the reactant feed (30) introduces mineral material, in particular clay, directly into the calciner (10) without preheating. Device according to claim 7, characterized in that the calciner (10) is connected directly, and thus without an intermediate preheater (70), to an exhaust gas treatment system or an exhaust outlet. Device according to one of claims 7 to 8, characterized in that a gas flow divider (80) is arranged in the gas flow leaving the preheater (70), wherein the gas flow divider (80) is connected to a return line, wherein the return line is connected to the calciner (10), a combustion chamber (130), or a material cooler (20), wherein the return line has a dust removal device.Device according to claim 9, characterized in that the dedusting device is connected to a dust return line, wherein the dust return line is connected to the calciner (10) or the preheater (70) on the side opposite the dedusting device. Device according to one of claims 9 to 10, characterized in that the reactant feed (30) has a reactant flow divider (90), wherein the reactant flow divider (90) is connected to a first partial reactant flow line (31) and a second partial reactant flow line (32), wherein the first. Partial duct flow line (31) is connected to the calciner (10) and the second partial duct flow line (32) is connected to the preheater (70). Device according to one of claims 7 to 11, characterized in that the device has a second duct feed, wherein the second duct feed is connected to the preheater. Device according to one of claims 7 to 12, characterized in that the device has at least one first temperature sensor (110), wherein the temperature sensor (110) is arranged in the calciner (10) or between the calciner (10) and the preheater (70), wherein the device has at least one auxiliary combustion device, wherein the auxiliary combustion device is arranged on the combustion chamber (130), between the combustion chamber (130) and the calciner (10) or in the calciner (10), wherein the device has a first control device (100), wherein the first control device (100) is connected to the first temperature sensor (110) and the auxiliary combustion device, wherein the first control device is designed to control the auxiliary combustion device depending on the temperature detected by the first temperature sensor (110). Device according to one of claims 7 to 13, characterized in that the device has at least one first NO x-analyser (120), wherein the NOx analyser (120) is arranged in the calciner (10) or between the calciner (10) and the preheater (70) or in the preheater (70) or after the preheater (70), wherein the device has at least one reactant flow divider (90) and / or a gas flow divider (80), wherein the device has a first control device (100) or a second control device (100), wherein the first control device (100) or the second control device (100) is connected to the first NOx analyser (120) and / or the temperature sensor (110) and the reactant flow divider (90) and / or the gas flow divider (80), wherein the first control device or the second control device (100) is for controlling the reactant flow divider (90) and / or the gas flow divider (80) as a function of the NOx analyser (120) recorded NO X- concentration and / or the temperature level detected by the temperature sensor (110). Device according to one of claims 7 to 14, characterized in that the device comprises at least one first organic analyzer, wherein the organic analyzer is arranged in the calciner (10) or between the calciner (10) and the preheater (70) or in the preheater (70) or after the preheater (70), wherein the device comprises at least one reactant flow divider (90) and / or one gas flow divider (80), wherein the device has a first Control device (100) or a second control device (100), wherein the first control device (100) or the second control device (100) is connected to the first organic analyzer and / or the temperature sensor (110) and the reactant flow divider (90) and / or the gas flow divider (80), wherein the first control device (100) or the second control device (100) is designed to control the reactant flow divider (90) and / or the gas flow divider (80) as a function of the organic concentration detected by the first organic analyzer and / or the temperature level detected by the temperature sensor (110). Device according to one of claims 7 to 15, characterized in that the device has at least one first NH3 analyzer, wherein the NH3 analyzer is arranged in the calciner (10) or between the calciner (10) and the preheater (70) or in the preheater (70) or after the preheater (70),wherein the device comprises at least one reactant flow divider (90) and / or one gas flow divider (80), wherein the device comprises a first control device (100) or a second control device (100), wherein the first control device (100) or the second control device (100) is connected to the first NH3 analyzer and / or the temperature sensor (110) and to the reactant flow divider (90) and / or the gas flow divider (80), wherein the first control device (100) or the second control device (100) is designed to control the reactant flow divider (90) and / or the gas flow divider (80) as a function of the NH3 concentration detected by the first NH3 analyzer and / or the temperature level detected by the temperature sensor (110).

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