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WO2016120253A1 - Procédé de traitement thermique d'une matière de départ - Google Patents

Procédé de traitement thermique d'une matière de départ Download PDF

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Publication number
WO2016120253A1
WO2016120253A1 PCT/EP2016/051536 EP2016051536W WO2016120253A1 WO 2016120253 A1 WO2016120253 A1 WO 2016120253A1 EP 2016051536 W EP2016051536 W EP 2016051536W WO 2016120253 A1 WO2016120253 A1 WO 2016120253A1
Authority
WO
WIPO (PCT)
Prior art keywords
reduction reactor
reactor
air
calcining
caiciniereinrichtung
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/EP2016/051536
Other languages
German (de)
English (en)
Inventor
Eike Willms
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 AG
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp AG
ThyssenKrupp Industrial Solutions 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 ThyssenKrupp AG, ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp AG
Publication of WO2016120253A1 publication Critical patent/WO2016120253A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • C04B2/00—Lime, magnesia or dolomite
    • C04B2/10—Preheating, burning calcining or cooling
    • 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
    • F27B7/2025—Arrangements of preheating devices for the charge consisting of a single string of cyclones
    • F27B7/2033—Arrangements of preheating devices for the charge consisting of a single string of cyclones with means for precalcining the raw material
    • 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
    • Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills

Definitions

  • the invention relates to a process for the heat treatment of a starting material, wherein the material is preheated, then calcined and finally cooled.
  • the invention is based on the object to provide an energy-efficient method for heat treatment of a starting material, in particular a calcium or magnesium-based starting material, in which using sulfur-rich fuels such as petroleum coke or substitute fuels, a product can be produced that meets all the requirements of the Product quality in terms of the maximum residual sulfur content and a high reactivity simultaneously met. According to the invention, this object is solved by the features of claim 1. Further embodiments of the invention are the subject of the other claims.
  • the starting material having a particle size of less than 5 mm of a preheating device is abandoned and preheated there in the air stream and then in at least one stage Calciner calcined under oxidizing conditions.
  • the at least partially calcined material emerging from the calcining means is subjected to further heat treatment in reducing conditions in a downstream reduction reactor and finally cooled in a cooling device, wherein a gas stream inserted in the reduction reactor subsequently flows through the calcining means and the preheater and between the reduction reactor, the calcining means and the preheating device forms a pollutant cycle, wherein contained in the gas stream pollutants accumulate in the preheater on the material and are released in the reduction reactor back into the gas phase and to relieve the Scha di compound cycle s part of the at least partially calcined material between calciner and reduction reactor is discharged and / or a portion of the gas stream between reduction reactor and preheater is discharged.
  • the above process enables the heat treatment of starting material, especially calcium or magnesium containing starting material with a high demand on the product quality, in particular with regard to a low sulfur content and a high product reactivity, using sulfur and / or chlorine-containing fuels, in particular solid fuels, such as petroleum coke or substitute fuels.
  • the fine-grained, powdered or partially agglomerated, preferably calcium or magnesium-containing material is preheated countercurrently in the preheating device formed, for example, by a cyclone preheater, applied to the calciner operated in an oxidizing gas atmosphere ( ⁇ > 1) and completely there or at least partially calcined and deposited.
  • the adsorption of sulfur in the preheater takes place almost completely on the preheated particle surfaces.
  • the sulfur is when entering the Calcinier worn thus mainly as calcium or magnesium sulfate, which is practically not thermally decomposed at given calcination temperatures of 600 to 900 ° C.
  • the decomposition of the sulfur takes place in the downstream, reducing operated reduction reactor.
  • the sulfate compounds are already quantitatively decomposed at about 900 ° C gas phase temperature.
  • the sulfur cycle thus forms between the reduction reactor and the preheater.
  • the solids flow is discharged between Caicinier driven and reduction reactor.
  • the partial gas stream may be withdrawn either at one or more points of the oxidizing calcination stage.
  • the sulfur contained in the gas phase is bound by gas cooling on the solid contained in exhaust gas.
  • the almost completely desulfurized product leaving the reduction stage is cooled to the desired final temperature in a cooling device.
  • the cooling device can be designed, for example, as a cyclone cooler, fluidized-bed cooler or the like, in which preferably the air required for the combustion is preheated, so that the heat consumption of the system is reduced.
  • the starting material to be supplied to the preheating device is preferably calcium or magnesium-containing material.
  • the starting material can furthermore be present in fine-grained or powdery or partially agglomerated form.
  • Both the reduction reactor and the Caicinier overlooked energy must be supplied.
  • the energy supply for the Caicinier styles can take place exclusively via the gas stream from the reduction reactor, at the outlet of which a certain amount of carbon monoxide is present, which is burned in the oxidizing atmosphere of the Caicinier Road under the supply of air.
  • the energy can also be supplied via several points of the reduction reactor and the Caicinier driving.
  • the energy that is made available to the reduction reactor and the Caicinier styles can be done for example by combustion or gasification of sulfur-containing, solid fuel.
  • the reduction reactor may consist of a flow reactor with downstream separator, care must be taken that the separator is operated completely reducing.
  • the reduction reactor consists of a fluidized bed reactor or a similar aggregate.
  • Another possible embodiment of the reduction reactor would be a conditioning drum with downstream at least one-stage cooling device, wherein a part of in the Cooling device resulting exhaust air, bypassing the conditioning drum of the oxidatively operated Caicinier Nurs.
  • the cooling device is designed such that at least two different exhaust air streams with different temperature levels are formed, the exhaust air flow at the lower temperature is advantageously supplied to the oxidizing-operated caustic device bypassing the conditioning drum.
  • targeted concentration of the atmosphere in the reduction reactor and / or in the calciner, gas recirculation and / or staged air / fuel addition is intended to bring about maximum enrichment of individual exhaust gas components such as C0 2 from the deacidification of the raw material and fuel conversion.
  • individual exhaust gas components such as C0 2 from the deacidification of the raw material and fuel conversion.
  • a concentration of 40 to 90% C0 2 based on dry exhaust gas is desired.
  • Such a concentration allows the use of this gas, for example in the production of soda.
  • the material to be treated is maintained in the oxidizing Caicinier Nurnier Nurs and in the reducing reaction reactor operated at the same or approximately the same material temperature.
  • the material from the oxidizing Caicinier Nurnier is treated in the reducing reaction reactor operated at a lower or higher temperature level than in the oxidizing Caicinier reminder.
  • the reduction reactor exhaust gas from the oxidizing Caicinier Nurs can be returned.
  • the at least partial use of the exhaust air from the cooling device as combustion air in the Caicinier teeth has a positive effect on the heat consumption.
  • Another possible embodiment is to use a combustor or carburettor for fuel delivery in the direction of gas flow before the reduction reactor and upstream of the calciner or into the reduction reactor and the calciner flightable fuel and preheated air, e.g. from the cooling device, so that the desired stoichiometric conditions are set.
  • the material from the oxidizing calciner is kept in the reducing reduction reactor operated at the same material temperature in order to achieve a uniform calcination.
  • air, fuel and material feed can each be stepped in the calcining device, ie at different levels.
  • the process of the invention primarily relates to the interactions in the heat treatment of fine-grained or powdered material, such as lime and dolomite, with respect to fuels rich in sulfur.
  • fine-grained or powdered material such as lime and dolomite
  • the decomposition of volatile components in a reducing atmosphere can also be used for other circuit-forming compounds be valid .
  • the preheating device is preceded by a drying unit and the bulk material in the drying unit is dried with exhaust gases from the preheating device and / or the cooling device. If the bulk material before drying does not yet have the desired particle size of less than 5 mm, preferably less than 3 mm, it can be provided that the bulk material is comminuted to the desired particle size before the drying unit or in a comminution unit integrated in the drying unit.
  • the process conditions are preferably adjusted to give, after cooling, a product containing less than 0.1% by weight of sulfur, preferably less than 0.05% by weight of sulfur and most preferably less than 0.03% by weight. Contains sulfur.
  • a product with a reactivity to DIN 459-2 of less than 2 minutes should preferably be formed.
  • the process described above may also be applied to other fine-grained or powdery or agglomerated bulk materials which are required to contain certain circulatory agents, e.g. Sulfur, in the final product to reduce.
  • certain circulatory agents e.g. Sulfur
  • Fig. 1 is a schematic representation of a plant for carrying out the method for heat treatment of a starting material according to a first embodiment
  • FIG. 2 shows a schematic representation of a plant for carrying out the method for heat treatment of a starting material according to a second exemplary embodiment
  • FIG Fig. 3 shows a schematic representation of a plant for carrying out the method for heat treatment of a starting material according to a third exemplary embodiment.
  • the plant for carrying out the process for heat treatment of a starting material, in particular a fine-grained or powdery or partially agglomerated material, according to FIG. 1 comprises a preheating device 1 formed by a multi-stage cyclone preheater, a calcining device 2, a reduction reactor 3 and a cooling device formed by a two-stage cyclone cooler 4 on.
  • the calcining device 2 and the reduction reactor 3 each have an entrained flow reactor (riser shaft) 2a, 3a with a downstream separator 2b, 3b. The entire heat treatment thus takes place in the flow stream.
  • the reduction reactor 3 is operated with exhaust gases 8a of the preheating device 1, exhaust gases 5 of the calcining device 2 and / or a mixture of these exhaust gases. Furthermore, the reduction reactor fuel 9 and exhaust gases 7a of the cooling device 4 are supplied as combustion air.
  • the preheating device 1 is a fine-grained or powdery or partially agglomerated material 10 having a particle size of less than 5 mm, preferably less than 3 mm, abandoned. If a bulk material 10 ' with a moisture content of more than 2% or even more than 5% is used as the material 10, this bulk material can be dried in an optional drying unit 11 with the exhaust gases of the preheating device 1. Furthermore, the bulk material 10 'in front of the drying unit or in a crushing device 12 integrated in the drying unit can be comminuted to a particle size of less than 5 mm, preferably less than 3 mm.
  • the material 10 is preheated in the preheater 1 in countercurrent to the exhaust gases of the Calcinier Anlagen 2 and passes as preheated material 10a in the Calcinier autism 2, where it with the exhaust gases of the reduction reactor 3 in an oxidizing atmosphere with the addition of oxygen-containing combustion air in the form of exhaust air 7b the cooling device 4 and with optional addition of fuel 13 is at least partially calcined.
  • the calcination temperatures in the Calcinier boots are in the lime in the range of 800 to 900 ° C and in the case of dolomite in the range of 600 to 700 ° C.
  • the combustion air addition and / or the fuel addition may also be stepped, i. E. in at least two different levels, done.
  • the at least partially calcined material 10b in the calcining means 2 is deposited and fed to the reduction reactor 3 where it is subjected to a further heat treatment under reducing conditions.
  • the reduction reactor 3 is operated at the same temperature as the calciner.
  • the separator 3b the further treated material 10c is deposited and cooled in the subsequent cooling device 4 by means of air 14 or another cooling medium. The cooled end product 10d is removed.
  • a pollutant cycle can be formed between the reduction reactor 3, the calcining device 2 and the preheating device 1, in particular when using a sulfur-containing fuel, pollutants present in the gas stream the preheating 1 attach to the material 10 and are released in the reduction reactor 3 again in the gas phase.
  • a portion 10e of the calcined material can be discharged between the calciner 2 and the reduction reactor 3.
  • a part 15 of the gas stream can be discharged to the reduction reactor 3 and before the preheater 1.
  • the part 15 of the gas stream is branched off in the transition region between reduction reactor 3 and calcining device 2 and processed in a manner known per se.
  • the embodiment according to FIG. 2 essentially corresponds to the first exemplary embodiment except for the supply of the fuel.
  • the fuel of Calcinier worn 2 and the reduction reactor 3 is not directly, but supplied via upstream combustion chambers 16, 17, wherein solid, liquid or gaseous fuels can be used.
  • the combustion chambers 16, 17 could also be applied directly to the reduction reactor 3 and / or the calcining device 2, in particular in the region of the riser shafts.
  • the additional combustors also allow for the use of more problematic fuels, especially refuse derived fuels, which can not be intentionally burned in the airstream.
  • FIG. 3 essentially corresponds to FIG. 1.
  • the reduction reactor 3 is formed by a conditioning drum.
  • the cooling device 4 consists for example of a fluidized bed cooler or similar cooling unit 18.
  • the hot air. 6 the cooling unit 18 is supplied to the conditioning drum as preheated combustion air in the amount of the task of the fuel 9. It can be taken at another point of the cooling device further preheated air 7, which can be used as combustion air 7b in the Caicinier Nur 2 and / or as drying air 7c in the drying unit 11.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Ceramic Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)

Abstract

Dans le procédé selon l'invention de traitement thermique d'une matière de départ, la matière de départ est amenée, avec une granulométrie inférieure à 5 mm, à un dispositif de préchauffage où elle est préchauffée dans le flux, puis calciné dans un dispositif de calcination à au moins un étage dans des conditions oxydantes. La matière, au moins partiellement calcinée dans le dispositif de calcination, est soumise à un autre traitement thermique dans un réacteur de réduction placé en aval dans des conditions au moins partiellement réductrices et enfin refroidie dans un dispositif de refroidissement. Un flux de gaz, utilisé dans le réacteur de réduction, passe ensuite à travers le dispositif de calcination et le dispositif de préchauffage et une circulation de polluants se forme entre le réacteur de réduction, le dispositif de calcination et le dispositif de préchauffage. Les polluants contenus dans le flux de gaz se fixent sur la matériau dans le dispositif de préchauffage et sont libérés dans le réacteur de réduction de nouveau sous forme phase gazeuse et, pour dégager le circuit de polluants, une partie de la matière au moins partiellement calcinée est déchargée entre le dispositif de calcination et le réacteur de réduction et/ou une partie du flux de gaz est déchargée entre le réacteur de réduction et le dispositif de préchauffage.
PCT/EP2016/051536 2015-01-28 2016-01-26 Procédé de traitement thermique d'une matière de départ Ceased WO2016120253A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102015101237.5 2015-01-28
DE102015101237.5A DE102015101237A1 (de) 2015-01-28 2015-01-28 Verfahren zur Wärmebehandlung von feinkörnigem oder pulverförmigem Material

Publications (1)

Publication Number Publication Date
WO2016120253A1 true WO2016120253A1 (fr) 2016-08-04

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DE (1) DE102015101237A1 (fr)
WO (1) WO2016120253A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11680013B2 (en) 2019-05-13 2023-06-20 Carmeuse Lime, Inc. Calciner using recirculated gases

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE1027979B1 (de) * 2020-01-09 2021-08-10 Thyssenkrupp Ind Solutions Ag Verfahren zur Wärmebehandlung und Farboptimierung von natürlichen Tonen
US20230131508A1 (en) * 2020-01-09 2023-04-27 Thyssenkrupp Industrial Solutions Ag Apparatus and process for thermal treatment of mineral solids
DE102024104811A1 (de) * 2024-02-21 2025-08-21 Khd Humboldt Wedag Gmbh Verfahren zur thermischen Behandlung von Rohmehl unter Verwendung einer elektrischen Heizvorrichtung und dazu korrespondierende Anlage

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5049198A (en) * 1988-06-10 1991-09-17 Ribas Roger S Calcium sulfate process for the coproduction of Portland cement clinker and concentrated sulfur dioxide adequate to manufacture sulfuric acid
WO1996000703A1 (fr) 1994-06-29 1996-01-11 F.L. Smidth & Co. A/S Installation pour un traitement thermique de materiaux en morceaux
WO2002046671A1 (fr) * 2000-12-05 2002-06-13 Polysius Ag Installation et procede de traitement thermique d'une matiere en morceaux
DE102009018099A1 (de) * 2009-04-20 2010-10-28 Polysius Ag Anlage zur Wärmebehandlung von stückigem Feststoff

Family Cites Families (1)

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Publication number Priority date Publication date Assignee Title
DE3140582C2 (de) * 1981-10-13 1985-01-17 Beckenbach, Ulrich, Dipl.-Ing., 4005 Meerbusch Verfahren und Ringschachtofen zum Brennen und Sintern von stückigem Gut, wie Kalkstein, Dolomit oder dergleichen

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5049198A (en) * 1988-06-10 1991-09-17 Ribas Roger S Calcium sulfate process for the coproduction of Portland cement clinker and concentrated sulfur dioxide adequate to manufacture sulfuric acid
WO1996000703A1 (fr) 1994-06-29 1996-01-11 F.L. Smidth & Co. A/S Installation pour un traitement thermique de materiaux en morceaux
WO2002046671A1 (fr) * 2000-12-05 2002-06-13 Polysius Ag Installation et procede de traitement thermique d'une matiere en morceaux
DE10060381A1 (de) 2000-12-05 2002-06-13 Krupp Polysius Ag Anlage und Verfahren zur thermischen Behandlung von stückigem Material
DE102009018099A1 (de) * 2009-04-20 2010-10-28 Polysius Ag Anlage zur Wärmebehandlung von stückigem Feststoff

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11680013B2 (en) 2019-05-13 2023-06-20 Carmeuse Lime, Inc. Calciner using recirculated gases

Also Published As

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