WO2001072656A1 - Procede pour augmenter la production de clinker dans une cimenterie existante et pour produire de la vapeur - Google Patents

Procede pour augmenter la production de clinker dans une cimenterie existante et pour produire de la vapeur Download PDF

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Publication number
WO2001072656A1
WO2001072656A1 PCT/IB2001/000466 IB0100466W WO0172656A1 WO 2001072656 A1 WO2001072656 A1 WO 2001072656A1 IB 0100466 W IB0100466 W IB 0100466W WO 0172656 A1 WO0172656 A1 WO 0172656A1
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WO
WIPO (PCT)
Prior art keywords
clinker
air
preheater
kiln
steam
Prior art date
Application number
PCT/IB2001/000466
Other languages
English (en)
Inventor
Vassilios Burdis
Enrico Malfa
Reinhard Schurian
Srivats Srinivasachar
Frank Steege
Majed Toqan
Original Assignee
Alstom (Switzerland) Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Alstom (Switzerland) Ltd filed Critical Alstom (Switzerland) Ltd
Priority to AU39495/01A priority Critical patent/AU3949501A/en
Publication of WO2001072656A1 publication Critical patent/WO2001072656A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
    • C04B7/47—Cooling ; Waste heat management
    • C04B7/475—Cooling ; Waste heat management using the waste heat, e.g. of the cooled clinker, in an other way than by simple heat exchange in the cement production line, e.g. for generating steam
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
    • Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods

Definitions

  • the invention relates to a method of increasing the clinker output of an existing cement plant and of producing steam, said method comprising the steps of preheating a raw meal in a preheater, said preheater being a multistage suspension type preheater including a plurality of serially connected cyclone type gas solids separators, burning the preheated raw meal in a rotary kiln to form clinker, and then cooling the clinker in a clinker cooler.
  • the cement raw meal is introduced at an inlet at the top of the preheater, passing through the preheater in counter-current with the exhaust gases from the kiln.
  • the exhaust gases are drawn up through the preheater and discharged by means of an exhaust gas fan.
  • the raw meal is conveyed from the preheater to the rotary kiln where, by means of heat from a burner, the raw meal is burnt into clinker.
  • the clinker drops into the cooler where it is cooled using air. It is known in cement technology that many materials for cement clinker manufacture contain secondary constituents such as alkali compounds, chlorine, sulfur, heavy metals, etc.
  • a method of preparing cement clinker from carboniferous shale is described in US 4, 256, 502.
  • the increase of the clinker output is done via a second tower by injecting shale into that second tower; the kiln gas is treated within this second tower, which in normal operation is to be considered as a 100% bypass. If this known plant is run with tower 13 alone then there is no kiln gas treatment. The gas is added to the cooling air prior to calciner 18. And there is no increase in clinker output, as limestone is introduced (which moreover has to be calcined after preheating).
  • the object of the invention is to increase the clinker output of an existing cement plant by utilizing major parts of the plant unchanged and to produce steam of high parameters with gaseous media of the cement plant in considerably reducing the above described disadvantages.
  • the raw meal fed to the preheater is calcined raw meal, consisting essentially of lime and combustion residues like ash, carbon and desulfurization residues.
  • the advantages of the invention are to be seen in that, inter alia, in avoiding calcination of the material fed to the preheater, a considerably reduction of the specific kiln heat consumption is performed. In fact if the raw meal is introduced in calcined form, a considerable increase in clinker production is performed while burning the same amount of the fuel in the kiln. Moreover, on the contrary to prior art arrangement of cement plants in which the hot clinker cooler air is one of the main sources of losses, in the proposed new arrangement it is possible to use the hot air of the clinker cooler to a maximum extend.
  • the use of hot cooler air for preheating the precalcined material as well as the use of the kiln gases for steam production means another reduction of the specific kiln heat consumption.
  • this air is free from SO 2 thus avoiding or at least significantly reducing the risk of blockages in the preheating zone, as the sulphurous material is introduced directly at the kiln inlet at a temperature greater than 800 C.
  • the new method allows to significantly reduce the flue gas generated per kg of produced clinker and therefore the specific energy losses associated with the kiln flue gases are less.
  • the method is particularly interesting when the cement plant and the power plant producing the calcined raw mix are located on the same site.
  • the use of the combustion products like ash and carbon of the power process in the cement process avoids disposal of solids from the power plant.
  • the kiln exhaust gases are quenched to a temperature of about 800-900°C prior to their heat exchange in the water/steam cycle. This measure avoids the building up of sticky material forwarded to the downstream boiler.
  • the NO x component of the gases shall be further reduced.
  • Part of the process air from the clinker cooler can be directed, after de-dusting, to a steam producing heat exchanger, which preferably is a heat recovery boiler.
  • the temperature of this process air can be increased using a supplementary firing system to produce steam of high parameters in the heat recovery boiler. This increases the output of the power plant.
  • the produced steam can also be used in other processes than power production.
  • the supplementary firing allows adjusting the steam parameters as required by the end user.
  • the existing equipment necessary for performing the cement production consists mainly of a raw mix preheater 50, a rotary kiln 16 and a clinker cooler 20.
  • the preheater 50 is a vertically arranged multistage suspension type preheater including a plurality of serially connected cyclone type gas/solids separators 51- 54.
  • the cyclones each have an inlet “a” for gaseous medium and entrained cement raw mix, an outlet “b” for separated gaseous medium and an outlet “c” for separated solids.
  • the preheater is equipped with an inlet 17 for cement raw mix. This inlet 17 is arranged in the conduit connecting the inlet "a” for gaseous medium and entrained cement raw meal of the uppermost cyclone 51 to the outlet "b" for separated gaseous medium of the adjacent cyclone 52.
  • Solids being separated in cyclone 51 flow down into a conduit connecting the air outlet of cyclone 53 to the inlet of the adjacent lower cyclone 52.
  • this conduit the solids are entrained and conveyed to cyclone 52, where they are separated.
  • solids are moving down to the next lower cyclones 53 and 54.
  • the raw mix is heated up by the gaseous medium supplied to the preheater tower. This air flows through the preheater in countercurrent relation to the flow of the raw mix, i.e. from cyclone 54 to cyclone 53, to cyclone 52 and finally to cyclone 51.
  • Spent preheating gaseous medium leaves the uppermost cyclone 51 via outlet "b" to a known dedusting system.
  • the preheated raw mix is supplied to the kiln 16 via a line 57.
  • This kiln has a feed end 44 and a discharge end 45 with a combustion zone near the discharge end.
  • the preheated and precalcined raw mix is burned into cement clinker.
  • a certain amount of fuel, i.e. coal is injected at the discharge end 45 via a burner together with primary air.
  • ambient air is introduced in the system by fans 22 to the clinker cooler and heated therein by cooling down the cement clinker.
  • the heated air exits the clinker cooler in a first stream and is supplied to the kiln 16 as kiln combustion (secondary) air.
  • the cement clinker is then forwarded from the discharge end 45 of the kiln into the cement cooler 20, which might be a moving grate.
  • the cooled clinker is finally supplied via line 21 to a cement grinder, which is not shown.
  • the gaseous medium used for preheating the raw mix is the kiln gas exhausting the feed end 44 of the kiln.
  • the gaseous medium used for preheating the raw mix is the kiln gas exhausting the feed end 44 of the kiln.
  • this is done by feeding calcined raw meal, consisting essentially of lime and combustion residues like ash, carbon and desulfurization residues, via inlet 17 into the preheater 50.
  • a second feature is to direct process air from the clinker cooler 20 in countercurrent flow to the direction of flow of the calcined raw meal.
  • air preheated in the clinker cooler is supplied to the preheater tower via tertiary air line 26 and via riser duct 56.
  • the clinker cooler 20 Due to the increased amount of produced clinker, it is understood that the clinker cooler 20 has to be replaced by a larger apparatus in order to perform its function.
  • the kiln exhaust gases are 100% vented and used for steam production in a boiler 60. Via a duct 46 they are fed into a quenching device 61 to cool them down to a temperature of about 800-900°C.
  • the kiln exhaust gases can be quenched either with air via line 62, either with water via line 75, or with solids like limestone via line 63 or like calcined raw meal via line 64.
  • This calcined raw meal may be withdrawn either from the feed line 17 of the preheater 50 or from the solids duct "c" of a cyclone of the preheater having the appropriate temperature for cooling down the kiln gas. It contributes to the desulfurization of the kiln gases.
  • the use of this fine ground material enhances the condensation of alkalis, chlorides, sulfates and heavy metals. The same advantages are obtained if limestone is injected. This limestone is a good heat sink as it is calcined to lime.
  • Using water for quenching allows evaporating wastewater from any part of the cement and/or power plant.
  • Using air is the most cost-effective solution, as air is sucked in the system due to its pressure level.
  • the kiln exhaust gases are then forwarded to a dust separator 65, which in the present example is a cyclone. After dedusting, the gases are fed to a boiler 60 and are used for steam generating. The steam produced in the boiler may be used in the water/steam cycle of the power plant. As the kiln gases have high temperature, high steam parameters can be obtained.
  • the new way of preheating precalcined raw mix and treating the exhaust gases it is possible to suppress the alkali and chloride circulation and the other volatile matters in the cement clinker combustion device, as well as to reduce their concentrations in the cement clinker.
  • These components are contained in the now bypassed kiln gases and thus are not internally recirculated. This will improve substantially the kiln operation, i.e. no ring formation.
  • the kiln exhaust gases might be treated in view of NO x and SO x reduction based on the local environmental requirements.
  • the kiln exhaust gases are fed by a fan 66 to a circulating fluidized bed boiler 1 of a power plant, in which boiler the NO x component of the gases is reduced.
  • a DeSox-system might be required before feeding the kiln gases to the circulating fluidized bed boiler.
  • This DeSox-system can be arranged either in the high temperature region (above 700°C) or at the low temperature end downstream the boiler 60. It is understood that depending on the heat content of the gases, they may be used for preheating the circulating fluidized bed boiler combustion air prior to their introduction in this boiler.
  • the remaining air of the clinker cooler 20 is not discharged - like in prior art plants - but is now used for steam production. Via line 67 it is forwarded to a de-duster 68, which in this example is a cyclone. After having been dedusted, the air is forwarded with a fan 69 to a steam producing heat exchanger 70.
  • This heat exchanger is preferably a heat recovery boiler with supplementary firing.
  • a hydrocarbon, i.e. coal is fed to the boiler via supply line 71 and is burned with a part of the process air withdrawn from the main air flow and forwarded by a fan 72 via a line 73 as combustion air.
  • the steam produced in the boiler may be forwarded in the water/steam cycle of the power plant; i.e. it can be fed into a common header. This steam insertion optimizes the efficiency of the total plant.
  • the flue gases from the heat recovery boiler are discharged via a line 74 to the stack of the power plant.
  • the solids separated in the cyclones 65 and 68 might be added to the cement clinker in line 21.
  • the drawing illustrates in its upper part in a simplified block diagram the clinker making process and shows how the calcined raw meal, consisting essentially of lime and combustion residues like ash, carbon and desulfurization residues, is produced in the combustor of a power plant.
  • a fan 27 sucks the major portion of ambient air in the system. This air is preheated in an air preheater 28. Via line 30 the air is fed to the combustor 1 , in which it penetrates via a fluidizing air supply 5 and a secondary or overbed air supply 4.
  • the gas/air mixture can be introduced into the combustor on different levels.
  • the reactor in which the reactor is an upright circulating fluidized-bed steam generator with a flow stream from bottom to top, the fluidizing air is introduced at the bottom through an air distributor.
  • the secondary air is fed through one or more elevations of ports in the lower combustor.
  • the reactor is provided with four other inlets.
  • One carbonaceous residue supplies line 6, one inlet 2 for the coal and two inlets 3 and 3a for the raw cement mix.
  • Coal is introduced mechanically or pneumatically to the lower portion of the reactor via supply 2.
  • This coal can be either crushed or pulverized. Like the air, coal may be injected on different levels of the reactor. If the coal is in form of crushed material with a size of approximately 6 mm, it can be fed by gravity.
  • Combustion takes place throughout the combustor, which is filled by bed material. Flue gas and entrained solids leave the combustor and enter one or more cyclones 8, where the solids are separated.
  • These separated gases are further treated before disposal. They are first cooled down in a gas cooler 33, thereby heating up water in an economizer 34 integrated in the water/steam cycle of a steam turbine island 42.
  • the gases in line 32 are cooled at a fast rate, i.e. greater than 30 K/sec. Downstream the gases are further cooled in the air preheater 28. The gas is supposed to leave this gas cooler 28 with a temperature of about 100-150°C. Downstream the gas cooler a solids filter 37 is provided in the line 38 to remove from the gas all the remaining solids.
  • This filter 37 could be a fabric filter or an electrostatic precipitator.
  • a fan 40 is installed in the gas line exiting the filter, preferably on the clean side of the filter 37. Its purpose is to control the pressure in the system close to atmospheric conditions.
  • the cleaned gas leaves the system via the stack 41.
  • the solids separated in the filter 37 are fed via line 39 to an appropriate location in the cement system.
  • the solids separated in the cyclone 8 are recycled to the combustor via line 6.
  • the major portion is directly returned to the fluidizing bed via line 7.
  • Some solid is diverted via line 10 to an external fluidized-bed heat exchanger 9 and then added to the portion in line 7.
  • the bed temperature in the combustor 1 is essentially uniform and is maintained at an optimum level for sulfur capture and combustion efficiency by heat absorption in the walls of the combustor.
  • the heat exchange is supposed to occur in an evaporator 35.
  • Superheating of the steam and - for large steam turbine units with a reheat cycle - reheating is performed preferably by further heat removal from the hot solids absorption in the fluidized-bed heat exchanger 9 and/or in the gas-cooler 33.
  • This heat exchanger 9 is containing immersed tube bundles.
  • the flow rate of the solids through apparatus 9 via line 10 can be used to control the steam temperature.
  • the produced superheated steam is fed to the turbine island 42 comprising at least one steam turbine driving a generator producing electrical power. Additional steam is produced for the turbine in the clinker cooler 20 from cooling the hot clinker discharged from the kiln 16 via line 19.
  • the CFB is now used for a coproduction of steam and calcined raw mix for the cement production, in which coproduction the ashes of the power production are used to replace part of the cement raw mix in the cement production.
  • coal ashes are similar in composition to calcined clays.
  • all of the coal residues are converted into cement; the sulfur is absorbed by clinker component CaO.
  • two inlets 3 and 3a for the raw cement mix are provided in the reactor 1.
  • a part of limestone is fed into the reactor in pulverized form; typically 90% of the limestone particles are smaller than 90 microns, the size being appropriate for the cement clinkering process.
  • Via line 3a the remaining part of crushed limestone is introduced to form bed and circulating material.
  • limestone CaCO 3 is calcined into CaO.
  • CaO combines with SO 2 released from coal combustion and oxygen to form gypsum CaSO 4 .
  • SO 2 can be disposed by standard wet or dry scrubbing methods using limestone.
  • Draining off solids controls solids inventory in the combustor.
  • the hot solids drained of the fluidizing bed via line 11 are cooled down through an ash cooler 43. They are introduced in a grinder 12 in which they are ground to an extent that 90% are below 90 ⁇ m. They are mixed with additives introduced in the grinder by a line 14 and with some of the cement raw mix (not shown). These corrective additives are used, if any essential chemical compound needed in the mixture of coal ash and limestone like iron oxide or silica content are not present in the required amount.
  • the ground material is supplied to a blender 13, in which is added the lime CaO via a supply 15.
  • This amount of lime is constituted by the solids separated in the filter 37 and is fed via line 39.
  • the cyclone 8 is designed to separate the predominant char and crushed cement material from the remaining components. Since the mean size of the ash and the lime is typically smaller than 50 ⁇ m it will escape the cyclone, while the char and the crushed lime/limestone, which is far greater in size will be retained in the cyclone. Thus the fly ash escaping the cyclone consists predominantly of lime and is forwarded with the flue gas in line 32.
  • the calcined raw mix of the correct size and composition for cement clinker making is then forwarded to the cement plant.
  • the clinker output is supposed to be at 37.5 kg/sec. To produce this amount, 87 kg/sec of ambient air is sucked by fan 22 into the clinker cooler 20 and cools the clinker down to around 70°C. Exhaust air in the amount of 34.5 kg/sec leaves the cooler at around 750°C and is fed to the preheater 50. Another part of the air leaving the cooler in the amount of 14.5 kg/sec is fed to the kiln as combustion air and as transportation and primary air for the coal, which is in the amount of 1.8 kg/sec.
  • the remaining air leaving the cooler in the amount of 38 kg/sec at 300°C is bypassing the kiln via line 67 and is forwarded to the boiler 60, where it is heated up by the supplementary firing to 850°C and produces steam of the required parameters which are preferably the live steam parameters
  • the gas amount out of the kiln is about 21.3 kg/sec at 1050°C.
  • this gas with a temperature of about 200°C may be used to preheat the combustion air of the CFB and is then forwarded into the CFB.
  • Raw mix of the correct size and composition and precalcined at 90% in the amount of 40.5 kg/sec is introduced into the preheater 50 at ambient temperature. It is heated up by the cooler air to around 720°C. After heat exchange in the tower, this air with a temperature of about 280°C may be used to dry the ready raw mix in a milling process, if any. Thereafter it is dedusted and discharged at a temperature of about 100°C.
  • the precalcined raw material produced in the power plant contains some carbon coming from the fly ash.
  • This carbon is separated in the filter 37 with the lime and is added to the bottom ash of the combustor in the blender 13. In this case either the coal amount to the kiln has to be reduced appropriately or the amount of air through the kiln has to be augmented to burn the supplemental carbon.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé pour augmenter la production de clinker dans une cimenterie existante et pour produire de la vapeur. Ce procédé consiste à préchauffer de la farine crue dans un préchauffeur (50), puis à la calciner dans un four rotatif (16) pour former le clinker, ce dernier étant ensuite refroidi dans un refroidisseur à clinker (20). La farine crue calcinée, constituée principalement de chaux et de résidus de combustion tels que de la cendre, du charbon et des résidus de désulfuration, est acheminée au préchauffeur (50). De l'air de processus provenant du refroidisseur de clinker (20) est acheminé au préchauffeur (50) dans une direction opposée au sens d'écoulement de la farine crue calcinée. Cette farine crue calcinée préchauffée est acheminée au four rotatif (16). Les gaz de combustion du four sont dérivés à 100 % et utilisés pour produire de la vapeur dans une chaudière (60). Les gaz de combustion du four sont refroidis brusquement à une température de l'ordre 800-900 °C avant de subir un échange de chaleur dans le cycle eau/vapeur.
PCT/IB2001/000466 2000-03-27 2001-03-09 Procede pour augmenter la production de clinker dans une cimenterie existante et pour produire de la vapeur WO2001072656A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU39495/01A AU3949501A (en) 2000-03-27 2001-03-09 Method of increasing the clinker output of an existing cement plant and of producing steam

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP00105998.9 2000-03-27
EP00105998 2000-03-27

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WO2001072656A1 true WO2001072656A1 (fr) 2001-10-04

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Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006081827A1 (fr) * 2005-02-06 2006-08-10 Khaled Osman Zaki Systeme ameliore de derivation de gaz pour four a ciment
WO2008151877A1 (fr) * 2007-06-12 2008-12-18 Flsmidth A/S Procédé et installation pour la production simultanée d'électricité et de clinker de ciment
CN102519268A (zh) * 2011-12-29 2012-06-27 阿克苏天山多浪水泥有限责任公司 水泥窑旁路放风发电锅炉含碱烟气引入工艺及其装置
CN102777895A (zh) * 2012-07-24 2012-11-14 武汉和信益科技有限公司 半塔式中温分离生物质循环流化床锅炉
CN104973811A (zh) * 2014-04-09 2015-10-14 河南工业大学 一种利用外排空气冷却基建水泥的装置
WO2021069386A1 (fr) * 2019-10-10 2021-04-15 Thyssenkrupp Industrial Solutions Ag Séparation d'eau à partir des gaz de fumée issus d'installation de cuisson de clinker
WO2022074552A1 (fr) * 2020-10-05 2022-04-14 Flsmidth A/S Procédé et système de manipulation de gaz de dérivation dans un circuit de four à ciment

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4256502A (en) * 1978-06-12 1981-03-17 Lafarge Conseils Et Etudes Method of preparing cement clinker from carboniferous shale
EP0847966A1 (fr) * 1995-08-14 1998-06-17 Bureau of Administrative Service, The Chinese Academy of Sciences Procede pour produire de la chaleur et des clinkers dans une chaudiere unique, produits obtenus, equipement utilise et applications
CH689830A5 (de) * 1998-09-02 1999-12-15 Zappa Luzius Integriertes Verfahren der simultanen Erzeugung von Zement-Klinker und Elektrizitaet.
DE19835734A1 (de) * 1998-08-07 2000-02-17 E Ulrich Mathieu Verfahren zur thermischen Behandlung von festen Stoffen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4256502A (en) * 1978-06-12 1981-03-17 Lafarge Conseils Et Etudes Method of preparing cement clinker from carboniferous shale
EP0847966A1 (fr) * 1995-08-14 1998-06-17 Bureau of Administrative Service, The Chinese Academy of Sciences Procede pour produire de la chaleur et des clinkers dans une chaudiere unique, produits obtenus, equipement utilise et applications
DE19835734A1 (de) * 1998-08-07 2000-02-17 E Ulrich Mathieu Verfahren zur thermischen Behandlung von festen Stoffen
CH689830A5 (de) * 1998-09-02 1999-12-15 Zappa Luzius Integriertes Verfahren der simultanen Erzeugung von Zement-Klinker und Elektrizitaet.

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006081827A1 (fr) * 2005-02-06 2006-08-10 Khaled Osman Zaki Systeme ameliore de derivation de gaz pour four a ciment
WO2008151877A1 (fr) * 2007-06-12 2008-12-18 Flsmidth A/S Procédé et installation pour la production simultanée d'électricité et de clinker de ciment
CN101765752A (zh) * 2007-06-12 2010-06-30 Fl史密斯公司 用于同时产生电和水泥熟料的方法和设备
CN101765752B (zh) * 2007-06-12 2012-12-05 Fl史密斯公司 用于同时产生电和水泥熟料的方法和设备
CN102519268A (zh) * 2011-12-29 2012-06-27 阿克苏天山多浪水泥有限责任公司 水泥窑旁路放风发电锅炉含碱烟气引入工艺及其装置
CN102777895A (zh) * 2012-07-24 2012-11-14 武汉和信益科技有限公司 半塔式中温分离生物质循环流化床锅炉
CN102777895B (zh) * 2012-07-24 2015-03-04 武汉和信益科技有限公司 半塔式中温分离生物质循环流化床锅炉
CN104973811A (zh) * 2014-04-09 2015-10-14 河南工业大学 一种利用外排空气冷却基建水泥的装置
WO2021069386A1 (fr) * 2019-10-10 2021-04-15 Thyssenkrupp Industrial Solutions Ag Séparation d'eau à partir des gaz de fumée issus d'installation de cuisson de clinker
WO2022074552A1 (fr) * 2020-10-05 2022-04-14 Flsmidth A/S Procédé et système de manipulation de gaz de dérivation dans un circuit de four à ciment

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