DK151376B - METHOD AND PLANT FOR MULTI-STEP CALCINATION OF FRAME, SPECIAL FOR CEMENT MANUFACTURING - Google Patents
METHOD AND PLANT FOR MULTI-STEP CALCINATION OF FRAME, SPECIAL FOR CEMENT MANUFACTURING Download PDFInfo
- Publication number
- DK151376B DK151376B DK200982A DK200982A DK151376B DK 151376 B DK151376 B DK 151376B DK 200982 A DK200982 A DK 200982A DK 200982 A DK200982 A DK 200982A DK 151376 B DK151376 B DK 151376B
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- Prior art keywords
- calcining
- raw flour
- raw
- separator
- calcined
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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
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/434—Preheating with addition of fuel, e.g. calcining
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Ceramic Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Furnace Details (AREA)
- Curing Cements, Concrete, And Artificial Stone (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
Description
i 151376in 151376
Opfindelsen angår en fremgangsmåde til kalcinering af råmel, især til cementfremstilling, hvor dele af råmelet efter en forvarmning under varmetilførsel kaleineres i mindst to · trin, før det brændes i en ovn.The invention relates to a process for calcining raw flour, in particular to cement production, where parts of the raw flour, after preheating during heat supply, are calcined in at least two steps before being burned in an oven.
5 For at man i vid udstrækning skal kunne dække varme behovet ved kalcineringen af råmel ud fra brændingsprocessens varmetilbud afsyres eller afcarboniseres råmelet på gængs måde i en kalcinator, som er sluttet til afgangsgasstrømmen fra brændeovnen eller til afgangsluftstrømmen fra en efter ov-10 nen indkoblet køler, hvilket nedsætter et yderligere brændstofbehov. Trods dette kræves der en større brændstofindsats end teoretisk udledelig, fordi man ved de kendte kalcinatorer næppe kan tage hensyn til reaktionstidens afhængighed af korn-størrelsen. Som undersøgelser har vist, synker den til kalcine-15 ringen nødvendige reaktionstid med tiltagende råmeltemperatur og med aftagende kornstørrelse« Der må derfor tilføres varmemængder svarende til den i råmelet forekommende groveste kornstørrelse til sikring af en fuldstændig afsyring eller afcarbonisering af også den groveste del af kornene. Den mere 20 finkornede del af råmelet behøver imidlertid ikke disse varmemængder, hvoraf forskellen mellem det teoretiske varmebehov og den faktisk nødvendige brændstofmængde opstår. Forbundet med den større brændstofmæng* er imidlertid også en højere afgangsgastemperatur og dermed en ringere termisk virknings-25 grad.5 In order to be able to cover to a large extent the need for the calcination of raw flour based on the heat supply of the burning process, the raw material is acidified or decarbonised in a conventional manner in a calciner connected to the exhaust gas flow from the stove or to the exhaust air flow from an after-oven heater. , which reduces an additional fuel demand. Despite this, a greater fuel effort is required than theoretically deducible, because the known calcinators can hardly take into account the reaction time dependence on the grain size. As studies have shown, the reaction time required for calcination decreases with increasing crude temperature and with decreasing grain size. Therefore, heat quantities corresponding to the coarsest grain size present in the raw flour must be added to ensure complete deacidification or decarbonisation of even the coarsest part of the grains. . However, the more fine-grained portion of the raw flour does not need these quantities of heat, from which the difference between the theoretical heat demand and the actual amount of fuel actually arises. However, associated with the greater amount of fuel * is also a higher exhaust gas temperature and thus a lower thermal efficiency.
Til bedre udnyttelse af det til kalcineringen nødvendige brændstof er det kendt fra tysk offentliggøfcelsesskrift nr, 27 24 654 at gennemføre kalcineringen af det forvarmede råmel i mindst 2 trin og at udskille råmelet af gasstrømmen 30 fra det forudgående kalcineringstrin, før det afleveres til det efterfølgende kalcineringstrin. Derved opnås ganske vist, at den i hvert kalcineringstrin tilførte, kun en del af det samlede brændstofbehov udgørende brændstofmængde blandes og forbrændes med råmelet, hvorved der fås en af varmeudveks-35 lingen ved råmelsbevægelsen under udskillelsesprocessen understøttet udligning af råmeltemperaturen, som i høj grad forhindrer en lokal overhedning af råmelet, men også ved denne kendte fremgangsmåde tilføres råmelets grovkorndel og finkorndel 151376 2 samme varmemængde ved samme reaktionstid, så at en forøget brændstofindsats er nødvendig.For better utilization of the fuel needed for the calcination, it is known from German Publication Publication No. 27 24 654 to perform the calcination of the preheated crude meal in at least 2 steps and to separate the crude of the gas stream 30 from the preceding calcining step before delivering it to the subsequent calcining step. . Thus, it is obtained that in each calcining step, only a portion of the total fuel demand constituting the amount of fuel is mixed and incinerated with the raw flour, thereby obtaining a heat exchange during the separation process during the separation process, which is supported by the high temperature temperature equalizer. a local superheat of the raw flour, but also by this known method, the coarse grain and fine grain portion of the raw flour are added to the same amount of heat at the same reaction time, so that an increased fuel insertion is necessary.
Til grund for opfindelsen ligger således den opgave at anvise en fremgangsmåde til kalcinering af råmel, ved 5 hvilken det til kalcinering af råmelet nødvendige yderlige re brændstofbehov i sammenligning med den teoretisk nødvendige varmemængde vælges i afhængighed af de forskellige andele af de forskellige kornstørrelser i råmelet.Thus, the object of the invention is to provide a method for calcining raw flour, in which the additional fuel needs necessary for calcining the raw material in comparison with the theoretically required amount of heat are selected depending on the different proportions of the different grain sizes in the raw flour.
10 Opfindelsen løser den stillede opgave ved, at frem gangsmåden gennemføres som angivet i krav 1's kendetegnende del.The invention solves the stated task by carrying out the procedure as set out in the characterizing part of claim 1.
Ved udskillelsen af den mere finkornede råmelandel efter hvert kalcineringstrin behøver man til hvert kalci-15 neringstrin kun at føre den varmemængde, som er nødvendig til, at den mere finkornede andel af råmelet afsyres eller afcarboniseres. Det til en kalcinering af de mere grovkornede råmelandele nødvendige yderligere brændstof tilføres i det efterfølgende kalcineringstrin, hvorfra den allerede 20 kalcinerede mere finkornede råmelandel udskilles og føres til ovnen. Den mere finkornede råmelandel opvarmes følgelig ikke unødvendigt sammen med grovkornandelen, så at der sikres en tilnærmelse af den faktisk nødvendige brændstof-mængde til den teoretisk nødvendige. Derved synker brænd-25 stofbehovet ved samme kalcineringsydelse. Desuden fås der en lavere afgangsgastemperatur og dermed en højere termisk virkningsgrad.In the separation of the finer-grained crude portion after each calcining step, for each calcining step only the amount of heat necessary to acidify or decarbonate the finer-grained portion of the crude flour is required. The additional fuel needed for calcining the more coarse-grained raw parts is added in the subsequent calcining step, from which the already calcined more fine-grained raw parts are separated and fed to the furnace. Consequently, the finer-grained raw material portion is not unnecessarily heated together with the coarse-grained portion, so as to ensure approximation of the actual quantity of fuel actually needed to the theoretically necessary. Thereby, the fuel demand decreases at the same calcining performance. In addition, a lower exhaust gas temperature is obtained and thus a higher thermal efficiency.
Opfindelsen angår endvidere et anlæg, som består af en kalcinator, en i afgangsgasstrømmen fra kalcinatoren 30 anbragt og med ovnen forbundet udskiller for det kalcine rede råmel og en med afgangsgasserne fra kalcinatoren eller ovnen opvarmet flertrins varmeveksler for råmelet, hvorhos kalcinatoren i det mindste har to gennem en råmel-udskiller med hinanden forbundne kalcineringsenheder, 35 hvilket anlæg er ejendommeligt ved, at råmeludskilleren mellem kalcineringsenhederne er udformet som grovkornudskiller, hvis udføringsledning er forbundet med den i henseende til råmelstrømmen efterkoblede kalcineringsenhed, 151376 3 og hvis afgangsgasledning er forbundet med en til ovnen sluttet finkornudskiller.The invention further relates to a plant consisting of a calciner, a separator for the calcined crude meal and a heat exchanger of the calcinedator or furnace heated in the exhaust gas stream from calciner 30 and at least two heat exchangers for which the calciner has at least two through a raw flour separator interconnected calcining units 35, which is characterized in that the raw separator between the calcining units is designed as coarse grain separator whose output conduit is connected to the recirculating unit coupled to the raw flour flow, and whose outlet gas conduit is connected connected fine grain separator.
Af grovkornudskilleren bliver det fra den første kaloineringsenhed kommende råmel i afhængighed af kornstør-5 reisen opdelt i to delstrømme, nemlig en finkomdel og en grovkorndel, idet der ved fin- og grovkorn skal forstås de finere og grovere kornstørrelser af de til enhver tid forekommende kornstørrelsefordelinger. Finkornandelen, som allerede er helt afsyret eller afcarboniseret· føres over grov-10 koraudskiIlerens gasudløbsledning til en finkornudskiller, hvor det finkornede råmel fra bæregasstrømmen udskilles og føres til ovnen til brænding. Over udføringsledningen i grovkornudskilleren afleveres det mere grovkornede råmel til en anden kalcineringsenhed til fuldstændiggørelse af kalcine-15 ringsprooessen. Alt efter kornstørrelsesfordelingen kan der benyttes to eller flere kalcineringsenheder med en mellemudskillelse af en delstrøm ved det allerede kalcinerede råmel.From the coarse grain separator, the feedstock coming from the first calibration unit, depending on the grain size, is divided into two partial streams, namely a fine grain and a coarse grain, with the finer and coarser grain sizes of the grain sizes present at all times being understood. . The fine grain portion, which has already been fully acidified or decarbonized, is passed over the coarse 10 gas discharge pipe of a coarse grain separator to a fine grain separator where the fine grained crude from the carrier gas stream is separated and fed to the furnace for firing. Over the execution line in the coarse grain separator, the more coarse-grained flour is delivered to another calcining unit to complete the calcination process. Depending on the grain size distribution, two or more calcining units may be used, with an intermediate separation of a partial flow at the already calcined raw flour.
Opfindelsen skal forklares nærmere i forbindelse med tegningen, hvor 20 fig, 1 viser et anlæg til fremstilling af cement med en indretning ifølge opfindelsen til kalcinering af råmelet i et skematisk diagram, og fig, 2 en konstruktionsvariant af en kalcineringsindretning ligeledes i diagram.The invention will be explained in more detail in connection with the drawing, in which Fig. 20 shows a plant for making cement with a device according to the invention for calcining the raw flour in a schematic diagram, and Fig. 2 shows a construction variant of a calcining device also in diagram.
25 Det i fig. 1 viste anlæg til fremstilling af cement består i hovedsagen af en flervrinsvarmeveksler for råmelet, som efter sin forvarmning trinvis i to kalcineringsenheder 1 og 2 i en kalcinator afsyres eller afcarboniseres, før det brændes til cementklinker i en roterovn 3. Varmeudveksleren 30 har da i to afgangsgasstrenge 4 og 5 sammenfattede og af cykloner bestående varmeudvekslerenheder 4a og 4b henholdsvis 5a, 5b og 5o, som hver beskikkes med en delstrøm 6a og 6b af råmelet, hvorhos de to råmelstrømme 6a og 6b. før deres indtræden i den i henseende til råmelstrømmen første kalcinerings-35 enhed 1 forenes' til en fælles råmels t røm 6. I kalcine ringsenheden 1, som er sluttet til roterovnens 3 afgangsledning 7 151376 4 og forsynes med yderligere varme over en brænder 8, afsyres eller afcarboniseres det forvarmede råmel i et første trin 1 en sådan udstrækning, at den finkornede bestanddel i råmelet kalcineres helt, men ikke den mere grovkornede del. Det 5 med afgangsgasstrømmen, der til forskel fra den med punktere de linier tegnede råmelbane er vist med fuldt optrukne linier, og som udtages fra kalcineringsenheden, deles i en grovkornudskiller 9 i to delstrømme 10a og 10b, idet den fra afgangs-gasstrømmen udskilte grovkornandel 10b føres til kaleinerings-10 enheden 2 til fuldstændiggørelse af afsyringen eller afcarbo-niseringen. Den allerede afsyrede eller afcarboniserede og med afgangsgasstrommen fra grovkornudskilleren 9 udførte mere finkornede del 10a af råmelet føres til en finkornudskiller 11, hvorfra denne råmelandel føres til brænding i ovnen 3· Af-15 gangs gas strømmen fra finkornudskilleren 11 benyttes til opr-varmning af varmevekslerstrengen 4.The embodiment of FIG. 1, cement production plants essentially consist of a multi-stage heat exchanger for the raw flour which, after its preheating, is acidified or decarbonated in two calcination units 1 and 2 in a calciner before burning it to cement clinker in a rotary kiln 3. The heat exchanger 30 then has two exhaust gas strings 4 and 5 are summarized and consisting of cyclones heat exchanger units 4a and 4b and 5a, 5b and 5o respectively, each of which is provided with a partial stream 6a and 6b of the raw flour, the two raw flour streams 6a and 6b respectively. prior to their entry into the first calcining unit 1 with respect to the raw flour stream, the stream 6 of a common raw material is combined in the calcining unit 1, which is connected to the discharge line 7 of the rotary kiln 3 and provided with additional heat over a burner 8, in a first step 1, the preheated raw flour is acidified or decarbonated to such an extent that the fine-grained component of the raw flour is completely calcined, but not the more coarse-grained portion. The exhaust gas flow 5, which is shown in full drawn lines unlike the punctured line runway, which is taken out of the calcining unit, is divided into a coarse grain separator 9 into two partial streams 10a and 10b, the coarse grain portion 10b separated from the waste gas stream. is fed to the calcining unit 2 to complete the deacidification or decarbonization. The already acidified or decarbonized and finely grained portion 10a of the crude grain produced with the exhaust gas stream from the coarse grain separator 9 is fed to a fine grain separator 11, from which this crude portion is fed to firing in the furnace 3. The off gas gas flow from the fine grain separator 11 is used to heat the heat exchanger 11. 4th
Til fuldstændig afsyring eller afcarbonisering af den mere grovkornede del 10b af råmelet forsynes kalcineringsenheden 2 med den varme afgangsluft fra en efter ovnen 3 indkob-20 let køler 12 over en afgangsluftledning 13 samt opvarmes yderligere ved hjælp af en brænder 8. Til den mere grovkornede råmelandel føres der altså i et andet trin den til en fuldstændig kalcinering nødvendige varmemængde, så at den mere finkornede råmelandel ikke behøver unødvendigt at blive op-25 varmet sammen med grovkornandelen« Det i kalcineringsenheden 2 afsyrede eller afcarboniserede råmel med en grovere kornandel bliver efter fraskillelsen fra afgangsgasstrømmen fra kalcineringsenheden 2 ved hjælp af en udskiller 14 ført til ovnen 3# Den i kalcineringsenheden 2 opvarmede afgangsgas- 30 strøm tjener på analog måde til opvarmning af varmeveksler strengen 5. Hvis der foreligger et større korostørrelseom-råde for råmelet, kan kalcineringen også gennemføres i mere end to trin, hvilket tillader en bedre tilpasning af brænd-stofmængderae til de pågældende kornstørrelseandele og der-35 med en yderligere brændstofbesparelse.To completely deactivate or decarbonize the more coarse-grained portion 10b of the raw flour, the calcining unit 2 is supplied with the hot exhaust air from a cooler 12 coupled to the furnace 3 over a discharge air line 13 and further heated by a burner 8. For the more coarse-grained raw material portion thus, in a second step, the amount of heat needed for a complete calcination is introduced so that the finer-grained raw material does not need to be heated unnecessarily with the coarse-grain portion «The acidified or decarbonized raw-material with a coarser grain-portion becomes after the separation from the exhaust gas stream from the calcining unit 2 by means of a separator 14 fed to the furnace 3 # The exhaust gas stream heated in the calciner unit 2 serves in an analogous manner to heat the heat exchanger string 5. If a larger chorus size range is available for the raw flour, the calcination can also be carried out. in more than two steps, allowing a better fit addition of fuel volumes to the respective grain size portions and therefor with an additional fuel saving.
På grund af den målrettede og tf'l råmelets komstør-relseandele afstemte varmetilførsel til kalcineringsenhedeme 151376 5 1 og 2 fås også lavere afgangsgastemperaturer, hvilket er gunstigt for den termiske virkningsgrad. Desuden kan varmevekslerstrengenes 4 og 5 afgangsgasblæsere 15 konstrueres til lavere temperaturer, 5 Til forskel fra udførelseseksemplet ifølge fig. l bliver ifølge indretningen i fig. 2 den i køleren 12 opvarmede afgangsluft over ledningerne 15a og 13b ført til begge kalcineringsenheder 1 og 2, medens ovnens 3 afgangsgasledning 7 udmunder i den nederste varmevekslerenhed 16 i en ikke nær-10 mere vist flertrinsvarmeveksler, hvori også afgangsgasstrømmene fra kalcineringsenhedeme 1 og 2 finder anvendelse til forvarmning af råmelet. Da det i sig selv til den trinvise kalcinering i afhængighed af kornstørrelsen er af underordnet betydning, hvorledes varmeveksleren er opbygget, har man i 15 fig, 2 set bort fra den nærmere gengivelse af varmeveksleren.Because of the targeted and by volume of the raw flour's portion sizes, the adjusted heat supply to the calcining units 15 and 76 also results in lower exhaust gas temperatures, which is favorable for the thermal efficiency. In addition, the exhaust gas blowers 15 and 5 of the heat exchanger strings can be designed for lower temperatures. 5 Unlike the embodiment of FIG. 1 according to the device of FIG. 2, the exhaust air heated in the cooler 12 over the lines 15a and 13b leads to both calcining units 1 and 2, while the exhaust gas line 7 of the furnace 3 opens into the lower heat exchanger unit 16 in an unexplained multistage heat exchanger, in which also the exhaust gas streams from the calcining units 1 and use for preheating the raw flour. As the step-by-step calcination, depending on the grain size, is of minor importance in how the heat exchanger is constructed, the detailed description of the heat exchanger has been disregarded in Fig. 2.
På grund af føringen af ovnafgangsgas s eme umiddelbart ind i den nederste varmevekslerenhed 16 er det muligt, at afkøle ovnafgangsgassen under kalcinatorens 1 afgangsgas-temperatur. I sammenhæng med en i forhold til fig, 1 lavere 20 afgangsgasmængde fra kalcineringsenheden 1 kan der således opnås en lavere afgangsgassluttemperatur og dermed en bedre varmeudnyttelse. Afgangsgas- og råmaterialetilførslen mellem den nederste varmevekslerenhed 16 og ovnen 3 forbliver i sig selv den samme. Udføringsledningen 17 fra åen efter kalcine-25 ringsenheden 1 indkoblede grovkornudskiller 9 er atter forbundet med kalcineringsenheden 2, medens gasudtrædelsesledningen 18 står i forbindelse med finkornudskilleren 11. Råmel-strømmen fra kalcineringsenheden 1 deles følgelig ved hjælp af grovkornudskilleren 9 i to delstrømme 10a og 10b, af hvil-30 ke den mere finkornede delstrøm føres til ovnen 3» medens den mere grovkornede delstrøm 10b føres til kalcineringsenheden 2. Som udskillere kan man benytte cyklonudskiliere. På grund af det ringe tryktab kan man imidlertid også benytte beroligelseskamre eller omstyringsudskillere til opdeling af 35 råmelstrømmen.Due to the flow of furnace exhaust gas directly into the lower heat exchanger unit 16, it is possible to cool the furnace exhaust gas below the exhaust gas temperature of the calciner 1. Thus, in connection with a lower exhaust gas quantity from the calcining unit 1 in relation to Fig. 1, a lower exhaust gas end temperature can be achieved and thus better heat utilization. The exhaust gas and feedstock supply between the lower heat exchanger unit 16 and the furnace 3 remains the same in itself. The output line 17 from the stream after the calcining unit 1 connected coarse grain separator 9 is again connected to the calcining unit 2, while the gas exit line 18 is connected to the fine grain separator 11. The raw flour flow from the calcining unit 1 is divided by coarse grain separator 10 and two grain separator 10 and two. of which 30 the more fine-grained partial stream is fed to the furnace 3, while the more coarse-grained partial stream 10b is fed to the calcining unit 2. Cyclone separators can be used as separators. However, due to the small pressure loss, soothing chambers or diverting separators can also be used to divide the feedstock flow.
Claims (2)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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AT199781 | 1981-05-06 | ||
AT199781A AT369720B (en) | 1981-05-06 | 1981-05-06 | METHOD AND DEVICE FOR CALCINATING RAW FLOUR, ESPECIALLY FOR THE PRODUCTION OF CEMENT |
Publications (3)
Publication Number | Publication Date |
---|---|
DK200982A DK200982A (en) | 1982-11-07 |
DK151376B true DK151376B (en) | 1987-11-30 |
DK151376C DK151376C (en) | 1988-07-18 |
Family
ID=3525598
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
DK200982A DK151376C (en) | 1981-05-06 | 1982-05-05 | METHOD AND PLANT FOR MULTI-STEP CALCINATION OF FRAME, SPECIAL FOR CEMENT MANUFACTURING |
Country Status (10)
Country | Link |
---|---|
EP (1) | EP0064489B1 (en) |
AT (1) | AT369720B (en) |
CS (1) | CS250215B2 (en) |
DD (1) | DD201669A5 (en) |
DE (1) | DE3260345D1 (en) |
DK (1) | DK151376C (en) |
ES (1) | ES511784A0 (en) |
PL (1) | PL130594B1 (en) |
RO (1) | RO82959B (en) |
YU (2) | YU43639B (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT381694B (en) * | 1985-01-11 | 1986-11-10 | Voest Alpine Ag | METHOD AND DEVICE FOR THERMALLY TREATING FINE-GRAINED GOODS, IN PARTICULAR FOR BURNING CEMENT FLOUR |
AT405513B (en) * | 1998-02-12 | 1999-09-27 | Oemag Montananlagenbau Gmbh | METHOD AND SYSTEM FOR BURNING POWDERED RAW MATERIAL |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2724654C2 (en) * | 1977-06-01 | 1984-01-26 | Klöckner-Humboldt-Deutz AG, 5000 Köln | Method and device for burning fine-grained to powdery material, in particular raw cement meal |
-
1981
- 1981-05-06 AT AT199781A patent/AT369720B/en not_active IP Right Cessation
-
1982
- 1982-02-23 DE DE8282890027T patent/DE3260345D1/en not_active Expired
- 1982-02-23 EP EP82890027A patent/EP0064489B1/en not_active Expired
- 1982-03-17 YU YU58682A patent/YU43639B/en unknown
- 1982-03-19 DD DD23830382A patent/DD201669A5/en not_active IP Right Cessation
- 1982-04-02 RO RO107143A patent/RO82959B/en unknown
- 1982-04-16 CS CS274882A patent/CS250215B2/en unknown
- 1982-04-28 ES ES511784A patent/ES511784A0/en active Granted
- 1982-05-04 PL PL23628282A patent/PL130594B1/en unknown
- 1982-05-05 DK DK200982A patent/DK151376C/en not_active IP Right Cessation
-
1984
- 1984-08-28 YU YU146984A patent/YU146984A/en unknown
Also Published As
Publication number | Publication date |
---|---|
YU43639B (en) | 1989-10-31 |
RO82959B (en) | 1984-01-30 |
EP0064489B1 (en) | 1984-07-11 |
ES8305219A1 (en) | 1983-04-01 |
RO82959A (en) | 1984-01-14 |
YU146984A (en) | 1988-04-30 |
ATA199781A (en) | 1982-06-15 |
DD201669A5 (en) | 1983-08-03 |
AT369720B (en) | 1983-01-25 |
DK200982A (en) | 1982-11-07 |
PL130594B1 (en) | 1984-08-31 |
DK151376C (en) | 1988-07-18 |
CS250215B2 (en) | 1987-04-16 |
YU58682A (en) | 1984-12-31 |
EP0064489A1 (en) | 1982-11-10 |
PL236282A1 (en) | 1983-01-03 |
DE3260345D1 (en) | 1984-08-16 |
ES511784A0 (en) | 1983-04-01 |
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