EP0249057B1 - Verfahren und Vorrichtung zum Herstellen einer feinkeramischen Masse grosser Homogenität und hohen Feinheitsgrades - Google Patents

Verfahren und Vorrichtung zum Herstellen einer feinkeramischen Masse grosser Homogenität und hohen Feinheitsgrades Download PDF

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Publication number
EP0249057B1
EP0249057B1 EP87107191A EP87107191A EP0249057B1 EP 0249057 B1 EP0249057 B1 EP 0249057B1 EP 87107191 A EP87107191 A EP 87107191A EP 87107191 A EP87107191 A EP 87107191A EP 0249057 B1 EP0249057 B1 EP 0249057B1
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EP
European Patent Office
Prior art keywords
liquid
component materials
granulate
process according
mixer
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
EP87107191A
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German (de)
English (en)
French (fr)
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EP0249057A1 (de
Inventor
Emil-Karl Dr.-Ing. Köhler
Dieter Seltmann
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.)
Porzellanfabrik Schirnding AG
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Porzellanfabrik Schirnding AG
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Filing date
Publication date
Application filed by Porzellanfabrik Schirnding AG filed Critical Porzellanfabrik Schirnding AG
Priority to AT87107191T priority Critical patent/ATE46092T1/de
Publication of EP0249057A1 publication Critical patent/EP0249057A1/de
Application granted granted Critical
Publication of EP0249057B1 publication Critical patent/EP0249057B1/de
Expired legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/50—Mixing liquids with solids
    • B01F23/59—Mixing systems, i.e. flow charts or diagrams

Definitions

  • the invention relates to a method for producing a granulated fine ceramic mass of great homogeneity and high degree of fineness from ceramic raw materials, liquids, additives and. The like., With the feed materials being finely ground, liquid added and, if appropriate, partially removed at a later time.
  • the quality of the fine ceramic products depends not only on shaping, drying and firing processes, but also on chemical analysis, the mineralogical structure, the grain size distribution and the homogeneity and degree of fineness of the used fine ceramic masses. The preparation of the mass that meets these requirements is therefore of the utmost importance.
  • the input materials, in particular the solid materials, namely the raw materials and the additives, are ground so finely that they can pass through a sieve which has 10,000 meshes on the cm 2 .
  • some of the raw materials are ground wet in drum mills to the required degree of fineness.
  • These drum mills are cylindrical bodies that are driven around horizontal axes and have a resistant lining.
  • the hard feedstocks are introduced together with liquid, in particular water, and grinding media into the drum mill, which is then rotated, for example for 12 hours, until the desired degree of fineness is achieved.
  • the other input materials are usually processed accordingly by the raw material suppliers in a liquid preparation process and delivered dry. These ingredients (soft materials) are in a whisk with the addition of z. B. 50 to 70% of water is converted into a suspension, to which the hard material suspension of the liquefied, ground starting materials is then added.
  • the other known process which leads to free-flowing or free-flowing granules, coincides in its initial processing steps with the production of the fine ceramic mass in the form of a lever, until the suspension of the hard and soft starting materials is whisked. Only comparatively less water is used.
  • the slip thus formed is subjected to spray drying by being expelled through nozzles in a spray tower under high pressure and moving in free fall through the spray tower from top to bottom.
  • Sprühtrum is from bottom to top, that is, the direction of fall, hot gas opposite performed which may have a temperature of 400 to 600 ° C.
  • the process of spray drying is then to be carried out in such a way that the nebulously injected slip drops contract into spherical granules during the fall in the spray tower, which have a small size adapted to the use and a moisture content of about 2 to 5% when they are removed from the spray tower .
  • These free-flowing granules have to behave like a liquid, that is to say they melt between your fingers, even though they are solid bodies is present.
  • this consistency is important for the production of fine ceramic products, for example porcelain, using dry pressing processes, in particular isostatic pressing.
  • the main disadvantage of producing this fine ceramic mass in the form of the free-flowing granulate is the high energy consumption that is required in spray drying. This process is also mechanically complex.
  • Another disadvantage is the shape of the granules. Hollow grain formation occurs during spray drying, i. H. the single pellet, which in turn is composed of a large number of the finest mass particles, is hollow on the inside, approximately like a thick-walled ball, so that the pellet can be pressed together, but on the other hand there is a certain resilience, which ensures the smoothness and flatness of the surfaces of the fine ceramic product can impair.
  • the invention has for its object to provide a method and an apparatus with which a mass suitable for fine ceramic purposes can be produced much more economically than before. It is particularly important to avoid the liquid phase. On the one hand, it should be possible to produce free-flowing granules as a fine ceramic mass, which is particularly suitable for isostatic pressing. Further processing steps should make it possible to be able to use this mass to also produce plastic levers or, on the other hand, a casting slip.
  • this is achieved in the process of the type described in the introduction in that the starting materials are ground dry or moist and all or some of the starting materials are guided in free fall from above into and through a vertically arranged container, with or part of the liquid being injected under Exposure to turbulence can be brought into contact and agglomerated into granules. It is therefore important that the feedstocks are no longer ground wet, but dry or, if necessary, damp, the moisture already being matched to the final moisture content of the granules or the fine ceramic mass.
  • This granulate is particularly suitable for the isostatic pressing of moldings in the porcelain industry, because the agglomeration produces a whole grain, in contrast to the hollow grain of spray drying.
  • the use Formation of this whole grain results in a smoother surface, especially with isostatic pressing.
  • more stable bodies are formed when the fine ceramic products are fired, so that the preparation process ultimately advantageously leads to the fact that, for. B. a plate or a cup can have a smaller wall thickness than before, so that new ways of design are opened in this way.
  • the granules produced are of course not or must not be powder, although the dimensions of the individual granules are very small. A powder would also not have the required flow or flow properties, and therefore could not be processed accordingly.
  • the starting materials for producing a splintery grain are ground in a fine grinding mill, preferably an impact mill.
  • a fine grinding mill preferably an impact mill.
  • a more or less round grain with a spherical surface is formed.
  • an impact mill on the other hand, a splintered grain is formed with a surface that has several surfaces offset from one another.
  • This splintery grain promotes the growth of the granulate during agglomeration and results in good cohesion of the mass, especially in the dry-pressed ceramic molded body. This may be due to the fact that the splintery grain can be destroyed or assembled more easily than a hollow grain of spherical shape during dry pressing, so that the comparatively greater smoothness and increased strength of the fine ceramic product can also be explained in this way.
  • all the feedstocks are first premixed and then ground together, so that all the feedstocks required for the particular recipe are mixed and homogenized in this initial process step.
  • the fine ceramic mass is to be in the form of granules, it is usually necessary to add a slightly higher moisture to the granulate formation than it corresponds to the fine ceramic mass in its condition required for further processing.
  • agglomerated granulate is dried, which is possible in particular in a fluidized bed process in order to avoid any abrasion and destruction of the granulate shape as far as possible.
  • entrained current processes or fluidized bed processes can also be used here.
  • the fine ceramic mass should ultimately be in the form of a lever, in order, for. B. to produce porcelain products in the turning process, then the drying step is dispensed with and the agglomerated granules are deaerated and plasticized in a vacuum extruder and then removed in the form of a lever.
  • the moisture content required for the agglomeration largely coincides with the moisture content required for rotating the shaped bodies, so that a drying step is advantageously omitted at this time.
  • this does not rule out the fact that the turned porcelain moldings have to be subjected to a drying process, while the moldings pressed dry from the granulate then no longer have to be dried.
  • liquids or suspensions to be injected it is also possible, in particular, to add additives which have a strengthening effect.
  • the method allows easy feeding at a point in time at which the starting materials are already homogenized.
  • the finely ground feedstocks are placed in a tumbling, helical turbulence in the container by means of a high-speed mixer; the or part of the liquid is sprayed nebulously under pressure, the speed of the mixer and the amount of liquid being matched to one another in such a way that the agglomeration of the starting materials and the liquid takes place to form a free-flowing granulate.
  • the intimate and intensive mixing of the input materials or the offset and the agglomeration therefore run practically simultaneously at the same time; the granules which can be obtained in this way or after the subsequent drying are extremely homogeneous and of such flowability or flowability which meets high technical requirements and in particular permits rapid pressing cycles.
  • the agglomerated granulate can be further processed into a pouring slurry with the addition of liquid. This is done by means of a screw whisk in a mixing tub.
  • additives in addition to water, additives (liquefiers) can also be added.
  • the device for carrying out the method works with a mill for fine grinding of the feed materials and is characterized according to the invention in that a vertically arranged container with a feed device opening into its upper region is provided for the dry or wet ground feed materials, in the tubes with nozzle-like openings for atomizing liquid and a fast-running mixer are arranged below it, the mixer having mixing arms.
  • the mixing arms which rotate at a correspondingly high number of revolutions, put the feed materials in their already finely ground form into a turbulently moving dust cloud, which is briefly brought into contact with the injected liquid and thus agglomerated.
  • a drier can be connected downstream of the container, in which the moisture and the temperature of the granules are influenced. This is the case when the granulate is used in free-flowing form for the dry pressing of fine ceramic products.
  • the dryer can be a fluid bed dryer or an entrained flow dryer, it being expedient to work with a cooling station in its last part in order to avoid the separation of liquid which leads to a coexistence menbacken the granules could lead, so that the flowability would be impaired.
  • the mixer expediently has adjustable mixing arms.
  • the speed of the mixing arms is also adjustable or changeable, so that the residence time of the individual particles of the starting materials can also be influenced by the choice of the appropriate setting angle of the mixing arms. This affects the granule size, strength, etc. It must be ensured that the granules do not disintegrate until they are used in dry pressing.
  • corresponding transport elements and discharge devices must be provided between the vertical container or the mixer and the dryer and downstream of this.
  • Ceramic raw materials and aggregates i.e. the hard and soft feedstocks, are drawn off from several silos (1) in the pre-metering required for the offset and fed into an impact mill (3) or another fine grinding mill with a transport device (2).
  • a line (4) allows the addition of liquid, in particular water, in order to moisten the feedstocks if necessary. In any case, the liquid grinding is prevented, but in the impact mill (3) there is a dry or moist grinding of the feed materials, resulting in a splintery grain with the required fineness, whereby the offset is already homogenized.
  • the ground feed materials enter from above into a container (6) with a vertically arranged axis (7), at the upper end of which they are fed into the cross-section in the desired manner by means of a distributing device and initially in free fall a section of the Fall through container (6).
  • a mixer (8) with mixing arms (9) is arranged in the container (6) according to the axis (6), the shaft (10) of which is driven in a rapidly running manner by a motor (11) which is expediently arranged at the top.
  • the speed of the shaft (10) can be in the order of 2500 to 6000 revolutions / min. The speed is changeable and can be adapted to the respective application.
  • the mixing arms (9) are also adjustable.
  • Spray pipes (12) are provided above the mixer (8) and have nozzle-like openings through which liquids and / or additives - also in the form of suspensions - can be injected from storage containers (13) under appropriate pressure by means of a pump (14). This liquid, too, is distributed nebulously and comes into intimate contact with the agitated feedstocks, agglomeration taking place.
  • the accumulation of the individual grains of the input materials and the caking together result in fine granules, the individual granule balls being designed as whole grains.
  • This granulate sinks downward in the container (6) and reaches the area of the container outlet (15), where appropriate transport devices are provided in order to convey the granulate further.
  • the quantity and composition of the liquid injected from the storage containers (13) into the container (6) is matched to the desired moisture content of the granules for further processing as a ceramic mass.
  • the moisture content must be adapted to the formation of agglomerates.
  • the moisture content can thus also be set somewhat above the desired moisture content for a free-flowing granulate for further processing in the dry pressing process into porcelain products or the like.
  • the granulate formed at the container outlet (15) is fed by means of transport devices (16) to a fluid bed dryer (17) which is expediently divided into several treatment chambers.
  • a fluid bed dryer (17) which is expediently divided into several treatment chambers.
  • heating devices (18) are provided which can be designed, for example, as hot gas generators.
  • the dryer also has the task of cooling.
  • the flowable and free-flowing granules with the desired moisture content of about 2 to 5% reach the storage container (20) from the fluid bed dryer (17), from which the granules (21) can be removed in a usable manner.
  • These granules (21) are particularly suitable for isostatic dry pressing of ceramic products.
  • Hubel (22) are to be manufactured for the production of fine ceramic products using the turning process, the drying step is dispensed with because the Hubel generally have a higher moisture content.
  • the granules pass from the container outlet (15) into a vacuum extrusion press (24) via transport devices (23), in which they are deaerated, compressed and driven by a mouthpiece in the form of a strand.
  • the individual levers (22) are created by subdivision.
  • the third method variant is the possibility of producing a casting slip.
  • the granulate is transferred from the container outlet (15) via a transport device (25) to a stirring tub (26), in which the ceramic slip is formed with the addition of water and possibly other liquids and / or liquefiers according to arrow (27) .
  • a screw agitator (28) works in the stirring tub (26) and ensures the homogenization of the suspension.
  • the feedstocks mentioned are ground dry together in a fine grinding plant to a grain size of less than 60 J.l.m. In this already mixed form, they reach the container (6) via the feed device (5).
  • the amount of liquid used is somewhat higher than the desired moisture content of the dry-compressible granules, but the moisture content shown in the mixer is necessary for agglomeration reasons.
  • the resulting granulate at the container outlet (15) passes into the fluid bed dryer, in which it is dried and cooled, so that ultimately the granulate (21) arriving in the storage container (20) has the desired moisture content of e.g. B. has 2%.
  • kaolins that cannot be used are used.
  • Eurit is a stone kaolin that cannot be used in plastic processing.
  • Kaolin D H 1 is a kaolin, which also has a very limited usability for porcelain production after it has poor raw breaking strength.
  • D K 1 and K K 1 are paper kaolins, which are also unsuitable for porcelain production due to their poor raw breaking strength.
  • these raw materials can be used due to the new processing method with additives to increase the raw breaking strength.
  • the raw materials are ground wet with a maximum moisture content of up to 10%.
  • Both ground groups of feedstocks are introduced together into the container (6) via the feed device (5), liquids being added to a suspension of water and plasticizers, so that a total moisture content of approximately 18% is achieved. The final and desired moisture content of the hub is thus achieved.
  • the granulate obtained at the container outlet (15) is passed through the vacuum extrusion press (24), at the outlet of which the levers (22) are produced.
  • the offset formulation of a conventional casting slip and its rational analysis differs from an offset formulation for granules essentially in the kaolines.
  • the kaolins used in the pouring slurry are characterized by the fact that a high degree of liquefaction is achieved with little addition of electrolyte in order to give the pouring slurry the highest possible liter weight, so that in the subsequent pouring process for the production of castings, the plaster molds required for this do not become too quickly with water soak it up, thereby enabling the formation of cullet to be sufficiently rapid and strong during the casting process.
  • the input materials are processed in two groups. Feldspar and quartz are ground in a drum mill, sieved and mixed together in a whisk with the second component kaolin for the finished batch.

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  • Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Preparation Of Clay, And Manufacture Of Mixtures Containing Clay Or Cement (AREA)
  • Compositions Of Oxide Ceramics (AREA)
  • Noodles (AREA)
EP87107191A 1986-06-07 1987-05-18 Verfahren und Vorrichtung zum Herstellen einer feinkeramischen Masse grosser Homogenität und hohen Feinheitsgrades Expired EP0249057B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87107191T ATE46092T1 (de) 1986-06-07 1987-05-18 Verfahren und vorrichtung zum herstellen einer feinkeramischen masse grosser homogenitaet und hohen feinheitsgrades.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3619272 1986-06-07
DE19863619272 DE3619272A1 (de) 1986-06-07 1986-06-07 Verfahren und vorrichtung zum herstellen einer feinkeramischen masse grosser homogenitaet und hohen feinheitsgrades

Publications (2)

Publication Number Publication Date
EP0249057A1 EP0249057A1 (de) 1987-12-16
EP0249057B1 true EP0249057B1 (de) 1989-09-06

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP87107191A Expired EP0249057B1 (de) 1986-06-07 1987-05-18 Verfahren und Vorrichtung zum Herstellen einer feinkeramischen Masse grosser Homogenität und hohen Feinheitsgrades

Country Status (7)

Country Link
US (1) US4897029A (ja)
EP (1) EP0249057B1 (ja)
JP (1) JPS6367108A (ja)
AT (1) ATE46092T1 (ja)
BR (1) BR8702869A (ja)
DE (2) DE3619272A1 (ja)
ES (1) ES2010689B3 (ja)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DK161743C (da) * 1989-07-03 1992-02-17 Niro Atomizer As Fremgangsmaade og apparat til agglomerering af et pulverformigt materiale
JPH0494407U (ja) * 1990-12-26 1992-08-17
DE4304809A1 (de) * 1993-02-17 1994-08-18 Glatt Ingtech Gmbh Verfahren zur Herstellung von feinkeramischem Preßgranulat mittels Wirbelschichtgranulationstrocknung
DE4425412A1 (de) * 1994-07-19 1996-01-25 Buehler Ag Verfahren und Vorrichtung zur Aufbereitung von Stoffen für die Verwertung oder Entsorgung
US6126100A (en) * 1996-10-14 2000-10-03 Barth; Gerold Processing device for crushing, conveying and plastifying thermoplastic synthetic material
FR2759723B1 (fr) * 1997-02-19 1999-03-19 Ind Regionale Batiment Procede de fabrication de tuiles a emboitement
US8715720B2 (en) * 2011-09-14 2014-05-06 Scott Murray Cloud mixer and method of minimizing agglomeration of particulates
CN110355876B (zh) * 2019-07-25 2024-03-08 辽宁科技大学 用于混凝土搅拌的超细粉、水泥、减水剂与水雾化的设备
CN110606384B (zh) * 2019-09-16 2021-05-11 安徽格闰科技控股有限公司 一种智能化自动上料系统
CN113070998A (zh) * 2021-03-04 2021-07-06 安徽致和节能科技有限公司 用于建筑外墙的抹面砂浆生产工艺及其设备
CN113084999B (zh) * 2021-04-21 2022-12-23 怀仁市雅宸瓷业有限责任公司 一种陶瓷制作稀土釉混合设备

Family Cites Families (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3077439A (en) * 1963-02-12 Processing of raw petroleum coke
US3143428A (en) * 1962-10-10 1964-08-04 American Sugar Method and apparatus for agglomeration
DE1924922C3 (de) * 1969-05-16 1975-01-16 Draiswerke Gmbh, 6800 Mannheim Im kontinuierlichen Durchlauf betriebene Mischmaschine
US3636188A (en) * 1969-11-26 1972-01-18 Cities Service Co Process for wet pelletizing carbon black
US3981659A (en) * 1970-06-17 1976-09-21 Cities Service Company Apparatus for drying carbon black pellets
US4050871A (en) * 1974-07-06 1977-09-27 Gottfried Bischoff Bau Kompl. Gasreinigungs-Und Wasserruckkuhlanlagen Kommanditgesellschaft Apparatus for making pellets usable as aggregate or filler
JPS5376168A (en) * 1976-12-17 1978-07-06 Okawara Mfg Pelletization apparatus
DE2756034A1 (de) * 1977-12-15 1979-06-21 Netzsch Maschinenfabrik Verfahren zum aufbereiten von versatzrohstoffen zu keramischer masse
CH628521A5 (de) * 1978-05-20 1982-03-15 Kaiser Wirz Max Verfahren und vorrichtung zum beimischen von fluessigen komponenten in schuettbare gueter.
DE2950248A1 (de) * 1978-12-13 1980-06-26 Netzsch Maschinenfabrik Verfahren und vorrichtung zum aufbereiten von versatzstoffen zu keramischen massen, glasuren oder fritten
DE2926713A1 (de) * 1979-07-03 1981-01-22 Koeppern & Co Kg Maschf Vorrichtung zur befeuchtung von salzgranulaten
FR2482578A1 (fr) * 1980-05-17 1981-11-20 Hoechst Ag Procede pour refroidir le carbure de calcium fondu et appareillage pour sa mise en oeuvre
JPS6055176B2 (ja) * 1982-09-27 1985-12-04 不二パウダル株式会社 造粒方法とその装置
DD216390B1 (de) * 1983-02-28 1987-06-03 Manfred Klins Verfahren und vorrichtung zum herstellen von granulaten
JPS60179130A (ja) * 1984-02-24 1985-09-13 Fuji Paudaru Kk 造粒方法とその装置
SU1318279A1 (ru) * 1985-03-25 1987-06-23 П.Д. Косарев и Ю.И. Макаров Гранул тор

Also Published As

Publication number Publication date
BR8702869A (pt) 1988-03-01
US4897029A (en) 1990-01-30
ES2010689B3 (es) 1989-12-01
DE3619272C2 (ja) 1989-08-31
DE3760522D1 (en) 1989-10-12
ATE46092T1 (de) 1989-09-15
EP0249057A1 (de) 1987-12-16
JPS6367108A (ja) 1988-03-25
DE3619272A1 (de) 1987-12-10

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