EP0000739A1 - 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
EP0000739A1
EP0000739A1 EP78100518A EP78100518A EP0000739A1 EP 0000739 A1 EP0000739 A1 EP 0000739A1 EP 78100518 A EP78100518 A EP 78100518A EP 78100518 A EP78100518 A EP 78100518A EP 0000739 A1 EP0000739 A1 EP 0000739A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
zone
fuel
cooling
air flow
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.)
Granted
Application number
EP78100518A
Other languages
German (de)
English (en)
Other versions
EP0000739B1 (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 DE19772735140 external-priority patent/DE2735140A1/de
Priority claimed from DE19772735084 external-priority patent/DE2735084A1/de
Priority claimed from DE19782822395 external-priority patent/DE2822395A1/de
Priority claimed from DE19782822377 external-priority patent/DE2822377A1/de
Priority claimed from DE19782822419 external-priority patent/DE2822419A1/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.
  • cement-lime gypsum 1970, pp. 343 to 347 and DE-AS 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 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 of Cement clinker with particularly low alkali content permitted.
  • the fluidized bed is relieved of a large part of the heat work that would otherwise have to be done, which has significant 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 significantly improved combustion conditions in the fluidized bed due to the strong precalcination and the rapid, even distribution of precalcined material and fuel in the fluidized bed also ensure good functioning of the cooling zone arranged directly under the fluidized bed and in particular closes Be drive disruptions due to caking of goods in the cooling zone.
  • the method according to the invention thus delivers very homogeneously fired clinker beads of approximately uniform grain size.
  • the rapid and uniform distribution of the pre-calcined material in the fluidized bed can be 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 very high pulse between 5 and 10 kps.
  • a cross-sectional constriction advantageously sets approximately the same gap level as in the upper region of the fluidized bed, expediently a gap degree between 0.5 and 0.8, preferably between 0.6 and 0.7.
  • 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 at which the precalcined material is fed. Another part of the fuel can be on the surface of the fluidized bed or together with the recycled part of the fired material are introduced into the fluidized bed.
  • 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 quantity of material located in the fluidized bed is 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 as a function of the gas pressure (by either the quantity of material discharged from the fluidized bed or the cooling zone or the quantity introduced into the fluidized bed. Quantity or both quantities can be controlled accordingly).
  • the quantity of material located in the fluidized bed is expediently regulated 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 in such a differential pressure control .
  • the preheating and precalcination zone is expediently supplied with an adjustable part of the exhaust gases from the fluidized bed and preferably an adjustable part of the cooling air flow, while the remaining part of the exhaust gases from the fluidized bed is 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) of the reaction chamber 3 and additional fuel (arrow 10) is very high, preferably 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 so that in the lower region of the fluidized bed intended for the introduction of the precalculated material, ie approximately at the level of the conveying lines 13, 14, approximately the same gap level, preferably between 0.6 and 0.7, as set in the upper region of the fluidized bed.
  • the pre-calcined material is fired into cement clinker. After a certain clinker size has been reached, the fired material reaches 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 fan 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 - expediently below the level of the conveying lines 13, 14 - as additional sides air are introduced into the fluidized bed 4 (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 can be diverted, bypassing the precalcination zone 2 and the preheater 1, in particular if the alkali content is high (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 material introduction, 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 being discharged by the controller 39 direction 20 in each case only the quantity of good located above the target value is discharged from the cooling zone 5 and thus from the fluidized bed 4 or by supplying a quantity of good missing from the target value in each case through the good feed metering device 41.
  • 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 / seed clinker is 4: 1.
  • the preheated and pre-calcined material is introduced into the fluidized bed 4 at a temperature of approximately 840 ° C.
  • 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 ⁇ and 8.8%> 200 ⁇ .
  • the air volumes can be selected as follows: 1.00 Nm 3 / kg of clinker are fed to the cooling zone 5 from below. Of this, 0.33 Nm 3 / kg Kl get directly into the fluidized bed from below (arrows 23), while 0.67 Nm 3 / kg Kl are drawn off laterally (arrow 24) from the cooling zone. From this latter part, 0.17 Nm 3 / kg Kl 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 Kl directly (arrow 31) Precalcination zone 2 are supplied. An equal amount of air (0.5 Nm '/ kg Kl) 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 800 and 1200 mm WS, the differential pressure between the pressure measuring points 35 and 37 between 250 and 400 mm WS.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Organic Chemistry (AREA)
  • Structural Engineering (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Furnace Details (AREA)
  • Curing Cements, Concrete, And Artificial Stone (AREA)
  • Vertical, Hearth, Or Arc Furnaces (AREA)
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
DE19772735140 DE2735140A1 (de) 1977-08-04 1977-08-04 Verfahren und anlage zur herstellung von zement
DE2735084 1977-08-04
DE2735140 1977-08-04
DE19772735084 DE2735084A1 (de) 1977-08-04 1977-08-04 Verfahren und anlage zur herstellung von zement
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
DE2822377 1978-05-23
DE19782822419 DE2822419A1 (de) 1978-05-23 1978-05-23 Verfahren und anlage zur herstellung von zement
DE2822395 1978-05-23

Publications (2)

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

Family

ID=27510504

Family Applications (1)

Application Number Title Priority Date Filing Date
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)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2474478A1 (fr) * 1980-01-30 1981-07-31 Creusot Loire Procede et dispositif de fabrication de clinker de ciment
FR2519128A1 (fr) * 1981-12-28 1983-07-01 Ishikawajima Harima Heavy Ind Dispositif pour la cuisson de materiaux en poudre
EP0059508B1 (fr) * 1981-02-28 1984-12-05 Metallgesellschaft Ag Procédé de préparation de clinker de ciment
EP0165034A2 (fr) * 1984-06-11 1985-12-18 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Procédé et appareil pour la fabrication de clinker de ciment blanc
EP0463156A1 (fr) * 1990-01-18 1992-01-02 Gas Research Institute Procede et four vertical a suspension de production de ciment

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5829112A (ja) * 1981-08-12 1983-02-21 Pioneer Video Corp 磁気記録再生方法
US5188668A (en) * 1991-08-06 1993-02-23 Gas Research Institute Cement advanced furnace and process

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
NL6908171A (fr) * 1968-05-30 1969-12-02

Family Cites Families (4)

* 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
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

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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
NL6908171A (fr) * 1968-05-30 1969-12-02

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2474478A1 (fr) * 1980-01-30 1981-07-31 Creusot Loire Procede et dispositif de fabrication de clinker de ciment
EP0033688B1 (fr) * 1980-01-30 1984-02-22 Creusot-Loire Entreprises Procédé et dispositif de fabrication de clinker de ciment
EP0059508B1 (fr) * 1981-02-28 1984-12-05 Metallgesellschaft Ag Procédé de préparation de clinker de ciment
FR2519128A1 (fr) * 1981-12-28 1983-07-01 Ishikawajima Harima Heavy Ind Dispositif pour la cuisson de materiaux en poudre
EP0165034A2 (fr) * 1984-06-11 1985-12-18 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Procédé et appareil pour la fabrication de clinker de ciment blanc
EP0165034A3 (en) * 1984-06-11 1987-07-29 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Method and apparatus for producing white cement clinker
EP0463156A1 (fr) * 1990-01-18 1992-01-02 Gas Research Institute Procede et four vertical a suspension de production de ciment
EP0463156A4 (en) * 1990-01-18 1992-07-15 Gas Research Institute Cement shaft suspension furnace and process

Also Published As

Publication number Publication date
PT68379A (de) 1978-09-01
EP0000739B1 (fr) 1981-04-15
CA1115297A (fr) 1981-12-29
IT7826440A0 (it) 1978-08-03
US4213790A (en) 1980-07-22
DK347078A (da) 1979-02-05
DE2860617D1 (en) 1981-05-07
IT1097686B (it) 1985-08-31
JPS5434325A (en) 1979-03-13
JPS5711862B2 (fr) 1982-03-06
GR64304B (en) 1980-03-03

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