EP0177090B1 - Device for the production of inflammable solid/gas suspensions - Google Patents

Device for the production of inflammable solid/gas suspensions Download PDF

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Publication number
EP0177090B1
EP0177090B1 EP85201500A EP85201500A EP0177090B1 EP 0177090 B1 EP0177090 B1 EP 0177090B1 EP 85201500 A EP85201500 A EP 85201500A EP 85201500 A EP85201500 A EP 85201500A EP 0177090 B1 EP0177090 B1 EP 0177090B1
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EP
European Patent Office
Prior art keywords
burner
diffuser
gas
mixing
mixing stage
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 - Lifetime
Application number
EP85201500A
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German (de)
French (fr)
Other versions
EP0177090A2 (en
EP0177090A3 (en
Inventor
Adalbert Bartsch
Georg Dr. Rer. Nat. Gospos
Lars Kersten
Arno Wolfgang Bartsch
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Aurubis AG
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Norddeutsche Affinerie AG
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Publication date
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Publication of EP0177090A3 publication Critical patent/EP0177090A3/en
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D1/00—Burners for combustion of pulverulent fuel
    • F23D1/02—Vortex burners, e.g. for cyclone-type combustion apparatus
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/312—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof
    • B01F25/3121—Injector mixers in conduits or tubes through which the main component flows with Venturi elements; Details thereof with additional mixing means other than injector mixers, e.g. screens, baffles or rotating elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B01F33/82—Combinations of dissimilar mixers
    • B01F33/821—Combinations of dissimilar mixers with consecutive receptacles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J9/00—Preventing premature solidification of molten combustion residues
    • 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
    • B01F23/30—Mixing gases with solids
    • B01F23/32—Mixing gases with solids by introducing solids in gas volumes

Definitions

  • the invention relates to a device for generating ignitable solid / gas suspensions with a vertical feed for the solid / primary gas suspension and a secondary gas channel concentrically surrounding it, and a mixing stage for both streams.
  • burners - can have uniformly arranged, partially stationary, partially movable feeds which initially produce a mixture of fuel and primary air and then combine them with secondary air (DE-PS 891 597).
  • secondary air DE-PS 891 597.
  • the primary air should be given a swirl by means of an insert in the primary air pipe before the addition of coal dust, which after the addition of the coal dust result in a swirled coal dust / air suspension should.
  • the swirl of the air is greatly reduced or almost completely eliminated, and the desired good mixing of all components is therefore not achieved.
  • a swirl chamber which has the outline shape of a logarithmic spiral in cross section and an inlet opening which is larger than the outlet opening.
  • a feed line for the solid leads through the inlet opening and runs coaxially to the pole and ends approximately in the cross-sectional plane of the outlet opening.
  • a device known from DE-OS 32 12 100 for carrying out metallurgical processes, in particular of sulfidic non-ferrous metal concentrates provides an approximately vertically arranged lance which has gas / solid mixing devices and an acceleration nozzle which is surrounded in a ring by a burner nozzle.
  • the burner nozzle is equipped with a feed for the fuel / ignition mixture.
  • the heterogeneous mixture of solid, melt and gas is directed at the melt in a hearth furnace in a small nozzle at the speed of sound.
  • the residence times of the solid in the jet are extremely short, so that the unreacted particle jet triggers a violent reaction in the bath and a strong bath turbulence.
  • the disadvantage of the known device is that the gas / solid suspension cannot be mixed sufficiently and the extremely short residence time of the solid particles in the gas jet, so that the known device can only be operated in reactors with melt baths.
  • GB-PS 218701 shows an injector burner for pulverized or liquid fuel, and several Venturi mixing stages can also be arranged one behind the other.
  • a device for generating ignitable solid / gas suspensions is known with a vertical feed for the solid / primary gas suspension and a concentrically surrounding secondary gas channel and mixing stage for both streams, which consists of two series-connected mixing stages, whereby the first mixing stage is surrounded concentrically by the secondary gas channel and the second mixing stage is designed as a venturi diffuser and in the area of the diffuser outlet there is a gas flame-holding burner surrounding it in a ring shape.
  • the known device is used to burn pulverized coal.
  • the invention is based on the object of providing a device for producing ignitable solid / gas suspensions, in particular of sulfidic ore concentrates, which does not have the disadvantages of the known devices, particularly those mentioned above, and which permits simple operation with simple construction.
  • the feeder for the solid / primary gas suspension which precedes the two mixing stages (I, 11) is designed as an expansion pot (2) which is arranged tangentially , essentially horizontally opening inlet line (1) for the supplied solid / primary gas suspension, that the first mixing stage (I) is also designed as a venturi diffuser and that in the second mixing stage (11) in the area of the cooling chamber (18 ) provided diffuser outlet which is attached to this ring-shaped gas flame holding burner (G) with alternating fuel gas and oxygen nozzles (14, 14a).
  • the primary and secondary gas required to generate the ignitable solid / gas suspension naturally contains oxygen. Air, oxygen-enriched air or technically pure oxygen itself can be used.
  • an ignitable gas / solid suspension fed into the device is completely homogenized in the mixing stages and at the output of the second mixing stage a reliable ignition process and a practically complete conversion of the solid particles into the molten state is effected within the fuel jet .
  • the gas flame retardant burner is essential for the spontaneous ignition of the fuel jet, for flame maintenance and for a heat energy boost in the backflow area. The result of this burner design is a considerable flattening of the ignition profile cone.
  • a solid / primary gas suspension such as complex sulfidic ore concentrate
  • the relaxation pot expediently has an inner ceramic wear protection layer, for example made of concrete.
  • a gas / solid suspension enters the venturi diffuser of the first mixing stage at a flow rate of approximately 15 m / sec.
  • the mixing stage designed as a venturi diffuser consists of the convergent orifice part 5, the cylindrical mixing section 6 and the diffuser part 7.
  • the venturi diffuser of the mixing stage I is connected to the cyclone-like expansion pot 2 via a flange connection.
  • a gas stream laden with, for example, about 17 to 27 kg of solids / m is accelerated and reaches a high degree of turbulence in the cylindrical mixing section 6.
  • the diffuser part 7 has an opening or inclination angle of approximately 3 to 7 degrees. An angle of inclination of 5 ° has proven to be expedient.
  • the device parts 5, 6, 7 of mixing stage I serve to homogenize a solid / gas suspension fed in with a swirl and to break down the swirl.
  • the high degree of turbulence produces a movement of the fluid particles transversely to the flow axis, which, with a corresponding dwell time, remaining relative movement between gas and solid as well as between finer and coarser solid particles, results in an effective homogenization of the mixture flow. Due to the length of the mixing section 6 of, for example, 4 to 5 times the diameter, vortices or jet separations, which result in the convergent part 5, are reduced before the jet enters the diffuser 7. The low angle of inclination of the diffuser avoids jet and therefore density irregularities.
  • the secondary gas channel 8 is expediently designed as a pipe bend, the vertical part of which concentrically surrounds the diffuser. In the area of the diffuser outlet 7, the secondary gas channel merges into a cylindrical part 10 of a smaller diameter, this smaller diameter practically corresponding to the diameter of the diffuser outlet.
  • the secondary gas channel is used to introduce a reaction gas stream, e.g. an air flow enriched with oxygen.
  • the cross-sectional transition 9 of the secondary gas channel 8 into the mixing section 10 is designed without a cross-sectional jump, for example curved (convex, concave) or conical. In this way, possible solid deposits that lead to loading irregularities or irregular material flow density as a result of unstable behavior are avoided.
  • Vortex formation would lead to irregularities in the beam ignition - for example completely or selectively limited re-ignition in the diffuser - and thus to considerable disturbances, for example caking.
  • Cross-sectional transition, conicity and mouth diameter of the diffuser part 7 are thus coordinated with one another in the device according to the invention in such a way that complete mixing of the two streams - secondary gas stream, solid / gas suspension stream - and homogeneous solid distribution occurs in the mixing stage 11.
  • the device according to the invention is operated at a speed of the secondary gas flow which is higher than that of the solid / gas suspension flow, a relative speed of 5 to 15 m / sec being set.
  • a second venturi diffuser 11 is connected vertically behind the first and connected to it via a flange 10a.
  • This second venturi diffuser forms the mixing stage 11.
  • the angle of inclination of the diffuser is 1.5 to 4, preferably 2 to 3 degrees.
  • An angle of inclination of 2.5 ° has proven to be particularly advantageous.
  • the torch arranged in a ring has separate distributor pipes 16 for fuel gas and oxygen in each case.
  • the respective separate nozzles 14, 14a for fuel gas and oxygen are arranged alternately and coaxially on a ring circle at a pitch of approximately 40 mm.
  • the distance from the tear-off edge 17 is approximately 35 to 40 mm.
  • the nozzle heads are by means of screw threads interchangeably connected to the supply members 15, 15a.
  • the feed members 15, 15a are passed through the cooling chamber 18 and welded in the upper and lower burner bottoms so as to be watertight.
  • An inner guide ring 19 serves for the uniform distribution of the cooling water.
  • the annular cooling chamber has a height of 10 to 30 and preferably 15 to 20 cm.
  • Stainless steel containing chromium and nickel (for example stainless steel of material no. 4571) is used as the material for the gas flame-retardant burner.
  • a cutting-like tear-off edge 17 projecting beyond the plane is attached.
  • This protruding tear-off edge of a height between 10 and 20 mm serves to precisely fix the start of ignition outside the burner mouth, but directly on it. This measure causes the high-temperature returning combustion gases and the solid / gas mixture jet to meet at an acute angle. In this way, the ring base of the gas flame retardant burner offers practically no possibilities of attack for solid batches.
  • the tear-off edge 17 prevents ignition irregularities which can occur in the case of a fluid jet which is disturbed by eddies before exiting the venturi diffuser 11. These irregularities place stress on the inside of the diffuser due to early reaction, overheating and caking.
  • Suitable protective layers are those made of e.g. Cobalt or zirconium, which at the operating temperatures of the device according to the invention tend neither to scale nor to alloy with molten constituents of the solid suspension, such as copper or lead.
  • the tear-off edge 17 is - like the other construction parts of the device - expediently made entirely or partially of chromium-nickel steel. To further improve the service life, it can be useful to coat the outer area, namely the cutting edge of the tear-off edge, by melting or sintering a material based on e.g. To protect cobalt or zirconium. The choice of material depends on the solvency of the solid-liquid components in the reaction jet.
  • the materials withstand the operating conditions of the device according to the invention from high temperature and exit speeds of the mixture jet of approximately 19 to 28 m / s without damage.
  • the length of the combustion shaft is approximately 180 cm.
  • d A can be larger and thus the flame length x and the length of the burner shaft smaller.
  • the cyclone chamber has a length of usually about 1 m and a diameter of about 95 cm.
  • a further embodiment of the invention provides, in the region of the confluence of the combustion shaft 13 in the horizontal combustion chamber 20, a two-chamber premix burner, known per se, which acts as a pilot burner.
  • This pilot burner is mounted in the bottom of the horizontally lying cyclone chamber, preferably in the jacket of the cyclone, and the jet axis is directed towards the lower inner wall of the cyclone chamber.
  • a spark plug 29 is provided within a hood made of refractory ramming compound. The stable flame jet emerging from the hood is directed into a suddenly expanded cylindrical combustion channel 24.
  • the two-chamber premix burner 23 in the ignition channel 24 is axially equipped with a high-pressure full jet nozzle 25.
  • a reducing agent such as oil, can be introduced into this nozzle and injected into the cyclone chamber through the gas fuel jet of the premix burner 23.
  • the reducing agent is used in a manner known per se to reduce slag which is expediently reduced before the melt runs out of the cyclone chamber into a usually downstream intermediate vessel.
  • the nozzle is advantageously replaced by the (not yet ignited) gas / air Electricity cooled and nozzle damage caused by cracking processes avoided. Flame monitoring can be carried out by means of optical devices via the central connecting piece 28.
  • the pilot burner 23 can be operated in a dependent circuit with all other burners to ensure safe melting operation.
  • the device according to the invention is particularly suitable for the pyrometallurgical treatment of sulfidic non-ferrous metal ores or sulfidic non-ferrous metal ore concentrates.
  • a rapid and complete ignition of the mixture jet emerging from the mixing stages with a small flame length and high flame temperature is achieved at a short distance from the burner mouth. This results in a practically complete transition of the solid particles into the molten state at jet exit speeds in the known range of below 30 m / sec.
  • the further treatment of the melt film running on the inner wall of the cyclone is carried out in a known manner. This means that at the exit of the cyclone chamber, the melt film collected runs off as a jet through an exit slot into a secondary chamber and reaches a forehearth via a vertical chute. In the forehead, the melting components of different weights, such as stone and slag, are separated and removed separately.
  • the device according to the invention is applicable to the treatment of a large number of solids.
  • Sulfidic non-ferrous metal ores or non-ferrous metal concentrates and sulfidic iron ores or iron ore concentrates are particularly suitable. However, it is also ideally suited for the treatment of oxidic, possibly pre-reduced iron ores or iron ore concentrates as well as for the treatment of metallurgical intermediates.
  • the solid / gas suspension to be used is introduced through the inlet connection 1 into the expansion pot 2.
  • This has a conical part in 3 and a cylindrical part in 4 as a connecting piece.
  • This connecting piece is connected to the mixing stage I via a flange 4a.
  • This mixing stage is formed from a venturi diffuser with the convergent part 5, the cylindrical mixing section part 6 and the diffuser part 7.
  • the venturi diffuser is surrounded concentrically by the secondary gas channel 8.
  • the secondary gas channel is designed as a pipe bend, which tapers via the transition 9 into a cylindrical mixing section part 10 of reduced diameter.
  • the mixing stage is connected to mixing stage II via flange 10a.
  • the venturi diffuser 11 is equipped with an annular gas flame-holding burner G at its outlet part.
  • the gas flame-holding burner has separate manifolds 16 for fuel gas and oxygen, respectively, which are connected to the separate feed pipes 15, 15a for fuel gas and oxygen.
  • the supply pipes 15, 15a are provided with replaceable nozzles 14, 14a at their outlet via screw threads. With 17 an annular tear-off edge is designated.
  • the cooling chamber 18 is provided with an inner guide ring 19 for the uniform distribution of the pressurized cooling water.
  • the burner sits on the burning shaft 13 by means of flange 13a.
  • the burner mouth 12 flows seamlessly into the burner shaft 13.
  • FIG. 2 shows the transition or the opening of the combustion shaft 13 into the horizontal cyclone chamber 20.
  • a two-chamber premix burner 23 with ignition channel 24 is installed in the cylinder base 22 of the cyclone chamber 21.
  • the beam direction 27 of this burner is directed onto the lower inner wall of the cyclone chamber.
  • a spark plug 29 ignites the gas mixture 28 and the jet 26 of liquid fuel emerging via the full jet nozzle 25.
  • 7,000 kg / h of copper concentrate are fed from upstream bunker, drying, distributor and mixing systems with 390 m 3 of primary air as carrier gas via a delivery pipe to the inlet port 1 of the expansion vessel 2.
  • Si0 2 is supplied in the form of sand in an amount of 1.3 t / h to the concentrate air stream before entering the nozzle 1 in order to bind the FeO that forms in a slag.
  • Si0 2 is supplied in the form of sand in an amount of 1.3 t / h to the concentrate air stream before entering the nozzle 1 in order to bind the FeO that forms in a slag.
  • sand with a residual moisture of 0.1% and a grain size of up to 0.7 mm is used.
  • the fluid flow from 7,000 kg / h concentrate, 1,300 kg / h sand and 350 m 3 / h conveying air passes through the connector 1 into the expansion vessel 2 and enters the mixing section 6 of the mixing stage II via the constriction 5, in which the Beam is accelerated to a speed of 39 m / s.
  • the ratio L: D is 5.
  • the beam then passes through the transition from mixing section 6 to diffuser 7, which is infinitely variable with a radius of 100 mm, and has an inclination of 5 angular degrees and a largest diameter of 95 mm.
  • the homogenized fluid jet emerges from the venturi diffuser 7 at a speed of, for example, 15.9 m / s and together with the secondary flow mixture of 600 m 3 / h of air with 1,800 m 3 / h of oxygen within the secondary gas channel 8 into the catching part of the mixing section 10 of the Venturi mixer stage II.
  • the relative speed between the jet emerging from the diffuser 7 and the secondary stream surrounding it within the secondary gas channel 8 is 9.3 m / s.
  • the jet mixture is now transferred into the diffuser 11 of the mixing stage II.
  • the diffuser 11 has an inclination of 2.5 degrees.
  • the still unignited fluid jet emerges from the burner mouth 12 at a mean speed of 18.5 m in a vortex-free manner.
  • the amount of fuel used for flame control is approx. 30 m 3 natural gas with a concentrate throughput of 6,000 to 10,000 kg / h.
  • the homogenized fluid jet emerges in a vortex-free manner via the tear-off edge 17, without detachments and vortex formation occurring at the end of the diffuser 11 in the boundary layer region.
  • the directed jet plunges freely into the combustion shaft 13 via the tear-off edge 17 at an acute angle - and via the highly reactive return flow surrounding it, which is intensified by the flame-holding burner.
  • an ignition profile according to FIG. 3 results in the region of the entry into the combustion shaft 13.
  • the reacting solid particles become partly deflected in the direction of the cooled shaft wall and in the arrangement according to the invention reacted and melted onto the shaft wall.
  • the melt film running down the shaft wall solidifies to a thickness that corresponds to the heat transfer to the cooling pipes of the shaft wall and forms a protective layer on the cooling pipe jacket.
  • the edge-bound portion of the melt runs off without residue and with the desired stabilization in the direction of the cyclone vessel.
  • the burnout takes place within the combustion shaft according to the diagram of FIG. 4, the beam according to FIG. 4 shortly reaching x the maximum temperature of 1,640 ° C. and shortly thereafter entering the cyclone chamber 20 tangentially to separate the gas phase and melt.
  • the process is autogenous.
  • additional fuel e.g. Coal dust, fed.
  • the exhaust gas emerging from the cyclone vessel 20 in the axial direction has a temperature of 1,320 ° C. and contains 56% SO 2 and 5% residual oz.
  • the flame-monitored pilot burner 23 arranged in the cyclone vessel wall 22 serves for ignition and flame protection of the entire melting unit during the melting operation and for the ignition and monitoring of the natural gas flame during the heating phase, in which heating takes place up to an oven chamber temperature of 1200 ° C.
  • the gas nozzles of the flame-retarding burner G are operated with up to 150 m 3 / h natural gas without oxygen.
  • the required oxygen is supplied in the form of air via the secondary gas channel 8, mixing section 10 and diffuser 11 to the combustion shaft 13.
  • the two-chamber premix burner 23 is equipped with a high-pressure full jet nozzle, which for the purpose of reduction in the melting area of the cyclone 20 with a reducing agent, e.g. Oil.
  • a reducing agent e.g. Oil

Description

Die Erfindung betrifft eine Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen mit einer vertikalen Zuführung für die Feststoff/Primärgas-Suspension und einem diese konzentrisch umgebenden Sekundärgaskanal sowie Mischstufe für beide Ströme.The invention relates to a device for generating ignitable solid / gas suspensions with a vertical feed for the solid / primary gas suspension and a secondary gas channel concentrically surrounding it, and a mixing stage for both streams.

In der Feuerungstechnik, aber auch bei metallurgischen Prozessen ist es häufig erforderlich, Feststoffe, die verbrannt oder einer chemischen Umsetzung unterworfen werden sollen, in Form einer Suspension dem eigentlichen Feuerungsraum oder Reaktor zuzuführen.In furnace technology, but also in metallurgical processes, it is often necessary to add solids to the actual furnace or reactor in the form of a suspension that are to be burned or subjected to a chemical reaction.

Zur Erzeugung derartiger Suspensionen bekannte - häufig als Brenner bezeichnete - Vorrichtungen können gleichmäßig ineinander angeordnete, teilweise ortsfeste, teilweise bewegliche Zuführungen besitzen, die zunächst ein Gemisch von Brennstoff und Primärluft erzeugen und diese anschließend mit Sekundärluft vereinigen (DE-PS 891 597). Um u.a. eine gute Vermischung von Kohlenstaub und Luft zu erreichen, soll bei einer Ausführungsform der bekannten Vorrichtung der Primärluft vor der Zugabe von Kohlenstaub mittels eines Einsatzes im Primärluftrohr ein Drall gegeben werden, der nach der Zugabe des Kohlenstaubes eine in Drall versetzte Kohlenstaub/Luft-Suspension ergeben soll. Tatsächlich wird jedoch infolge der - verglichen mit der Luft - hohen Masse des nachträglich zugegebenen Kohlenstaubs der Drall der Luft stark reduziert bzw. nahezu ganz abgebaut und damit die angestrebte gute Vermischung aller Komponenten nicht erzielt.Devices known to produce such suspensions - often referred to as burners - can have uniformly arranged, partially stationary, partially movable feeds which initially produce a mixture of fuel and primary air and then combine them with secondary air (DE-PS 891 597). To i.a. To achieve a good mixing of coal dust and air, in one embodiment of the known device the primary air should be given a swirl by means of an insert in the primary air pipe before the addition of coal dust, which after the addition of the coal dust result in a swirled coal dust / air suspension should. In fact, however, due to the high mass of the subsequently added coal dust compared to the air, the swirl of the air is greatly reduced or almost completely eliminated, and the desired good mixing of all components is therefore not achieved.

Bei der aus der DE-AS 12 92 631 bekannten Vorrichtung zum Vermischen von Feststoffteilen in einem gasförmigen Trägermittel ist eine Wirbelkammer vorgesehen, die im Querschnitt die Umrißform einer logarithmischen Spirale und eine gegenüber der Auslaßöffnung größere Einlaßöffnung besitzt. Durch die Einlaßöffnung führt eine koaxial zum Pol verlaufende und etwa in der Querschnittsebene der Auslaßöffnung endende Zuführleitung für den Feststoff. Bei Anwendung dieser Vorrichtung tritt der Nachteil auf, daß der Feststoff mit hoher vertikaler Bewegungskomponente in den Brenn- und Reaktionsraum gelangt und vor Ausreaktion Kontakt mit dessen Wandung erhält.In the device known from DE-AS 12 92 631 for mixing solid parts in a gaseous carrier, a swirl chamber is provided which has the outline shape of a logarithmic spiral in cross section and an inlet opening which is larger than the outlet opening. A feed line for the solid leads through the inlet opening and runs coaxially to the pole and ends approximately in the cross-sectional plane of the outlet opening. When this device is used, the disadvantage arises that the solid enters the combustion and reaction chamber with a high vertical movement component and is in contact with its wall before the reaction takes place.

Bei dem aus DE-AS 22 53 074 bekannten Verfahren zur pyrometallurgischen Behandlung von feinkörnigen, bei Behandlungstemperaturen schmelzflüssige Produkte ergebenden Feststoffen mit sauerstoffreichen Gasen und gegebenenfalls Energieträgern unter Verwendung einer Zyklonkammer werden sulfidische NE-Metallerze oder Metallerzkonzentrate, sauerstoffreiche Gase und gegebenenfalls Energieträger unterhalb der Reaktionstemperatur zu einer Suspension vermischt, mit einer eine Rückzündung ausschließenden Geschwindigkeit in eine vertikale Brennstrecke eingetragen und dort zur Reaktion gebracht. Die gebildete, überwiegend schmelzflüssige Partikeln enthaltende Suspension wird in die Zyklonkammer eingetragen.In the process known from DE-AS 22 53 074 for the pyrometallurgical treatment of fine-grained solids resulting in products which are molten at treatment temperatures with oxygen-rich gases and, if appropriate, energy sources using a cyclone chamber, sulfidic non-ferrous metal ores or metal concentrates, oxygen-rich gases and, if appropriate, energy sources below the reaction temperature mixed in a suspension, entered at a speed excluding re-ignition into a vertical burning section and reacted there. The suspension formed, which contains predominantly molten particles, is introduced into the cyclone chamber.

Eine aus DE-OS 32 12 100 bekannte Vorrichtung zur Durchführung metallurgischer Prozesse von insbesondere sulfidischen NE-Metallkonzentraten sieht eine annähernd vertikal angeordnete Lanze vor, die Gas/Feststoff-Mischeinrichtungen und eine Beschleunigungsdüse aufweist, welche von einer Brennerdüse ringförmig umgeben ist. Die Brennerdüse ist mit einer Zuführung für das Brennstoff-/Zündgemisch ausgestattet. Bei der vorbekannten Vorrichtung wird in einer kleinen Düse mit Schallgeschwindigkeit die heterogene Mischung von Feststoff, Schmelze und Gas auf die in einem Herdofen befindliche Schmelze gerichtet. Die Verweilzeiten des Feststoffes im Strahl sind extrem kurz, so daß der nicht ausreagierte Partikelstrahl eine heftige Reaktion im Bad und eine starke Badturbulenz auslöst. Bei der vorbekannten Vorrichtung liegt der Nachteil in einer nicht ausreichenden Mischmöglichkeit der Gas/Feststoff-Suspension und der extrem kurzen Verweilzeit der Feststoffpartikel im Gasstrahl, so daß die vorbekannte Vorrichtung nur in Reaktoren mit Schmelzbädern betrieben werden kann.A device known from DE-OS 32 12 100 for carrying out metallurgical processes, in particular of sulfidic non-ferrous metal concentrates, provides an approximately vertically arranged lance which has gas / solid mixing devices and an acceleration nozzle which is surrounded in a ring by a burner nozzle. The burner nozzle is equipped with a feed for the fuel / ignition mixture. In the known device, the heterogeneous mixture of solid, melt and gas is directed at the melt in a hearth furnace in a small nozzle at the speed of sound. The residence times of the solid in the jet are extremely short, so that the unreacted particle jet triggers a violent reaction in the bath and a strong bath turbulence. The disadvantage of the known device is that the gas / solid suspension cannot be mixed sufficiently and the extremely short residence time of the solid particles in the gas jet, so that the known device can only be operated in reactors with melt baths.

Der Druckschrift GB-PS 218701 ist ein Injektor-Brenner für pulverisierten oder flüssigen Brennstoff zu entnehmen, wobei auch mehrere Venturi-Mischstufen hintereinander angeordnet sein können.GB-PS 218701 shows an injector burner for pulverized or liquid fuel, and several Venturi mixing stages can also be arranged one behind the other.

Aus DE-OS 1451 567 ist eine Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen bekannt mit einer vertikalen Zuführung für die Feststoff/Primärgas-Suspension und einem diese konzentrisch umgebenden Sekundärgaskanal sowie Mischstufe für beide Ströme, die aus zwei hintereinander geschalteten Mischstufen besteht, wobei die erste Mischstufe vom Sekundärgaskanal konzentrisch umgeben ist und die zweite Mischstufe als Venturi-Diffusor ausgebildet ist und im Bereich des Diffusoraustritts ein diesen ringförmig umgebender Gas-Flammhaltebrenner angebracht ist. Die bekannte Vorrichtung dient der Verbrennung pulverisierter Kohle.From DE-OS 1451 567 a device for generating ignitable solid / gas suspensions is known with a vertical feed for the solid / primary gas suspension and a concentrically surrounding secondary gas channel and mixing stage for both streams, which consists of two series-connected mixing stages, whereby the first mixing stage is surrounded concentrically by the secondary gas channel and the second mixing stage is designed as a venturi diffuser and in the area of the diffuser outlet there is a gas flame-holding burner surrounding it in a ring shape. The known device is used to burn pulverized coal.

Der Erfindung liegt die Aufgabe zugrunde, eine Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen, insbesondere von sulfidischen Erzkonzentraten, bereitzustellen, welche die - insbesondere vorgenannten - Nachteile der bekannten Vorrichtungen nicht aufweist und bei einfacher Konstruktion eine sichere Betriebsweise gestattet.The invention is based on the object of providing a device for producing ignitable solid / gas suspensions, in particular of sulfidic ore concentrates, which does not have the disadvantages of the known devices, particularly those mentioned above, and which permits simple operation with simple construction.

Die Aufgabe wird gelöst, indem eine Vorrichtung der eingangs genannten Art entsprechend der Erfindung derart ausgestaltet wird, daß die den beiden Mischstufen (I, 11) vorgeschaltete Zuführung für die Feststoff/Primärgas-Suspension als Entspannungstopf (2) ausgebildet ist, der eine tangential angeordnete, im wesentlichen horizontal mündende Eintragsleitung (1) für die zugeführte Feststoff/Primärgas-Suspension aufweist, daß auch die erste Mischstufe (I) als Venturi-Diffusor ausgebildet ist und daß in der zweiten Mischstufe (11) im Bereich des mit einer Kühlkammer (18) versehenen Diffusoraustritts der diesen ringförmig umgebende Gas-Flammhaltebrenner (G) mit alternierenden Brenngas- und Sauerstoffdüsen (14, 14a) angebracht ist.The object is achieved by designing a device of the type mentioned at the outset in accordance with the invention in such a way that the feeder for the solid / primary gas suspension which precedes the two mixing stages (I, 11) is designed as an expansion pot (2) which is arranged tangentially , essentially horizontally opening inlet line (1) for the supplied solid / primary gas suspension, that the first mixing stage (I) is also designed as a venturi diffuser and that in the second mixing stage (11) in the area of the cooling chamber (18 ) provided diffuser outlet which is attached to this ring-shaped gas flame holding burner (G) with alternating fuel gas and oxygen nozzles (14, 14a).

Das zur Erzeugung der zündfähigen Feststoff/Gas-Suspension erforderliche Primär- und Sekundärgas ist naturgemäß sauerstoffhaltig. Es können Luft, mit Sauerstoff angereicherte Luft oder technisch reiner Sauerstoff selbst eingesetzt werden.The primary and secondary gas required to generate the ignitable solid / gas suspension naturally contains oxygen. Air, oxygen-enriched air or technically pure oxygen itself can be used.

Mit der erfindungsgemäßen Vorrichtung wird erreicht, daß eine in die Vorrichtung eingespeiste zündfähige Gas/Feststoff-Suspension in den Mischstufen völlig homogenisiert wird und am Ausgang der zweiten Mischstufe ein sicherer Zündvorgang und eine praktisch vollständige Überführung der Feststoffpartikel in den schmelzflüssigen Zustand innerhalb des Brennstrahls bewirkt wird. Insbesondere ist der Gas-Flammhaltebrenner wesentlich für die spontane Zündung des Brennstoffstrahls, für die Flammhaltung sowie für einen Wärmeenergieschub im Rückströmungsbereich. Im Ergebnis wird durch diese Brennerausgestaltung eine erhebliche Abflachung des Zündprofilkegels bewirkt.With the device according to the invention it is achieved that an ignitable gas / solid suspension fed into the device is completely homogenized in the mixing stages and at the output of the second mixing stage a reliable ignition process and a practically complete conversion of the solid particles into the molten state is effected within the fuel jet . In particular, the gas flame retardant burner is essential for the spontaneous ignition of the fuel jet, for flame maintenance and for a heat energy boost in the backflow area. The result of this burner design is a considerable flattening of the ignition profile cone.

In der erfindungsgemäßen Vorrichtung wird über den Eintrittsstutzen 1 in den zyklonartigen Entspannungstopf 2 eine Feststoff/Primärgas-Suspension, wie komplexes sulfidisches Erzkonzentrat, eingeführt. Der Entspannungstopf besitzt zweckmäßig eine innere keramische Verschleißschutzschicht, beispielsweise aus Beton. Infolge der pneumatischen Förderung des Feststoffs einer Korngröße von unter 40 11m und über 40 um bis 110 µm in den Entspannungstopf und infolge der Rotationsbewegung (Drall) in diesem wird der Feststoff beim Verlassen des zyklonartigen Entspannungstopfes 2 über den Anschlußstutzen 4 in die Mischstufe I mit einem gewissen Drall geschleudert. Beispielsweise tritt eine Gas/ Feststoff-Suspension mit einer Strömungsgeschwindigkeit von etwa 15 m/sec in den Venturi-Diffusor der ersten Mischstufe ein. Die als Venturi-Diffusor ausgeführte Mischstufe besteht aus dem konvergenten Einmündungsteil 5, der zylindrischen Mischstrecke 6 und dem Diffusorteil 7. Der Venturi-Diffusor der Mischstufe I ist über eine Flanschverbindung auswechselbar mit dem zyklonartigen Entspannungstopf 2 verbunden. Im konvergenten Teil 5 des Venturi-Diffusors wird ein mit- z.B. etwa 17 bis 27 kg Feststoff/m beladener Gasstrom beschleunigt und erreicht in der zylinderförmigen Mischstrecke 6 einen hohen Turbulenzgrad. In der Mischstrecke der Mischstufe der erfindungsgemäßen Vorrichtung werden bei einer Länge der Mischstrecke 6 von beispielsweise etwa dem 4- bis 6-fachen des Durchmessers Turbulenzgrade von Re = 1,5 bis 1,7 x 105 erreicht. Der Diffusorteil 7 besitzt einen Öffnungs- bzw. Neigungswinkel von etwa 3 bis 7 Winkelgraden. Als zweckmäßig hat sich ein Neigungswinkel von 5° erwiesen. Die Vorrichtungsteile 5, 6, 7 der Mischstufe I dienen der Homogenisierung einer mit einem Drall eingespeisten Feststoff/Gas-Suspension sowie dem Abbau des Dralls. Der hohe Turbulenzgrad erzeugt eine Bewegung der Fluidteilchen quer zur Strömungsachse, wodurch bei entsprechender Verweilzeit, verbleibender Relativbewegung zwischen Gas und Feststoff sowie zwischen feineren und gröberen Feststoffpartikeln eine wirksame Homogenisierung des Gemischstromes erreicht wird. Durch die Länge der Mischstrecke 6 von beispielsweise dem 4- bis 5-fachen des Durchmessers werden Wirbel bzw. Strahlablösungen, die sich im konvergenten Teil 5 ergeben, abgebaut, bevor der Strahl in den Diffusor 7 eintritt. Der geringe Neigungswinkel des Diffusors vermeidet Strahl- und damit Dichteunregelmäßigkeiten.In the device according to the invention, a solid / primary gas suspension, such as complex sulfidic ore concentrate, is introduced into the cyclone-like expansion pot 2 via the inlet connection 1. The relaxation pot expediently has an inner ceramic wear protection layer, for example made of concrete. As a result of the pneumatic conveying of the solids with a grain size of less than 40 11 m and more than 40 μm to 110 μm in the expansion pot and due to the rotational movement (swirl) in this, the solid is discharged from the cyclone-type expansion pot 2 via the connecting piece 4 into the mixing stage I with a thrown a certain twist. For example, a gas / solid suspension enters the venturi diffuser of the first mixing stage at a flow rate of approximately 15 m / sec. The mixing stage designed as a venturi diffuser consists of the convergent orifice part 5, the cylindrical mixing section 6 and the diffuser part 7. The venturi diffuser of the mixing stage I is connected to the cyclone-like expansion pot 2 via a flange connection. In the convergent part 5 of the venturi diffuser, a gas stream laden with, for example, about 17 to 27 kg of solids / m is accelerated and reaches a high degree of turbulence in the cylindrical mixing section 6. In the mixing section of the mixing stage of the device according to the invention, with a length of the mixing section 6 of, for example, approximately 4 to 6 times the diameter, degrees of turbulence of Re = 1.5 to 1.7 × 10 5 are achieved. The diffuser part 7 has an opening or inclination angle of approximately 3 to 7 degrees. An angle of inclination of 5 ° has proven to be expedient. The device parts 5, 6, 7 of mixing stage I serve to homogenize a solid / gas suspension fed in with a swirl and to break down the swirl. The high degree of turbulence produces a movement of the fluid particles transversely to the flow axis, which, with a corresponding dwell time, remaining relative movement between gas and solid as well as between finer and coarser solid particles, results in an effective homogenization of the mixture flow. Due to the length of the mixing section 6 of, for example, 4 to 5 times the diameter, vortices or jet separations, which result in the convergent part 5, are reduced before the jet enters the diffuser 7. The low angle of inclination of the diffuser avoids jet and therefore density irregularities.

Der Sekundärgaskanal 8 ist zweckmäßig als Rohrkrümmer ausgebildet, dessen vertikaler Teil den Diffusor konzentrisch umgibt. Im Bereich des Diffusoraustritts 7 geht der Sekundärgaskanal in einen zylinderförmigen Teil 10 eines kleineren Durchmessers über, wobei dieser kleinere Durchmesser praktisch dem Durchmesser des Diffusoraustritts entspricht. Der Sekundärgaskanal dient der Einführung eines Reaktionsgasstromes, wie z.B. eines mit Sauerstoff angereicherten Luftstromes.The secondary gas channel 8 is expediently designed as a pipe bend, the vertical part of which concentrically surrounds the diffuser. In the area of the diffuser outlet 7, the secondary gas channel merges into a cylindrical part 10 of a smaller diameter, this smaller diameter practically corresponding to the diameter of the diffuser outlet. The secondary gas channel is used to introduce a reaction gas stream, e.g. an air flow enriched with oxygen.

Der Querschnittsübergang 9 des Sekundärgaskanals 8 in die Mischstrecke 10 ist ohne Querschnittssprung ausgebildet, beispielsweise kurvenförmig (konvex, konkav) oder konusartig. Auf diese Weise werden eventuelle Feststoffablagerungen, die infolge instabilen Verhaltens zu Beladungsunregelmäßigkeiten bzw. unregelmäßiger Stoffstromdichte führen, vermieden. Der Durchmesser der Mischstrecke 10 ist so gewählt, daß ein erheblicher Turbulenzgrad von Re = 3 bis 7 x 105 erreicht wird. Maßnahmen, wie Länge der Mischstrecke 10 von z.B. dem 5- bis 8-fachen des Durchmessers, gleitender Übergang in den nachgeschalteten Diffusor 11 mit einer engen Neigung von beispielsweise 2,5°, dienen dazu, Ablösung bzw. Wirbelbildung am Brennermund 12 zu vermeiden. Wirbelbildungen würden zu Unregelmäßigkeiten in der Strahlzündung - z.B. ganz oder selektiv begrenzter Rückzündung in den Diffusor - und damit zu erheblichen Störungen, z.B. Verbackung, führen. Querschnittsübergang, Konizität sowie Mündungsdurchmesser des Diffusorteils 7 sind somit in der erfindungsgemäßen Vorrichtung derart aufeinander abgestimmt, daß eine völlige Vermischung der beiden Ströme - Sekundärgasstrom, Feststoff/Gas-Suspensionsstrom - und homogene Feststoffverteilung in der Mischstufe 11 eintritt. Zeckmäßig wird die erfindungsgemäße Vorrichtung mit einer Geschwindigkeit des Sekundärgasstromes betrieben, die höher als diejenige des Feststoff/Gas-Suspensionsstromes ist, wobei eine Relativgeschwindigkeit von 5 bis 15 m/sec eingestellt wird.The cross-sectional transition 9 of the secondary gas channel 8 into the mixing section 10 is designed without a cross-sectional jump, for example curved (convex, concave) or conical. In this way, possible solid deposits that lead to loading irregularities or irregular material flow density as a result of unstable behavior are avoided. The diameter of the mixing section 10 is selected so that a considerable degree of turbulence of R e = 3 to 7 x 10 5 is achieved. Measures such as the length of the mixing section 10 of, for example, 5 to 8 times the diameter, smooth transition into the downstream diffuser 11 with a narrow inclination of 2.5 °, for example, serve to avoid detachment or eddy formation at the burner mouth 12. Vortex formation would lead to irregularities in the beam ignition - for example completely or selectively limited re-ignition in the diffuser - and thus to considerable disturbances, for example caking. Cross-sectional transition, conicity and mouth diameter of the diffuser part 7 are thus coordinated with one another in the device according to the invention in such a way that complete mixing of the two streams - secondary gas stream, solid / gas suspension stream - and homogeneous solid distribution occurs in the mixing stage 11. In terms of purpose, the device according to the invention is operated at a speed of the secondary gas flow which is higher than that of the solid / gas suspension flow, a relative speed of 5 to 15 m / sec being set.

In der erfindungsgemäßen Vorrichtung ist ein zweiter Venturi-Diffusor 11 vertikal hinter den ersten geschaltet und mit diesem über einen Flansch 10a verbunden. Dieser zweite Venturi-Diffusor bildet die Mischstufe 11. Der Neigungswinkel des Diffusors beträgt 1,5 bis 4, vorzugsweise 2 bis 3 Winkelgrade. Ein Neigungswinkel von 2,5° hat sich als besonders vorteilhaft erwiesen. Am Ende des Venturi-Diffusors 11 bzw. in dessen Austrittsbereich ist ein Gas-Flammhaltebrenner angebracht, der den Diffusoraustritt ringförmig umgibt. Der ringförmig angeordnete Brenner besitzt getrennte Verteilerrohre 16 für jeweils Brenngas und Sauerstoff. Die jeweiligen getrennten Düsen 14, 14a für Brenngas und Sauerstoff sind alternierend und in einem Teilungsabstand von etwa 40 mm koaxial auf einem Ringkreis angebracht. Der Abstand zur Abreißkante 17 beträgt etwa 35 bis 40 mm. Die Düsenköpfe sind mittels Schraubgewinde auswechselbar mit den Zuführungsorganen 15,15a verbunden. Die Zuführungsorgane 15,15a sind durch die Kühlkammer 18 hindurchgeführt und im oberen und unteren Brennerboden druckwasserdicht eingeschweißt. Ein innerer Leitring 19 dient der gleichmäßigen Verteilung des Kühlwassers. Im allgemeinen hat die ringförmige Kühlkammer eine Höhe von 10 bis 30 und vorzugsweise von 15 bis 20 cm. Als Werkstoff für den Gas-Flammhaltebrenner dienen Chrom- und Nickel-haltige Edelstähle (beispielsweise Edelstahl der Werkstoff-Nr. 4571). Diese Werkstoffe und auch die Ausstattung des Diffusors 11 mit einer Kühlkammer bieten einen guten und ausreichenden sicherheitstechnischen Schutz gegen Verzunderung des Werkstoffes. Am Austritt des Venturi-Diffusors 11 ist im Bereich der Ebene des Brennermundes 12 eine über die Ebene hinausragende, schneidenartige Abreißkante 17 angebracht. Diese vorspringende Abreißkante einer Höhe zwischen 10 und 20 mm dient der genauen Fixierung des Zündbeginns außerhalb des Brennermundes, jedoch unmittelbar an diesem. Diese Maßnahme bewirkt, daß die hochtemperierten rückströmenden Verbrennungsgase und der Feststoff/Gas-Gemischstrahl in einem spitzen Winkel aufeinandertreffen. Auf diese Weise bietet die Ringgrundfläche des Gas-Flammhaltebrenners praktisch keine Angriffsmöglichkeiten für Feststoffansätze. Ferner verhindert die Abreißkante 17 Zündunregelmäßigkeiten, die bei einem durch Wirbel gestörten Fluidstrahl vor Austritt aus dem Venturi-Diffusor 11 auftreten können. Diese Unregelmäßigkeiten bewirken eine Belastung der Diffusor-Innenfläche durch frühzeitige Reaktion, Überhitzung und Verbackung.In the device according to the invention, a second venturi diffuser 11 is connected vertically behind the first and connected to it via a flange 10a. This second venturi diffuser forms the mixing stage 11. The angle of inclination of the diffuser is 1.5 to 4, preferably 2 to 3 degrees. An angle of inclination of 2.5 ° has proven to be particularly advantageous. At the end of the venturi diffuser 11 or in its outlet area there is a gas flame-holding burner which surrounds the diffuser outlet in a ring. The torch arranged in a ring has separate distributor pipes 16 for fuel gas and oxygen in each case. The respective separate nozzles 14, 14a for fuel gas and oxygen are arranged alternately and coaxially on a ring circle at a pitch of approximately 40 mm. The distance from the tear-off edge 17 is approximately 35 to 40 mm. The nozzle heads are by means of screw threads interchangeably connected to the supply members 15, 15a. The feed members 15, 15a are passed through the cooling chamber 18 and welded in the upper and lower burner bottoms so as to be watertight. An inner guide ring 19 serves for the uniform distribution of the cooling water. In general, the annular cooling chamber has a height of 10 to 30 and preferably 15 to 20 cm. Stainless steel containing chromium and nickel (for example stainless steel of material no. 4571) is used as the material for the gas flame-retardant burner. These materials and also the equipment of the diffuser 11 with a cooling chamber offer good and adequate safety protection against scaling of the material. At the outlet of the venturi diffuser 11, in the area of the plane of the burner mouth 12, a cutting-like tear-off edge 17 projecting beyond the plane is attached. This protruding tear-off edge of a height between 10 and 20 mm serves to precisely fix the start of ignition outside the burner mouth, but directly on it. This measure causes the high-temperature returning combustion gases and the solid / gas mixture jet to meet at an acute angle. In this way, the ring base of the gas flame retardant burner offers practically no possibilities of attack for solid batches. Furthermore, the tear-off edge 17 prevents ignition irregularities which can occur in the case of a fluid jet which is disturbed by eddies before exiting the venturi diffuser 11. These irregularities place stress on the inside of the diffuser due to early reaction, overheating and caking.

Dennoch ist ein zusätzlicher Schutz der Bauteile des Gas-Flammhaltebrenners an den insbesondere hohen Temperaturen ausgesetzten Bereichen zweckmäßig, wie die Flächen des Brennermundes 12, der untere Boden und die Mantelflächen der Kühlkammer 18. Geeignete Schutzschichten sind solche aus z.B. Cobalt oder Zirconium, die bei den Betriebstemperaturen der erfindungsgemäßen Vorrichtung weder zur Verzunderung noch zum Legieren mit geschmolzenen Bestandteilen der Feststoff-Suspension, wie Kupfer oder Blei, neigen. Die Abreißkante 17 ist - wie auch die übrigen Konstruktionsteile der Vorrichtung - zweckmäßig ganz oder teilweise aus Chromnickelstählen hergestellt. Zur weiteren Verbesserung der Standzeit kann es zweckmäßig sein, den äußeren Bereich, nämlich die Schneide der Abreißkante, durch Schmelz- oder Sinterauftrag eines Werkstoffes auf Basis z.B. Cobalt oder Zirconium, zu schützen. Die Auswahl des Werkstoffes richtet sich nach dem Lösungsvermögen der Fest-Flüssig-Bestandteile im Reaktionsstrahl.Nevertheless, additional protection of the components of the gas flame-retardant burner is expedient in the areas exposed to particularly high temperatures, such as the surfaces of the burner mouth 12, the lower floor and the outer surfaces of the cooling chamber 18. Suitable protective layers are those made of e.g. Cobalt or zirconium, which at the operating temperatures of the device according to the invention tend neither to scale nor to alloy with molten constituents of the solid suspension, such as copper or lead. The tear-off edge 17 is - like the other construction parts of the device - expediently made entirely or partially of chromium-nickel steel. To further improve the service life, it can be useful to coat the outer area, namely the cutting edge of the tear-off edge, by melting or sintering a material based on e.g. To protect cobalt or zirconium. The choice of material depends on the solvency of the solid-liquid components in the reaction jet.

Unter den vorgenannten Ausbildungen halten die Werkstoffe den Betriebsbedingungen der erfindungsgemäßen Vorrichtung von hoher Temperatur und Austrittsgeschwindigkeiten des Gemischstrahls von etwa 19 bis 28 m/s ohne Schaden stand.Under the aforementioned designs, the materials withstand the operating conditions of the device according to the invention from high temperature and exit speeds of the mixture jet of approximately 19 to 28 m / s without damage.

Nach einer weiteren Ausgestaltung der Erfindung sitzt der Gas-Flammhaltebrenner bzw. die gesamte Vorrichtung auf dem oberen Rand eines an sich bekannten vertikalen Brennschachtes 13 mittels Flanschverbindung 13a - mit sprungartigem Übergang - auf, während der untere Rand des Brennschachtes in an sich bekannter Weise auf einer horizontalen Schmelzzyklonkammer in fester Verbindung aufsitzt. Die Länge des Brennschachtes 13 richtet sich nach der Größe des sogenannten Konzentratbrenners. Die Brennschachtlänge ist um so kürzer, je kleiner der Abstand x des Punktes der maximalen Flammentemperatur vom Brennermund ist. Dieser Abstand x ist durch die Beziehung festgelegt

Figure imgb0001
worin bedeuten:

  • f = Funktion
  • WA = Austrittsgeschwindigkeit am Brennermund
  • dA = Durchmesser Brennermund
  • k = Brennerbeiwert
According to a further embodiment of the invention, the gas flame-holding burner or the entire device sits on the upper edge of a vertical burner shaft 13 known per se by means of a flange connection 13a - with a sudden transition - while the lower edge of the burner shaft in a manner known per se horizontal melting cyclone chamber sits firmly in place. The length of the burner shaft 13 depends on the size of the so-called concentrate burner. The smaller the distance x of the point of the maximum flame temperature from the burner mouth, the shorter the length of the burner shaft. This distance x is determined by the relationship
Figure imgb0001
 in which mean:
  • f = function
  • W A = exit velocity at the burner mouth
  • d A = diameter of the burner mouth
  • k = burner coefficient

Beispielsweise beträgt bei einem Durchsatz von etwa 8 t/h bestimmter Kupferkonzentrate die Länge des Brennschachtes etwa 180 cm. Mit größerwerdender Produktionseinheit (Konzentratbrenner) kann dA größer und damit die Flammenlänge x und die Brennschachtlänge kleiner werden. Die Zyklonkammer weist bei einer Länge von üblicherweise etwa 1 m einen Durchmesser von etwa 95 cm auf.For example, with a throughput of approximately 8 t / h of certain copper concentrates, the length of the combustion shaft is approximately 180 cm. As the production unit (concentrate burner) grows, d A can be larger and thus the flame length x and the length of the burner shaft smaller. The cyclone chamber has a length of usually about 1 m and a diameter of about 95 cm.

Eine weitere Ausgestaltung der Erfindung sieht im Bereich der Einmündung des Brennschachtes 13 in die horizontale Brennkammer 20 einen als Zündbrenner wirkenden, an sich bekannten Zweikammer-Vorgemischbrenner vor. Dieser Zündbrenner ist im Boden der horizontal liegenden Zyklonkammer, vorzugsweise im Mantel des Zyklons, angebracht und die Strahlachse ist auf die untere Innenwandung der Zyklonkammer gerichtet. Für die Zündung dieses Zündbrenners 23 ist eine Zündkerze 29 innerhalb einer aus feuerfester Stampfmasse bestehenden Haube vorgesehen. Der aus der Haube austretende stabile Flammstrahl wird in einen sprunghaft erweiterten zylindrischen Brennkanal 24 geleitet.A further embodiment of the invention provides, in the region of the confluence of the combustion shaft 13 in the horizontal combustion chamber 20, a two-chamber premix burner, known per se, which acts as a pilot burner. This pilot burner is mounted in the bottom of the horizontally lying cyclone chamber, preferably in the jacket of the cyclone, and the jet axis is directed towards the lower inner wall of the cyclone chamber. For the ignition of this pilot burner 23, a spark plug 29 is provided within a hood made of refractory ramming compound. The stable flame jet emerging from the hood is directed into a suddenly expanded cylindrical combustion channel 24.

In einer besonders vorteilhaften Ausgestaltung der Erfindung ist der Zweikammer-Vorgemischbrenner 23 im Zündkanal 24 achsial mit einer Hochdruck-Vollstrahldüse 25 ausgerüstet. In diese Düse kann ein reduzierend wirkendes flüssiges Mittel, wie Öl, eingegeben und durch den Gas-Brennstrahl des Vorgemischbrenners 23 hindurch in die Zyklonkammer eingespritzt werden. Das Reduktionsmittel dient in an sich bekannter Weise der Reduktion anfallender Schlacke, welche zweckmäßig vor Ablauf der Schmelze aus der Zyklonkammer in ein üblicherweise nachgeschaltetes Zwischengefäß reduziert wird. Bei dieser Anordnung der Düse wird in vorteilhafter Weise die Düse durch den (noch nicht gezündeten) Gas/Luft-Strom gekühlt und Beeinträchtigungen der Düse durch Crack-Prozesse vermieden. Über den zentralen Stutzen 28 kann die Flammenüberwachung durch optische Vorrichtungen vorgenommen werden. Darüber hinaus kann der Zündbrenner 23 zur Gewährleistung eines sicheren Schmelzbetriebes in Abhängigkeitsschaltung mit allen anderen Brennern betrieben werden.In a particularly advantageous embodiment of the invention, the two-chamber premix burner 23 in the ignition channel 24 is axially equipped with a high-pressure full jet nozzle 25. A reducing agent, such as oil, can be introduced into this nozzle and injected into the cyclone chamber through the gas fuel jet of the premix burner 23. The reducing agent is used in a manner known per se to reduce slag which is expediently reduced before the melt runs out of the cyclone chamber into a usually downstream intermediate vessel. With this arrangement of the nozzle, the nozzle is advantageously replaced by the (not yet ignited) gas / air Electricity cooled and nozzle damage caused by cracking processes avoided. Flame monitoring can be carried out by means of optical devices via the central connecting piece 28. In addition, the pilot burner 23 can be operated in a dependent circuit with all other burners to ensure safe melting operation.

Die erfindungsgemäße Vorrichtung eignet sich insbesondere zur pyrometallurgischen Behandlung von sulfidischen NE-Metallerzen oder sulfidischen NE-Metallerzkonzentraten. Mit der erfindungsgemäßen Vorrichtung werden eine rasche und vollständige Durchzündung des aus den Mischstufen austretenden Gemischstrahls bei kleiner Flammenlänge und hoher Flammentemperatur in kurzem Abstand vom Brennermund erzielt. Hierdurch erfolgt bei Strahlaustrittsgeschwindigkeiten im an sich bekannten Bereich von unter 30 m/sec ein praktisch vollständiger Übergang der Feststoffpartikel in den schmelzflüssigen Zustand.The device according to the invention is particularly suitable for the pyrometallurgical treatment of sulfidic non-ferrous metal ores or sulfidic non-ferrous metal ore concentrates. With the device according to the invention, a rapid and complete ignition of the mixture jet emerging from the mixing stages with a small flame length and high flame temperature is achieved at a short distance from the burner mouth. This results in a practically complete transition of the solid particles into the molten state at jet exit speeds in the known range of below 30 m / sec.

Die Weiterbehandlung des an der Innenwandung des Zyklons ablaufenden Schmelzfilms erfolgt in bekannter Weise. Das heißt, am Austritt der Zyklonkammer läuft der gesammelte Schmelzfilm als Strahl durch einen Austrittsschlitz in eine Sekundärkammer ab und gelangt über einen vertikalen Fallschacht in einen Vorherd. Im Vorherd werden die Schmelzkomponenten von unterschiedlichem Gewicht, wie Stein und Schlacke, separiert und getrennt abgezogen.The further treatment of the melt film running on the inner wall of the cyclone is carried out in a known manner. This means that at the exit of the cyclone chamber, the melt film collected runs off as a jet through an exit slot into a secondary chamber and reaches a forehearth via a vertical chute. In the forehead, the melting components of different weights, such as stone and slag, are separated and removed separately.

Die erfindungsgemäße Vorrichtung ist auf die Behandlung einer Vielzahl von Feststoffen anwendbar. Besonders geeignet sind sulfidische NE-Metallerze oder NE-Metallkonzentrate und sulfidische Eisenerze oder Eisenerzkonzentrate. Sie ist jedoch auch bestens geeignet für die Behandlung oxidischer, gegebenenfalls vorreduzierter Eisenerze oder Eisenerzkonzentrate sowie auch für die Behandlung von hüttenmännischen Zwischenprodukten.The device according to the invention is applicable to the treatment of a large number of solids. Sulfidic non-ferrous metal ores or non-ferrous metal concentrates and sulfidic iron ores or iron ore concentrates are particularly suitable. However, it is also ideally suited for the treatment of oxidic, possibly pre-reduced iron ores or iron ore concentrates as well as for the treatment of metallurgical intermediates.

Die Erfindung wird anhand der Figuren und des Ausführungsbeispiels näher und beispielhaft erläutert.The invention is explained in more detail and by way of example with reference to the figures and the exemplary embodiment.

Es veranschaulichen

  • Fig. 1 einen Schnitt durch die erfindungsgemäße Vorrichtung;
  • Fig. 2 einen Schnitt durch den Brennschacht und die Zyklonkammer als unteren Teil der erfindungsgemäßen Vorrichtung.
Illustrate it
  • 1 shows a section through the device according to the invention.
  • Fig. 2 shows a section through the combustion shaft and the cyclone chamber as the lower part of the device according to the invention.

In der Vorrichtung gemäß Fig. 1 wird die einzusetzende Feststoff/Gas-Suspension durch den Eintrittsstutzen 1 in den Entspannungstopf 2 gegeben. Dieser besitzt in 3 einen konischen Teil und in 4 einen zylindrischen Teil als Anschlußstutzen. Dieser Anschlußstutzen ist über einen Flansch 4a mit der Mischstufe I verbunden. Diese Mischstufe wird gebildet aus einem Venturi-Diffusor mit dem konvergenten Teil 5, dem zylinderförmigen Mischstreckenteil 6 und dem Diffusorteil 7. Der Venturi-Diffusor wird von dem Sekundärgaskanal 8 konzentrisch umgeben. Der Sekundärgaskanal ist als Rohrkrümmer ausgebildet, der sich über den Übergang 9 in einen zylindrischen Mischstreckenteil 10 verminderten Durchmessers verjüngt. Über Flansch 10a ist die Mischstufe mit der Mischstufe II verbunden. Der Venturi-Diffusor 11 ist an seinem Austrittsteil mit einem ringförmigen Gas-Flammhaltebrenner G ausgerüstet. Der Gas-Flammhaltebrenner besitzt getrennte Verteilerrohre 16 für jeweils Brenngas und Sauerstoff, die an die getrennten Zuleitungsrohre 15,15a für Brenngas und Sauerstoff angeschlossen sind. Die Zuleitungsrohre 15, 15a sind an ihrem Austritt über Schraubgewinde mit auswechselbaren Düsen 14, 14a versehen. Mit 17 ist eine ringförmige Abreißkante bezeichnet. Die Kühlkammer 18 ist mit einem inneren Leitring 19 für die gleichmäßige Verteilung des unter Druck stehenden Kühlwassers versehen. Mittels Flansch 13a sitzt der Brenner auf dem Brennschacht 13 auf. Der Brennermund 12 mündet übergangslos in den Brennschacht 13.In the device according to FIG. 1, the solid / gas suspension to be used is introduced through the inlet connection 1 into the expansion pot 2. This has a conical part in 3 and a cylindrical part in 4 as a connecting piece. This connecting piece is connected to the mixing stage I via a flange 4a. This mixing stage is formed from a venturi diffuser with the convergent part 5, the cylindrical mixing section part 6 and the diffuser part 7. The venturi diffuser is surrounded concentrically by the secondary gas channel 8. The secondary gas channel is designed as a pipe bend, which tapers via the transition 9 into a cylindrical mixing section part 10 of reduced diameter. The mixing stage is connected to mixing stage II via flange 10a. The venturi diffuser 11 is equipped with an annular gas flame-holding burner G at its outlet part. The gas flame-holding burner has separate manifolds 16 for fuel gas and oxygen, respectively, which are connected to the separate feed pipes 15, 15a for fuel gas and oxygen. The supply pipes 15, 15a are provided with replaceable nozzles 14, 14a at their outlet via screw threads. With 17 an annular tear-off edge is designated. The cooling chamber 18 is provided with an inner guide ring 19 for the uniform distribution of the pressurized cooling water. The burner sits on the burning shaft 13 by means of flange 13a. The burner mouth 12 flows seamlessly into the burner shaft 13.

In Fig. 2 ist der Übergang bzw. die Einmündung des Brennschachts 13 in die horizontale Zyklonkammer 20 dargestellt. Im Bereich der Einmündung ist im Zylinderboden 22 der Zyklonkammer 21 ein Zweikammer-Vorgemischbrenner 23 mit Zündkanal 24 eingebaut. Die Strahlrichtung 27 dieses Brenners ist auf die untere Innenwandung der Zyklonkammer gerichtet. Eine Zündkerze 29 zündet das Gasgemisch 28 sowie den über die Vollstrahldüse 25 austretenden Strahl 26 flüssigen Brennstoffs.2 shows the transition or the opening of the combustion shaft 13 into the horizontal cyclone chamber 20. In the area of the confluence, a two-chamber premix burner 23 with ignition channel 24 is installed in the cylinder base 22 of the cyclone chamber 21. The beam direction 27 of this burner is directed onto the lower inner wall of the cyclone chamber. A spark plug 29 ignites the gas mixture 28 and the jet 26 of liquid fuel emerging via the full jet nozzle 25.

AusführungsbeispielEmbodiment

7.000 kg/h Kupferkonzentrat werden aus vorgeschalteten Bunker-, Trocknungs-, Zuteiler- und Mischanlagen mit 390 m3 Primärluft als Trägergas über eine Förder-Rohrleitung dem Eintrittsstutzen 1 des Entspannungsgefäßes 2 zugeführt.7,000 kg / h of copper concentrate are fed from upstream bunker, drying, distributor and mixing systems with 390 m 3 of primary air as carrier gas via a delivery pipe to the inlet port 1 of the expansion vessel 2.

Das Konzentrat mit einer Zusammensetzung von

  • Cu = 21 - 23%
  • Fe = 22 - 25%
  • S = 30 - 33%
  • Zn = 7 - 10%
  • Pb = 6 - 9%
  • Si02 = 1%
    und einer Korngröße zwischen 0,5 und 100 11m und einem Anteil von 53% im Bereich zwischen 15 und 100 11m besitzt eine Restfeuchte von 0,1 bis 0,3%.
The concentrate with a composition of
  • Cu = 2 1 - 2 3%
  • Fe = 22 - 25%
  • S = 30 - 33%
  • Zn = 7-10%
  • Pb = 6 - 9%
  • Si0 2 = 1%
    and a grain size between 0.5 and 100 11m and a proportion of 53% in the range between 15 and 100 11m has a residual moisture of 0.1 to 0.3%.

Als Schlackenbildner wird Si02 in Form von Sand in einer Menge von 1,3 t/h dem Konzentrat-Luftstrom vor Eintritt in den Stutzen 1 zugeführt, um das sich bildende FeO in einer Schlacke abzubinden. Hierzu wird Sand mit einer Restfeuchte von 0,1% und einer Korngröße bis 0,7 mm verwendet.As a slag former, Si0 2 is supplied in the form of sand in an amount of 1.3 t / h to the concentrate air stream before entering the nozzle 1 in order to bind the FeO that forms in a slag. For this, sand with a residual moisture of 0.1% and a grain size of up to 0.7 mm is used.

Der Fluidstrom aus 7.000 kg/h Konzentrat, 1.300 kg/h Sand und 350 m3/h Förderluft gelangt über den Stutzen 1 in das Entspannungsgefäß 2 und tritt aus diesem über die Einschnürung 5 in die Mischstrecke 6 der Mischstufe II ein, in der der Strahl auf eine Geschwindigkeit von 39 m/s beschleunigt wird. Bei dem gewählten Durchmesser der Mischstrecke 6 wird ein Turbulenzgrad von Re = 1,67 x 105 erreicht. Das Verhältnis L : D beträgt 5. Der Strahl passiert alsdann den mit einem Radius von 100 mm stufenlos ausgebildeten Übergang von Mischstrecke 6 in den Diffusor 7, der eine Neigung von 5 Winkelgraden und einen größten Durchmesser von 95 mm hat.The fluid flow from 7,000 kg / h concentrate, 1,300 kg / h sand and 350 m 3 / h conveying air passes through the connector 1 into the expansion vessel 2 and enters the mixing section 6 of the mixing stage II via the constriction 5, in which the Beam is accelerated to a speed of 39 m / s. With the selected diameter of the mixing section 6, a degree of turbulence of Re = 1.67 x 10 5 is achieved. The ratio L: D is 5. The beam then passes through the transition from mixing section 6 to diffuser 7, which is infinitely variable with a radius of 100 mm, and has an inclination of 5 angular degrees and a largest diameter of 95 mm.

Der homogenisierte Fluidstrahl tritt aus dem Venturi-Diffusor 7 mit einer Geschwindigkeit von z.B. 15,9 m/s aus und zusamen mit dem Sekundärstromgemisch aus 600 m3/h Luft mit 1.800 m3/h Sauerstoff innerhalb des Sekundärgaskanals 8 in den Fangteil der Mischstrecke 10 der Venturi-Mischstufe II ein.The homogenized fluid jet emerges from the venturi diffuser 7 at a speed of, for example, 15.9 m / s and together with the secondary flow mixture of 600 m 3 / h of air with 1,800 m 3 / h of oxygen within the secondary gas channel 8 into the catching part of the mixing section 10 of the Venturi mixer stage II.

Die Relativgeschwindigkeit zwischen dem aus Diffusor 7 austretenden Strahl und dem ihn umgebenden Sekundärstrom innerhalb des Sekundärgaskanals 8 beträgt 9,3 m/s.The relative speed between the jet emerging from the diffuser 7 and the secondary stream surrounding it within the secondary gas channel 8 is 9.3 m / s.

Die Mischung beider Ströme erfolgt in der Mischstrecke 10 bei einer mittleren Strahlgeschwindigkeit von 70,5 m/s und einem Streckenverhältnis L : D = 5,4 und einem anfänglichen Turbulenzgrad von Re = 6 x 105. Die Strahlmischung wird nunmehr in den Diffusor 11 der Mischstufe II übergeführt. Zur Vermeidung von Strahlablösungen hat der Diffusor 11 eine Neigung von 2,5 Winkelgraden. Aus dem Brennermund 12 tritt der noch ungezündete Fluidstrahl mit einer mittleren Geschwindigkeit von 18,5 m wirbelfrei aus.The two streams are mixed in the mixing section 10 at an average jet speed of 70.5 m / s and a section ratio L: D = 5.4 and an initial degree of turbulence of Re = 6 × 10 5 . The jet mixture is now transferred into the diffuser 11 of the mixing stage II. To avoid beam separation, the diffuser 11 has an inclination of 2.5 degrees. The still unignited fluid jet emerges from the burner mouth 12 at a mean speed of 18.5 m in a vortex-free manner.

Infolge des Durchmessersprunges von 230 mm am Brennermund 12 auf 500 mm im Brennschacht 13 sowie der axialen Ausrichtung des homogenisierten austretenden Strahles ergibt sich eine äußere Rückströmung von heißen Verbrennungsprodukten und Gasen, die zusammen mit der Flammhalte-Einrichtung 14 und 14a unmittelbar an der Abreißkante 17 zur Durchzündung des Fluidstrahles führt.As a result of the jump in diameter from 230 mm at the burner mouth 12 to 500 mm in the burner shaft 13 and the axial alignment of the homogenized emerging jet, there is an external backflow of hot combustion products and gases which, together with the flame-holding device 14 and 14a, lead directly to the tear-off edge 17 Ignition of the fluid jet leads.

Die eingesetzte Brennstoffmenge für die Flammhaltung beträgt bei einem Konzentratdurchsatz von 6.000 bis 10.000 kg/h ca. 30 m3 Erdgas. Im Bereich des Brennermundes 12 tritt der homogenisierte Fluidstrahl über die Abreißkante 17 wirbelfrei aus, ohne daß es im Grenzschichtbereich der Diffusor-Innenwand am Ende des Diffusors 11 zu Ablösungen und Wirbelbildungen kommt.The amount of fuel used for flame control is approx. 30 m 3 natural gas with a concentrate throughput of 6,000 to 10,000 kg / h. In the area of the burner mouth 12, the homogenized fluid jet emerges in a vortex-free manner via the tear-off edge 17, without detachments and vortex formation occurring at the end of the diffuser 11 in the boundary layer region.

Der gerichtete Strahl taucht über die Abreißkante 17 im spitzen Winkel - und über die ihn umgebende hochreaktive, durch den Flammhaltebrenner intensivierte Rückströmung - frei in den Brennschacht 13 ein. Es ergibt sich unter Berücksichtigung der Strahlaustrittsgeschwindigkeit von 18,5 m/s am Brennermund und der Flugbahn der Feststoffreaktanten ein Zündprofil gemäß Figur 3 im Bereich des Eintritts in den Brennschacht 13. Infolge des Querschnittssprunges Brennermund 12 zu Schacht 13 und der Verbrennungsreaktion werden die reagierenden Feststoffteilchen z.T. in Richtung der gekühlten Schachtwand abgelenkt und treffen bei der erfindungsgemäßen Anordnung ausreagiert und schmelzflüssig auf die Schachtwand. Der an der Schachtwand ablaufende Schmelzenfilm erstarrt bis zu einer Dicke, die dem Wärmedurchgang zu den Kühlrohren der Schachtwand entspricht und bildet eine Schutzschicht auf dem Kühlrohrmantel aus. Auf der erstarrten Schicht läuft der randgängige Anteil der Schmelze rückstandslos und in gewünschter Stabilisierung in Richtung Zyklongefäß ab.The directed jet plunges freely into the combustion shaft 13 via the tear-off edge 17 at an acute angle - and via the highly reactive return flow surrounding it, which is intensified by the flame-holding burner. Taking into account the jet exit velocity of 18.5 m / s at the burner mouth and the trajectory of the solid reactants, an ignition profile according to FIG. 3 results in the region of the entry into the combustion shaft 13. As a result of the cross-sectional jump in burner mouth 12 to shaft 13 and the combustion reaction, the reacting solid particles become partly deflected in the direction of the cooled shaft wall and in the arrangement according to the invention reacted and melted onto the shaft wall. The melt film running down the shaft wall solidifies to a thickness that corresponds to the heat transfer to the cooling pipes of the shaft wall and forms a protective layer on the cooling pipe jacket. On the solidified layer, the edge-bound portion of the melt runs off without residue and with the desired stabilization in the direction of the cyclone vessel.

Der Ausbrand erfolgt innerhalb des Brennschachtes entsprechend dem Diagramm der Fig. 4, wobei der Strahl gemäß Fig. 4 auf kurzem Wege x die maximale Temperatur von 1.640°C erreicht und kurz danach zur Trennung von Gasphase und Schmelze tangential in die Zyklonkammer 20 eintritt.The burnout takes place within the combustion shaft according to the diagram of FIG. 4, the beam according to FIG. 4 shortly reaching x the maximum temperature of 1,640 ° C. and shortly thereafter entering the cyclone chamber 20 tangentially to separate the gas phase and melt.

Im vorliegenden Beispiel verläuft der Prozeß autogen. In Fällen der Verarbeitung von weniger Reaktionswärme enthaltenden Mischungen wird über den Stutzen 1 zusätzlich Brennstoff, z.B. Kohlenstaub, zugeführt.In the present example, the process is autogenous. In the case of processing mixtures containing less heat of reaction, additional fuel, e.g. Coal dust, fed.

Aus der über die gekühlten Wandungen der Reaktoranlage abgeführten Reaktionswärme ergibt sich eine Dampfproduktion von 0,9 bis 1 t Dampf (60 bar) je t Konzentrat.The heat of reaction removed via the cooled walls of the reactor system results in a steam production of 0.9 to 1 t steam (60 bar) per t concentrate.

Die aus dem Zyklongefäß 20 abgeführten Produkte sind:

  • Kupferstein der Zusammensetzung:
    • Cu = 73,5%
    • Pb = 2,0%
    • Fe = 2,0%
    • S = 21,6%
    • Zn = 0,9%
  • Schlacke mit Gehalten von:
    • Cu = 1,9%
    • Pb = 1,8%
    • Zn = 8,0%
    • Fe = 37,0%
    • Si02 = 31,0% Kupferstein und Schlacke werden zusammen mit einer Schmelzentemperatur von 1.300°C aus dem unteren Berich des liegenden Zyklongefäßes abgeführt.
The products discharged from the cyclone vessel 20 are:
  • Copper stone of the composition:
    • Cu = 73.5%
    • Pb = 2.0%
    • Fe = 2.0%
    • S = 21.6%
    • Zn = 0.9%
  • Slag with a content of:
    • Cu = 1.9%
    • Pb = 1.8%
    • Zn = 8.0%
    • Fe = 37.0%
    • Si0 2 = 31.0% Copper stone and slag are discharged together with a melt temperature of 1,300 ° C from the lower area of the lying cyclone vessel.

Das in axialer Richtung aus dem Zyklongefäß 20 austretende Abgas hat eine Temperatur von 1.320°C und enthält 56% S02 sowie 5% Rest-Oz.The exhaust gas emerging from the cyclone vessel 20 in the axial direction has a temperature of 1,320 ° C. and contains 56% SO 2 and 5% residual oz.

Mit dem Abgas wird oxidisch-sulfatischer Flugstaub mitgeführt einer Zusammensetzung:

  • Cu = 6%
  • Pb = 16%
  • Zn = 24%
  • S = 14%
  • Fe = 4%
The exhaust gas is used to carry oxidic-sulfatic flying dust with a composition:
  • Cu = 6%
  • Pb = 16%
  • Zn = 24%
  • S = 14%
  • Fe = 4%

Der in der Zyklongefäßwand 22 angeordnete flammüberwachte Pilotbrenner 23 dient der Zünd- und Flammsicherung des Gesamtschmelzaggregates während des Schmelzetriebes sowie der Zündung und Überwachung der Erdgasflamme während der Aufheizphase, in der bis zu einer Ofenraumtemperatur von 1.200°C aufgeheizt wird. Zum Aufheizen werden die Gasdüsen des Flammhaltebrenners G mit bis zu 150 m3/h Erdgas ohne Sauerstoff betrieben. Der erforderliche Sauerstoff wird dabei in Form von Luft über den Sekundärgaskanal 8, Mischstrecke 10 und Diffusor 11 dem Brennschacht 13 zugeführt.The flame-monitored pilot burner 23 arranged in the cyclone vessel wall 22 serves for ignition and flame protection of the entire melting unit during the melting operation and for the ignition and monitoring of the natural gas flame during the heating phase, in which heating takes place up to an oven chamber temperature of 1200 ° C. For heating, the gas nozzles of the flame-retarding burner G are operated with up to 150 m 3 / h natural gas without oxygen. The required oxygen is supplied in the form of air via the secondary gas channel 8, mixing section 10 and diffuser 11 to the combustion shaft 13.

Der Zweikammer-Vorgemischbrenner 23 ist mit einer Hochdruck-Vollstrahldüse ausgerüstet, die zum Zwecke der Reduktion im Schmelzenbereich des Zyklon 20 mit einem Reduktionsmittel, z.B. Öl, betrieben wird.The two-chamber premix burner 23 is equipped with a high-pressure full jet nozzle, which for the purpose of reduction in the melting area of the cyclone 20 with a reducing agent, e.g. Oil.

Claims (8)

1. Apparatus for producing ignitable solids-gas suspensions comprising a feeder for vertically feeding the solids-primary gas suspension, and a secondary gas passage concentrically surrounding said feeder, and a mixing stage for both streams, consisting of two mixing stages connected in series, wherein the first mixing stage is surrounded concentrically by the secondary gas passage, and the second mixing stage is constructed as a venturi diffuser and in the region of the diffuser outlet a flame-sustaining gas burner is arranged, surrounding the latter in an annular manner, characterized in that the feeder for the solids-primary gas suspension, which is connected in front of the two mixing stages (I, II), is constructed as a pressure relief vessel (2), which has a tangentially arranged supply line (1), opening out substantially horizontally, for the solids primary gas suspension which is fed in, that also the first mixing stage (I) is constructed as a venturi diffuser, and that in the second mixing stage (II) in the region of the diffuser outlet, which is provided with a cooling chamber (18), the flame-sustaining gas burner (G) with alternating fuel gas and oxygen nozzles (14,14a) is arranged, which burner surrounds the diffuser outlet in an annular manner.
2. Apparatus according to Claim 1, characterized in that the pressure relief vessel (2) and the mixing stages (I, II) are connected with each other by flange joints (4a, 10a).
3. Apparatus according to Claim 1 or 2, characterized in that in the region of the outlet (7) of the diffuser, the secondary gas passage (8) merges into a cylindrical part (10), which is smaller in diameter and is virtually equal in diameter to that of the diffuser outlet (7).
4. Apparatus according to Claims 1 to 3, characterized in that the outlet of the diffuser of the second mixing stage (II) has a separation-inducing edge (17), which is similar to a knife edge, in the region of the orifice of the burner, protruding beyond the plane.
5. Apparatus according to Claims 1 to 4, characterized in that the burner (G) or respectively the entire burner apparatus rests on the top rim of a vertical combustion shaft (13) by means of flange connection (13a).
6. Apparatus according to Claims 1 to 5, characterized in that the lower rim of the combustion shaft rests on a horizontal melting cyclone chamber (20).
7. Apparatus according to Claims 1 to 6, characterized in that a two-chamber premix burner (23) is incorporated into the bottom of the cyclone chamber (20), preferably in the shell thereof, in the region of the opening of the combustion shaft (13) into the horizontal cyclone chamber (20), and with the burner axis directed to the lower portion of the inner wall.
8. Apparatus according to Claims 1 to 7, characterized in that the premix burner (23) is additionally provided in the igniting passage (24) with a high-pressure solid-jet nozzle (25).
EP85201500A 1984-10-05 1985-09-19 Device for the production of inflammable solid/gas suspensions Expired - Lifetime EP0177090B1 (en)

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DE19843436624 DE3436624A1 (en) 1984-10-05 1984-10-05 DEVICE FOR GENERATING FLAMMABLE SOLID / GAS SUSPENSIONS
DE3436624 1984-10-05

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EP0177090A2 EP0177090A2 (en) 1986-04-09
EP0177090A3 EP0177090A3 (en) 1987-08-19
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PL255660A1 (en) 1986-07-29
CN85107375A (en) 1986-09-03
EP0177090A2 (en) 1986-04-09
PT81259B (en) 1992-06-30
JPS6196044A (en) 1986-05-14
PT81259A (en) 1985-11-01
ES547532A0 (en) 1986-03-16
BR8504911A (en) 1986-07-22
FI79348C (en) 1989-12-11
YU157285A (en) 1988-02-29
KR860003354A (en) 1986-05-23
IN160230B (en) 1987-07-04
DE3578206D1 (en) 1990-07-19
FI853836A0 (en) 1985-10-03
US4665842A (en) 1987-05-19
AU4833585A (en) 1986-04-10
FI853836L (en) 1986-04-06
YU44137B (en) 1990-02-28
DE3436624A1 (en) 1986-04-10
CN1007923B (en) 1990-05-09
PL148450B1 (en) 1989-10-31
PH23693A (en) 1989-09-27
EP0177090A3 (en) 1987-08-19
AU582971B2 (en) 1989-04-13
FI79348B (en) 1989-08-31
ZA857675B (en) 1987-06-24
CA1264252A (en) 1990-01-09
ES8605300A1 (en) 1986-03-16

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