EP0222433B1 - Verfahren zur Durchführung von Hochtemperaturreaktionen - Google Patents

Verfahren zur Durchführung von Hochtemperaturreaktionen Download PDF

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Publication number
EP0222433B1
EP0222433B1 EP86201796A EP86201796A EP0222433B1 EP 0222433 B1 EP0222433 B1 EP 0222433B1 EP 86201796 A EP86201796 A EP 86201796A EP 86201796 A EP86201796 A EP 86201796A EP 0222433 B1 EP0222433 B1 EP 0222433B1
Authority
EP
European Patent Office
Prior art keywords
gas
temperature
solids
heated
solid
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
EP86201796A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0222433A1 (de
Inventor
Paul Broedermann
Harald Dr. Sauer
Werner Stockhausen
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.)
GEA Group AG
Original Assignee
Metallgesellschaft 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
Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Priority to AT86201796T priority Critical patent/ATE40923T1/de
Publication of EP0222433A1 publication Critical patent/EP0222433A1/de
Application granted granted Critical
Publication of EP0222433B1 publication Critical patent/EP0222433B1/de
Expired legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B15/00—Fluidised-bed furnaces; Other furnaces using or treating finely-divided materials in dispersion
    • F27B15/003—Cyclones or chain of cyclones

Definitions

  • the invention relates to a method for carrying out high-temperature reactions between hot gas and previously heated solids, which lose their free-flowing properties in the high-temperature treatment, in a substantially vertical conveying path with subsequent cooling and separation from the gas.
  • the object of the invention is to provide a method for carrying out high-temperature reactions between hot gas and previously heated solids, which does not have the known, in particular the aforementioned disadvantages, allows a flawless procedure and is also universally applicable and easy to carry out.
  • the object is achieved in that the method of the type mentioned at the outset is designed in accordance with the invention in such a way that the heated solids are introduced from below and in the direction of conveyance through a burner flame located in the lower region of the conveying path, are passed through a sufficiently long reaction zone and after the end of the Reaction with unchanged flow direction by means of separate addition of coolant downstream in the flow direction cools to at least the temperature at which flowability is achieved.
  • the gas / solid suspension goes through the critical reaction phase between heating to high temperature and cooling to a temperature which makes the gas / solid suspension easy to handle allowed, without redirection and therefore without the possibility of forming a base
  • the downstream separate coolant adding the respective needs justice to dwell in it for order- union high temperature can be adjusted accurately.
  • the average gas velocity to be set in the conveyor section is to be dimensioned such that high relative velocities occur between the solid and the wall.
  • the average gas velocity is usually in the range of 2 and 10 m / sec (indicated as empty tube velocity).
  • the entry of the preheated solid into the conveyor section is advantageously carried out in the form of a gas / solid suspension through the center of an annular burner, the z. B. is operated with gas as fuel.
  • This type of solids supply ensures practically instantaneous heating to the desired temperature. Depending on the feed material and the desired result, it is approximately in the range from 1,300 to 1,700 ° C., preferably between 1,400 and 1,500 ° C.
  • the length of the conveyor line is measured according to the required dwell time depending on the reaction type. As a rule, a few seconds are sufficient, so that the length of the conveyor line is max. 20 m, generally 5 to 15 m, should be.
  • the cooling required after the high-temperature reaction has ended can be carried out using gaseous, liquid or solid coolants. Your entry should be done in such a way that a rapid swirling takes place with the gas / solid suspension and comes into contact with the wall of the conveyor line is avoided. An entry in the tangential direction at high speed perpendicular to or at an angle up to 60 ° against or with the flow direction is particularly expedient.
  • the gas / solid separation takes place in a conventional manner, e.g. B. in a cyclone separator.
  • the solids to be subjected to the high-temperature reaction can be heated in any desired manner.
  • the heating which is generally also associated with a chemical reaction, takes place particularly advantageously in a so-called circulating fluidized bed.
  • the circulating fluidized bed is characterized by the fact that - in contrast to the "classic" fluidized bed, in which a dense phase is separated from the gas space above by a clear density jump - there are distribution states without a defined boundary layer. A leap in density between the dense phase and the dust space above it does not exist, but the solids concentration within the reactor decreases continuously from bottom to top.
  • L. Reh et al describes "fluidized bed processes for the chemical and metallurgical industry, energy conversion and environmental protection", Chem. Ing. Techn. 55 (1983), No. 2, pages 87-93 and the DE-PS 1767628 and US-PS 3 579 616 referenced.
  • the advantage of the circulating fluidized bed lies in the high throughput per reactor area and in the possibility of being able to set the residence time of the solid to be heated so high that the chemical reaction associated with the heating is practically complete. Then only the actual high-temperature reaction is to be carried out within the process according to the invention, ie. H. there are practically no reactions that can also be carried out at a lower temperature level.
  • a preferred embodiment of the invention consists in integrating the high-temperature treatment according to the invention into the overall process with solid heating and final cooling in such a way that the individual gas streams can be used mutually.
  • oxygen-containing gas can be preheated in the cooler, which is then entered in the heating and / or high-temperature treatment stage.
  • the exhaust gas from the conveyor line can be entered in the heating zone.
  • An optimal management of the overall process consists in heating the feed material in a circulating fluidized bed, which in turn has preheaters operated with the exhaust gases, and the final cooling in a fluidized bed cooler with several cooling chambers flowing through one after the other.
  • the solid can be cooled directly and / or indirectly with oxygen-containing gases which are then fed to the conveying section as conveying gas and / or the circulating fluidized bed as fluidizing gas.
  • the fluidizing gases used in the fluidized bed cooler can finally serve as a cooling medium for the conveying section, and the exhaust gases of the conveying section of the circulating fluidized bed can serve as secondary gas.
  • the figure shows a flow diagram of a composite circuit of the aforementioned type.
  • the material to be treated is fed to a last venturi exchanger 2 on the gas side via a metering device 1, heated by the sensible heat of the exhaust gas and separated from the gas in the cyclone separator 3.
  • a conveyor system 4 then leads to a further preheating system, which consists of a Venturi exchanger 5 with associated cyclone separator 6 and a Venturi exchanger 7 with a cyclone separator 8.
  • a bypass line 9 conveyed solid can be fed directly to the venturi exchanger 7 bypassing a preheating stage.
  • the solid is introduced into a circulation system consisting of a fluidized bed reactor 10, return cyclone 11 and return line 12.
  • the fluidized bed reactor 10 is supplied via line 13 with fuel, via line 14 with fluidizing gas and via line 15 with secondary gas.
  • the heated material passes via line 16 to the lower region of the conveyor section 17 and is introduced from below into the burner flame generated from fuel (line 18) and oxygen-containing gas (line 19).
  • line 18 fuel
  • line 19 oxygen-containing gas
  • the gas / solid suspension is discharged via line 21 and separated in the cyclone separator 22. The solid enters the fluidized bed cooler 23, the gas via line 15 as secondary gas into the fluidized bed reactor 10.
  • the fluidized bed cooler 23 is divided into a plurality of cooling chambers through which the solid flows successively and has a total of three cooling sections.
  • oxygen-containing gas is heated, which is then fed via line 19 to the conveyor section 17.
  • the oxygen-containing gas to be fed to the fluidized bed reactor 10 via line 14 is heated.
  • the final cooling of the solid takes place by means of cooling water, which is supplied via conduit gen 24 and 25 is supplied or discharged.
  • the cooled product is discharged via device 26.
  • the fluidizing gas flows used in the fluidized bed cooler 23 are collected and fed via line 20 to the conveyor section 17 as a cooling medium.
  • Filter-moist aluminum hydroxide is to be converted into high-fired aluminum oxide.
  • Aluminum hydroxide with a moisture content of 12% by weight and a temperature of 60 ° C is fed in an amount of 8.69 t / h via the metering device 1 to the Venturi exchanger 2.
  • the gases of 390 ° C. brought in by the cyclone separator 6 the aluminum hydroxide is heated to 160 ° C. and the gas is cooled to approximately the same temperature.
  • the preheated aluminum hydroxide in the venturi exchanger 5 is brought into contact with the hot exhaust gases of the cyclone separator 8 by means of the conveying device 4 in the venturi exchanger 5. This heats up the solid or cools the gas down to approx. 390 ° C.
  • the solid enters the Venturi exchanger 7, which is charged with the exhaust gases of 1,150 ° C. from the circulating fluidized bed.
  • the intimate mixing results in a gas / solid suspension with a temperature of 510 ° C.
  • the solid gets into the circulating fluidized bed.
  • the fluidized bed reactor 10 of the circulating fluidized bed is via line 14 with 2000 Nm 3 / h fluidizing air of 580 ° C (originating from the second section of the fluidized bed cooler 23), via line 15 with 4800 Nm 3 / h secondary air of 1 020 ° C (from the Cyclone separator 22 originating) and supplied via line 13 with 390 Nm 3 / h of natural gas. This results in a temperature of 1,150 ° C., which is practically constant over the entire circulation system formed from fluidized bed reactor 10, return cyclone 11 and return line 12.
  • a solid stream corresponding to the feed quantity is fed continuously via line 16 to the conveying path 17 and heated to 1,400 ° C. by the burner flame or the burner exhaust gases.
  • the burner is fed with 110 Nm 3 Jh natural gas and 1 200 Nm 3 / h air at 650 ° C (originating from the first section of the fluidized bed cooler 23).
  • the high-temperature reaction is complete after approx. 4 sec.
  • the gas / solid suspension is cooled by introducing 3500 Nm 3 / h of air at a temperature of 470 ° C. (originating from the fluidized bed cooler 23). As a result, the suspension cools down to a temperature of 1,020 ° C. at which the free-flowing properties of the solid are ensured.
  • the gas / solid suspension is then separated in the cyclone separator 22, the gas (4,800 Nm 3 / h) to the fluidized bed reactor 10 as secondary gas, and the solid to the fluidized bed cooler 23.
  • the solid is cooled in several sections to a final temperature of 80 ° C.
  • first section 1 200 Nm 3 / h air which is heated to 650 ° C
  • second section 2000 Nm 3 / h air which is heated to 580 ° C
  • third section 20 m 3 / h water which is warmed up from 35 ° C to 65 ° C.
  • gas streams are returned to the process.
  • the production is 5 t / h aluminum oxide with a BET surface area of 3 m 2 / g.

Landscapes

  • Engineering & Computer Science (AREA)
  • Dispersion Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
  • Crystals, And After-Treatments Of Crystals (AREA)
  • Treating Waste Gases (AREA)
  • Catalysts (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
EP86201796A 1985-11-13 1986-10-16 Verfahren zur Durchführung von Hochtemperaturreaktionen Expired EP0222433B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86201796T ATE40923T1 (de) 1985-11-13 1986-10-16 Verfahren zur durchfuehrung von hochtemperaturreaktionen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19853540206 DE3540206A1 (de) 1985-11-13 1985-11-13 Verfahren zur durchfuehrung von hochtemperaturreaktionen
DE3540206 1985-11-13

Publications (2)

Publication Number Publication Date
EP0222433A1 EP0222433A1 (de) 1987-05-20
EP0222433B1 true EP0222433B1 (de) 1989-02-22

Family

ID=6285845

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86201796A Expired EP0222433B1 (de) 1985-11-13 1986-10-16 Verfahren zur Durchführung von Hochtemperaturreaktionen

Country Status (12)

Country Link
EP (1) EP0222433B1 (es)
JP (1) JPS62114642A (es)
AT (1) ATE40923T1 (es)
AU (1) AU582025B2 (es)
BR (1) BR8605585A (es)
CA (1) CA1276433C (es)
CZ (1) CZ815386A3 (es)
DE (2) DE3540206A1 (es)
ES (1) ES2008033B3 (es)
GR (2) GR880300146T1 (es)
HU (1) HU206279B (es)
IN (1) IN164695B (es)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3725512A1 (de) * 1987-07-29 1989-02-09 Kettenbauer Gmbh & Co Verfahre Schwebegas-reaktor
DE19750475C1 (de) * 1997-11-14 1999-04-08 Treibacher Schleifmittel Ag Verfahren und Aggregat zur thermischen Behandlung von feinkörnigen Stoffen
CN112858384B (zh) * 2021-01-08 2023-06-23 湖南中冶长天节能环保技术有限公司 一种活性炭烟气净化装置高温检测-冷却处理方法及系统

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2350768C3 (de) * 1973-10-10 1982-09-02 Krupp Polysius Ag, 4720 Beckum Verfahren zum Brennen oder Sintern von feinkörnigem Gut
DE2846584C2 (de) * 1978-10-26 1984-12-20 Klöckner-Humboldt-Deutz AG, 5000 Köln Verfahren und Vorrichtung zur Wärmebehandlung von feinkörnigem Gut
FR2465694A1 (fr) * 1979-09-24 1981-03-27 Lafarge Sa Procede de fabrication de produits a base de silicates et/ou aluminates calciques
ES509795A0 (es) * 1982-02-22 1983-12-16 Empresa Nac Hulleras Norte Metodo para la fabricacion de clinker de cemento.
FR2554107B1 (fr) * 1983-10-28 1986-02-21 Fives Cail Babcock Procede et appareil pour la calcination des matieres minerales reduites en poudre
JPS60156541A (ja) * 1984-01-27 1985-08-16 Denki Kagaku Kogyo Kk 無機質溶融球状体の製造用溶融炉
FR2563119B1 (fr) * 1984-04-20 1989-12-22 Creusot Loire Procede de mise en circulation de particules solides a l'interieur d'une chambre de fluidisation et chambre de fluidisation perfectionnee pour la mise en oeuvre du procede

Also Published As

Publication number Publication date
ATE40923T1 (de) 1989-03-15
JPS62114642A (ja) 1987-05-26
GR3000062T3 (en) 1990-10-31
BR8605585A (pt) 1987-08-18
CA1276433C (en) 1990-11-20
HUT45921A (en) 1988-09-28
DE3540206A1 (de) 1987-05-14
CZ815386A3 (en) 1994-12-15
ES2008033B3 (es) 1989-07-16
AU6504086A (en) 1987-05-21
IN164695B (es) 1989-05-13
AU582025B2 (en) 1989-03-09
GR880300146T1 (en) 1989-03-08
DE3662164D1 (en) 1989-03-30
EP0222433A1 (de) 1987-05-20
HU206279B (en) 1992-10-28

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