EP0937957B1 - Verfahren und Anlage zum Brennen von pulverförmigen Rohmaterial - Google Patents
Verfahren und Anlage zum Brennen von pulverförmigen Rohmaterial Download PDFInfo
- Publication number
- EP0937957B1 EP0937957B1 EP99890051A EP99890051A EP0937957B1 EP 0937957 B1 EP0937957 B1 EP 0937957B1 EP 99890051 A EP99890051 A EP 99890051A EP 99890051 A EP99890051 A EP 99890051A EP 0937957 B1 EP0937957 B1 EP 0937957B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- calciner
- furnace
- branch
- partial stream
- fuel
- 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.)
- Revoked
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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 peculiar to 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
- F27B7/2058—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 each string
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges
Definitions
- the invention relates to a method for burning powdered raw material in a plant with a parallel working, multi-stage cyclone preheater with one Kiln line and a calciner line having a calciner, an oven and a cooling unit for cooling the burned material by means of air, of which a partial flow as secondary air through the furnace and further into the furnace line flows and a partial flow other than tertiary air Calciner of the calciner strand is fed and on flows into the calciner train, whereby abandoned raw material preheated in the kiln and calciner line, then calcined and finally sintered in the furnace.
- the invention also relates to an installation for carrying out the method.
- AT 346 753 B is known from the prior art known a method and an installation of the aforementioned Kind of revealed.
- the object of the invention disclosed herein consists primarily in the creation of an improved one Process for reducing impurity concentrations in the cyclones and risers and consequently in reducing the risk of constipation.
- This known method is the raw material to be treated inserted at the top of the preheater strands, then calcined in the calciner and finally in the Furnace introduced for sintering, taking at least part of the material flow originating from the calciner train lower cyclone of the kiln line before being introduced into the Calciner is fed.
- a process for burning powdered raw materials should also ensure low heat consumption and, with regard to the lowest possible environmental impact, low pollutant emissions and, in particular, low nitrogen oxide (NO x ) emissions.
- these requirements are in no way satisfactorily met in the case of the method and system known from the prior art.
- the object of the invention is now to create a method of the type mentioned, its implementation with a low heat consumption is possible and the low Pollutant emissions and especially low nitrogen oxide emissions occur.
- the method according to the invention is used to achieve this object characterized in that the directly through the Partial flow conducted to the furnace into a furnace stream assigned to the at least from the material flow of the calciner strand fed calciner, in the lower, Fuel area facing the entry of the partial flow is fed and in the upper part above the Another fuel supply derived from the cooler unit Partial stream is introduced as tertiary air, and that in the loaded with the total material flow Calciner of the calciner train above the junction of the tertiary air partial flow of fuel in two at a distance superimposed levels is fed.
- the advantage of this method is, on the one hand, a low heat consumption, which means a low use of fuel, so that low pollutant emissions occur as a result. Furthermore, the nitrogen oxides (NO x ) thermally generated during combustion in the furnace and the subsequent calciner in the furnace train are reduced by creating sections with a reducing atmosphere. Subsequent addition of preheated combustion air from the cooling unit ensures that complete combustion can still take place. By introducing fuel into the calciner of the calciner train in two levels one above the other, the temperature peaks occurring in the calciner are reduced by a staged combustion, which leads to the avoidance of pollutant formation.
- NO x nitrogen oxides
- the invention also relates to a plant for implementation of the aforementioned method with a working in parallel, multi-stage cyclone preheater with one kiln line and one Calciner strand, a furnace and a cooling unit with a line for dividing the exhaust air the cooler unit and for forwarding a partial flow in the furnace and another partial flow in the calciner train.
- the system is characterized according to the invention in that that at the bottom of the kiln line Calciner is arranged, in the lower part of a supply line for the partial flow passed through the furnace flows into and in the mouth of the supply line facing area a burner in a above the confluence the supply line is provided, that a supply line for a further tertiary air partial flow from the cooler unit to the calciner of the kiln line is provided in the upper part of the calciner opens above the burner and that the calciner of the Calciner line above the confluence of the tertiary air partial flow line in two spaced one above the other Levels is equipped with at least one burner each.
- FIG. 1 is a schematic view of a first Embodiment of an inventive designed and working Appendix
- Fig. 2 is a schematic view of a second embodiment of a designed according to the invention and working system show.
- a system which consists of a working in parallel multi-stage cyclone preheater, each from a calciner Ca1; Ca2 in each line, an oven K and a cooler unit C stands.
- the kiln line is made up of process gases from the Furnace K and the calciner Ca2 come flowing through while the calciner train from the process gases coming out of the calciner Ca1 come, is flowed through.
- the calciner Ca1 des The main deacidification takes place in the calciner line.
- the powdered raw material is 40% to 100% in the top level K1 at Ik of the kiln line and at 0% to 60 % in the top level C1 at Ic of the calciner train given up.
- this top stage K1 of the kiln line takes place the heat exchange of the cold powdered raw material with the hotter process gases from the one below Stage K2 of the kiln line takes place.
- the temperature of the powdery raw material is increased, that of the process gas thereby diminished.
- K is the powdery raw material burned ready.
- the cooling air that heats up is called combustion air for the kiln burner on the kiln head KH, for the calciner burner in the calciner Ca1 of the calciner train and used in the calciner Ca2 of the kiln line.
- the process gases are conducted in parallel lines.
- the through kiln K, calciner Ca2 of the kiln line and cyclone preheater stages K4 to K1 of the kiln stream flowing Gases are generated by a fan Fk and by the calciner Ca1 of the calciner train and cyclone preheater stages C4 to C1 of the gases flowing from the calciner train Fan Fc deducted.
- the division of fuel at the burners are made so that part of the total fuel (30% to 70%) in the calciner Ca1 of the calciner train and part of the total fuel (30% to 70 %) in kiln K and in calciner Ca2 of the kiln line becomes.
- the fuel feed into the calciner Ca1 of the calciner train can be in this range between 30% and 70 % are freely chosen and is therefore relatively independent of the fuel feed in the kiln line. There is a dependency So only in that the total fuel supply always Makes 100%. That means that in the oven always that Residual combustion quantity must be burned to 100%. Also the fuel feed in the calciner Ca2 of the kiln line can be independent of the fuel in the rest Burners can be chosen relatively freely, but should be in the range up to approx. 15% of the total fuel supply.
- the preheated combustion air for the burners from the furnace K from the calciner Ca2 of the kiln line and from the calciner Ca1 of the calciner line is removed from the cooler C. Part of the total combustion air is fed as secondary air into the furnace K and part of the total combustion air as tertiary air in lines TL k and TL c to the calcinators Ca1 and Ca2 in the ratio of the fuel feed.
- the tertiary air is regulated by means of a slide S1 in the feed line TL k to the calciner Ca2 of the kiln line in such a way that the division takes place in accordance with the ratio of the fuel feed.
- the combustion takes place in at least two combustion levels, at least one burner being arranged in one combustion level.
- At the lowest combustion level B1a approx. 2/6 of the total fuel is given up.
- At this level 100% of the powdered raw material is brought. This prevents high temperature peaks in the calciner Ca1. This in turn reduces the NO x formation in the combustion chamber.
- the remaining fuel of approx. 1/6, based on the total amount of fuel, is now introduced in the higher, second combustion level.
- the second combustion level B1b which is provided at a distance above the lower combustion level B1a, is arranged in the region of the calciner Ca1 in such a way that the fuel can still burn entirely in the calciner Ca1 and the residence time for the pulverulent raw material is sufficiently long. Otherwise the gas temperature after the calciner Ca1 would rise undesirably. This in turn would lead to a higher total heat consumption, which must be avoided.
- Approx. 1/6 of the Total fuel burned fulfilled several tasks.
- the furnace K is reduced by a Fuel feed of approx. 2/6, based on the total amount of fuel, exposed to less thermal stress.
- the combustion air for the Ca2 calciner Oven strand is not led through the oven K, but instead removed from cooler C via its own supply line. Thereby result from lower gas velocities in the furnace K also lower dust cycles.
- Another task of the calciner Ca2 of the kiln line is to reduce the NO x generated by combustion in kiln K. Since the combustion air of the calciner Ca2 of the kiln line is not passed through kiln K, the combustion in kiln K can take place with a lower excess of air. Lower air excess during combustion means lower thermal NO x formation in the combustion chamber.
- the fuel is introduced into the calciner Ca2 of the kiln line in the lower part, so that a section with a reducing atmosphere is formed. In this reducing atmosphere, the NO x generated in the furnace is now reduced.
- the preheated tertiary air is supplied as combustion air so that the unburned fuel can burn completely.
- the combustion air for the combustion of the fuels in the calciners is taken from the cooler C as tertiary air via the furnace head KH or directly via the cooler wall and fed to the calciners Ca1 and Ca2 through the tertiary air lines TL k and TL c .
- the powdery Raw material is related to both strands split the fuel task. After the heat exchange the powdered raw material in the respective cyclone separator these stages C1, K1 separated from the process gases and led to the levels C2, K2 below. There the process is repeated. The material flow changes not the strand. Only after the second to last cyclone stage C3 of the calciner train changes the material flow of the Calciner strand the strand and is together with the powdered raw material from the penultimate stage K3 of the Furnace strand placed in the calciner Ca2.
- the calciner Ca2 pre-deacidifies the powder Raw material instead, which is then in the subsequent calciner Ca1 of the calciner strand is almost completely deacidified becomes.
- the cyclone separator of the lowest level C4 of the The calciner strand then becomes the powdered raw material separated from the gas stream and placed in the furnace K.
- the powdered raw material is burned.
- the downstream cooler C becomes the hot one that arises Cement clinker cooled by the air, which heats up Cooling air is used as combustion air for the furnace burner on the kiln head KH, for the calciner burners in the calciner Ca1 of the calciner strand and in the calciner Ca2 des Oven strand used.
- the management of the process gases, Fuel feed, combustion and combustion air supply takes place as described above with reference to FIG. 1.
- the combustion air supply to the burners B1a, B1b of the calciner Ca1 of the calciner line is regulated via the blower Fc of the calciner line, depending on the gas analysis (CO, O 2 ) of the process gases of the calciner line.
- the monitoring of O 2 , CO in the process gases takes place via gas samples and analysis by means of an analysis measuring device A3 after the cyclone stage C4 of the calciner train.
- the combustion air supply to the furnace burner B3 and the burner B2 in the calciner Ca2 of the furnace branch is regulated via the fan Fk of the furnace branch, depending on the gas analysis (CO, O 2 ) of the process gases of the furnace branch.
- the monitoring of O 2 , CO in the process gases takes place via gas samples and analysis by means of an analysis measuring device A2 after the cyclone stage K4 of the kiln line.
- the distribution of the combustion air supply between the furnace burner B3 and the burner B2 in the calciner Ca2 in the kiln line takes place via the slide S1 in the tertiary air line TL k to the calciner Ca2 of the kiln line.
- a gas analysis measurement by means of an analysis measuring device A1 arranged in front of the calciner Ca2 of the kiln line in the line of the flue gases coming from the kiln monitors the O 2 , CO values of the process gases from the kiln K. to reduce the formation of NO x from the outset.
- complete combustion in furnace K is sought.
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Furnace Details (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Claims (11)
- Verfahren zum Brennen von pulverförmigem Rohmaterial in einer Anlage mit einem parallel arbeitenden, mehrstufigen Zyklonvorwärmer mit einem Ofenstrang und einem einen Kalzinator aufweisenden Kalzinatorstrang, einem Ofen (K) und einer Kühlereinheit (C) zum Kühlen des gebrannten Materials mittels Luft, von der ein Teilstrom als Sekundärluft durch den Ofen (K) und weiter in den Ofenstrang strömt und ein anderer Teilstrom als Tertiärluft dem Kalzinator (Ca1) des Kalzinatorstrangs zugeführt wird und weiter in den Kalzinatorstrang strömt, wobei aufgegebenes Rohmaterial im Ofen- und Kalzinatorstrangs vorerwärmt, danach kalziniert und schließlich im Ofen (K) gesintert wird dadurch gekennzeichnet, dass der direkt durch den Ofen (K) geleitete Teilstrom in einen dem Ofenstrang zugeordneten, wenigstens vom Materialstrom des Kalzinatorstranges beschickten Kalzinator (Ca2) geleitet wird, in dessen unterem, dem Eintritt des Teilstroms zugekehrten Bereich Brennstoff zugeführt wird und in dessen oberen Teil oberhalb der Brennstoffzuführung ein weiterer, von der Kühlereinheit abgeleiteter Teilstrom als Tertiärluft eingeführt wird, und dass in den mit dem Gesamtmaterialstrom beschickten Kalzinator (Ca1) des Kalzinatorstrangs oberhalb der Einmündung des Tertiärluft-Teilstromes Brennstoff in zwei im Abstand übereinander liegenden Ebenen zugeführt wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass pulverförmiges Rohmaterial zu 40 % bis 100% in die oberste Stufe des Ofenstrangs und zu 0 % bis 60 % in die oberste Stufe des Kalzinatorstrangs aufgegeben wird.
- Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass die Brennstoffaufteilung im Ofenstrang und Kalzinatorstrang im Bereich von 30 % bis 70 % erfolgt.
- Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die Brennstoffaufgabe im Kalzinator des Kalzinatorstrangs zwischen 30 % und 70 % bezogen auf 100 % Gesamtbrennstoffaufgabe und die Brennstoffaufgabe im Kalzinator des Ofenstrangs bis etwa 15 % der Gesamtbrennstoffaufgabe liegt.
- Verfahren nach einem der Ansprüche 1 bis 4, dadurch gekennzeichnet, dass im Ofen ca. 2/6 und im Kalzinator des Ofenstrangs ca. 1/6 und im Kalzinator des Kalzinatorstrangs auf der unteren Verbrennungsebene ca. 2/6 und auf der oberen Verbrennungsebene ca. 1/6 des Gesamtbrennstoffs verbrannt werden.
- Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass die Verbrennungsluftzufuhr in den Ofen und in den Kalzinator des Ofenstranges sowie in den Kalzinator des Kalzinatorstranges mittels Regelung von jeweils dem Ofen- und Kalzinatorstrang zugeordnetem Gebläse in Abhängigkeit von einer Gasanalysenmessung der Prozessgase im Ofen- und Kalzinatorstrang gesteuert wird.
- Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, dass eine Aufteilung der Verbrennungsluftzufuhr zwischen Ofen und Kalzinator des Ofenstranges mittels Regelung der Teriärluftzuführung zum Kalzinator des Ofenstranges in Abhängigkeit von einer Gasanalysenmessung der aus dem Ofen austretentenden Prozessgase gesteuert wird.
- Anlage zur Durführung des Verfahrens nach einem der vorhergehenden Ansprüche mit einem parallel arbeitenden, mehrstufigen Zyklonvorwärmer mit einem Ofenstrang und einem einen Kalzinator aufweisenden Kalzinatorstrang, einem Ofen (K) und einer Kühlereinheit (C) mit einer Leitung zur Aufteilung der Abluft der Kühlereinheit und zur Weiterleitung eines Teilstroms in den Ofen (K) und eines anderen Teilstroms in den Kalzinatorstrang, dadurch gekennzeichnet, dass am unteren Ende des Ofenstrangs ein Kalzinator (Ca2) angeordnet ist, in dessen unteren Teil eine Zufuhrleitung für den durch den Ofen (K) geleiteten Teilstrom einmündet und in dessen der Einmündung der Zufuhrleitung zugekehrten Bereich ein Brenner (B2) in einer oberhalb der Einmündung der Zufuhrleitung liegenden Ebene vorgesehen ist, dass eine Zuleitung TLk für einen weiteren Tertiärluft-Teilstrom von der Kühlereinheit (C) zum Kalzinator (Ca2) des Ofenstrangs vorgesehen ist, die in den oberen Teil des Kalzinators (Ca2) oberhalb des Brenners (B2) einmündet und dass der Kalzinator (Ca1) des Kalzinatorstranges oberhalb der Einmündung der Tertiärluft-Teilstromleitung (TLc) in zwei im Abstand übereinanderliegenden Ebenen mit mindestens je einem Brenner (B1a, B1b) ausgestattet ist.
- Anlage nach Anspruch 8, dadurch gekennzeichnet, dass in der Zuleitung (TLk) des Tertiärluft-Teilstroms von der Kühlereinheit (C) zum Kalzinator (Ca2) des Ofenstrangs ein Regelorgan (S1), vorzugsweise ein Schieber angeordnet ist.
- Anlage nach Anspruch 8 und 9, dadurch gekennzeichnet, dass das Regelorgan (S1) zu seiner Steuerung mit einem in der Verbindungsleitung zwischen Ofen (K) und Kalzinator (Ca2) des Ofenstrangs angeordneten Analysenmessgerät (A1) für die Prozessgase in Wirkverbindung steht.
- Anlage nach Anspruch 8, dadurch gekennzeichnet, dass im Ofen- und Kalzinatorstrang jeweils vorzugsweise nach der untersten Zyklonstufe (K4; C4) ein Analysenmessgerät ((A2; A3) für die Prozessgase angeordnet ist, das zur Steuerung eines jeweils dem Ofen- und Kalzinatorstrang zugeordneten Gebläses (Fk; Fc) in Wirkverbindung steht.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE29924941U DE29924941U1 (de) | 1998-02-12 | 1999-02-10 | Anlage zum Brennen von pulverförmigem Rohmaterial |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AT0025498A AT405513B (de) | 1998-02-12 | 1998-02-12 | Verfahren und anlage zum brennen von pulverförmigem rohmaterial |
AT25498 | 1998-02-12 |
Publications (3)
Publication Number | Publication Date |
---|---|
EP0937957A2 EP0937957A2 (de) | 1999-08-25 |
EP0937957A3 EP0937957A3 (de) | 2001-08-22 |
EP0937957B1 true EP0937957B1 (de) | 2004-10-13 |
Family
ID=3485656
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99890051A Revoked EP0937957B1 (de) | 1998-02-12 | 1999-02-10 | Verfahren und Anlage zum Brennen von pulverförmigen Rohmaterial |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0937957B1 (de) |
AT (2) | AT405513B (de) |
DE (1) | DE59910786D1 (de) |
DK (1) | DK0937957T3 (de) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10317307B4 (de) * | 2003-04-14 | 2007-11-15 | Rheinkalk Gmbh | Vorrichtung sowie Verfahren zum Brennen von Kalkstein oder Dolomit |
DE102011052963B4 (de) | 2011-08-24 | 2016-05-19 | Ikn Gmbh | Klinkerofenanlage mit Schieber für Tertiärluftleitung |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2603594A1 (de) * | 1976-01-30 | 1977-08-04 | Smidth & Co As F L | Verfahren und anlage zum brennen von granulat- oder pulverfoermigem rohmaterial |
AT369720B (de) * | 1981-05-06 | 1983-01-25 | Voest Alpine Ag | Verfahren und vorrichtung zum kalzinieren von rohmehl, insbesondere fuer die zementherstellung |
DE3244943A1 (de) * | 1982-12-04 | 1984-06-07 | Klöckner-Humboldt-Deutz AG, 5000 Köln | Verfahren und anlage zum brennen von zementklinker |
-
1998
- 1998-02-12 AT AT0025498A patent/AT405513B/de not_active IP Right Cessation
-
1999
- 1999-02-10 DE DE1999510786 patent/DE59910786D1/de not_active Expired - Lifetime
- 1999-02-10 DK DK99890051T patent/DK0937957T3/da active
- 1999-02-10 EP EP99890051A patent/EP0937957B1/de not_active Revoked
- 1999-02-10 AT AT99890051T patent/ATE279703T1/de not_active IP Right Cessation
Also Published As
Publication number | Publication date |
---|---|
ATA25498A (de) | 1999-01-15 |
DK0937957T3 (da) | 2005-01-24 |
EP0937957A2 (de) | 1999-08-25 |
DE59910786D1 (de) | 2004-11-18 |
EP0937957A3 (de) | 2001-08-22 |
ATE279703T1 (de) | 2004-10-15 |
AT405513B (de) | 1999-09-27 |
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