EP0000739B1 - Procédé et appareillage pour la préparation de ciment dans un lit fluidisé. - Google Patents

Procédé et appareillage pour la préparation de ciment dans un lit fluidisé. Download PDF

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Publication number
EP0000739B1
EP0000739B1 EP78100518A EP78100518A EP0000739B1 EP 0000739 B1 EP0000739 B1 EP 0000739B1 EP 78100518 A EP78100518 A EP 78100518A EP 78100518 A EP78100518 A EP 78100518A EP 0000739 B1 EP0000739 B1 EP 0000739B1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
zone
air flow
fuel
precalcined
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.)
Expired
Application number
EP78100518A
Other languages
German (de)
English (en)
Other versions
EP0000739A1 (fr
Inventor
Klaus Bauer
Wolf Goldmann
Horst Kretzer
Heinrich Weber
Rüdiger Beyer
Wilfried Kreft
Frank Dr. Schaberg
Rudolf Weber
Herbert Schmelter
Horst Dr. Ritzmann
Erich Schnieder
Georg Schepers
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Krupp Polysius AG
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE19772735084 external-priority patent/DE2735084A1/de
Priority claimed from DE19772735140 external-priority patent/DE2735140A1/de
Priority claimed from DE19782822419 external-priority patent/DE2822419A1/de
Priority claimed from DE19782822395 external-priority patent/DE2822395A1/de
Priority claimed from DE19782822377 external-priority patent/DE2822377A1/de
Application filed by Krupp Polysius AG filed Critical Krupp Polysius AG
Publication of EP0000739A1 publication Critical patent/EP0000739A1/fr
Application granted granted Critical
Publication of EP0000739B1 publication Critical patent/EP0000739B1/fr
Expired legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • 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
    • C04B7/44—Burning; Melting
    • C04B7/45—Burning; Melting in fluidised beds, e.g. spouted beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00026—Controlling or regulating the heat exchange system
    • B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2208/00044—Temperature measurement
    • B01J2208/00061—Temperature measurement of the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B60—VEHICLES IN GENERAL
    • B60Y—INDEXING SCHEME RELATING TO ASPECTS CROSS-CUTTING VEHICLE TECHNOLOGY
    • B60Y2200/00—Type of vehicle
    • B60Y2200/10—Road Vehicles
    • B60Y2200/14—Trucks; Load vehicles, Busses
    • B60Y2200/143—Busses

Definitions

  • the invention relates to a method for producing cement by firing powdered raw material in a fluidized bed, into which preheated raw material, fuel, preheated air and a recycled part of the fired material are introduced, the material discharged from the fluidized bed subsequently being passed through a cooling zone by a Cooling air flow is cooled, and a device for performing the method.
  • a process for the production of cement is known (CH-A 292 727), in which the drying, preheating and deacidification of the raw material takes place in fluidized beds of a shaft-shaped reactor arranged one above the other, while the final firing of the material (ie the clinker formation) takes place in a funnel shape downward tapering reaction space occurs, to which fuel is fed in the lower region and the material to be burned in the upper region, a cooling zone adjoining the lower outlet end of this reaction chamber.
  • the heat treatment of the material in the drying, preheating and deacidification stage is carried out by the hot exhaust gases from the finished combustion zone and possibly by additional fuel.
  • a disadvantage of this method is above all the difficulty in precisely controlling the time the goods are in the finished firing zone and ensuring uniform heat treatment of all good particles in the finished firing zone.
  • cement-lime gypsum 1970, pp. 343 to 347, FR-A 1 192 838 and DE-B 1 433 913.
  • the disadvantages here are the effort involved in granulating the raw material and the inadequate uniformity of the heat treatment of the inner and outer material zones of the granules.
  • the fired clinker is either drawn off from the fluidized bed by an overflow or a central outlet (see DE-B 1 156 012 or CH-A 381 590) or discharged together with the gases upward from the fluidized bed reactor (see. NL-A 69 08 171).
  • the problem with the known process is still the strong alkali vaporization when burning in the fluidized bed.
  • This results in an extraordinarily high alkali content in the exhaust gases of the fluidized bed in the case of strongly alkaline raw materials, which in many cases excludes the use of these exhaust gases for preheating the raw material and thus leads to an undesirably high heat requirement.
  • the invention is therefore based on the object of avoiding these deficiencies to provide a method for firing powdered cement raw material in a fluidized bed, which is characterized by a particularly stable operation of the fluidized bed, a very evenly fired end product and a comparatively low heat consumption, and also the production permitted by cement clinker with a particularly low alkali content.
  • the fluidized bed is relieved of a large part of the heat work that would otherwise have to be done, which has substantial advantages:
  • the fluidized bed can be dimensioned smaller, requires less fuel and delivers a smaller amount of exhaust gas.
  • the substantial reduction in the amount of exhaust gas from the fluidized bed makes it possible, in the case of a particularly high alkali content of the raw material, to dispense with the use of these exhaust gases for preheating and precalcination of the raw material, in whole or in part, without significantly increasing the heat requirement.
  • the rapid and even distribution of the pre-calcined material in the fluidized bed is further promoted by the fact that the pre-calcined material is introduced into the fluidized bed from the side by part of the cooling air flow, preferably with a pulse between 49 and 98 Ns.
  • this measure achieves a very good distribution of the pre-calcined material in the fluidized bed even when the material insertion point is very deep, i.e. is just above the cooling zone.
  • the significantly improved combustion conditions in the fluidized bed due to the strong precalcination and the rapid, even distribution of pre-calcined material and fuel in the fluidized bed also ensure that the cooling zone immediately below the fluidized bed functions properly and, in particular, prevents operational disruptions due to caking of the material in the cooling zone.
  • the method according to the invention thus delivers very homogeneously fired clinker beads of approximately uniform grain size.
  • the quantity of material present in the fluidized bed is kept approximately constant irrespective of fluctuations in the quantity of material supplied and discharged.
  • the necessary constant maintenance of the quantity of material cannot be achieved by simple volumetric control of the quantity of material supplied and removed.
  • the amount of material in the fluidized bed is therefore regulated as a function of a gas pressure measured in the fluidized bed.
  • a gas pressure measured in the fluidized bed is a very sensitive and reliable measure of the amount of material present in the fluidized bed, so that the latter can be kept constant depending on the gas pressure (by either the quantity of material discharged from the fluidized bed or the cooling zone or the quantity of material introduced into the fluidized bed or both quantities of material are controlled accordingly).
  • the quantity of material located in the fluidized bed is expediently controlled as a function of the difference between a gas pressure measured in the fluidized bed and a gas pressure measured in the exhaust gas line of the fluidized bed, since an increase in the amount of exhaust gas in the fluidized bed has no influence on the setpoint value set in such a differential pressure control .
  • At least part of the fuel is expediently introduced into the fluidized bed from below from below the surface of the fluidized bed, preferably approximately at the level of the supply of the pre-calcined material. Another part of the fuel can be introduced into the fluidized bed via the surface of the fluidized bed or together with the recycled part of the fired material.
  • the part of the fuel which is pneumatically introduced into the fluidized bed from the side is preferably introduced into the fluidized bed together with the pre-calcined material, and advantageously at several locations distributed uniformly over the circumference of the fluidized bed. This results in a particularly rapid and even distribution of material and fuel in the fluidized bed.
  • the preheating and precalcination zone will An adjustable part of the exhaust gases of the fluidized bed and preferably an adjustable part of the cooling air flow are expediently supplied, while the remaining part of the exhaust gases of the fluidized bed are removed bypassing the preheating and precalcination zone.
  • the entire exhaust gases of the fluidized bed can also be removed bypassing the preheating and precalcination zone and the latter can be fed exclusively with cooling air.
  • the plant contains a preheater 1, a precalcination zone 2 and a shaft-shaped reaction chamber 3 with a fluidized bed 4 and a cooling zone 5.
  • the pulverulent raw material fed in at 6 is preheated in countercurrent by hot gases (arrow 7) and then passes (arrow 8) into the precalcination zone 2, where it is caused by the hot exhaust gases (arrow 9) the reaction chamber 3 and additional fuel (arrow 10) is pre-calcined to a degree of deacidification of 80 to 95%.
  • the pre-calcined material is then fed (arrows 11, 12) to conveying lines 13, 14, via which it is pneumatically introduced into the fluidized bed 4 along with fuel 15 or 16 at least two mutually opposite points (arrows 17).
  • the clear cross section of the reaction space 3 is narrowed in the region of the mouth of the delivery lines 13, 14 and widens conically upwards from this feed zone.
  • the cross section of the reaction chamber 3 and the flow velocities of the air are dimensioned such that in the lower region of the fluidized bed, i.e. the area intended for the introduction of the pre-calcined material, i. approximately at the level of the delivery lines 13, 14, approximately the same gap degree, preferably between 0.6 and 0.7 as in the upper region of the fluidized bed.
  • the pre-calcined material is fired into cement clinker. After reaching a certain clinker size, the fired material gels into the cooling zone 5, to which a cooling air flow (arrows 19) is fed from below through the air-permeable base 18.
  • the cooled goods are drawn off by a rotating discharge device 20 (arrow 21). Part of the material is recycled into the fluidized bed 4 as seed clinker (arrow 22).
  • a part of the cooling air flow identified by the arrows 23 is introduced into the fluidized bed 4 as loosening and combustion air from below.
  • Another part (arrow 24) is drawn off laterally on the circumference of the upper region of the cooling zone 5 by an air extraction line, possibly dedusted in a cyclone 25 and by a blower 26 to the delivery lines 13, 14 as conveying air for the pre-calcined material (arrows 11, 12) and the fuel (arrows 15, 16) supplied (arrows 27, 28).
  • blower 26 Another part of this air conveyed by the blower 26 can be usefully introduced into the fluidized bed 4 as additional side air below the level of the conveying lines 13, 14 (arrows 29, 30).
  • Another portion of the air conveyed by the blower 26 to the cooling zone 5 can be fed to the precalcination zone 2 as additional combustion air (arrow 31). Any excess air (arrow 32) can be discarded or otherwise used. Likewise, a certain proportion of the exhaust gases from the fluidized bed 4 - in particular with a high alkali content - can be branched off bypassing the precalcination zone 2 and the preheater 1 (arrow 33).
  • the system contains four pressure measuring points 34, 35, 36 and 37, of which the pressure measuring point 34 lies approximately in the area of the introduction of the material, the measuring point 35 approximately to 1/3 to 1/2 the height of the fluidized bed 4, the pressure measuring point 36 in the upper third of the fluidized bed and the pressure measuring point 37 in the exhaust pipe of the fluidized bed.
  • the four pressure measuring points are connected to a pressure transducer 38 which is connected to a regulator 39.
  • This regulator 39 acts on the one hand on the discharge device 20 (control line 40) and on the other hand on a feed metering device 41 (control line 42).
  • the controller 39 keeps the quantity of material in the fluidized bed 4 constant, for example by means of the discharge device 20 controlled by the controller 39 only discharging the quantity of material located above the setpoint from the cooling zone 5 and thus from the fluidized bed 4 or by the material feed metering device 41 In each case a quantity of good missing at the setpoint is fed.
  • a pressure value supplied by the pressure measuring points 34 to 37 is used as a measure of the quantity of material in the fluidized bed 4, for example the difference between the pressures determined at the measuring points 34 and 37.
  • the grain size of the seed clinker is 2 to 4 mm; the ratio of raw flour to seed clinker is 4: 1.
  • the preheated and pre-calcined material is placed in the at a temperature of approx. 840 ° C Fluid bed 4 introduced.
  • the temperature in this fluidized bed is between 1300 and 1350 ° C.
  • the material is cooled to a temperature of 80 to 120 ° C.
  • the loss on ignition of the raw material after the preheater is 5%.
  • the grain size of the deacidified raw material is 44%> 90 / 1m and 8.8%> 200 fl m.
  • the air volumes can be selected as follows;
  • the cooling zone 5 is fed from below 1.00 Nm 3 / kg clinker. From this, 0.33 Nm 3 / kg of KI get directly into the fluidized bed from below (arrows 23), while 0.67 Nm 3 / kg of KI are removed from the side of the cooling zone (arrow 24). From this latter part, 0.17 Nm 3 / kg KI as conveying air (arrows 27, 28) for precalcined material and fuel enter the fluidized bed 4 from the side, while 0.5 Nm 3 / kg KI directly (arrow 31) Precalcination zone 2 are supplied. An equal amount of air (0.5 Nm 3 / kg KI) reaches the precalcination zone 2 as exhaust gases from the fluidized bed (arrow 9).
  • the differential pressure measured between the pressure measuring points 34 and 37 is between 78 and 118 m bar, the differential pressure between the pressure measuring points 35 and 37 between 25 and 39 m bar.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Organic Chemistry (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Curing Cements, Concrete, And Artificial Stone (AREA)
  • Vertical, Hearth, Or Arc Furnaces (AREA)
  • Furnace Details (AREA)

Claims (10)

1. Procédé de production de ciment par cuisson de matière première pulvérulente dans une couche fluidisée dans laquelle sont introduits la matière première réchauffée, du combustible, de l'air réchauffé et une partie recyclée de la matière ayant subi la cuisson, la' matière déchargée de la couche fluidisée passant ensuite dans une zone de refroidissement par un flux d'air, procédé caractérisé par la combinaison des particularités suivantes:
a) la matière première réchauffée passe avant d'être chargée dans la couche fluidisée dans une zone de calcination initiale avec un complément de combustible de manière que sont taux de désacidification atteigne 80 à 95%;
b) la matière ayant subi la cuisson parvient de la région inférieure de la couche fluidisée dans une zone de refroidissement qui est formée par une partie du lit de matière se trouvant immédiatement au-dessous de la couche fluidisée;
c) une partie du flux d'air de refroidissement est introduite par le bas et une autre partie de cet air est introduite par le côté dans la couche fluidisée;
d) la partie du flux d'air de refroidissement introduite par le côté dans la couche fluidisée charge dans cette dernière la matière ayant subi la calcination initiale;
e) un rétrécissement de section régie le taux de vides approximativement à la même valeur, de préférence à une valeur comprise entre 0, 5 et 0,8, dans la région inférieure de la couche fluidisée, qui est destinée à l'introduction de la matière ayant subi la calcination initiale, et dans la région supérieure de cette couche;
f) la quantité de matière se trouvant dans la couche fluidisée est réglée en fonction d'une pression de gaz mesurée dans cette couche.
2. Procédé selon la revendication 1, caractérisé en ce que la matière ayant subi la calcination initiale est introduite dans la couche fluidisée par une impulsion d'une intensité comprise entre 49 et 98 N.
3. Procédé selon la revendication 1, caractérisé en ce qu'au moins une partie du combustible est introduite par le côté dans la couche fluidisée sous la surface de cette dernière, de préférence approximativement au niveau de l'admission de la matière ayant subi la calcination initiale.
4. Procédé selon la revendications 1 et 3, caractérisé en ce qu'une partie du flux d'air de refroidissement introduit par le côté, dans la couche fluidisée, au moins une partie du combustible avec la matiére ayant subi la calcination initiale, en plusieurs emplacements de préférence répartis régulièrement à la circonférence de cette couche.
5. Procédé selon la revendication 1, caractérisé en ce que la quantité de matière se trouvant dans la couche fluidisée est réglée en fonction de la différence entre une pression de gaz mesurée dans la couche fluidisée et une pression de gaz mesurée dans la canalisation d'évacuation des gaz d'échappement de la couche fluidisée.
6. Procédé selon la revendication 1, caractérisé en ce qu'environ 50 à 90%, de préférence environ les deux tiers de la quantité totale d'air sont introduits par le bas et environ 10 à 50%, de préférence environ un tiers de cette quantité totale d'air sont introduits par le côté dans le couche fluidisée.
7. Procédé selon la revendication 1, caractérisé en ce qu'une partie réglable des gaz d'échappement de la couche fluidisée ainsi que de préference une partie réglable du flux d'air de refroidissement sont dirigées dans les zones de réchauffage et de calcination initiale tandis que le reste des gaz d'échappement de la couche fluidisée est évacué en dérivation sur ces zones de réchauffage et de calcination initiale.
8.. Dispositif pour la mise en oeuvre du prodédé selon la revendication 1, comprenent une chambre de réaction de type à cuve (3) qui comprend dans la région inférieure une zone de refroidissement (5) et, au-dessus de cette dernière, une couche fluidisée (4), ledit dispositif comprenant par ailleurs un réchauffeur
(1) conformé en échangeur de chaleur à plusieurs étages à contre-courant ainsi qu'une zone de calcination initiale (2) alimentée en un complément de combustible (10), dispositif caractérisé en ce qu'au moins une canalisation de soutirage d'air (flèche 24) raccordée à la circonférence de la région supérieure de la zone de refroidissement (5) est reliée par l'intermédiaire d'une soufflante (26) à une canalisation de transfert pneumatique (13, 15) par laquelle la matière ayant subi la calcination initiale est introduite par le côté dans la région inférieure de la couche fluidisée (4), à une canalisation (flèches 29, 30) d'introduction d'un autre flux d'air par le côté par la couche fluidisée
(4) ainsi que de préférence à une canalisation (flèche 31) par laquelle de l'air comburant est dirigé dans la zone de calcination initiale (2) et la section libre de la chambre de réaction (3) s'élargit en cône vers le haut de la zone d'introduction de la matière (canalisations de transfert 13, 14).
EP78100518A 1977-08-04 1978-07-27 Procédé et appareillage pour la préparation de ciment dans un lit fluidisé. Expired EP0000739B1 (fr)

Applications Claiming Priority (10)

Application Number Priority Date Filing Date Title
DE2735140 1977-08-04
DE2735084 1977-08-04
DE19772735084 DE2735084A1 (de) 1977-08-04 1977-08-04 Verfahren und anlage zur herstellung von zement
DE19772735140 DE2735140A1 (de) 1977-08-04 1977-08-04 Verfahren und anlage zur herstellung von zement
DE19782822419 DE2822419A1 (de) 1978-05-23 1978-05-23 Verfahren und anlage zur herstellung von zement
DE2822377 1978-05-23
DE2822419 1978-05-23
DE19782822395 DE2822395A1 (de) 1978-05-23 1978-05-23 Verfahren zur herstellung von zement
DE19782822377 DE2822377A1 (de) 1978-05-23 1978-05-23 Verfahren zur herstellung von zement
DE2822395 1978-05-23

Publications (2)

Publication Number Publication Date
EP0000739A1 EP0000739A1 (fr) 1979-02-21
EP0000739B1 true EP0000739B1 (fr) 1981-04-15

Family

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EP78100518A Expired EP0000739B1 (fr) 1977-08-04 1978-07-27 Procédé et appareillage pour la préparation de ciment dans un lit fluidisé.

Country Status (9)

Country Link
US (1) US4213790A (fr)
EP (1) EP0000739B1 (fr)
JP (1) JPS5434325A (fr)
CA (1) CA1115297A (fr)
DE (1) DE2860617D1 (fr)
DK (1) DK347078A (fr)
GR (1) GR64304B (fr)
IT (1) IT1097686B (fr)
PT (1) PT68379A (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2474478B1 (fr) * 1980-01-30 1986-02-28 Creusot Loire Procede et dispositif de fabrication de clinker de ciment
DE3107711A1 (de) * 1981-02-28 1982-10-07 Creusot-Loire Entreprises, 92150 Suresnes Verfahren zur herstellung von zementklinker
JPS5829112A (ja) * 1981-08-12 1983-02-21 Pioneer Video Corp 磁気記録再生方法
JPS58115047A (ja) * 1981-12-28 1983-07-08 石川島播磨重工業株式会社 粉末原料の焼成設備
JPS60264350A (ja) * 1984-06-11 1985-12-27 秩父セメント株式会社 白セメントクリンカの製造方法とその装置
US4975046A (en) * 1990-01-18 1990-12-04 Gas Research Institute Cement shaft suspension furnace and process
US5188668A (en) * 1991-08-06 1993-02-23 Gas Research Institute Cement advanced furnace and process

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2409707A (en) * 1943-01-29 1946-10-22 Standard Oil Dev Co Cement manufacture
CH292727A (fr) * 1951-01-30 1953-08-31 Anonima Ammonia Casale Societa Procédé de fabrication de ciment artificiel.
CH381590A (fr) * 1958-10-07 1964-08-31 Pyzel Robert Procédé de préparation d'un ciment hydraulique et appareil pour sa mise en oeuvre
DE1767628C3 (de) * 1968-05-30 1985-03-14 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur Durchführung endothermer Prozesse
JPS49111926A (fr) * 1973-02-26 1974-10-24
AT352430B (de) * 1975-06-17 1979-09-25 Eumig Optische signaleinrichtung von elektro- akustischen uebertragungseinrichtungen
DE2528290C3 (de) * 1975-06-25 1979-09-13 Schubert & Salzer Maschinenfabrik Ag, 8070 Ingolstadt Arbeitsverfahren und Vorrichtung zum Überwachen des gesponnenen Fadens an Offen-End-Rotorspinnmaschinen

Also Published As

Publication number Publication date
IT7826440A0 (it) 1978-08-03
PT68379A (de) 1978-09-01
US4213790A (en) 1980-07-22
JPS5711862B2 (fr) 1982-03-06
CA1115297A (fr) 1981-12-29
GR64304B (en) 1980-03-03
DK347078A (da) 1979-02-05
EP0000739A1 (fr) 1979-02-21
IT1097686B (it) 1985-08-31
JPS5434325A (en) 1979-03-13
DE2860617D1 (en) 1981-05-07

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