CEMENT-MANUFACTURING PLANT AND PROCESS FOR PRODUCING CEMENT CLINKER

Abstract

A cement production plant may include a preheater for preheating raw meal, a calciner for calcining the preheated raw meal, and a furnace with a furnace burner for firing the raw meal to form cement clinker. The furnace has a combustion gas inlet for admitting a combustion gas with an oxygen content of 30% to 75% into the furnace. The cement production plant may also include a cooler for cooling the cement clinker. The calciner and the furnace each have at least one respective fuel inlet for admitting at least one fuel into the calciner and the furnace. The calciner and the furnace each have at least one respective inert gas inlet for respectively admitting inert gas into the calciner and the furnace.

Description

The invention relates to a cement production plant and a method for producing cement clinker, wherein inert gas is introduced into at least one combustion process.

It is known from the prior art to feed oxygen-containing gas for the combustion of carbonaceous fuel into the rotary furnace or the calciner of a cement production plant. In order to reduce the amount of exhaust gas and to be able to dispense with complex purification processes, it is known, for example, from DE 10 2018 206 673 A1 to use a combustion gas that is as rich in oxygen as possible so that the CO2 content in the exhaust gas is high, Document DE 10 2018 206 673 A1 discloses the introduction of an oxygen-rich gas into the cooler inlet region for preheating the gas and cooling the clinker.

When using oxygen-enriched combustion gases that have a high oxygen content of at least 30% to 100%, very high temperatures can occur in the calciner and the furnace. If these high temperatures occur for a longer period of time or permanently in the region near the wall of the calciner, this can result in damage to the inner wall of the calciner. When hot zones occur in combination with the hot meal introduced, melting phases of the hot meal to be calcined are also to be expected. Based on this, it is the object of the present invention to provide a cement production plant and a method for producing cement, wherein a safe operation of the furnace line is ensured and at the same time an exhaust gas with a high CO2 content is obtained. An extended object is to charge the preheated raw meal into the calciner in an evenly distributed manner and to bring it into interaction with the hot gases produced as a result of the calciner firing. A preferred object of the invention is to realize the calciner firing by the targeted introduction of fuels, oxygen-containing gases, and hot raw meal in a staged form, so that a complete conversion of the introduced fuels, a complete calcination of the introduced raw meal particles, and the transport of the solid particles along the riser of the calciner are ensured without overheating in the riser and agglomeration of the solid particles along the riser.

In accordance with the invention, this object is achieved by a cement production plant having the features of independent Device claim 1 and by a method having the features of independent Method claim 12. Advantageous developments can be found in the dependent claims.

According to one aspect of the invention, a cement production plant comprises:

• • a preheater for preheating raw meal,
  • a calciner for calcining the preheated raw meal,
  • a furnace with a furnace burner, such as a burner lance, for firing the calcined hot meal to form cement clinker, wherein the furnace has a combustion gas inlet for admitting a combustion gas with an oxygen content of 30% to 100% into the furnace, and
  • a cooler for cooling the cement clinker, 1

wherein the calciner and the furnace each have at least one respective fuel inlet for admitting fuel into the calciner and into the furnace.

The calciner and the furnace each have at least one respective inert gas inlet for respectively admitting inert gas into the calciner and the furnace.

The preheater of the cement production plant preferably comprises a plurality of cyclone stages, each with at least one cyclone for separating solids from the gas flow. The invention makes it possible to operate the preheater with a significantly lower gas volume compared to a cement production plant that uses air as combustion gas. For example, the exhaust gas volume flow after the preheater is about 0.50 to 0.90 Nm3/kg clinker. The ratio of the feed quantity of raw meal to exhaust gas is accordingly higher possibly than in plants that are operated with air and is, for example, up to 3 kg/kg solids to gas, preferably 1.3 to 1.9 kg/kg solids to gas. In the preheater, the raw meal fed to the uppermost, first cyclone stage is preheated in counterflow to the furnace exhaust gases and passes here through the cyclone stages one after the other.

Between the last and the penultimate cyclone stage, the calciner is arranged, which has a riser into which the raw meal is heated by means of a calciner firing, which may consist of one or more firing positions. The calciner preferably comprises a fuel charging apparatus comprising the fuel inlet and the inert gas inlet. The fuel charging apparatus is for example tubular or formed as a radial bulge on the riser pipe of the calciner, Preferably, the fuel charging apparatus opens out into the riser pipe of the calciner so that fuel and/or inert gas are fed into the riser pipe of the calciner via the fuel charging apparatus. The fuel charging apparatus is a thermal treatment chamber that is used for heating and controlled addition of fuel into the riser.

Advantageously, the solids-to-gas ratio in the calciner is significantly higher compared to conventional systems with air as the oxidizer. For example, solids loadings of more than 2 kg per kg of gas occur locally, for example 2 to 8 kg per kg of gas. In the calciner, preferably the largest part, more than 60%, for example about 80%, of the fuel heat is converted. Due to the raw meal introduced at the lower end of the calciner, despite an initial oxygen concentration of 40-80%, which initiates intensive firing, there is a sufficient heat sink to prevent overheating. If lumpy substitute fuel, for example with edge lengths of >100 mm, is to be burned, an inclined region with a higher residence time for the fuel should preferably be provided. Examples of such inclined regions are stair treads, push grates, push-back grates or other mechanical or pneumatic devices. These devices function, for example, as combustion chambers, pre-combustion chambers or serve only for drying and preheating or partial gasification of the introduced fuels. The fuels can be of any type with regard to their particle size distribution and calorific value.

For example, the calcination reaction takes place under CO2 partial pressures between 10%-60% at the beginning of the calciner and up to 98% at the end of the calciner. Accordingly, the calcination reaction preferably proceeds at higher temperatures of 700 to 1100° C., preferably 900-1000° C., than in the conventional plant.

The raw meal preheated in the preheater and calcined in the calciner is then fed to the furnace. The furnace is preferably a rotary furnace with a rotary tube that can be rotated about its longitudinal axis and is preferably slightly inclined in the direction of conveyance of the material to be fired, so that the material is moved in the direction of conveyance due to the rotation of the rotary tube and gravity. The furnace preferably has a material inlet at one end thereof for admitting preheated, calcined raw meal and a material outlet at its end opposite the material inlet for discharging the fired clinker into the cooler. At the end of the furnace on the material outlet side, there is preferably a furnace head comprising the furnace burner for firing the material and preferably at least one fuel inlet for admitting fuel into the furnace, preferably via a furnace burner and/or via a fuel lance. The furnace preferably comprises a sintering zone in which the material is at least partially melted and in particular has a temperature of 1500° C. to 1900° C., preferably 1450° C. to 1750° C. The sintering zone comprises, for example, the furnace head, preferably the rear third of the furnace in the direction of conveyance of the material.

For example, all or part of the oxygen-containing combustion gas is introduced directly into the furnace head, wherein the furnace head has, for example, a combustion gas inlet. Preferably, the combustion gas is fully or partially introduced into the furnace via the material outlet of the furnace. The combustion gas supplied to the furnace has, for example, an oxygen content of more than 30% to 75%, preferably more than 95%. For example, the combustion gas consists entirely of pure oxygen, wherein in this case the oxygen content of the combustion gas is 100%. The furnace burner may be, for example, a burner lance. The cooler for cooling the cement clinker is preferably connected to the material outlet of the furnace.

The cooler has a conveying device for conveying the bulk material in the direction of conveyance through the cooling gas chamber. The cooling gas chamber comprises a first cooling gas chamber portion with a first cooling gas flow and, adjoining this in the direction of conveyance of the bulk material, a second cooling gas chamber portion with a second cooling gas flow. The cooling gas chamber is preferably bounded at the top by a cooling gas chamber ceiling and at the bottom by a dynamic and/or static grate, preferably by the bulk material lying thereon. The cooling gas chamber is in particular the entire chamber of the cooler above the bulk material through which cooling gas flows. The cooling gas flow passes through the dynamic and/or static grate, in particular through the conveying device, through the bulk material and into the cooling gas chamber. The first cooling gas chamber portion is preferably arranged, in the direction of flow of the bulk material to be cooled, directly after the cooler inlet, in particular the material outlet of the furnace. Preferably, the clinker falls out of the furnace into the first cooling gas chamber portion.

The first cooling chamber portion preferably has a static grate and/or dynamic grate arranged below the material outlet of the furnace so that the clinker exiting the furnace falls onto the static grate due to gravity. Preferably, only the first cooling gas flow flows into the first cooling gas chamber portion and is accelerated, for example, by means of a fan or pressure-loaded boiler or corresponding other device. The second cooling gas chamber portion adjoins the first cooling gas chamber portion in the direction of conveyance of the bulk material and is preferably separated from the first cooling gas chamber portion in terms of gas by means of a separating device. Preferably, only the second cooling gas flow, which is accelerated by means of at least one fan, flows into the second cooling gas chamber portion.

The second cooling gas chamber portion preferably has a dynamic grate for conveying the bulk material through the cooling gas chamber. The first cooling gas flow flowing through the first cooling gas chamber portion is, for example, pure oxygen or a gas with a content of less than 35 vol %. in particular less than 21 vol %, preferably 15 vol % or less of nitrogen and/or argon and/or with an oxygen content of more than 20.5%, in particular more than 30% to 75%, preferably more than 95%. The first cooling gas chamber portion preferably connects directly to the material outlet of the furnace, preferably to the furnace head of the furnace, so that the cooling gas is heated in the cooler and subsequently flows into the rotary furnace and is used as combustion gas. The second cooling gas flow is, for example, air.

The cooler preferably has a separating device for separating the cooling gas chamber portions from each other in terms of gas.

The inert gas is for example CO2 or water vapour. The introduction of inert gas into the calciner and/or the furnace offers the advantage of delaying, in particular slowing down, the combustion so that damage to the furnace and/or the calciner is prevented.

According to a first embodiment, the fuel inlet and the inert gas inlet are arranged separately from one another and each form an inlet into the furnace and/or the calciner. For example, the inert gas inlet is formed as an annular inlet around the fuel inlet. The conduit for conducting the fuel and the inert gas is formed, for example, as a double pipe, preferably as concentric pipes with different diameters. Preferably, the inert gas is conducted directly in the vicinity of the fuel inlet or the fuel charging apparatus. This enables an economical supply of the costly inert gas.

According to a further embodiment, the fuel inlet and the inert gas inlet together form an inlet. The fuel and the inert gas are preferably each fed to the calciner or the furnace in a common line. This is constructively less complex and thus more cost-effective.

According to a further embodiment, the calciner and/or the furnace have/has a respective plurality of inert gas inlets, in particular for admitting different inert gases. R is also conceivable that the calciner has a plurality of fuel charging apparatuses, in particular two or three fuel charging apparatuses, each of which is assigned an inert gas inlet. The fuel charging apparatuses are preferably arranged at a distance from one another along the length and/or width of the riser. For example, the fuel charging apparatuses are arranged offset from one another at an angle of 0°, preferably 60° to 270° across the cross section of the riser of the calciner. Different types of fuel charging apparatuses can be combined with each other and also arranged differently.

According to a further embodiment, the calciner has at least one raw meal inlet for admitting raw meal into the calciner, said raw meal inlet being arranged upstream of the fuel inlet and the inert gas inlet in the direction of flow of the gas within the calciner. For example, the raw meal inlet is located between two fuel charging apparatuses or fuel inlets in the calciner. Preferably, at least one raw meal inlet is arranged upstream of the fuel inlet in the direction of flow. This prevents overheating of the raw meal. The combustion zone created by the calciner firing can deliver the heat directly to the particles of the raw meal. The inert gas preferably additionally serves as a temperature sink and also prevents spontaneous ignition of the introduced fuel directly at the burner or burner lance mouth or at the inlet of the fuel charging apparatus.

According to a further embodiment, the calciner has at least one, preferably two or more raw meal inlets for admitting raw meal into the calciner and wherein at least one of the raw meal inlets and preferably at least one fuel inlet is arranged upstream of the fuel inlet, in particular upstream of the fuel charging apparatus, in the direction of flow of the gas within the calciner riser. Preferably, at least one or all of the raw meal inlets is arranged upstream of one or all of the fuel inlets. For example, the raw meal inlet is arranged at a distance from the fuel charging apparatus in the calciner.

According to a further embodiment, the cement production plant comprises a control device which is connected to a temperature measuring device within the calciner and which is configured in such a way that it controls/regulates the quantity of raw meal, inert gas and/or fuel in the calciner in dependence on the temperature ascertained by the temperature measuring device. The temperature measuring device is preferably connected to the control device in such a way that it transmits the ascertained temperature to the control device. The temperature measuring device is arranged, for example, downstream of one of the fuel charging apparatuses. The calciner has, for example, a plurality of temperature measuring devices, each of which is connected to the control device for transmitting the ascertained temperature. For example, a temperature measuring device is connected downstream of each fuel charging apparatus. It is also conceivable that a plurality of temperature measuring devices are arranged within the riser of the calciner, preferably evenly distributed.

For example, the quantity of fuel in the individual fuel charging apparatuses is controlled depending on the temperature. This ensures even and controlled combustion within the calciner with a homogenized temperature distribution and avoids temperature peaks that can damage the calciner or cause the material to melt.

The control device is designed, for example, in such a way that it compares the ascertained temperature with a predetermined setpoint value and, if the ascertained temperature deviates from the setpoint value, it controls the quantity of fuel, the quantity of inert gas and/or the quantity of raw meal in the calciner. If the ascertained temperature exceeds the predetermined setpoint, for example, the control device is designed in such a way that it reduces the fuel quantity, increases the raw meal quantity and/or increases the inert gas quantity. If the ascertained temperature falls below the predetermined setpoint, for example, the control device is designed in such a way that it increases the fuel quantity, reduces the raw meal quantity and/or reduces the inert gas quantity.

According to a further embodiment, at least one cross-sectional constriction of the calciner cross section is configured within the calciner. For example, the calciner has a plurality of cross-sectional constrictions in the riser. This accelerates the flow within the riser and then slows it down, so that flow-calmed regions are preferably formed.

According to a further embodiment, at least one guide element for guiding the gas flow is arranged within the calciner. This preferably achieves better mixing of the gas with the raw meal. This function is of particular importance for process control with high oxygen and low nitrogen contents in that the reduced gas quantity in the calciner due to the lack of nitrogen content results in a higher loading after the material has been fed in than in systems operated with air as the oxidant. It is therefore advantageous for the load-bearing capacity of the particles if the material is distributed evenly over the cross section of the riser of the calciner, Sinking of the meal into a deeper downstream zone of the calciner riser is prevented. The guide element is designed, for example, as a plate, a box, a cone and/or a pyramid. Preferably, a plurality of guide elements are arranged within the riser, for example evenly spaced apart. The guide elements are made of ceramic or a ceramic fibre composite material, for example. The guide elements are arranged in particular within the riser and/or in the fuel charging apparatus. Preferably, a guide element is arranged at the outlet of the fuel charging apparatus into the riser, so that the inlet of fuel into the riser is guided by means of the guide element. Preferably, the guide element extends from the fuel charging apparatus into the riser, For example, the guide element is formed and arranged to guide the fuel at an angle to the inner wall of the riser. For example, the guide element forms a diffuser with a widening cross section relative to the fuel charging apparatus.

According to a further embodiment, the calciner has a plurality of fuel charging apparatuses which each comprise a fuel inlet and an inert gas inlet, and wherein a guide element is assigned to each fuel charging apparatus. The respective fuel charging apparatus is arranged, for example, at the same height level as the guide element or is connected directly upstream or downstream of the guide element. This allows an optimized distribution of the raw meal and the inert gas within the riser, in particular in the region of the fuel charging apparatus.

According to a further embodiment, a combustion chamber is arranged between the furnace and the calciner or only in the calciner, said combustion chamber having a meal inlet, a fuel inlet, for example a fuel charging apparatus, and an inert gas inlet. The combustion chamber has, for example, a round cross section or is cyclone-shaped. It is also conceivable that the combustion chamber is designed as a calciner reaction chamber for simultaneous calcination, so that two calciners are connected in series or in parallel. This provides for regulation of the fuel conversion and calcination within the calciner or calciners.

The invention also comprises a method for producing cement clinker, comprising the following steps:

• • preheating raw meal in a preheater,
  • calcining the preheated raw meal in a calciner,
  • firing the preheated and calcined raw meal in a furnace with a furnace burner to form cement clinker, wherein a combustion gas with an oxygen content of 30% to 100% is supplied to the furnace, and 1vcooling the cement clinker in a cooler, wherein a fuel is supplied to the furnace and to the calciner.

An inert gas is supplied to each of the furnace and the calciner.

The above-described embodiments and advantages of the cement production plant also apply to the method for producing cement clinker.

According to a further embodiment, the inert gas is supplied to the calciner and/or to the furnace together with or separately from the fuel and/or the raw meal. For example, at least two different inert gases are introduced into the calciner and/or the furnace.

According to a further embodiment, the raw meal is admitted into the calciner in the direction of flow of the gas within the calciner prior to the fuel and the inert gas. For example, at least part of the raw meal and the fuel is admitted into the calciner in the direction of flow of the gas within the calciner upstream of a fuel charging apparatus. Preferably, the raw meal has a temperature of 700 C to 900° C. when admitted into the calciner.

According to a further embodiment, the temperature within the calciner is ascertained and the quantity of raw meal, inert gas and/or fuel that is supplied to the calciner is controlled/regulated in dependence on the ascertained temperature.

According to a further embodiment, a flow-calmed region is configured within the calciner by means of at least one guide element or at least one cross-sectional constriction of the calciner cross section.

Description of the drawings

The invention is explained in more detail below by means of several exemplary embodiments with reference to the accompanying figures.

FIG. 1 shows a schematic representation of a cement production plant with a calciner and a furnace according to an exemplary embodiment.

FIG. 2 shows a schematic representation of a calciner with an inert gas inlet according to a further exemplary embodiment.

FIG. 3 shows a schematic representation of a calciner with an inert gas inlet according to a further exemplary embodiment.

FIG. 4 shows a schematic representation of a calciner with a guide element according to two further exemplary embodiments.

FIG. 1 shows a cement production plant 10 with a single-line preheater 12 for preheating raw meal, a calciner 14 for calcining the raw meal, a furnace 16, in particular a rotary furnace for firing the raw meal to form clinker, and a cooler 18 for cooling the clinker fired in the furnace 16.

The preheater 12 comprises a plurality of cyclones 20 for separating the raw meal from the raw meal gas flow. By way of example, the preheater 12 has five cyclones 20 arranged in four cyclone stages one below the other. The preheater 12 has a material inlet, not shown, for admitting raw meal into the uppermost cyclone stage of the preheater 12 comprising two cyclones 20. The raw meal successively flows through the cyclones 20 of the cyclone stages in counterflow to the furnace and/or calciner exhaust gas and is thereby heated. The calciner 14 is arranged between the last and the penultimate cyclone stage. The calciner 14 has a riser, in particular a riser pipe, with at least one calciner firing for heating the raw meal, so that calcination of the raw meal takes place in the calciner 14. Furthermore, the calciner 14 comprises a fuel inlet for admitting fuel and an inert gas inlet for admitting an inert gas into the riser. The calciner 14 further comprises a combustion gas inlet 26 for admitting oxygen-containing combustion gas into the riser of the calciner 14. The combustion gas is in particular the furnace exhaust gas enriched with oxygen. The oxygen content of the combustion gas is at most 85% between the furnace 16 and the calciner 14. The calciner exhaust gas is introduced into the preheater 12, preferably into the penultimate cyclone stage, and leaves the preheater 12 downstream of the uppermost cyclone stage as preheater exhaust gas 22.

The furnace 16 is connected downstream of the preheater 12 in the direction of flow of the raw meal, so that the raw meal preheated in the preheater 12 and calcined in the calciner 14 flows into the furnace 16. The material inlet/gas outlet 25 of the furnace 16 is directly connected to the riser of the calciner 14, so that the furnace exhaust gas flows into the calciner 14 and then into the preheater 12. The furnace 16 is, by way of example, a rotary furnace with a rotary tube rotatable about its longitudinal axis and arranged at a slight downward angle. The furnace 12 has a furnace burner 28 and an assigned fuel inlet 30 at the material outlet end within the rotary furnace tube. The material outlet of the furnace 16 is located at the opposite end of the rotary tube from the material inlet 25, such that the raw meal is conveyed within the rotary tube by rotation of the rotary tube towards the furnace burner 28 and the material outlet. The raw meal is fired within the furnace 16 to form cement clinker. The sintering zone 32 comprises the rear region of the rotary tube on the material outlet side, preferably the rear third in the direction of material flow.

The cooler 18 for cooling the clinker is connected to the material outlet of the furnace 16. The cooler 18 has a cooling gas chamber 34 in which the clinker is cooled by a cooling gas flow. The clinker is conveyed in a direction of conveyance F through the cooling gas chamber 34. The cooling gas chamber 34 has a first cooling gas chamber portion 36 and a second cooling gas chamber portion 38, which adjoins the first cooling gas chamber portion 36 in the direction of conveyance F. The furnace 16 is connected to the cooler 18 via the material outlet of the furnace 16, so that the clinker fired in the rotary furnace 20 falls into the cooler 18.

The first cooling gas chamber portion 36 is arranged below the material outlet of the furnace 16, so that the clinker from the furnace 16 falls into the first cooling gas chamber portion 36. The first cooling gas chamber portion 36 constitutes an inflow region of the cooler 18 and preferably comprises a static grate 40 which receives the clinker exiting the furnace 16. In particular, the static grate 40 is completely arranged in the first cooling gas chamber portion 36 of the cooler 10. Preferably, the clinker from the furnace 16 falls directly onto the static grate 40. The static grate 40 preferably extends completely at an angle of 10° to 35°, preferably 14° to 33°, in particular 21 ° to 25° to the horizontal, so that the clinker slides along the static grate 40 in the direction of conveyance.

The first cooling gas chamber portion 36 is adjoined by the second cooling gas chamber portion 38 of the cooler 18. In the first cooling gas chamber portion 36 of the cooler 18, the clinker is cooled in particular to a temperature of less than 1000° C., wherein the cooling is performed in such a way that a complete solidification of liquid phases present in the clinker into solid phases takes place. When leaving the first cooling gas chamber portion 36 of the cooler 18, the clinker is preferably completely in the solid phase and at a temperature of 1000° C. or less. In the second cooling gas chamber portion 38 of the cooler 18, the clinker is further cooled, preferably to a temperature of less than 100° C. Preferably, the second cooling gas flow can be divided into a plurality of partial gas flows which have different temperatures.

The static grate of the first cooling gas chamber portion 36 has, for example, passages through which a cooling gas enters the cooler 18 and the clinker. The cooling gas is generated, for example, by at least one fan, blower or pressure vessel arranged below the static grate 40, so that a first cooling gas flow 42 flows from below through the static grate into the first cooling gas chamber portion 36. The first cooling gas flow 42 is, for example, pure oxygen or a gas containing 15 vol % or less of nitrogen and 30 vol % or more of oxygen. The first cooling gas flow 42 flows through the clinker and then flows into the furnace 16. The first cooling gas flow forms, for example, part or all of the combustion gas of the furnace 16. The high proportion of oxygen in the combustion gas results in a preheater exhaust gas consisting substantially of CO2 and water vapour, and has the advantage of eliminating the need for costly downstream purification processes for exhaust gas purification. Furthermore, a reduction of the process gas quantities is achieved, so that the plant can be dimensioned considerably smaller.

Inside the cooler 18, the clinker to be cooled is moved in the direction of conveyance F. The second cooling gas chamber portion 38 preferably has a dynamic, in particular movable, grate 44, which adjoins the static grate 40 in the direction of conveyance F. Below the dynamic grate 44, a plurality of fans are arranged by way of example, by means of which the second cooling gas flow 46 is blown from below through the dynamic grate 44. The second cooling gas flow 46 is, for example, air.

In FIG. 1, a comminution device 48 is connected to the dynamic grate 44 of the second cooling gas chamber portion 38 by way of example. A further dynamic grate 50 is connected to the comminution device 48 below the comminution device 48. Preferably, the cold clinker 52 has a temperature of 100° C. or less when leaving the cooler 18.

For example, cooler exhaust air 54 is discharged from the second cooling gas chamber portion 38 and fed into a separator 56, such as a cyclone, for separating solids. The solids are fed back to the cooler 18, for example. An air-to-air heat exchanger 58 is connected downstream of the separator 56, so that the cooler exhaust air preheats air within the heat exchanger 58, which is fed to a raw mill, for example.

FIG. 2 shows a detail of a cement production plant 10 according to FIG. 1, wherein the regions not shown correspond, for example, to those of FIG. 1 and like reference signs represent like elements. The calciner 14 shown in FIG. 2 has two fuel charging apparatuses 60 by way of example. R is also conceivable that the calciner 14 has only exactly one fuel charging apparatus 60 or more than two fuel charging apparatuses 60. The two fuel charging apparatuses 60 are mounted at a distance from each other on the riser 62 of the calciner 14. By way of example, the fuel delivery devices 60 are mounted at different height levels on the riser 62. Each fuel charging apparatus 60 is assigned a fuel inlet 24 and an inert gas inlet 64, such that fuel and inert gas are directed into the fuel charging apparatus 60. The fuel charging apparatuses 60 are arranged offset from each other by 180°, by way of example. For example, the fuel charging apparatus comprises a means for transporting the fuel, such as a screw conveyor or a chute. The fuel or fuels can also be fed in pneumatically, for example, by conveying with the aid of an inert gas.

FIG. 2 further shows that a fuel inlet 30 and an inert gas inlet 68 are assigned to the furnace burner 28 so that fuel and inert gas are supplied to the furnace burner 28. The fuel inlet 24, 30 and the inert gas inlet 64, 68 are formed, for example, separately from each other or as a common inlet into the calciner 14 or the furnace 16. The inert gas is, for example, CO2 or water vapour. The inert gas may serve both as a conveying agent and to influence the ignition or control of the combustion process,

In FIG. 2, the raw meal inlet 70 in the calciner 14 is formed by way of example by the solids outlet of the penultimate cyclone stage. The raw meal inlet 70 is arranged, for example, between the two calciner burners 60. Alternatively, the raw meal can preferably be fed below each of the individual combustion zones downstream of the fuel inlets 30. Another possibility for feeding raw meal and fuel is to use a combustion chamber arranged parallel to the riser of the calciner to feed fuel and meal simultaneously in a low-oxygen zone. Preferably, the fuel is fed centrally into a downwardly directed combustion chamber. Around the fuel feed, the raw meal is fed on a radial circumference or on the circumference of the cylindrical combustion chamber in such a way that the fuel is surrounded by a curtain of meal. At the lower end of the combustion chamber, this connects to the upwardly directed riser of the calciner. The fuel encased by the meal is introduced into the oxygen-rich calciner flow, where it is ignited. The heat is directly consumed by the calcining reaction of the raw meal.

The calciner 14 has, by way of example, a temperature measuring device 66 for ascertaining the temperature inside the calciner 14. The cement plant 10 further comprises a control device 72 which is connected to the temperature measuring device in such a way that the temperature measuring device 66 transmits the ascertained temperature to the control device 72. The control device 72 is connected to the fuel inlet 24, the raw meal inlet 70 and/or the inert gas inlet 64 and is designed in such a way that it controls/regulates the quantity of fuel, raw meal and/or inert gas in the calciner 14 in dependence on the ascertained temperature.

FIG. 3 shows a further example of a calciner 14 of FIGS. 1 and 2, wherein like reference signs represent like elements. The riser 62 of the calciner 14 has a plurality of different cross-sectional areas. The fuel charging apparatuses 60 of the calciner 14 are attached to the same side of the riser 62, for example without angular offset, but at different height levels. In the direction of flow of the gas within the riser 62, each fuel charging apparatus 60 has a respective raw meal inlet 70 directly upstream and/or downstream. The fuel inlet 24 and the inert gas inlet 64 are each arranged at the fuel charging apparatus 60 of the calciner 14, in particular at the same level as the respective fuel charging apparatus 60.

The cross-sectional constrictions ensure balanced mixing within the riser and thus lead to even combustion and temperature distribution in the longitudinal and transverse directions of the riser of the calciner.

In FIG. 4 is a detail of a calciner 14, wherein like reference signs represent like elements. The calciner 14 has a guide element 73, which in the left-hand illustration is attached by way of example within the riser 62 and in the right-hand illustration is attached by way of example to the fuel charging apparatus 60 in the specific form of a flue.

In the left-hand illustration, the guide element 73 is arranged in such a way that it causes a constriction of the cross section of the riser 62. The guide element 73 is in particular in plate form, chamber form or box form and is attached to the inner wall of the riser 62, moreover, by way of example, at the same height and opposite the fuel charging apparatus 60.

In the right-hand illustration, the guide element 73 has the exemplary form of a diffuser, wherein the cross section of the guide element 73 increases in the direction of flow of the fuel. The guide element 73 is attached to the fuel charging apparatus 60, in particular at the mouth of the fuel charging apparatus 60 into the riser 62, and in particular allows a targeted introduction of the fuel into the riser 62. It is also conceivable that the guide element 73 is flush with the riser and does not project into it, so that a uniform inlet of the fuel into the riser 62 is allowed.

The guide element 73 is formed, for example, from a high-temperature-resistant ceramic or a fibre composite material.

LIST OF REFERENCE SIGNS

10 cement production plant

12 preheater

14 calciner

16 furnace

18 cooler

20 cyclone

22 preheater exhaust gas

24 fuel inlet of the calciner

25 material inlet into the furnace

26 combustion gas inlet of the calciner

28 burner or burner lance of the furnace

30 fuel inlet of the furnace

32 sintering zone

34 cooling gas chamber

36 first cooling gas chamber portion

38 second cooling gas chamber portion

40 static grate

42 first cooling gas flow

44 dynamic grate

46 second cooling gas flow

48 comminution device

50 dynamic grate 50

52 cold clinker

54 cooler exhaust air

56 separator

58 heat exchanger

60 fuel charging apparatus

62 riser of the calciner

66 temperature measuring device

64 inert gas inlet

68 inert gas inlet into the furnace

70 raw meal inlet into the calciner

72 control device

73 guide element

Claims

1.-16. (canceled)

17. A cement production plant comprising: a preheater configured to preheat raw meal;a calciner configured to calcine the raw meal that has been preheated;a furnace with a furnace burner configured to fire the raw meal to form cement clinker, wherein the furnace has a combustion gas inlet configured to admit a combustion gas with an oxygen content of 30% to 100% into the furnace; anda cooler configured to cool the cement clinker;wherein the calciner and the furnace have a respective fuel inlet configured to admit fuel into the calciner and the furnace, wherein the calciner and the furnace have a respective inert gas inlet for respectively admitting inert gas into the calciner and the furnace.

18. The cement production plant of claim 17 wherein the fuel inlet and the inert gas inlet are arranged separately from one another and each forms an inlet.

19. The cement production plant of claim 17 wherein the fuel inlet and the inert gas inlet together form an inlet.

20. The cement production plant of claim 17 wherein at least one of the calciner or the furnace has multiple inert gas inlets.

21. The cement production plant of claim 17 wherein the calciner has a raw meal inlet configured to admit raw meal into the calciner, wherein the raw meal inlet is arranged upstream of the fuel inlet and the inert gas inlet in a direction of flow of gas within the calciner.

22. The cement production plant of claim 17 wherein the calciner has a raw meal inlet configured to admit raw meal into the calciner, wherein the raw meal inlet is arranged downstream of the fuel inlet and the inert gas inlet in a direction of flow of gas within the calciner.

23. The cement production plant of claim 17 wherein the calciner has at least two raw meal inlets configured to admit raw meal into the calciner, wherein at least one of the at least two raw meal inlets is arranged upstream of the fuel inlet in a direction of flow of gas within the calciner.

24. The cement production plant of claim 17 comprising a control device that is connected to a temperature measuring device within the calciner and that is configured to regulate a quantity of at least one of raw meal, inert gas, or fuel in the calciner based on a temperature ascertained by the temperature measuring device.

25. The cement production plant of claim 17 wherein at least one cross-sectional constriction of a calciner cross section is configured within the calciner.

26. The cement production plant of claim 17 comprising a guide element for guiding at least one of gas flow or fuel within the calciner.

27. The cement production plant of claim 27 comprising multiple of the guide element, wherein the calciner includes fuel charging apparatuses that each comprises a fuel inlet and an inert gas inlet, wherein one of the guide elements is assigned to each fuel charging apparatus.

28. The cement production plant of claim 17 comprising a combustion chamber disposed between the furnace and the calciner, the combustion chamber having a raw material inlet, a fuel inlet, and an inert gas inlet.

29. A method for producing cement clinker, the method comprising: preheating raw meal in a preheater;calcining in a calciner the raw meal that has been preheated;firing in a furnace with a furnace burner the raw meal that has been preheated and calcined to form cement clinker, wherein a combustion gas with an oxygen content of 30% to 100% is supplied to the furnace; andcooling the cement clinker in a cooler; andsupplying a fuel and an inert gas to the furnace and to the calciner.

30. The method of claim 29 comprising supplying the inert gas to the calciner and/or to the furnace together with the fuel.

31. The method of claim 29 comprising supplying the inert gas to the calciner and/or to the furnace separately from the fuel.

32. The method of claim 29 comprising admitting the raw meal into the calciner in a direction of flow of gas within the calciner prior to the fuel and the inert gas.

33. The method of claim 29 comprising: ascertaining a temperature within the calciner; andregulating a quantity of at least one of raw meal, inert gas, or fuel that is supplied to the calciner based on the temperature.

34. The method of claim 29 wherein a flow-calmed region is configured within the calciner by way of a guide element or a cross-sectional constriction of a cross section of the calciner.