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WO2010060855A1 - Procédé et installation de fabrication de ciment - Google Patents

Procédé et installation de fabrication de ciment Download PDF

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Publication number
WO2010060855A1
WO2010060855A1 PCT/EP2009/065485 EP2009065485W WO2010060855A1 WO 2010060855 A1 WO2010060855 A1 WO 2010060855A1 EP 2009065485 W EP2009065485 W EP 2009065485W WO 2010060855 A1 WO2010060855 A1 WO 2010060855A1
Authority
WO
WIPO (PCT)
Prior art keywords
mineral mixture
latent hydraulic
hydraulic mineral
clinker
plant
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/EP2009/065485
Other languages
German (de)
English (en)
Inventor
Sebastian Frie
Wilfried Kreft
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Polysius AG
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 Polysius AG filed Critical Polysius AG
Publication of WO2010060855A1 publication Critical patent/WO2010060855A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • F27B7/20—Details, accessories or equipment specially adapted for rotary-drum furnaces
    • F27B7/2016—Arrangements of preheating devices for the charge
    • F27B7/2041—Arrangements of preheating devices for the charge consisting of at least two strings of cyclones with two different admissions of raw material
    • 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
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • C04B7/367—Avoiding or minimising carbon dioxide emissions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B15/00—Fluidised-bed furnaces; Other furnaces using or treating finely-divided materials in dispersion
    • F27B15/02—Details, accessories or equipment specially adapted for furnaces of these types
    • 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
    • C04B2290/00—Organisational aspects of production methods, equipment or plants
    • C04B2290/20—Integrated combined plants or devices, e.g. combined foundry and concrete plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/50—Carbon dioxide
    • 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
    • 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
    • Y02P40/18—Carbon capture and storage [CCS]

Definitions

  • the invention relates to a method for the production of cement by cutting hydraulic clinker and a latent hydraulic mineral mixture, wherein the hydraulic clinker is fired separately from the latent hydraulic mineral mixture.
  • the DE-Al-42 35 125 also discloses a process for the production of synthesis gas, wherein CO 2 -containing exhaust gases are used in the burning of lime in the cement production.
  • DE-C2-33 10 129 describes a process for producing different hydraulic binders from common raw materials in a firing process, wherein a partial flow of the gas / solid stream in the region of the calciner is indicated.
  • a binder composition is known in which deacidified cement raw meal with a latent hydraulic hardening substance, such as blast furnace slag, in particular blast furnace slag, is mixed.
  • a latent hydraulic hardening substance such as blast furnace slag, in particular blast furnace slag
  • a fast-curing hydraulic binder is also known from DE-T2-693 15 078, which is formed by a mixture of natural cement with natural or artificial pozzolans, such as industrial waste, in particular silicic acid fumes.
  • the invention is therefore based on the object of specifying a method and a plant for the production of cement, which allow a saving of heat energy and a reduction of the CO 2 emission even in such cases.
  • the hydraulic clinker is fired separately from latent hydraulic mineral mixture.
  • the latent hydraulic mineral mixture is doing by compilation desired raw materials and subsequent firing and / or melting of these raw materials and cooling, wherein the resulting in the preparation of the latent hydraulic mineral mixture exhaust gases are fed to a CO 2 - treatment, wherein the exhaust gases are compressed.
  • the plant according to the invention for the production of cement according to the method described above consists essentially of at least one furnace for burning the hydraulic clinker and a reactor for burning and / or melting the latent hydraulic mineral mixture, means for combining the hydraulic clinker and the latent separately prepared therefrom hydraulic mineral mixture, a comminuting device for the common or separate comminution of the hydraulic clinker and the latent hydraulic mineral mixture and a CO 2 -Avemrungs adopted for the resulting in the production of the latent hydraulic mineral mixture exhaust gas, wherein the CO 2 -Avemrungs shark comprises a compressor.
  • the raw materials for the latent hydraulic mineral mixture are preheated separately from the raw materials for the hydraulic clinker before the firing and / or melting process. Furthermore, at least a subset of the preheated raw materials is precalcined.
  • the hydraulic clinker and the latent hydraulic mineral mixture can be crushed either separately or together. Depending on whether they are mixed together after or before shredding.
  • the firing and melting process of the latently hydraulic mineral mixture it is possible in particular to burn the mineral mixture in a manner similar to the hydraulic clinker, but other temperatures are used or, as in the known blast furnace process, a melt is used over which Floating slag forms. In this case, however, slag-forming raw material is supplied. In addition, as the main product of the melting process, not the melt, but the slag is withdrawn, while the melt is retained to more than 50%, preferably more than 90%.
  • the latent hydraulic mineral mixtures can be produced very economically on an industrial scale. This in turn allows for a higher proportion of blastfurnace slag in the cement, which can reduce C ( ⁇ emissions in cement production.
  • the latent hydraulic mineral mixture is produced by targeted composition of desired raw materials and subsequent firing or melting of these raw materials and cooling.
  • the proportion of the latent hydraulic mineral mixture in the cement can be increased, wherein in addition to a saving of heat energy, a corresponding reduction of the CO 2 - emission is achieved.
  • the exhaust gas in the preparation of the latent hydraulic mineral mixture is also supplied to a CO 2 treatment, the CO 2 emissions can be reduced even further.
  • C Another potential for C ( ⁇ reduction is provided by the process for preparing the latent hydraulic mineral mixture.
  • air in particular cooler exhaust air, can be used.
  • air has a high nitrogen content, so a large amount of air is required for combustion. Separate disposal of these amounts of exhaust gas is not economically feasible. It is therefore desirable to increase the CO 2 concentration in the exhaust gas, thereby enabling economical treatment, storage or utilization / utilization.
  • combustion air which has an oxygen content of at least 75 mol%, preferably at least 90 mol%, in the production of the latently hydraulic mineral mixture.
  • Such a combustion air can be used both during precalcining and during the firing and / or melting process. Only by the measure, the CO 2 concentration in the exhaust gas can be increased to more than 70%.
  • the energy required to maintain the melt is supplied by adding fuel to the melt.
  • fuel In the method described above, about 60% of the CO 2 emissions are produced from the raw material-containing limestone, while about 40% result from the combustion.
  • one measure may be that hydrogen is used as fuel during the firing and / or melting process.
  • the CO 2 -containing exhaust gas produced during the production of the latently hydraulic mineral mixture can furthermore be subjected to CO 2 scrubbing or is dehumidified and compacted and, if appropriate, subjected to a low-temperature phase separation.
  • Another possibility is to supply the CO 2 -containing exhaust gas as a nutrient to a bioreactor by using plants, in particular algae.
  • the plants used can then be used as fuel in the firing or melting process.
  • the slag removed is cooled down so rapidly that at least the major part of the slag solidifies glassy. It is conceivable that the cooling takes place in two stages, being cooled first with a liquid cooling medium and then with a gaseous cooling medium.
  • the cooled slag is finely crushed, wherein at least a portion of the cooled slag is crushed to a fineness of at least 3,500 to 8,000 Blaine, preferably at least 10,000 Blaine.
  • At least part of the latent hydraulic mineral mixture prepared by the above process is used, at least part of the total latent hydraulic mineral mixture having the fineness given in the preceding paragraph.
  • the melting process is operated according to a preferred embodiment under a reducing atmosphere and with a metallic melt, wherein the melting process is fed slag-forming raw material and the main product of the melting process, the slag is withdrawn, while the melt is largely retained.
  • the resulting in the production of hydraulic clinker exhaust gases are either separately or together with the exhaust gases of the latent hydraulic mineral mixture of a CO 2 treatment, a CO 2 storage and / or a CO 2 use / recovery supplied.
  • 1 is a block diagram of a plant for the production of cement by blending of hydraulic clinker and a latent hydraulic mineral mixture
  • FIG. 2 is a block diagram of a plant for the production of latent hydraulic mineral mixture according to a first embodiment
  • FIG. 3 is a block diagram of a plant for the production of latent hydraulic mineral mixture according to a second embodiment
  • Fig. 4 is a block diagram of a plant for the production of latent hydraulic mineral mixture according to a third
  • Fig. 5 is a block diagram of a plant for the production of latent hydraulic mineral mixture according to a fourth exemplary embodiment
  • Fig. 6 is a block diagram of a plant for the production of latent hydraulic mineral mixture according to a fifth embodiment.
  • the plant shown in Fig. 1 consists essentially of a first process strhack 100 for producing a hydraulic clinker 21 and a second process strand 200 for producing a latent hydraulic
  • the first process line 100 comprises a furnace 101 for burning the hydraulic clinker and a downstream cooler 102.
  • the raw materials 104 required for the production of the hydraulic clinker 21 are supplied to the furnace 101 in suitable form. Before the actual firing process, the raw materials are preheated in the usual manner and / or precalcined.
  • a reactor 3 for firing and / or melting is provided to produce the latent hydraulic mineral mixture 20 by assembling desired raw materials 6, then firing or melting these raw materials and subsequently cooling.
  • means 103 for merging the hydraulic clinker 21 and latent hydraulic mineral mixture 20 are provided. These means can be formed for example by dosing belt cars. The ratio of the two components can thereby be adapted to the corresponding requirements.
  • the proportion of the hydraulic clinker is preferably in the range from 30 to 40% by weight, preferably in the range from 20 to 30% by weight.
  • the resulting mixture is optionally crushed with the addition of other additives 22, such as gypsum and other ingredients in a crushing plant 5 to cement 23.
  • the provision of two combustion units has the advantage that they can be adapted to the material to be fired.
  • the energy expenditure for firing the raw materials 6 for the latent hydraulic mineral mixture is much lower than when firing the raw materials of the hydraulic clinker 21, since for the deacidification of the lime-poor raw materials. 6 less heat input is required.
  • the latent hydraulic mineral mixture preferably has a constituent of 30 to 40% by weight of CaO, while the corresponding constituent of CaO in the case of the hydraulic clinker is preferably between 60 to 70% by weight.
  • the heat requirement can be reduced by about 30% compared to a cement made from pure hydraulic clinker.
  • the emission of CO 2 from CaCO 3 and CO 2 from fuel combustion is reduced even more. This results in great benefits for the heat industry and a significantly reduced environmental impact.
  • the plant shown in Fig. 2 for the production of latent hydraulic mineral mixture contains a preheater 1 and a calciner 2 for slag-forming, fine-grained raw material, a melt reactor 3, a cooling device 4 and a crushing plant. 5
  • the slag-forming raw material 6 is fed to the preheater 1, then passes as preheated raw material 7 in the calciner 2 and is finally registered as precalcined raw material 8 in the melt 9 of the melt reactor 3.
  • the exhaust gases 10 of the melt reactor 3 are fed to the calciner 2, which also fuel 11 and combustion air 12 is supplied as the warm Exhaust air from the cooling device 4 can come.
  • the exhaust gases 13 of the calciner enter the preheater 1.
  • the melt reactor 3, fuel 15 and combustion air 16 is supplied, which in turn can come as a warm exhaust air from the cooling device 4.
  • the combustion air in the calciner or the combustion air 16 in the melt reactor is preferably formed by pure oxygen or oxygen-enriched combustion air.
  • the withdrawn from the melt reactor liquid slag 17 is cooled in the cooling device 4 so quickly that at least the majority of the slag solidifies glassy.
  • the withdrawn slag can be cooled in two stages, wherein first with a liquid cooling medium 19, for example water, and then with a gaseous cooling medium 24, in particular air, is cooled.
  • the thus produced, predominantly amorphous, latent hydraulic mineral mixture 20 is then finely comminuted in the comminution plant 5, wherein the comminution of the latent hydraulic mineral mixture can be carried out either separately or together with the comminution of clinker 21 and other additives 22.
  • standard cement 23 is removed with the desired particle size distribution and with a high proportion of latent hydraulic mineral mixture.
  • the constituents of the cement are homogenized in a mixer to give cement.
  • the plant shown in Fig. 2 for the production of latent hydraulic mineral mixture further provides an air separation plant 25 and a CO 2 - treatment device 26 before. Furthermore, it comprises a return of a part 14 'of the exhaust gases of the preheater 1 into the calciner 2 and / or the melt reactor 3.
  • the air separation plant 25 serves to produce oxygen, which can be used as combustion air 12 in the calciner 2 and / or as combustion air 16 in the melt reactor 3. It is conceivable that the combustion air consists of pure oxygen or has an oxygen content of at least 75 mol%, preferably at least 95 mol%.
  • the use of oxygen or oxygen enriched air significantly reduces the amount of combustion air required for combustion, as the proportion of nitrogen is reduced accordingly.
  • the CO 2 concentration in the exhaust gas 14 after the preheater 1 can be increased from about 25% to 70 to 75% compared to a plant operated with normal combustion air.
  • the calciner 2 is designed as a flow current calciner, a minimum amount of carrier gas is required, which is usually composed of the exhaust gas 10 of the melt reactor and the combustion air 12. If, however, the amount of combustion air is reduced by the high oxygen content, it may be necessary to recirculate a partial quantity 14 'of the exhaust gas of the preheater 1 or also a partial amount of the exhaust gas of the calciner to the calciner 2 in order to provide a sufficient amount of carrier gas there.
  • the amount of carrier gas can be reduced so far that no recirculation of calciner and / or preheater exhaust gases is required. This would have the advantage that the Recarbonattician caused by the recirculation can be prevented.
  • the preheater 1 is expediently formed by a cyclone heat exchanger, in which, however, it inevitably leads to significant amounts of false air during preheating. Nevertheless, in this variant, a CO 2 concentration in the exhaust gas 14 of about 70 to 75% can be achieved. At the current state of development, however, CO 2 storage / storage only makes sense from concentrations of at least 96%.
  • the exhaust gas 14 is supplied to a CO 2 treatment device 26, the exhaust gas successively passing through a device 26a for dehumidification, a device 26b for compression and a device 26c for degassing. Further concentration of the exhaust gas could be achieved with a means 26d for cryogenic phase separation.
  • the CO 2 -containing gas present at the end of this process is so highly concentrated that economic storage and / or other use / utilization is possible.
  • the remaining residual gas 27 is vented to the atmosphere or otherwise used.
  • two preheaters 1a, 1b are provided, one preheater 1a being connected to the exhaust gas line of the calciner 2 and the other preheater 1b being connected to the exhaust gas line of the melt reactor 3.
  • the preheater Ib is thus only flowed through by the exhaust gases 10 of the melt reactor 3, while the preheater Ia is acted upon by the exhaust gases 13 of the calciner 2. Accordingly, the slag-forming raw material in two subsets 6a and 6b is the two preheaters Ia and Ib abandoned.
  • the preheater Ib preheated portion of the raw material 7b is passed directly into the melt reactor 3
  • the preheater Ia preheated partial amount 7a is first precalcined in calciner 2 and passes as precalcined raw material portion 8a in the melt reactor.
  • the calciner 2 is also operated with pure oxygen or at least with an oxygen-enriched combustion air, a very high CO 2 concentration is formed in the already exhaust gas 13 of the calciner or in the exhaust gas 14 of the preheater 1 a . Since the raw material is divided into two preheaters, resulting in correspondingly smaller preheater, so that the false air intake is about halve. This has the consequence that set at approximately the same thermal energy consumption higher CO 2 concentrations, which can be over 80%.
  • the exhaust gas 28 of the preheater Ib flowing through the exhaust gases of the melt reactor 3 escapes unhindered.
  • the proportion of CO 2 in the exhaust gas of the preheater Ib could however be reduced by heat treatment of preferably no carbonates in the preheater Ib, but only Al 2 O 3 , FeO 3 and SiO 2 carriers.
  • the hydrogen can be produced in a steam reformer 29 by means of natural gas and in a device 30 of pyrolyzed coal 31.
  • the steam reformer is expediently operated with the waste heat 32 of the cooling device.
  • the hydrogen is separated from the carbon dioxide.
  • 4 shows an alternative system with two preheaters 1a and 1b, wherein the preheater 1a flows through the exhaust gas 13 of the calciner 2 and the preheater 1b flows through the exhaust gases 10 of the melt reactor 3.
  • the preheater 1a flows through the exhaust gas 13 of the calciner 2 and the preheater 1b flows through the exhaust gases 10 of the melt reactor 3.
  • the partial quantity 7b of the raw material preheated in the preheater 1b does not pass directly into the melt reactor 3, but is first precalcined in the calciner 2 together with the other partial quantity 7a of the raw material preheated in the preheater 1a.
  • combustion air used in the calciner 2 can be preheated with the waste heat 32 of the cooling device 4 in a heat exchanger 34.
  • the principle of preheating the combustion air 12 for the calciner 2 is also maintained in the embodiment of FIG. 5.
  • only one preheater 1 is provided, which, however, in contrast to the first two embodiments, only flows through the exhaust gas 10 of the melt reactor 3.
  • the raw material 6 fed to the preheater 1 is supplied as preheated raw material 7 to the calciner 2, which is supplied with preheated combustion air 12, fuel 11 and a recirculated part 13 'of the calciner exhaust gas 13.
  • the exhaust gas 13 of the calciner is fed immediately after the calciner of the CO 2 - Aufleungs learned 26, so that any false air inlet is avoided in the preheater for this exhaust.
  • a cooling device 37 for example in the form of a steam reformer, is interposed.
  • the cooling device can then be used for example for power generation or hydrogen production.
  • CO 2 concentrations in the exhaust gas 13 of 96% and more can be achieved, so that only dehumidification and subsequent compression is required if the CO 2 is to be stored.
  • the gas can also be used for other purposes or recovery.
  • the melt reactor 3 can be operated with hydrogen. This fuel would also be in the embodiment of FIG. 4 is a good way to avoid the CO 2 - share due to the fuel.
  • the high temperatures of the exhaust gas 28 cause a significantly increased heat consumption.
  • FIG. 6 shows a system in which the CO 2 treatment device 26 is formed by a device 26e for scrubbing CO 2 of the exhaust gas 14 and a device 26f for regenerating the solvent used.
  • the device 26f can be operated by the waste heat 32 of the cooling device 4.
  • the device 26e for CO 2 scrubbing is preceded by a device 38 for desulfurization.
  • the production of latent hydraulic mineral mixture produces significantly less CO 2 emissions than clinker production, an increase in the latent hydraulic mineral mixture content in the cement already leads to a significant reduction in CO 2 emissions.
  • the CO 2 emissions in the production of the latently hydraulic mineral mixture can be additionally reduced.
  • the CO 2 -containing gas can be stored in appropriate deposits.
  • the CO 2 -containing exhaust gas for the production of fuel, which is ideally used as fuel in the production of latent hydraulic mineral mixture.
  • This can be done with plants, In particular algae, equipped bioreactor can be provided, through which the CO 2 - containing exhaust gases are passed. In combination with light, the algae convert the CO 2 into biomass and oxygen through photosynthesis. The biomass can then be used as fuel in the fuel or smelting reactor 3.
  • a CO 2 treatment is not required, so that the exhaust gas can be passed directly after the calciner or the preheater in the bioreactor.
  • a bioreactor 35 is indicated by dashed lines. But it can also be used in the other embodiments.
  • the exhaust gas can be freed from dust by a dedusting device 36 before entering the bioreactor 35. Since the algae naturally have a high moisture content after harvesting, optionally the heat of the gaseous cooling medium heated in the cooler 24 can be used to dehumidify the algae in a drier 39.

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Abstract

L'invention concerne un procédé et une installation de fabrication de ciment par mélange de clinker hydraulique et d'un mélange minéral à hydraulicité latente, le clinker hydraulique étant cuit séparément du mélange minéral à hydraulicité latente. Le mélange minéral à hydraulicité latente est produit par association de matières premières souhaitées, puis par cuisson et/ou fusion et refroidissement de ces matières premières, les gaz de combustion issus de la production du mélange minéral à hydraulicité latente étant acheminés dans une unité de traitement de CO2 dans laquelle ils sont comprimés.
PCT/EP2009/065485 2008-11-28 2009-11-19 Procédé et installation de fabrication de ciment Ceased WO2010060855A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008059370A DE102008059370B4 (de) 2008-11-28 2008-11-28 Verfahren und Anlage zur Herstellung von Zement
DE102008059370.2 2008-11-28

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WO2010060855A1 true WO2010060855A1 (fr) 2010-06-03

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Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8864878B2 (en) * 2011-09-23 2014-10-21 Alstom Technology Ltd Heat integration of a cement manufacturing plant with an absorption based carbon dioxide capture process
DE102012105977B4 (de) * 2012-07-04 2015-11-05 Thyssenkrupp Industrial Solutions Ag Verfahren und Anlage zur Herstellung von Zementklinker aus Zementrohmehl
EP3231779B1 (fr) * 2016-04-15 2018-11-14 HeidelbergCement AG Procédé et installation de fabrication de ciment dans le mode d'oxycombustion
CN119768656A (zh) 2022-08-30 2025-04-04 蒂森克虏伯伯利休斯有限公司 在水泥熟料生产中co2排放的减少
BE1030823B1 (de) * 2022-08-30 2024-03-26 Thyssenkrupp Ind Solutions Ag Reduktion von CO2-Emissionen bei der Herstellung von Zementklinker

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH243052A (de) * 1944-12-29 1946-06-30 Bbc Brown Boveri & Cie Verfahren und Einrichtung zur Herstellung von Zement.
WO1999067182A1 (fr) * 1998-06-24 1999-12-29 'holderbank' Financiere Glarus Ag Procede de fragmentation et de reduction de scories contenant un oxyde metallique
WO2002070423A1 (fr) * 2001-02-06 2002-09-12 Tribovent Verfahrensentwicklung Gmbh Procede de fabrication d'un additif pour ciments melanges, et dispositif pour la mise en oeuvre de ce procede
US20080022903A1 (en) * 2006-07-25 2008-01-31 Council Of Scientific & Industrial Research Process for the production of portland slag cement using granulated blast furnace slag
WO2008050289A2 (fr) * 2006-10-26 2008-05-02 Foster Wheeler Energy Corporation Procédé et appareil de captage de co2 en oxycombustion
DE102007025094A1 (de) * 2007-05-30 2008-12-04 Polysius Ag Verfahren und Anlage zur Herstellung von Zement

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3310129A1 (de) 1983-03-21 1984-09-27 Klöckner-Humboldt-Deutz AG, 5000 Köln Verfahren und vorrichtung zur herstellung von hydraulischen bindemitteln
DE3412357A1 (de) 1984-04-03 1985-10-10 Klöckner-Humboldt-Deutz AG, 5000 Köln Hydraulisch haertbare, anorganische bindemittelzusammensetzung
FR2694552B1 (fr) 1992-08-05 1994-10-28 Vicat Liants hydrauliques à prise et durcissement rapides, leur préparation et leur utilisation pour la préparation de mortiers et bétons.
DE4235125C2 (de) * 1992-10-17 1994-09-29 Zsw Verfahren zur Herstellung von Synthesegas und Vorrichtung zum Durchführen des Verfahrens
EP1741683A3 (fr) 2005-07-08 2010-09-01 Alexander Kehrmann Mélange des matières brutes pour la production d'un clinker de ciment, clinker de ciment et ciment

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH243052A (de) * 1944-12-29 1946-06-30 Bbc Brown Boveri & Cie Verfahren und Einrichtung zur Herstellung von Zement.
WO1999067182A1 (fr) * 1998-06-24 1999-12-29 'holderbank' Financiere Glarus Ag Procede de fragmentation et de reduction de scories contenant un oxyde metallique
WO2002070423A1 (fr) * 2001-02-06 2002-09-12 Tribovent Verfahrensentwicklung Gmbh Procede de fabrication d'un additif pour ciments melanges, et dispositif pour la mise en oeuvre de ce procede
US20080022903A1 (en) * 2006-07-25 2008-01-31 Council Of Scientific & Industrial Research Process for the production of portland slag cement using granulated blast furnace slag
WO2008050289A2 (fr) * 2006-10-26 2008-05-02 Foster Wheeler Energy Corporation Procédé et appareil de captage de co2 en oxycombustion
DE102007025094A1 (de) * 2007-05-30 2008-12-04 Polysius Ag Verfahren und Anlage zur Herstellung von Zement

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