EP0215210B1 - Procédé et installation de fabrication à chaud de briquettes sans liant - Google Patents

Procédé et installation de fabrication à chaud de briquettes sans liant Download PDF

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Publication number
EP0215210B1
EP0215210B1 EP86108912A EP86108912A EP0215210B1 EP 0215210 B1 EP0215210 B1 EP 0215210B1 EP 86108912 A EP86108912 A EP 86108912A EP 86108912 A EP86108912 A EP 86108912A EP 0215210 B1 EP0215210 B1 EP 0215210B1
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EP
European Patent Office
Prior art keywords
heated
fluidised
gas
finely divided
inert gas
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
EP86108912A
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German (de)
English (en)
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EP0215210A1 (fr
Inventor
Werner Kaas
Rudolf Auth
Lothar Seidelmann
Erich Dr. Höffken
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Thyssen Stahl AG
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Thyssen Stahl AG
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Publication date
Application filed by Thyssen Stahl AG filed Critical Thyssen Stahl AG
Priority to AT86108912T priority Critical patent/ATE46541T1/de
Publication of EP0215210A1 publication Critical patent/EP0215210A1/fr
Application granted granted Critical
Publication of EP0215210B1 publication Critical patent/EP0215210B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B1/00—Preliminary treatment of ores or scrap
    • C22B1/14—Agglomerating; Briquetting; Binding; Granulating
    • C22B1/24—Binding; Briquetting ; Granulating

Definitions

  • the invention relates to a method and a plant for the production of binderless hot briquettes made of iron-containing pyrophoric, finely divided solids.
  • a method and a plant are of this type known from DE-PS 32 23 203 by means of which more than 4 wt .-% of metallic iron-containing fine-particle, dry solids with a temperature of more than 200 ° C, as described for example in steelmaking accruing after the oxygen inflation process in the CO recovery in filters, a fluidized bed (fluidized bed), which is directly downstream of the filters.
  • a fluidized bed fluidized bed
  • the finely divided solid is blown on the fluidized bed by means of an ascending, oxidizing, heated gas stream and held in a fluidized bed.
  • the gas flow is controlled in such a way that the temperature of the finely divided solid is increased to 450 to 650 ° C. by oxidation of part of the metallic iron.
  • the solid is hot briquetted.
  • a method for agglomerating finely divided metallurgical raw material is known by hot briquetting at temperatures between 200 and 600 ° C.
  • the material to be briquetted is either after a previous treatment process at high temperature, for example after the Roasting of flotation sulfur gravel, briquetting with the resulting high temperature or the cold goods are heated to the required hot briquetting temperatures in various ovens.
  • the cold goods can be heated in rotary ovens, deck ovens, suspension ovens of the fluidized bed type or in ovens in which the goods are suspended in a hot gas stream and separated in a cyclone.
  • the invention has for its object to avoid the disadvantages described and to propose a method and an associated system with which cooled, finely divided pyrophoric solids and solids with a reduced pyrophoric fraction can be hot briquetted in an energy-saving, accelerated manner while improving the vortex behavior of the solids in the Fluid bed if channel formation is avoided and if the dwell time of the solids in the fluid bed is adequately controlled.
  • the supply of heat from the outside advantageously heats the metallic iron to the ignition temperature.
  • the effect of vibrations on the fluidized bed prevents the formation of channels and the finely divided solids can be guided over the length of the fluidized bed.
  • the finely divided solid substances is blown both by means of the ascending oxidizing heated gas stream and by means of the ascending hot combustion gases and / or heated inert gas in order to accelerate the briquetting temperature of 450 to 800 ° C.
  • Heated air is preferably used as the heated oxidizing gas stream and nitrogen is used as the heated inert gas.
  • the air and / or the inert gas are heated by heat exchange by means of the hot, preferably cleaned exhaust gases emerging from the fluidized bed. This results in a particularly energy-saving way of working.
  • the heated air, the heated inert gas and the hot combustion gases are supplied to the fluidized bed in at least two, preferably in three or more, sections, the amount and temperature of the heated air, the heated inert gas and the hot combustion gases being independently controllable.
  • the temperature of the fluidized bed is measured at more than one, preferably at three, points and the temperature values are used to regulate / control the quantity and temperature of the heated air supplied to the fluidized bed, the heated inert gas and the hot combustion gases.
  • the amount of gases supplied to the fluidized bed is regulated / controlled so that the total amount of heated air, heated inert gas and hot combustion gases is constant.
  • the temperatures measured in the fluidized bed rise above the setpoint, the supply of hot combustion gases and then the supply of heated air is reduced and the supply of heated nitrogen is increased. If, on the other hand, the temperatures measured in the fluidized bed fall below the desired value, more heated air is supplied and then the supply of hot combustion gases is increased and the supply of heated nitrogen is reduced.
  • the residence time of the solids in the fluidized bed can be adjusted by changing the inclination of the fluidized bed or by changing the vibrations applied from the outside.
  • finely divided solid to be prepared does not consist entirely or predominantly of pyrophoric material
  • part of the finely divided solid can be replaced by finely divided solid fuel.
  • Up to 15% or up to 10% of the finely divided solids are preferably replaced by finely divided solid fuel.
  • Lignite coke dust and / or finely divided coal dust preferably from the treatment of flotation sludge, can be used as the finely divided solid fuel.
  • the solid can be preheated in countercurrent before entering the fluidized bed by hot, uncleaned exhaust gases from the fluidized bed. It is also possible to preheat the solid in the first part of the fluidized bed by means of heated cooling air from the briquette cooling.
  • the method according to the invention can also be carried out when the filter system is in the start-up state or when cold operating states occur.
  • Another advantage is that both the heating of the finely divided solids to the ignition temperature and the subsequent heating to the hot briquetting temperature in one device, i.e. can be carried out in the fluidized bed reactor according to the invention.
  • the balance of the thermal energy to be used is economically favorable and there are no transport losses for the fine-particle solid, which would occur, for example, if the fine-particle solids were first heated to the ignition temperature in a separate device and only then in a further device for heating to the hot briquetting would be directed.
  • a system for carrying out the process consisting of a fluidized bed reactor equipped with vibration exciters with gas feed lines to the underside of the fluidized bed, a subsequent briquette press and a briquette cooler is characterized in that the underside of the fluidized bed reactor is designed as a chamber which consists of at least two sections with separate gas feed lines. that the gas supply lines are connected to burners for generating hot combustion gases and to supply lines for a controllable supply line from a heated oxidizing gas stream and heated inert gas and that heating means are provided for heating the oxidizing gas and the inert gas.
  • the chamber preferably consists of three or more sections.
  • gas supply connecting pieces are arranged in the upper chamber wall of the chamber forming the bottom of the fluidized bed reactor, which protrude beyond the fluidized bed level and are equipped with siphon-like end pieces engaging in the fluidized bed.
  • the first section can be connected via a line to the cooling air collecting hood of the cooling belt of the briquette cooling.
  • the heated cooling air is fed via this line to the solid as it enters the fluidized bed reactor for preheating.
  • the fluidized bed reactor has a gas-tight hood with one or more, preferably two, exhaust pipes, which are equipped with control flaps.
  • the system is characterized by a dust separator which is connected to the hood of the fluidized bed reactor via the exhaust line (s).
  • the dust separator can also be connected to the hood of the fluidized bed reactor via the trough conveyor and a connecting line with control flaps. In this way, the solid can be preheated in countercurrent during transport to the fluidized bed reactor by means of uncleaned exhaust gases from the fluidized bed.
  • a heat exchanger connected to it via a line is advantageously arranged with heat exchanger elements for the heating of air and inert gas / exhaust gas.
  • the heating means for heating the oxidizing gas and the inert gas are preferably designed as heat exchanger elements.
  • Distributed across the fluidized bed reactor are preferably measuring devices for measuring the temperature of the fluidized bed, the temperatures and the supplied quantities of the hot combustion gases, the hot air and the hot inert gas and their distribution to the individual sections being known as a function of the measured temperatures
  • Control units are controllable.
  • the fluidized bed reactor preferably has adjusting devices with which the inclination of the reactor can be adjusted. It is also advantageous if the vibration exciters of the fluidized bed have adjusting devices with which the vibration amplitude / vibration frequency can be adjusted.
  • the pyrophoric filter dust retained in filters (not shown) of a CO recovery system of an oxygen inflation converter reaches, as shown in FIG. 1, via a line 1 into a dust silo 2, from which it is conveyed to the fluidized bed reactor 4 via a trough conveyor 3.
  • the elongated fluidized bed reactor which rests on vibration elements in the form of springs 5, has a gas-permeable bottom 6, gas feed lines 7 and a hood 8.
  • the fluidized bed reactor 4 is vibrated by vibration exciters, not shown.
  • the filter dust which has been heated to the briquetting temperature in the fluidized bed reactor 4, is fed via a discharge 9 to a briquette press 10, in which the filter dust is pressed into briquettes.
  • the finished briquettes are brought to a briquette cooler for cooling, which is designed in the form of an endless belt 11, the briquettes being cooled by the ambient air passing through them.
  • the heated cooling air is collected and discharged by a hood 33.
  • the cooled briquettes then go into a bunker, not shown, from which they can be removed for use in the steel mill.
  • the fluidized bed reactor 4 As shown in FIG. 2, has a chamber 13, the upper chamber wall 6 of which forms the bottom of the reactor 4 and is gas-permeable.
  • 6 gas supply stub 14 are arranged in the bottom, which protrude beyond the fluidized bed level.
  • the gas feed stubs 14 are equipped with siphon-like end pieces 15 which reach into the fluidized bed 12.
  • the hood 8 of the fluidized bed reactor 4 has two exhaust pipes 16 which are equipped with control flaps 17.
  • the hot exhaust gases are fed to a dust separator 18 via the exhaust gas lines.
  • the hot exhaust gases can also be passed in part through the trough conveyor 3 in countercurrent to the filter dust being conveyed and fed to the dust separator 18 via a connecting line 35 with control flaps 36.
  • the filter dust in the trough conveyor 3 is already preheated. This is particularly advantageous when processing cold, coarse filter dust.
  • the filter dust particles separated from the exhaust gas in the dust separator 18 return to the fluidized bed reactor 4 via the trough conveyor 3.
  • the hot cleaned exhaust gases are fed to a heat exchanger 20 via a line 19.
  • heat exchanger elements 21 are arranged for heating air and inert gas / exhaust gas.
  • the system also has three burners 24 for generating hot combustion gases. This is done by burning natural gas with air, which are supplied via lines 25 and 26.
  • the burners 24 are connected to the gas supply lines 7 of the fluidized bed reactor 4.
  • the gas supply lines 7 are also connected to the heat exchanger elements 21 of the heat exchanger 20 via the lines 27.
  • the chamber 13 of the fluidized bed reactor 4, as shown in FIG. 1, is divided into three sections 28, into which the gas feed lines 7 open.
  • temperature measuring devices 29 are arranged, with which the temperature of the fluidized bed 12 is measured in the individual areas.
  • the measured temperature values are the control / regulating elements 17, 30 and 31 known in the Lines 16 and 27 and the fans 32 are fed in lines 22, 23, 25 and 26, via which the temperatures and the supplied quantities of the hot combustion gases, the hot air and the hot inert gas are controlled.
  • the fluidized bed reactor 4 has adjusting devices, not shown, with which the inclination of the reactor can be adjusted.
  • the vibration exciters, not shown, are also equipped with adjusting devices, not shown, with which the vibration amplitude / vibration frequency can be adjusted.
  • FIG. 3 shows a system according to the invention which corresponds to that described in FIG. 1.
  • the reference numbers apply accordingly.
  • the fluidized bed reactor 4 has four sections 28, the first being connected via a line 34 to the cooling air collecting hood 33 of the cooling belt 11 and the three other sections, as in FIG. 1, being connected to the burners 24.
  • the heated cooling air collected by the hood 33 can advantageously be used to preheat the filter dust in the first part of the fluidized bed reactor.
  • the fine and coarse dusts of Examples 1, 2 and 3 come from the filter system of a CO recovery system of an oxygen inflation converter.
  • the fine and coarse dusts of Examples 1 and 2 were separated during the normal operating state.
  • the numbers show the cooling of the dusts by transport from the filter system to the fluidized bed reactor and by storage in the silo.
  • the fine dust from Example 3 was obtained when the filter system was started up. It therefore has a low temperature and a low pyrophoric content right from the start.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Geology (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Adhesives Or Adhesive Processes (AREA)
  • Furnace Housings, Linings, Walls, And Ceilings (AREA)

Claims (29)

1. Procédé de fabrication d'agglomérés à chaud sous liant convenant au traitement métallurgique à partir de solides finement divisés contenant du fer, avec les mesures suivantes:
a) la matière solide finement divisée est insufflée jusqu'à chauffage à la température d'ignition au moyen de gaz de combustion chaud ascendant et/ou de gaz inerte chauffé et est maintenue dans une couche fluidisée,
b) la matière solide chauffée est ensuite insufflée au moyen d'un courant de gaz oxydant chauffé ascendant et maintenue dans la couche fluidisée, le courant de gaz étant réglé de telle manière que, par oxydation d'au moins une partie du fer métallique, la température de la matière solide finement divisée est augmentée à 450 jusqu'à 800°C,
c) l'action des oscillations transmises par les particules de matière solide par l'intermédiaire du lit fluidisé est suspendue pour la couche fluidisée,
d) la matière solide chauffée est ensuite agglomérée à chaud.
2. Procédé selon la revendication 1, caractérisé en ce que, après avoir atteint la température d'ignition, la matière solide finement divisée est insufflée aussi bien au moyen du courant de gaz oxydant chauffé ascendant qu'également au moyen du gaz de combustion chauffé ascendant et/ou du gaz inerte chauffé pour atteindre de manière accélérée la température d'agglomération de 450 à 800°C.
3. Procédé selon la revendication 1 et 2, caractérisé en ce qu'on utilise comme courant gazeux oxydant chauffé de l'air chauffé.
4. Procédé selon la revendication 1 à 3, caractérisé en ce qu'on utilise comme gaz inerte chauffé de l'azote.
5. Procédé selon la revendication 1 à 4, caractérisé en ce que l'air et/ou le gaz inerte sont chauffés par échange thermique au moyen des gaz d'échappement chauds, avantageusement nettoyés, sortant de la couche fluidisée.
6. Procédé selon la revendication 1 à 5, caractérisé en ce que l'air chauffé, le gaz inerte chauffé et les gaz de combustion chauds peuvent être amenés dans au moins deux, avantageusement dans trois sections de lit fluidisé ou plus.
7. Procédé selon la revendication 1 à 6, caractérisé en ce que la quantité et la température de l'air chauffé, du gaz inerte chauffé et des gaz de combustion chauds pouvant être réglées/commandées indépendamment les unes des autres.
8. Procédé selon la revendication 1 à 7, caractérisé en ce que la température de lit fluidisé est mesurée en plus d'un point, avantageusement en trois points, et les valeurs de température sont utilisées pour la régulation/commande de la quantité et de la température et l'air chauffé, du gaz inerte chauffé et des gaz de combustion chauds amenés à la couche fluidisée.
9. Procédé selon la revendication 1 à 8, caractérisé en ce que la quantité des gaz amenés à la couche fluidisée est réglée/commandée de telle manière que la quantité totale d'air chauffé, du gaz inerte chauffé et des gaz de combustion chauds est constante.
10. Procédé selon la revendication 1 à 9, caractérisé en ce que, lorsque les températures mesurées dans la couche fluidisée montent au-dessus de la valeur de consigne, l'amenée de gaz de combustion chauds et ensuite l'amenée d'air chauffée est diminuée et l'amenée d'azote chauffé est augmentée.
11. Procédé selon la revendication 1 à 10, caractérisé en ce que, lorsque les températures mesurées dans la couche fluidisée descendent en-dessous de la valeur de consigne, on envoie plus d'air chauffé et ensuite l'amenée de gaz de combustion chaud est augmentée et l'amenée d'azote chauffé est réduite.
12. Procédé selon la revendication 1 à 11, caractérisé en ce que le temps de séjour des matières solides dans le lit fluidisé est réglé par modification de l'inclinaison du lit fluidisé.
13. Procédé selon la revendication 1 à 11, caractérisé en ce que le temps de séjour des matières solides dans le lit fluidisé est réglé par modification des oscillations transmises depuis l'extérieur.
14. Procédé selon la revendication 1 à 13, caractérisé en ce que jusqu'à 15%, avantageusement jusqu'à 10%, de la matière solide finement divisée est remplacée par un combustible solide finement divisé.
15. Procédé selon la revendication 14, caractérisé en ce qu'on utilise comme combustible solide finement divisé de la poussière de coke de lignite et/ou des poussières de charbon finement divisées, de préférence provenant de la préparation de schlich de flottation.
16. Procédé selon la revendication 1 à 15, caractérisé en ce que la matière solide est préchauffée avant l'entrée dans le lit fluidisé par des gaz évacués non nettoyés et chauds du lit fluidisé en contre- courant.
17. Procédé selon la revendication 1 à 15, caractérisé en ce que la matière solide est préchauffée dans la première partie du lit fluidisé par de l'air froid réchauffé provenant du refroidissement d'agglomération.
18. Installation pour la mise en oeuvre du procédé selon la revendication 1 à 17, constituée d'un réacteur à lit fluidisé équipé d'excitateurs d'oscillations, avec des conduites d'amenée de gaz sur la face inférieure du lit fluidisé, une presse d'agglomération suivante et un refroidisseur d'aggloméré, caractérisée en ce que la face inférieure du réacteur à lit fluidisé (4) est construite sous forme de chambre (13) qui est formée d'au moins deux sections (28) à conduites d'amenée de gaz (7) séparées, que les conduites d'amenée de gaz (7) sont reliées à des brûleurs (24) pour former des gaz de combustion chauds et sont également reliées à des conduites d'alimentation (27) pour une alimentation commandable/réglable d'un courant de gaz oxydant chauffé et de gaz inerte chauffé, et que des moyens de chauffage pour chauffer le gaz oxydant et le gaz inerte sont prévus.
19. Installation selon la revendication 18, caractérisée en ce que la chambre (13) est constituée de trois sections (28) ou plus.
20. Installation selon la revendication 18 et 19, caractérisée en ce que des manchons (14) de conduite d'amenée de gaz sont disposés dans la paroi de chambre (6) de la chambre (13) formant le fond du réacteur à lit fluidisé qui font saillie extérieurement au-dessus du niveau du lit fluidisé et sont équipés de pièce d'extrémité (15) pénétrant à la manière d'un siphon dans le lit fluidisé (12).
21. Installation selon la revendication 18 à 20, caractérisée en ce que la première section (28) est reliée par une conduite (34) avec la hotte de réception d'air froid (33) de la bande de refroidissement (11) du refroidissement d'agglomérés.
22. Installation selon la revendication 18 à 21, caractérisée en ce que le réacteur à lit fluidisé (4) présente une hotte (8) étanche aux gaz avec une ou plusieurs, avantageusement deux, conduites d'évacuation de gaz (16) qui sont équipées de volets de réglage (17).
23. Installation selon la revendication 18 à 22, caractérisée par un séparateur de poussière (18) qui est relié par l'intermédiaire de la conduite d'évacuation de gaz (ou les conduites d'évacuation de gaz (16) avec la hotte (8) du réacteur à lit fluidisé (4).
24. Installation selon la revendication 18 à 23, caractérisée en ce que le séparateur de poussière (18) est relié à la hotte (8) du réacteur à lit fluidisé (4) par le convoyeur à plateaux (3) et une conduite de liaison (35) avec clapets de régulation (36).
25. Installation selon la revendication 18 à 24, caractérisée en ce qu'un échangeur de chaleur (20) est disposé à la suite du séparateur de poussière (18) et en liaison avec celui-ci par une conduite (19), avec des éléments (21) d'échangeur de chaleur pour le chauffage de l'air et du gaz inerte/gaz d'échappement.
26. Installation selon la revendication 18 à 25, caractérisée en ce que les moyens de chauffage pour chauffer le gaz oxydant et le gaz inerte sont construits sous forme d'éléments d'échangeur de chaleur (21).
27. Installation selon la revendication 18 à 26, caractérisée en ce que des appareils de mesure (29) pour mesurer la température de la couche fluidisée sont disposés répartis sur le réacteur à lit fluidisé (4), la température et les quantités amenées des gaz de combustion chauds, de l'air chaud et du gaz inerte chaud et leur répartition sur les sections individuelles (28) pouvant être commandées/réglées par des organes de commande/réglage connus en soi en fonction des températures mesurées.
28. Installation selon la revendication 18 à 27, caractérisée en ce que le réacteur à lit fluidisé (4) présente des dispositifs de réglage par lesquels l'inclinaison du réacteur peut être réglée.
29. Installation selon la revendication 18 à 28, caractérisée en ce que les excitateurs d'oscillations du lit fluidisé (12) présentent des dispositifs de réglage par lesquels l'amplitude d'oscillation/fréquence d'oscillation peuvent être réglées.
EP86108912A 1985-08-14 1986-07-01 Procédé et installation de fabrication à chaud de briquettes sans liant Expired EP0215210B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86108912T ATE46541T1 (de) 1985-08-14 1986-07-01 Verfahren und anlage zur herstellung bindemittelloser heissbriketts.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3529084 1985-08-14
DE3529084A DE3529084C1 (de) 1985-08-14 1985-08-14 Verfahren und Anlage zur Herstellung bindemittelloser Heissbriketts

Publications (2)

Publication Number Publication Date
EP0215210A1 EP0215210A1 (fr) 1987-03-25
EP0215210B1 true EP0215210B1 (fr) 1989-09-20

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EP86108912A Expired EP0215210B1 (fr) 1985-08-14 1986-07-01 Procédé et installation de fabrication à chaud de briquettes sans liant

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US (2) US4853031A (fr)
EP (1) EP0215210B1 (fr)
JP (1) JPS6240323A (fr)
CN (1) CN1009738B (fr)
AT (1) ATE46541T1 (fr)
BR (1) BR8603884A (fr)
CA (1) CA1292621C (fr)
DE (2) DE3529084C1 (fr)
ES (1) ES2001223A6 (fr)
SU (1) SU1605927A3 (fr)
UA (1) UA7727A1 (fr)

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DE3711130C1 (de) * 1987-04-02 1988-07-21 Thyssen Stahl Ag Verfahren und Anlage zur Herstellung von bindemittellosen Heissbriketts
DE3732351A1 (de) * 1987-09-25 1989-04-06 Metallgesellschaft Ag Verfahren zur herstellung von bindemittellosen briketts aus stahlwerksstaeuben
US5918701A (en) * 1997-05-13 1999-07-06 Rogelja; Boris Roping device
CN100395163C (zh) * 2004-05-28 2008-06-18 上海宝钢国际经济贸易有限公司 热压铁块粉的堆放方法
CN1317217C (zh) * 2005-04-05 2007-05-23 蒋发学 水泥混凝土多功能助剂
JP4317579B2 (ja) * 2007-09-05 2009-08-19 新日本製鐵株式会社 還元鉄成形体の製造方法、及び銑鉄の製造方法
JP5198409B2 (ja) * 2009-11-04 2013-05-15 大同特殊鋼株式会社 排ガスダストの処理方法
JP5553915B2 (ja) * 2013-01-15 2014-07-23 大同特殊鋼株式会社 排ガスダストの処理方法

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JPH0258327B2 (fr) 1990-12-07
CN86105313A (zh) 1987-02-11
DE3665738D1 (en) 1989-10-26
CA1292621C (fr) 1991-12-03
ATE46541T1 (de) 1989-10-15
CN1009738B (zh) 1990-09-26
EP0215210A1 (fr) 1987-03-25
DE3529084C1 (de) 1986-10-16
UA7727A1 (uk) 1995-12-26
JPS6240323A (ja) 1987-02-21
SU1605927A3 (ru) 1990-11-07
ES2001223A6 (es) 1988-05-01
BR8603884A (pt) 1987-03-24
US4853031A (en) 1989-08-01
US4934665A (en) 1990-06-19

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