EP0256021A1 - Procede et dispositif pour diminuer le degagement d'oxyde de soufre et/ou de composes organiques volatils formes pendant le chauffage de la farine crue dans le circuit de prechauffage, en particulier dans l'echangeur de chaleur du dispositif de prechauffage par mise en suspension dans les gaz dans l - Google Patents

Procede et dispositif pour diminuer le degagement d'oxyde de soufre et/ou de composes organiques volatils formes pendant le chauffage de la farine crue dans le circuit de prechauffage, en particulier dans l'echangeur de chaleur du dispositif de prechauffage par mise en suspension dans les gaz dans l

Info

Publication number
EP0256021A1
EP0256021A1 EP19860906223 EP86906223A EP0256021A1 EP 0256021 A1 EP0256021 A1 EP 0256021A1 EP 19860906223 EP19860906223 EP 19860906223 EP 86906223 A EP86906223 A EP 86906223A EP 0256021 A1 EP0256021 A1 EP 0256021A1
Authority
EP
European Patent Office
Prior art keywords
sulfur oxide
organic compounds
raw meal
release
heating
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.)
Withdrawn
Application number
EP19860906223
Other languages
German (de)
English (en)
Inventor
Ludwig Kwech
Rainer Hoffmann
Harald Harmuth
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.)
Perlmooser Zementwerke AG
Original Assignee
Perlmooser Zementwerke 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 Perlmooser Zementwerke AG filed Critical Perlmooser Zementwerke AG
Publication of EP0256021A1 publication Critical patent/EP0256021A1/fr
Withdrawn legal-status Critical Current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
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/60—Methods for eliminating alkali metals or compounds thereof, e.g. from the raw materials or during the burning process; methods for eliminating other harmful components
    • 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
    • F27B7/205—Arrangements of preheating devices for the charge consisting of at least two strings of cyclones with two different admissions of raw material with precalcining means on the string supplied with exhaust gases from the cooler

Definitions

  • the present invention relates to the reduction of the emission of sulfur oxide and / or of volatile organic compounds formed during the heating of the raw meal in the preheating system, in particular in the floating gas heat exchanger during cement production. According to the invention, these emissions are reduced in that the sulfur oxide and or the volatile organic compounds are released in a partial gas stream, in particular a suspended gas heat exchanger, and are preferably fed back to the furnace system for integration during the cement firing process.
  • cement clinker is usually produced largely using the suspended gas heat exchanger process, in which finely ground zeolite powder is preheated in a single-strand or multi-strand heat exchanger using the sensible heat of the furnace exhaust gas and possibly a further combustion in suspension in the flue gas is then precalcined, depending on the procedure, or given to the rotary kiln immediately after preheating, is burned in the rotary kiln to form the desired clinker phases, after which the clinker is cooled in a clinker cooler.
  • the heat exchanger mentioned is usually a (often 4-stage) arrangement of cyclones which are successively flooded by the flue gas, the raw meal being fed into the gas line to the top cyclone, in which the flue gas is heated, after separation in the cyclone of the next lower stage, where heating takes place again, etc. It is customary to partially calcine the preheated hot meal in the gas line between the inlet of the furnace and the bottom cyclone of the heat exchanger, or also predominantly if fuel is introduced further. We also use our own pre-caicinators, which largely calcinate the hollow before entering the furnace. Conventional heat exchanger designs differ in the number of floods through which the flue gas to the calciner or furnace inlet flows in parallel, and in the type of flour guidance which can be carried out separately for each flood or can also cross from one to the other.
  • post-cleaning can be carried out to reduce the emission, which is preferably done in the combustion plant itself even in areas of higher temperature, for example can be carried out in the lowest heat exchanger stage, in the calcining device or in the stovepipe.
  • Preheating system in particular in the suspended gas heat exchanger in the cement production of sulfur oxide and / or volatile organic compounds, is accordingly characterized in that the formation and release of the sulfur oxide from the sulfur compounds and or the release of the organic compound of the raw meal at least partially with a portion gas flow takes place in a separate heating device and that the exhaust gas leaving this device, enriched with sulfur oxide and / or the organic compounds or their decomposition products, is subjected to a post-purification for separation and / or is returned to the existing furnace system in a temperature range, in which is a reaction and integration of the sulfur oxide and / or the organic compounds or their decomposition products.
  • the raw meal is heated in the device provided for the release of the sulfur oxide and / or the volatile organic compounds by supplying one of the existing heat exchanger system and / or the furnace inlet area and / or the furnace head and / or the amount of hot gas removed from the clinker cooling device.
  • the exhaust gas enriched with sulfur e ⁇ dd and / or the organic compounds is returned to that area of the furnace system in which the deacidification of the CaCO- takes place, preferably to the calciner.
  • the exhaust gas enriched with sulfur oxide and / or the organic compounds is fed to an independent flue gas scrubber according to a conventional method.
  • a further, expedient embodiment of the method according to the invention provides that the exhaust gas enriched with sulfur oxide and / or the organic compounds is fed to the furnace at the furnace outlet, preferably as secondary air.
  • a particularly advantageous variant of the method according to the invention is characterized in that the heating of the raw meal in the separate device provided for the release of the sulfur oxide and / or the volatile organic compounds in its entirety or, in combination with the above-mentioned heating of the raw meal with hot gas , partly by its own firing device, preferably its own burner.
  • the formation and release of the sulfur oxide is carried OF INVENTION ⁇ -making according to the designated special device advantageously in a temperature range between 280 ° C and 700 ° C, preferably between 300 ° C and 600 ° C, in particular between 380 ° C and 500 ° C *
  • the formation and release of the organic compounds takes place in the separate device provided for this purpose advantageously in a temperature range between 100 ° C. and 500 ° C., preferably 150 ° C. and 00 ° C., in particular between 200 ° C. and 300 ° C.
  • the temperature in the separate device provided for the formation and release of the sulfur oxide and / or the organic compound is advantageously controlled by a separate firing device for the heating device provided for the release of the sulfur oxide and / or the organic compounds and / or a quantity control of the hot gas supplied to this heating device.
  • the proportion of the current supplied to the heating apparatus gesondsp- th Rohmehles is in Depending ⁇ @ keitvom sulfur -halt of the clean gas regulated.
  • the purpose of this procedure is to minimize the amount of flour supplied to the heating device depending on the actual need due to the current emission, so that the additional heat consumption caused by the amount of flour supplied to the heating device is minimized as far as possible.
  • the furnace operation can be economically adapted to the respective raw material situation.
  • a further expedient embodiment of the method according to the invention provides for the feed of a raw meal partial stream or one or more raw meal components without preheating into the tertiary air, in particular a raw meal partial flow with an increased sulfide content or an increased content of volatile organic compounds.
  • the raw meal partial flow or the raw meal components * Part or all of it is fed to the furnace and any remaining portion is removed from the process and ensiled.
  • a simple solution can be found in the event that the sulfide or the volatile organic bistands are concentrated in one component. This can happen, for example, if the raw meal is made from lime and clay and that Sulfide is concentrated in the lower clay component.
  • the lime content of the raw meal in the heating device would be virtually ballast and would have an unfavorable thermal effect, whereas the low quantity ratio of the clay to the entire raw meal allows this special solution.
  • a heat exchange is carried out between flue gas after the heat exchanger and tertiary air after the heating device.
  • This special procedure can be advantageous, for example, if the raw material chemistry directly requires the entire raw meal stream to be fed onto the heating device without prior preheating. In this case, a sharp drop in temperature of the entire tertiary air and possibly additional firing can be expected, combined with an increased flue gas temperature after the heat exchanger.
  • a heat exchange between flue gas after the heat exchanger and tertiary air after the heating device can equalize the two temperatures. This heat exchange is advantageously carried out indirectly, so that the tertiary air can then be fed back to the calciner.
  • the present invention furthermore relates to a device for carrying out the method described above, which is characterized in that the device device for releasing the sulfur oxide and / or the organic compounds from the raw meal from a riser and a downstream cyclone.
  • the device for performing the method according to the invention is characterized in that the device for releasing the sulfur oxide and / or the organic compounds from the raw meal consists of a fluidized bed and a cyclone separator, in particular a circulating fluidized bed with recirculation of the material .
  • the quantity control of the hot gas supplied to the device provided for the formation and release of the sulfur oxide and / or the organic compounds is formed by a bypass bypass of the heating device.
  • FIG. 1 shows a schematic representation of a device suitable for carrying out the method according to the invention
  • FIG. 2 shows a modification of the device according to FIG. 1,
  • FIG. 3 shows a variant of the device according to FIG. 2.
  • the raw cement meal is fed via a feed device 1 to an upper heat exchanger area 2, which receives the flue gas from the lower heat exchanger area 6 via a riser 16.
  • the raw feed material thus reaches the heating device at the desired preheated temperature via a chute 3, a switch contained in the chute 3 optionally dividing the preheated flour into the heating device 4 and the lower heat exchanger area 6 in any desired manner Extent allowed. -
  • the raw meal can also be obtained directly without preheating the heating device - Device 4 are abandoned.
  • the raw meal passes through a chute 5 i Q to the lower heat exchanger area 6, which ensures further preheating and precalcination of the raw meal to the desired extent and can be provided with a firing device 21 for this purpose.
  • the preheated and expediently at least to a small extent precalcined flour passes through a chute 7 into the rotary kiln 8 provided with a furnace 20 and after the clinker fire into the clinker cooler 9.
  • the heating device 4 receives one or more of the gas streams 10, 11, 12, 10 being flue gas and 11 and 12 preheated hot air.
  • the quantity of these gas streams can preferably be regulated;
  • a firing device 22 can preferably provide for the supply of thermal energy.
  • the quantity of flue gas 13 can be regulated, so that the desired quantity of gas can be achieved in the preheating device by regulating the quantities of gas flows 10, 11, 12 and 13 ' or 14 and 13, • or 15 and 13.
  • a blower can be used in the gas line 14, which permits quantity regulation.
  • the hot gas after the heating device 4 can be supplied via a gas line 14 to the lower heat exchanger area 6, preferably in stages of raw meal extraction, and / or via a gas line 15 to an area 19 which is inside (for example furnace head) or outside the process (eg flue gas cleaning, grinding drying plant).
  • the remaining amount of gas is discharged from the system via the gas line 17 and a blower 18 and can be fed to a further flue gas utilization.
  • FIG. 2 shows a preferred modification of the method, as is used in particular for processing sulfide-containing cement raw meal with the lowest possible sulfur oxide emission.
  • the raw meal is fed to the double cyclone 31 of the heat exchanger via a feed device 1 and is already preheated in a riser in front of this cyclone by the flue gas, so that it is then already heated in the reaction chamber 4 via a chute 3 enters, which is supplied with hot air from the furnace head, which is conveyed via a line 32 to a clinker dust separator 33 and from which any proportion which can be selected enters the reaction chamber 4 or via a bypass 3 with quantity control device 35 with Um ⁇ the reaction chamber 4 and the separator 36 to the precalciner 37 is conveyed.
  • the crude meal is further heated and the sulfur oxide is released via a firing device 22, after which the solid is separated from the gas phase in a separator 3 and via a chute 38 in the riser 39 is conveyed in front of the cyclone 40 of the heat exchanger, where the further preheating and ultimately calcining takes place in several stages (further cyclones 41, 42 with chutes 43, 44 and risers 45, 46).
  • the hot gas passes after the separator 36, possibly after being mixed with the bypass amount, into the precalcination device 37.
  • the gas amount control required for temperature control can be provided by control devices (for example flaps or slides), specifically a flap 47 or flaps 47 and 35 additionally with the flap 48 in the riser 49 or with a combination of the flaps 48, 35 and 47 with the blower 50. If the blower 50 is not present, the " blower also takes over the pressure loss in the heating device.
  • the precalcination device 37 is fed on the one hand with the preheated flour to the cyclone 42 via a chute 52 and on the other hand with the furnace flue gas via a riser channel 49, and with the hot gas to the separator 36 and possibly bypass 34 through the gas line 53.
  • Part of the flour of the chute 52 is not integrated into the calcining device 37 but into the riser channel 49.
  • This has the advantage that this enables the pressure loss and thus the amount of gas in this riser to be influenced, and on the other hand the positive effect of cooling the flue gas after entering the oven by the flour with simultaneous preheating or beginning calcining. nation of flour is obtained.
  • This cooling of the gas leads to the condensation of volatile components contained in the gas, in particular alkali metal vapors, on the raw meal, as a result of which blockages of the riser pipe or clogging on its walls are avoided. Because of this positive effect, a combination of the methods of FIGS.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Ceramic Engineering (AREA)
  • Toxicology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Public Health (AREA)
  • Health & Medical Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Furnace Details (AREA)

Abstract

Selon le procédé, la formation et le dégagement de l'oxyde de soufre et/ou des composés organiques volatils ont lieu uniquement dans un courant de gaz partiel dans un dispositif de chauffage séparé et non pas lors du chauffage de la farine crue dans le courant de gaz total comme cela se fait normalement selon le procédé connu de mise en suspension dans les gaz. Les gaz de fumée quittant le dispositif de chauffage sont soumis à une épuration ultérieure et/ou ramenés au dispositif de chauffage à la température à laquelle a lieu une réaction et une fixation de l'oxyde de soufre et/ou des composés organiques ou de leurs produits de décomposition. Le dispositif pour la mise en oeuvre du procédé comprend un conduit ascendant (4) ou un lit fluidisé suivi d'un séparateur à cyclone (36).
EP19860906223 1986-02-11 1986-10-30 Procede et dispositif pour diminuer le degagement d'oxyde de soufre et/ou de composes organiques volatils formes pendant le chauffage de la farine crue dans le circuit de prechauffage, en particulier dans l'echangeur de chaleur du dispositif de prechauffage par mise en suspension dans les gaz dans l Withdrawn EP0256021A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AT34786A AT384177B (de) 1986-02-11 1986-02-11 Verfahren und vorrichtung zur verringerung der emission von waehrend der erhitzung des rohmehles im schwebegas-waermetauscher bei der zementherstellung gebildetem so2 und von fluechtigen organischen verbindungen
AT347/86 1986-02-11

Publications (1)

Publication Number Publication Date
EP0256021A1 true EP0256021A1 (fr) 1988-02-24

Family

ID=3488200

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19860906223 Withdrawn EP0256021A1 (fr) 1986-02-11 1986-10-30 Procede et dispositif pour diminuer le degagement d'oxyde de soufre et/ou de composes organiques volatils formes pendant le chauffage de la farine crue dans le circuit de prechauffage, en particulier dans l'echangeur de chaleur du dispositif de prechauffage par mise en suspension dans les gaz dans l

Country Status (3)

Country Link
EP (1) EP0256021A1 (fr)
AT (1) AT384177B (fr)
WO (1) WO1987004698A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015014472A1 (fr) * 2013-07-31 2015-02-05 Thyssenkrupp Industrial Solutions Ag Installation et procédé de traitement thermique d'un flux de matière

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19936375B4 (de) 1999-08-03 2008-01-17 Polysius Ag Verfahren zur Verringerung von flüchtigen Schadstoffen in den Abgasen eines Wärmetauschersytems
US7279039B2 (en) * 2004-12-30 2007-10-09 Envirocare International, Inc. Method and apparatus for controlling pollution from a cement plant
DE102017008532A1 (de) * 2017-10-07 2019-04-11 aixergee GmbH Vorrichtung und Verfahren zur Sinterung von Kalkstein zu Zementklinker

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3622363A (en) * 1969-05-26 1971-11-23 Edward M Van Dornick Reduction of alkali in cement production
CS166580B1 (fr) * 1973-10-29 1976-03-29
DE2356221C3 (de) * 1973-11-10 1984-05-17 Ishikawajima-Harima Jukogyo K.K., Tokio / Tokyo Anlage zur Vorerhitzung von pulverförmigem Rohmaterial zur Zementherstellung
FR2505813A1 (fr) * 1981-05-15 1982-11-19 Fives Cail Babcock Perfectionnements aux procedes et installations pour la fabrication du clinker de ciment par voie seche
US4440578A (en) * 1982-05-12 1984-04-03 Wadia Darius A Method and apparatus for processing raw meal having a high alkali chloride and/or sulfate content
DE3244241A1 (de) * 1982-11-30 1984-05-30 Krupp Polysius Ag, 4720 Beckum Verfahren zur herstellung von zement aus schwefelhaltigem rohmaterial
ATE13757T1 (de) * 1982-12-08 1985-06-15 Verein Deutscher Zementwerke E Verfahren und vorrichtung zur herstellung von zementklinker.
DE3320670A1 (de) * 1983-06-08 1984-12-13 Wolfram G. Dr.-Ing. 8183 Rottach-Egern Quittkat Verfahren und vorrichtung zur herstellung von bindemitteln unter verwendung heizwerthaltiger ausgangsstoffe
DE3333718A1 (de) * 1983-09-17 1985-04-04 Klöckner-Humboldt-Deutz AG, 5000 Köln Anlage zum brennen von feinkoernigem gut, insbesondere zu zementklinker
DE3341695A1 (de) * 1983-11-18 1985-05-30 Klöckner-Humboldt-Deutz AG, 5000 Köln Verfahren und anlage zum brennen von feinkoernigem gut, insbesondere zur herstellung von zementklinker aus zementrohmehl

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO8704698A1 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015014472A1 (fr) * 2013-07-31 2015-02-05 Thyssenkrupp Industrial Solutions Ag Installation et procédé de traitement thermique d'un flux de matière

Also Published As

Publication number Publication date
AT384177B (de) 1987-10-12
ATA34786A (de) 1987-03-15
WO1987004698A1 (fr) 1987-08-13

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