LU103009B1 - Thermal treatment of mineral material, in particular clays, for the cement industry, in particular for the production of artificial pozzolans - Google Patents

Abstract

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

Description

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 1/13

Thermal treatment of mineral material, in particular clays, for

Cement industry, especially for the production of artificial pozzolana

The invention relates to a method for the thermal treatment of mineral

Material, in particular clay, and a plant therefor, whereby the material properties are simultaneously used to reduce the air pollutants generated during production.

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 when cement clinker is produced, for example from limestone, CO, escapes from the raw material. In order to reduce the CO,-

To reduce emissions, switching to another raw material, currently clay for example, is an important step in avoiding climate-damaging emissions.

A disadvantage of clays is that they contain a range of substances with different

A substance which is used in the thermal treatment of

The substance that often escapes from the clay when the material is preheated is ammonia.

Since ammonia should not (and must not) be released into the atmosphere, a

Exhaust gas treatment is installed downstream, which 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 purification is state of the art today and is usually found in practically every industrial plant that works with materials at higher temperatures.

Another pollutant that often escapes when clay is heated is

Hydrocarbons and hydrocarbon-containing compounds, here and in the following summarized under C,H for the sake of simplicity (and neglecting other heteroatoms), which must also be removed from the exhaust gas.

DE 102011014498 A1 describes a method for producing a

clinker substitute known.

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 2/13

A manufacturing process for synthetic pozzolans is known from US 9458 059 B2.

The object of the invention is to provide a method which allows the thermal

Treatment of mineral material, especially clays, in the most energy-efficient and thus environmentally friendly way possible.

This object is achieved by the method with the features specified in claim 1

Features. Advantageous further developments emerge from the subclaims, the following description and the drawings.

The process according to the invention is used for the production of thermally treated mineral material, in particular clays, for example and in particular for

Production of artificial pozzolans for use in the cement industry.

Production takes place in a calciner. When clays are heated, pollutants are generated that should not be released into the environment. These include, for example, and in particular, ammonia NH; and hydrocarbons and hydrocarbon-containing substances.

Compounds. These pollutants are usually removed using energy-intensive processes in one of the

Manufacturing facility downstream exhaust gas treatment and thus removed.

However, this process is energy-intensive and therefore leads to further avoidable

CO- emissions. Therefore, the CO released when the clay is heated

Pollutants are thermally converted in the calciner. The calciner has the right temperature for the decomposition of pollutants. There is also an additional, very positive effect. Ammonia usually comes out of the clay. During the combustion, which is required to generate the temperature in the calciner, nitrogen oxides are produced. The

Nitrogen oxides from the combustion process synproportionate with the ammonia from the clay to form nitrogen and water. This creates a double benefit and can even be used for the usual and energy-intensive downstream

Exhaust gas treatment can be dispensed with.

In a further embodiment of the invention, at least part of the mineral material, in particular the clay, is fed directly and without preheating into the thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 3/13

Calciner. This seems counterintuitive at first, as it

In contrast to the state of the art, energy recovery in the preheater is omitted. However, if one looks at the entire process including the

Exhaust gas purification, it is surprising that the energy saved during the exhaust gas purification more than compensates for the lack of preheating. And if downstream exhaust gas purification is carried out, the reduction rates required there are significantly lower. In addition, the exhaust gas enters at a higher temperature, so that the energy required for this also decreases.

Without preheating in the sense of the invention is meant a heating in which a

Heating occurs close to the treatment temperature and thus a

However, clays in particular must be treated with the appropriate

For this purpose, the raw material is heated, but not above a temperature range of 70 °C to 120 °C (the maximum temperature varies depending on the drying method and the raw material used). In this

However, the emissions of pollutants according to the invention do not yet occur within this temperature window, 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.

In a further embodiment of the invention, at least part of the mineral material, in particular the clay, is introduced into a chamber adjacent to the calciner.

part of the preheater and preheated in the preheater and from there into the

Calciner. For example, the preheater is a

Cascade of two to six direct current heat exchangers with cyclone separators, in this case the mineral material, especially the clay, is separated into the warmest,

Calciner adjacent DC heat exchanger. This

Embodiment is preferred if the calciner is 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 so high that the mineral material, in particular the clay, can be reliably decomposed when heated. This allows a balance between

Heat recovery and effective pollutant minimization can be achieved.

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 4/13

In a further embodiment, a second mineral raw material is added to the

Preheater, whereby the second mineral raw material is a mineral

A raw material is selected that has no or very little

Typical examples are limestone or sand, which are mixed with artificial pozzolans in the

cement industry. This allows heat recovery with the less critical reactants and at the same time a complex

Exhaust gas purification can be prevented.

In a further embodiment of the invention, at least part of the mineral material, in particular the clay, is introduced into a preheater and preheated in the preheater and transferred from there to the calciner. Therefore, the

Pollutants are already removed from the mineral material in the preheater, especially the

Clay, and are thus in the gas stream coming from the preheater. Therefore, the gas coming from the preheater is at least partially fed into the calciner.

The gas stream coming from the preheater can, for example, be

combustion chamber, which is connected to the calciner. This also allows the pollutants to reach the calciner as is the case with the direct introduction of the mineral

material, especially clay, into the calciner and have the same positive

Effect, especially on the energy required to generate the temperature

Combustion produces nitrogen oxides.

In a further embodiment of the invention, the gas coming from the preheater is fed into the calciner via a material cooler. Between the

A combustion chamber can also be arranged between the material cooler and the calciner. This allows the heat released by the product from the calciner to be fed back into the process.

In a further embodiment of the invention, the gas coming from the preheater is fed to a dust removal device, which is designed as a fabric filter, ceramic filter or electrostatic precipitator, for example, before being fed into a combustion chamber. This separates the dust content in the gas coming from the preheater thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 5/13 and can be fed back into the system at a suitable point, for example the calciner or the preheater. This prevents the dust content in the combustion chamber from being heated to an undesirably high temperature and thus thermally deactivated.

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

Sulphur compounds are used, in particular for conversion into sulphate. Sulphate is a desired additive in the cement industry, so that in this way

Sulfur contamination can be used profitably.

In a further embodiment of the invention, the calciner is provided with 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.

In a further embodiment of the invention, a fuel is supplied to the calciner. The fuel is selected from the group comprising coal dust,

Natural gas, biogas, hydrogen, ammonia and synthesis gas. These fuels are highly energetic and allow good combustion.

In a further embodiment of the invention, sulphur-containing

Compounds from the mineral material, especially the clay, are oxidized to sulfate.

Sulphates are common additives in cement, so that in this way the sulfur can be bound in a value-creating manner and adds value to the finished product.

At the same time, environmentally harmful emissions are avoided.

In a further aspect, the invention relates to a device for thermal

Treatment of mineral material, in particular clay. The device has a calciner. The device also has a feedstock. It is essential that the feedstock contains mineral material, in particular clay, without

Preheating is introduced directly into the calciner. 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 thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 6/13

Hydrocarbon compounds are released precisely in the calciner at the high temperature of the calciner. Hydrocarbons and hydrocarbon-containing

Compounds are burned directly, ammonia with the at these high

Temperatures are converted into nitrogen and water. This

In this way, the pollutants are directly converted in the calciner.

Preheating of the reactant and thus recovery of energy from the exhaust gas is dispensed with. This seems illogical as it reduces efficiency. However, it has been found that this means that complex exhaust gas purification can be dispensed with, which also requires a lot of energy.

In a further embodiment of the invention, the calciner is connected directly to an exhaust gas treatment or an exhaust outlet without an intermediate preheater. In this embodiment, the material flow is completely and without

In addition, if additional treatment is required, the exhaust gas stream can be heated to the temperature of the gas outlet of the

Calciners, which eliminates the need for reheating of the exhaust gases.

In a further aspect, the invention relates to a device for thermal

Treatment of mineral material, in particular clays, wherein the device comprises a calciner and a preheater. This corresponds to the conventional

Structure. According to the invention, in the gas stream leaving the preheater, a

Gas flow divider is arranged. 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 equipped with a

The return line is used to

The recirculation line is connected to the calciner or a combustion chamber or a material cooler. This creates two

effects are used. On the one hand, the energy can be fed back into the process in the preheater, as before, at least in part by preheating the material to be thermally treated. On the other hand, the gas divider, the

Pollutants are at least partially transferred to the calciner and can be converted there. Since complete recirculation would lead to an enrichment, for example of the CO from the firing, a part of the gas flow must be used as

Exhaust air flow can also be released into the environment.

In a further embodiment of the invention, the return line has a

Dust extraction system.

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 extraction device, the other end is connected to the

Calciner or preheater. This also includes indirect

Connection includes, for example, the connection between the calciner and the preheater or a material feeding 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.

In a further embodiment of the invention, the reactant feed has a

Educt flow division. The educt flow division is connected to a first partial duct flow line and a second partial duct flow line. The first partial duct flow line is connected to the calciner and the second partial duct flow line is connected to the preheater. This allows a hybrid of the two aforementioned devices to be used for

implementation of the method according to the invention. The first

The partial product stream is thus fed directly to the calciner, which ensures optimal

At the same time, part of the thermal energy can be fed back into the process via the second partial product stream and the preheater. In addition, the device has a second product feed, whereby the

Secondary product feed is designed for the supply of a second mineral raw material. The secondary product feed is connected to the preheater and via the

By adding a second raw material, a second mineral raw material can be fed into the preheater and the recovery of thermal energy from the preheater's exhaust gas can be further improved. The second mineral raw material is, for example, limestone or sand, which releases no or very few pollutants during preheating and can therefore be used without any problems to recover thermal energy in the preheater.

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 8/13

In a further embodiment of the invention, the device has at least one first temperature sensor. The temperature sensor is in the calciner or between

Calciner and preheater are arranged. The device further comprises at least one

The auxiliary combustion device serves in particular to

compensate for temperature fluctuations and is therefore usually operated with a fuel that is easy to dose and has a constant calorific value, for example

Gas or coal dust. The auxiliary combustion device is located in the combustion chamber, between

Combustion chamber and 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

The control device is designed to control the auxiliary combustion device as a function of the temperature detected by the first temperature sensor.

In a further embodiment of the invention, the device has at least one first NOx analyzer. For example and in particular, the NOx analyzer detects

Analyser the NO, concentration by infrared spectroscopy in an extractive

Measurement. The NO, 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, 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 division and/or the gas flow divider depending on the flow from the first

NO, concentration recorded by the NO, analyzer, taking the prevailing temperatures into account. This makes it easy to adapt to a fluctuating composition of the starting material and thus to a fluctuating release of pollutants in the process.

In a further embodiment of the invention, the device has at least one first organic analyzer. An organic analyzer can be, for example, a thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 9/13

Flame ionization detector for measuring the concentration of hydrocarbon and

Hydrocarbon-containing compounds. The organic 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 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 for controlling the

Educt flow division and/or the gas flow divider depending on the flow from the first

Organic analyzer, taking the prevailing temperatures into account. This makes it easy to adapt to fluctuating composition of the starting material and thus to fluctuating release of pollutants in the process.

In a further embodiment of the invention, the device has at least one first NH2 analyzer. The NH2 analyzer is in the calciner or between

Calciner and preheater or arranged in the preheater or after 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

The first control device or the second control device is connected to the first NHzs analyzer and/or the 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

Educt flow division and/or the gas flow divider depending on the flow rate from the first NHz

NH3 concentration detected by the analyzer and/or the temperature sensor

temperature levels.

The aforementioned devices are particularly preferably designed to carry out the method according to the invention or the inventive

The method can particularly preferably be carried out on one of the aforementioned devices.

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 10/13

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

Fig. 1 first embodiment

Fig. 2 second embodiment

Fig. 3 third embodiment

Fig. 4 fourth embodiment

In Fig. 1, the direct feed of reactant 30 into the calciner 10 is shown. 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 take place. 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 supplied to the material cooler 20 via the gas supply 50 and from there preheated to the calciner 10. The calciner 10 has a combustion device which is either arranged in the calciner 10 or upstream of the calciner 10.

The nitrogen oxides produced during combustion are reacted with the ammonia from the clay, so that no or only tolerable emissions are produced. Hydrocarbons and hydrocarbon-containing

Compounds that originate from the clay are reliably burned in sufficient quantities. The lack of heat recovery in a preheater is compensated for by the fact that no additional energy has to be used for exhaust gas purification.

Fig. 2 shows a second, alternative embodiment. Here, as usual, the

Educt feed 30 to preheater 70, in which the heat from the gas coming from the calciner 10 is transferred to the educt. However, this leads to

Release of ammonia and/or hydrocarbons and hydrocarbon-containing compounds. In order to reduce these, the gas flow is led through a gas flow divider 80 after the preheater 70. A partial flow is discharged as exhaust air 80, another partial flow is combined with the gas supply 50 and fed to the material cooler and thus fed to the calciner 10 via the material cooler 20. In the calciner 10 thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 11/13 the nitrogen oxides produced by combustion are then converted again by ammonia released from the clay and hydrocarbons and

Hydrocarbon-containing compounds are burned. The preheated material is fed 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.

The third embodiment shown in Fig. 3 represents a hybrid of the first

Embodiment and the second embodiment. The reactant feed 30 is carried out to an reactant flow divider 90. Here the reactant flow is divided and a first

Partial duct flow line 31 leads an unpreheated partial flow of the educt directly into the

Calciner 10 and a second partial duct flow line 32 leads a partial flow of the educt into the preheater 70. As a result, a part is only heated in the calciner 10, so that the substances released here, in particular ammonia and hydrocarbons and

Hydrocarbon-containing compounds, can be converted directly in the calciner 10. The other partial flow can be part of the heat of the gas flow from the

Calciner 10. This also causes the undesirable substances to escape during heating in preheater 70. These are partly separated by the separation in the

Gas flow divider 80 is returned to the calciner and can be rendered harmless there. This third embodiment has the advantage that over two

Adjustment options (educt flow divider 90 and gas flow divider 80) can be used to adjust the flow. 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 and mixed with the first

After thermal treatment in the calciner 10, the

Material is transferred to the material cooler 20 and leaves the device as product stream 40.

Fig. 4 shows a fourth embodiment, which differs from the third embodiment in particular in that this fourth embodiment has a

Control device 100 which is connected to three temperature sensors 110, wherein a temperature sensor 110 in the calciner 10, a temperature sensor between

Calcinator 10 and preheater 70 and a further temperature sensor 110 is arranged in the calciner thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 12/13. Of course, further temperature sensors 110 can also be present.

In addition, the device has a NO, analyzer 120 which measures the NO, content in the

Exhaust gas of the preheater 70, and an NHz analyzer 122, which is the NHz content in the exhaust gas of the preheater 70. The control device 100 can be used in particular in

Dependence of the NO, concentration measured by the NO, analyzer 120 and the

The reactant flow divider 90 and/or the gas flow divider 80 can be controlled based on the NHz concentration detected by the NHz analyzer 122. This allows, for example, more

Educt can be introduced directly into the calciner 10 when the NOx concentration increases or more educt can be introduced into the preheater 70 in order to

concentrations to recover more energy. Likewise, at high NO,

Concentrations the proportion of recirculation in the gas flow divider can be increased.

In addition, the fourth embodiment shows a separate combustion chamber 130 in which, for example and in particular, alternative fuels, for example biomass, can be burned. In this case, the calciner 10 preferably has a (not shown here)

Auxiliary combustion device, 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.

Reference numerals 10 Calciner 20 Material cooler 30 Educt feed 31 First partial duct flow line 32 First partial duct flow line 40 Product flow 50 Gas feed 60 Exhaust air 70 Preheater 80 Gas flow divider 90 Educt flow division 100 Control device thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 13/13

110 Temperature sensor

120 NO, analyzer

122 NHz--Analyzer

130 Combustion chamber

Claims (21)

thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 1/5 Patent claims 1. 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). 2. Process according to claim 1, characterized in that at least part of the mineral material, in particular the clay, is introduced directly and without preheating into the calciner (10). 3. Process according to one of the preceding claims, characterized in that at least a second mineral raw material is selected. 4. Process according to claim 3, characterized in that the at least one second mineral raw material is selected from the group comprising limestone or sand. 5. 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), the gas coming from the preheater (70) being at least partially led into the calciner (10). 6. Process according to claim 5, characterized in that the gas coming from the preheater (70) is led into the calciner (10) via a material cooler (20). 7. Method according to one of claims 5 to 6, 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). 8. Method according to one of the preceding claims, characterized in that the calciner (10) is operated at a temperature between 600 °C and 1400 °C, thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 2/5 preferably between 750 °C and 1050 °C, particularly preferably between 800 °C and 1000 °C. 9. 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 coal dust and other solid fuels, natural gas, biogas, hydrogen, ammonia and synthesis gas as well as liquid fuels such as oil. 10. Process according to one of the preceding claims, characterized in that in the calciner (10) sulfur-containing compounds from the mineral material, in particular the clay, are oxidized to sulfate. 11.Device for the thermal treatment of mineral material, in particular clays, the device comprising a calciner (10), the device comprising a reactant feed (30), characterized in that the reactant feed (30) introduces mineral material, in particular clay, directly into the calciner (10) without preheating. 12. Device according to claim 11, characterized in that the calciner (10) is connected directly and thus without an intermediate preheater (70) to an exhaust gas treatment or an exhaust. 13. Device for the thermal treatment of mineral material, in particular clays, the device comprising a calciner (10) and a preheater (70), characterized in that a gas flow divider (80) is arranged in the gas flow leaving the preheater (70), the gas flow divider (80) being connected to a return line, the return line being connected to the calciner (10), a combustion chamber (130) or a material cooler (20). 14. Device according to claim 13, characterized in that the return line has a dust removal device. thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 3/5 15. Device according to claim 13, 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. 16. Device according to claim 11 in combination with one of claims 13 to 15, characterized in that the reactant feed (30) has an 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 reactant flow line (31) is connected to the calciner (10) and the second partial reactant flow line (32) is connected to the preheater (70). 17. Device according to one of claims 11 to 16, characterized in that the device has a secondary product feed, wherein the secondary product feed is connected to the preheater. 18. Device according to one of claims 11 to 17, 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). 19. Device according to one of claims 11 to 17, characterized in that the device has at least one first NOx analyzer (120), wherein the NOx analyzer (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) thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 4/5 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 analyzer (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 designed to control the reactant flow divider (90) and/or the gas flow divider (80) as a function of the NOx concentration detected by the first NOx analyzer (120) and/or the temperature level detected by the temperature sensor (110). 20. Device according to one of claims 11 to 19, characterized in that the device has 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 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 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 used to control the reactant flow divider (90) and/or the gas flow divider (80) is designed as a function of the organic concentration detected by the first organic analyzer and/or the temperature level detected by the temperature sensor (110). 21. Device according to one of claims 11 to 20, characterized in that the device has at least one first NHs analyzer, wherein the NHs 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 has at least one reactant flow divider (90) and/or a gas flow divider (80), wherein the device has a first control device thyssenkrupp Industrial Solutions AG 221314P00LU thyssenkrupp AG LU103009 5/5 (100) or a second control device (100), wherein the first control device (100) or the second control device (100) is connected to the first NHs 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) for Control of the reactant flow division (90) and/or the gas flow divider (80) is designed as a function of the NHs concentration detected by the first NHs analyzer and/or the temperature level detected by the temperature sensor (110).