The invention relates to a vertical-shaft kiln (2) for manufacturing a clinker, including:

TECHNICAL FIELD

The present invention relates to a vertical-shaft kiln for manufacturing a clinker, in particular sulfo-aluminous, sulfo-aluminous belite, alinite, fluoro-alinite, chloro-aluminous, or more generally any clinker forming into a solid solution without generating a liquid phase, as well as an installation equipped with this kiln.

BACKGROUND

The term “vertical-shaft kiln” designates any kiln of which the enclosure extends in a substantially vertical direction.

An installation for manufacturing a clinker usually has two objectives: to mass manufacture a clinker and manufacture a regular, that is to say a homogenous clinker.

It is known from the state of the art an installation for manufacturing a sulfo-aluminous clinker equipped with a cyclone preheater, a precalciner and a rotary kiln. Such an installation allows mass production but not the production of a regular clinker.

It is known, by document FR2928643, an installation for the manufacture of a sulfo-aluminous clinker equipped with a vertical-shaft kiln for decarbonatation and a continuous clinkering kiln.

The vertical-shaft kiln comprises an enclosure inside which a raw mix is poured containing in particular calcium, aluminum, silica, iron and sulfur in combined mineral form such as for example oxides, hydroxides, carbonates, chlorides or sulfates. The vertical-shaft kiln comprises supply furnace flues of a gas at a temperature ranging between 900° C. and 1150° C., in such a manner as to dehydrate and decarbonate the raw mix.

The continuous kiln comprises a furnace, inside which a plurality of moveable carriages circulate. One layer of raw mix from the vertical-shaft kiln is extended over each of the carriages. The continuous kiln comprises a plurality of burners distributed along the furnace. These burners take the raw mix to a temperature in the range of 1250° C. to 1450° C., in such a manner as to clinker it.

Such an installation allows to finely monitor the profile of temperatures during the clinkering by adjusting the power of the burners and the speed of displacement of the carriages. Thus, the manufactured clinker exhibits a very good regularity.

However, the thickness of the layers of raw mix disposed on the carriages of the continuous kiln is low. Moreover, the production capacity of such an installation is limited.

It is also known, by document CN1094383, an installation for the manufacture of a sulfo-aluminous clinker equipped with a vertical-shaft kiln. This vertical-shaft kiln comprises a furnace inside which is poured a raw mix containing calcium, aluminum, silica, iron, and sulfur mixed with a solid combustible such as coal.

A drawback of such an installation is that the raw mix exhibits an irregular granulometry. In addition, when this raw mix is poured into the furnace, the air circulates in unequal quantity between the pellets forming the raw mix, and the combustible is mixed in a heterogeneous manner. Thereafter, the combustion of the combustible is unequal, and the achieved clinker is irregular.

Furthermore, the proximity of the combustible and the raw mix pellets causes the formation of reducing zones in the furnace, that is to say zones without oxygen. These reducing zones lead to the loss of sulfur and a degradation of the chemical composition sought. Particularly, a C12A7phase, called mayenite, appears. This phase highly accelerates the hydraulic setting up of a cement, and is consequently detrimental.

Finally, a vertical-shaft kiln, of the type described in document CN1094383, is generally provided with an ambient air inlet mouth in lower portion of the furnace.

Such a mouth allows the intake of combustion air of the solid combustible mixed with the raw mix.

Such a mouth further allows the cooling of the clinker before extraction from the furnace. On the other hand, the sticking risks, and after the blinding of the furnace, by the clinker may be limited.

A drawback of such a type of vertical-shaft kiln is that the cooling is undergone rather than mastered. However, it is known that the cooling speed of the clinker determines the setting up time and the demand for water of the cement achieved based on this clinker.

As a result, a cement achieved from a clinker manufactured in this type of kiln exhibits a badly mastered setting up time and demand for water.

BRIEF SUMMARY

The purpose of the invention is to remedy to all or part of the aforementioned drawbacks.

The invention aims in particular to provide a vertical-shaft kiln for manufacturing a regular sulfo-aluminous clinker and as part of a mass production.

The invention relates to a vertical-shaft kiln for manufacturing a clinker, characterized in that it comprises:a tubular enclosure comprising from top to bottom:a feeder section extending substantially vertically, designed for receiving a raw mix;a decarbonatation section exhibiting a lower surface slanted with respect to the vertical;a clinkering section exhibiting a lower surface slanted with respect to the vertical;a first collection section extending substantially vertically;first extraction means arranged for extracting the clinker from the first collection section, suitable for modulating the extraction output of the clinker;first generation means arranged for generating a first gas exhibiting a temperature ranging between 950° C. and 1250° C.;first supply means arranged to supply the first gas in the decarbonatation section;second generation means arranged for generating a second oxidizing gas exhibiting a temperature ranging between 1250° C. and 1450° C.;second supply means arranged to supply the second oxidizing gas in the clinkering section; andfirst suction means for suctioning the first and second gas from the feeder section.

According to a first embodiment, the lower surface of the clinkering section is oriented transversally to the lower surface of the carbonatation section.

According to a second embodiment, the lower faces of the decarbonatation and clinkering sections are slanted in the same direction. Preferably, they have the same inclination. They may be shifted with respect to one another, a downward setback being provided between the lower end of the lower surface of the decarbonatation section and the upper end of the lower surface of the clinkering section.

The clinker manufactured by the kiln according to the invention may be a sulfo-aluminous clinker, a sulfo-aluminous belite, alinite, fluoro alinite, chloro-aluminous, or more generally any clinker forming into a solid solution without generating a liquid phase.

The use of the second oxidizing gas, that is to say with excess air, is particularly advantageous in that it prevents the formation of reducing zones in the clinkering section, and after prevents the formation of the prejudicial C12A7phase.

The use of decarbonatation and clinkering sections exhibiting lower slanted surfaces allows distributing the load on the lower surfaces and not on the pellets forming the raw mix anymore, in such a manner as to reduce the sticking and blinding risk of the decarbonatation and clinkering sections.

The lower surfaces of the decarbonatation and clinkering sections oriented transversally allow forming a ramp through which the first and/or the second gas ascends in counter current. Thus, the thermal exchanges between the raw mix and the first and second gas are maximized.

The dissociation of the first and second supply means allows to finely monitor the temperature profile in the decarbonatation and clinkering section.

The first extraction means allows to finely adjust the residence time of the raw mix in the clinkering section.

Thus, the regularity of a clinker manufactured with an installation equipped with a vertical-shaft kiln according to the invention is:better than that of a clinker manufactured with the installation described in document CN1094383; andsubstantially identical to that of a clinker manufactured with the installation described in document FR2928643.

An installation equipped with the vertical-shaft kiln according to the invention exhibits a production capacity higher than that of the installation described in document FR2928643.

Finally, the vertical-shaft kiln according to the invention no longer requires that the raw mix be mixed with a solid combustible, thus allowing to be rid of the drawbacks linked to the use of a solid combustible.

The vertical-shaft kiln according to the invention may comprise one or several of the following features.

According to a feature, the decarbonatation section and the clinkering section exhibit rectangular transversal sections;the decarbonatation section and the clinkering section exhibit upper surfaces slanted with respect to the vertical;the lower edge of the lower surface of the decarbonatation section extends substantially vertically in line with the lower edge of the upper surface of this decarbonatation section; andthe lower edge of the lower surface of the clinkering section extends substantially vertically in line with the lower edge of the upper surface of this clinkering section.

Preferably, the lower surfaces of the decarbonatation and clinkering sections form an angle ranging between 80° and 140°.

Preferably, the lower surfaces of the decarbonatation and clinkering sections form an angle which is lower than 45° with respect to the vertical.

Advantageously, the first generation means are distinct from the second generation means.

Advantageously, the first supply means are arranged to supply the first gas in the decarbonatation section, from the downstream end of this decarbonatation section; andthe second supply means are arranged to supply the second gas in the clinkering section, from the downstream end of this clinkering section.

Thus, the first and second gases bring up the raw mix in counter current over the entire length of the decarbonatation and clinkering sections, in such a manner that the thermal exchanges are maximized.

In this description, the terms “upstream” and “downstream” are used with reference to the flow direction of the raw mix in the enclosure.

Advantageously still, the decarbonatation section exhibits a plurality of longitudinal walls dividing this section into a plurality of ducts; and/or

the clinkering section exhibits a plurality of longitudinal walls dividing this section into a plurality of ducts.

Such walls allow homogenizing the speed profile of the raw mix over the entire width of the decarbonatation and clinkering sections, and then homogenizing the residence time of the raw mix in each of the decarbonatation and clinkering sections.

Furthermore, such walls allow distributing the load on the walls and no longer on the pellets forming the raw mix, in such a manner as to reduce the risk of sticking and blinding the decarbonatation and clinkering sections.

According to a feature, the first supply means comprise a plurality of first furnace flues each opening at the downstream end of a duct of the decarbonatation section; andthe second supply means comprise a plurality of second furnace flues each opening at the downstream end of a duct of the clinkering section.

Such an arrangement allows ensuring that each of the ducts of the decarbonatation section and of the clinkering section receives a same output of first or second gas. Thus, the thermal treatment of the raw mix is identical in each of the ducts.

Advantageously, the kiln comprises:a second collection section disposed between the decarbonatation section and the clinkering section;second extraction means arranged for extracting the decarbonated raw mix contained in the second collection section and supply it to the clinkering section, these second extraction means being suitable for modulating the extraction output of the decarbonated raw mix.

The second extraction means allow to finely adjust the residence time of the raw mix in the decarbonatation section.

Preferably, the first and/or second extraction means comprise:an upper stationary part and a lower moveable part delimiting a connecting section, this section being provided with an inlet mouth and an outlet mouth shifted vertically and horizontally;the lower moveable part being able to be displaced in a determined direction alternatively between an advanced position and a receded position, to allow the flow, respectively, of the clinker and the decarbonated raw mix in the connecting section; andmeans for displacing and guiding the moveable part relatively to the stationary part.

The first and/or second extraction means thus comprise extraction means of reciprocating feeder type.

The residence time of the raw mix in the decarbonatation section and/or in the clinkering section may be adjusted by playing on the frequency and the travel of the moveable part.

Advantageously, the upper stationary part of the first extraction means exhibits an ambient air supply pipe equipped with means for regulating the supplied ambient air output.

Such a pipe allows regulating the air output in the second extraction means and then mastering the cooling of the clinker.

The cooling of the clinker allows limiting the risks of sticking and blinding of the first extraction means.

According to a feature, the kiln comprises second suction means arranged between the decarbonatation section and the clinkering section to suction all or part of the second gas from the clinkering section.

In these conditions, the second gas ascends into the clinkering section and is then discharged from the enclosure. Only a tiny part of the second gas ascends into the decarbonatation section. Monitoring the thermal profile in the decarbonatation section is thus mastered better.

According to another feature, the kiln comprises means for adjusting the position of the upper slanted surface of the clinkering section with respect to the lower slanted surface of the clinkering section, in such a manner as to make the residence time of the clinker in the clinkering section vary.

This flexibility allows making the clinkering section cross-section vary and hence acts on the clinkering time by keeping a constant pellet height.

According to another feature, the kiln comprises:first means for measuring the temperature of the first and second supplied gases;second means for measuring the pressure of the first and second supplied gases; and/orthird means for measuring the temperature of the raw mix inside the decarbonatation and clinkering sections; anda controlling unit arranged for controlling the first supply means and the second supply means according to the measurements achieved by the first, second and/or third measuring means.

The controlling unit may thus implement a monitoring rule in such a manner that the temperatures and pressures in the decarbonatation and clinkering sections be regulated around setpoint values.

According to another feature, the enclosure comprises an outer metallic envelope, and an inner envelope achieved by stacking at least:a first coating in a thermally insulating material mounted on the outer metallic envelope; anda second coating in a refractory material mounted on the first coating.

The first coating protects the outer metallic envelope from thermal dilation. The second coating protects the first coating from abrasion.

The combined presence of a first coating in a thermally insulating material and a second coating in a refractory material allows protecting the outer metallic envelope of the enclosure from weakening which could normally be caused if the latter reached the temperature of the raw mix, of which the temperature gradually increases as the raw mix flows into the enclosure.

The invention also relates to an installation for manufacturing a clinker comprising:a kiln such as exhibited here-before; anda cooler, preferably a reciprocating grate cooler, arranged to cool the clinker extracted by the first extraction means.

The cooler allows to perfectly master the cooling of the clinker and no longer undergoes it. Thus, a cement achieved from a clinker manufactured by such an installation exhibits mastered setting up time and demand for water.

The invention finally relates to a method for manufacturing a clinker comprising the following steps:providing a kiln according to the invention;supplying a first gas exhibiting a temperature ranging between 950° C. and 1250° C. in the decarbonatation section; andsupplying a second oxidizing gas exhibiting a temperature ranging between 1250° C. and 1450° C. in the clinkering section.

DETAILED DESCRIPTION

The enclosure4comprises an outer metallic envelope6, and an inner envelope8achieved by stacking:of a coating10in a thermally insulating material mounted on the outer envelope6; andof a coating12in a refractory material mounted on the coating10.

The coating10in a thermally insulating material is characterized by a thermal conductivity at 1000° C. ranging between 0.05 and 0.4 W/m·K, a density ranging between 50 and 500 kg/m3, and a compression resistance ranging between 0.1 and 0.5 MPa.

The coating12in a refractory material is characterized by a thermal conductivity at 1000° C. ranging between 0.2 and 2.5 W/m·K, a density ranging between 1000 and 3000 kg/m3, and a compression resistance ranging between 20 and 120 MPa. For example, the refractory material may of silicon carbide.

The enclosure4comprises from top to bottom a feeder section14, a decarbonatation section16, a clinkering section18, and a collection section20.

The feeder14and collection20sections extend substantially vertically. The decarbonatation16and clinkering18sections are slanted with respect to the vertical.

The lower16aand upper16bsurfaces of the decarbonatation section16form an angle α in the range of 40° with respect to the vertical. Likewise, the lower and upper surfaces of the clinkering section form an angle α′ in the range of 40° with respect to the vertical.

The lower surfaces16aand18aof the decarbonatation16and clinkering sections form an angle ranging between 80° and 140°.

The decarbonatation16and clinkering18sections are arranged in such a manner that:the lower edge of the lower surface16aof the decarbonatation section16extends substantially vertically in line with the lower edge of the upper surface16bof this decarbonatation section16, andthe lower edge of the lower surface18aof the clinkering section18extends substantially vertically in line with the lower edge of the upper surface18bof this clinkering section18.

The position of the upper surface18bof the clinkering section is adjustable with respect to the lower surface18athereof. This adjusting, may be carried out for example by means of jacks19which displace all or part of the upper surface18bwith respect to the lower surface18a, which remains stationary.

The kiln2comprises a lock30for introducing pellets of raw mix in the feeder section14. In the example, the lock30is rotatable. The lock30is permeable in such a manner as to limit the ambient air output liable to penetrate into the enclosure4.

The kiln2comprises means32(represented onFIG. 5) for generating a first gas exhibiting a temperature ranging between 950° C. and 1250° C. The first gas may be an oxidizing or reducing gas.

A first reducing gas would not be detrimental in as far as this first gas ascends from the decarbonatation section16in the direction of the feeder section14located directly above without crossing the clinkering section18located directly below. The means32for generating the first gas are described below.

The kiln2comprises means for supplying the first gas in the decarbonatation section. These means for supplying the first gas comprise four furnace flues34(represented onFIG. 4) each opening at the downstream end of a duct24of the decarbonatation section16.

The kiln2comprises means36(represented onFIG. 5) for generating a second gas exhibiting a temperature ranging between 1250° C. and 1450° C. This second gas is oxidizing such as to prevent the formation of reducing zones in the clinkering section18and then prevent the formation of the C12A7phase detrimental during the clinkering. The means36for generating the second gas are described below.

The kiln2comprises means for supplying the second gas in the clinkering section18. These supply means comprise four furnace flues38each opening at the downstream end of a duct28of the clinkering section18.

The kiln2comprises means for suctioning the first and second gases from the feeder section. These suction means comprise a furnace flue40opening into the feeder section and a suction ventilator41(represented onFIG. 5).

The kiln2comprises extraction means arranged for extracting the clinker contained in the collection section. The extraction means are here achieved in the form of a drawer extractor42.

The drawer extractor42comprises an upper stationary part42aand a lower moveable part42bdelimiting a connecting section. This section is provided with an inlet mouth44connected to the collection section20and an outlet mouth46connected to a cooler48(represented onFIG. 5). The inlet44and outlet46mouths are shifted vertically and horizontally.

The upper stationary part42aof the drawer extractor42is equipped with an ambient air supply pipe50and means for regulating the output of ambient air. These regulating means are here achieved in the form of a valve52.

The lower moveable part42bis displaceable in a determined direction54alternatively between an advanced position and a receded position, to allow the flow of the clinker contained in the collection section20.

The drawer extractor42comprises means for displacing and guiding the moveable part42brelatively to the stationary part42a. The displacement means comprise for example a pneumatic jack56.

The guiding means comprise wheels58fixed under the moveable part42band meshed in rails60.

The clinker extraction output may be modulated by playing on the frequency and the travel of the moveable part. An increase in the frequency increases the extraction output. A decrease in the frequency decreases the extraction output. An elongation of the travel increases the extraction output. A shortening of the travel reduces the extraction output.

Finally the kiln2comprises:temperature sensors of the first and second gases supplied (not represented);sensors for measuring the pressure of the first and second gas supplied (not represented);sensors for measuring the temperature of the raw mix inside the decarbonatation16and clinkering18sections (not represented), such as pyrometers; anda controlling unit (not represented) arranged for controlling the means32and36for generating first gases and second gases according to the measurements achieved by the measuring sensors.

An method of operating the kiln2is now described.

Pellets of raw mix containing calcium, aluminum, silica, iron, sulfur, preferably in combined mineral form such as oxides, hydroxides, carbonates, chlorides or sulfates, are poured into the feeder section14by means of the lock30. The pellets of raw mix flow by gravity into the enclosure4.

As the pellets of raw mix flow into the feeder section14, the first and second gases ascend into the enclosure4as a result of the suction ventilator41, and take the pellets of raw mix to a temperature of the order of 600° C. The pellets of raw mix are dried, pre-heated, and undergo certain chemical transformations, such as the dehydroxylation of the bauxite.

The length and cross-section of the feeder section14are sized in order to ensure a minimum residence time of the pellets of raw mix in the feeder section14. In fact, it is necessary that these chemical transformations be not too rapid in order to prevent the alteration of the pellets of raw mix.

The pellets of raw mix then flow in the decarbonatation section16. The lower slanted surface16aallows the formation, at its downstream end, of a ramp from which the first and second gases ascend. The pellets of raw mix are taken to a temperature ranging between 850° C. and 950° C., and are decarbonated.

The length and cross-section of the decarbonatation section16are sized in such a manner that the residence time of the pellets of raw mix in the decarbonatation section16is equal to a determined time.

The pellets of raw mix hence flow in the clinkering section18. The lower slanted surface18aallows, at the downstream end thereof, the formation of a ramp from which only the second gas ascends. The pellets of raw mix are taken to a temperature ranging between 1280° C. and 1450° C., and are clinkered.

The length and cross-section of the clinkering section are sized in such a manner that the residence time of the pellets of raw mix in the clinkering section18is equal to a determined time.

Finally, the clinkered pellets of raw mix are collected in the collection section20.

The drawer extractor42extracts, at a determined output, the clinker pellets from the collection section20as a result of the alternative displacement of the moveable part42arelatively to the stationary part42b, and supplies these clinker pellets in the cooler48connected to the outlet mouth46of the drawer extractor42.

An installation62equipped with the kiln and its operating method are now described with reference toFIG. 5.

Initially, the raw mix is crushed, homogenized and pelletized, for example by a roller press64.

A handling device, for example a bucket elevator66, collects the pellets of raw mix and feeds the lock30of the kiln2.

The kiln2hence chemically transforms the pellets of raw mix into clinker pellets (such as described here-before). The drawer extractor42supplies the clinker pellets inside the cooler48.

The cooler48is here a reciprocating grate cooler, rather than a rotary cooler or a balloon cooler. The cooler48comprises a ventilator battery68blowing air into a chamber70through which the clinker is conveyed.

The cooled clinker is gathered downstream of the cooler48by a conveyor72, for example a chain conveyor, suitable for transporting the clinker at a temperature in the range of 150° C. to 250° C. The conveyor72transports the clinker to a silo74, where the latter is stored with a view to be crushed.

The air blown by the ventilators68, after having been heated in the contact of the clinker, is extracted from the chamber70by a sheath76opening at an upstream end of the cooler48and by a sheath78opening at a downstream end of the cooler48.

The hottest air, extracted by the sheath76, is lead inside a mixing pot79of which the function will become apparent afterwards. The sheath76is equipped with a valve77.

The least hot air, extracted by the sheath78, is lead to sheaths80and82. The sheath80feeds a system for drying the raw mix prior to crushing (not represented) as a result of a suction ventilator81.

The sheath82joins the furnace flue40to feed a sheath84. The air lead by the sheath82increases the temperature of the first and second gas lead by the furnace flue40above the dew point. The sheath82is equipped with a valve83.

The sheath84leads the first and second gases and the hot air coming from the cooler towards a filter86, for example a bag filter. The filter86dedusts and releases the first and second gas and the hot air from the cooler into the atmosphere through a chimney88, as a result of a suction ventilator41.

The sheath84is connected to a sheath90for supplying fresh air. This sheath90is equipped with a valve92liable to be open when the temperature upon suction of the filter86exceeds a maximum value specified by the provider.

The means32for generating the first gas are now described. The generation means32comprise a generator94of a gas at very high temperature and the mixing pot79. The generator94comprises a furnace96, a ventilator98, and a combustible source100. The generator94is for example a pulverized coal generator. The gas at very high temperature produced by the generator94is supplied to the pot by a furnace flue102. The furnace flue102is equipped with a valve104.

The pot79forms the first gas by mixing the hot air coming from the cooler supplied by the sheath79and the hot gas supplied by the furnace flue102. The pot79is connected to the decarbonatation section16by the furnace flues34.

The pot79is equipped with burners106, for example gas burners. The burners106allow ensuring assistance during startup phases, and regulating the temperature of the first gas formed in the pot79.

The generation means36of the second gas are now described. The generation means36comprise a furnace108, such as a burner, a ventilator110, and a combustible source112, such as natural gas, configured for generating the second oxidizing gas.

The circulation of the cooling air and the first and second gases in the installation62is ensured by the suction ventilator41disposed downstream of the filter86and by the suction ventilator81.

Particularly, the ventilator41generates a pressure gradient inside the enclosure4, in such a manner that the highest pressure point of the enclosure4is the collection section20, substantially at atmospheric pressure, and the least high pressure point of the enclosure4is the feeder section14. Thus, the first and second gases ascend in the enclosure4in counter current of the pellets of raw mix, and then are suctioned by the furnace flue40.

The ventilator41and81are sized in such a manner as to overcome the head losses resulting from the presence of the pellets of raw mix in the enclosure4, of the presence of the filter86, of the presence of the furnace flues34,40and102, the sheaths76,78,80,82,84, and90, of the presence of the pot79and of the presence of the valves77,83and104. In proportion to their closing degree, these valves77,83and104cause a more or less important head loss. Thus, the valves77,83, and104allow equilibrating the head losses in the installation.

FIG. 6represents a second vertical-shaft kiln200, which constitutes an alternative embodiment of the kiln2and in which the same elements are designated by the same references as onFIG. 1. The kiln200comprises an additional collection section202disposed between the decarbonatation section16and the clinkering section. This additional collection section extends substantially vertically.

The kiln200comprises extraction means arranged to extract the raw mix contained in the collection section16and supply it in the clinkering duct18. These extraction means are suited for modulating the extraction output of the raw mix.

The extraction means are achieved in the form of a drawer extractor204identical to the drawer extractor42, except that the stationary part does not have the ambient air supply pipe50and the valve52.

The kiln200finally comprises suction means arranged between the decarbonatation section16and the clinkering section18to suction all or part of the second gas from the clinkering section18. These suction means comprise a furnace flue206.

FIG. 7represents a third vertical-shaft kiln300, which constitutes an alternative embodiment of the kiln2ofFIG. 1and in which the same elements are designated by the same references as onFIG. 1. This kiln300is distinguished from the kiln2, in that the two respectively the decarbonatation316and clinkering318sections are slanted in the same direction. The lower surfaces316aand318ahave the same inclination, shifted with respect to each other, and a downward setback319is provided between the lower end of the lower surface316aof the decarbonatation section and the upper end of the lower surface318aof the clinkering section. The upper surface318bis moveable with respect to the lower surface318a.

FIG. 8represents a fourth kiln400, which constitutes an alternative embodiment of the kiln200ofFIG. 6, and in which the same elements are designated by the same references as onFIG. 6.

The kiln400comprises a connecting section402connecting the drawer extractor204to the clinkering section18.

The device for adjusting the position of the lower and upper surfaces18aand18bof the clinkering section18by jacks is replaced with the acceptance of a variation in height of the layer in the clinkering section. The variation of the head loss of the gas crossing this layer, resulting from the variation in height of the layer, is compensated by the displacement of a valve404equipping the connecting section402. The valve404is controlled by a jack406.

As it is known per se, the invention is not limited to the sole embodiments of the kiln described above by way of examples, but on the contrary encompasses all the alternative embodiments.

The lock30may be replaced by a valve lock.

The outer metallic envelope6may be replaced by an outer reinforced concrete envelope.

The drawer extractor42may be replaced by a helmet-type extractor.

The jack56may be replaced by a hydraulic jack or a connecting rod mechanism associated with a motor.

The roller press64may be replaced by a disk pelletizer.

The bucket elevator66may be replaced by a conveyor belt, a chain conveyor, or a vibrating conveyor.

The conveyor72may be replaced by an apron conveyor, or any other type of conveyor allowing to ensure the transport of a clinker at a temperature in the range of 150° C. to 250° C.

The silo74may be replaced by a storage warehouse.

The first and second gas and the cooling air from the filter86may be used in a cogeneration system rather than be released into the atmosphere by the chimney88.

The filter86may be replaced by an electrostatic filter.

The generator94may be replaced by an oil coke generator, or by any other solid or liquid combustible having a low cost and allowing to generate the first gas, a raw coal stoker, a coal pyrolyser, biomass pyrolyser, waste pyrolyser or similar.

The burners106may be fuel oil burners.

The generation means36may comprise a gas burner other than a natural gas one, with fuel oil, gas oil or a pulverized coal, or a petroleum coke generator, or any other solid or liquid combustible having a low cost and allowing to generate the second gas.