EP0177090B1 - Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen - Google Patents

Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen 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
Authority
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
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0177090A2 (de
EP0177090A3 (en
Inventor
Adalbert Bartsch
Georg Dr. Rer. Nat. Gospos
Lars Kersten
Arno Wolfgang Bartsch
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.)
Aurubis AG
Original Assignee
Norddeutsche Affinerie 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 Norddeutsche Affinerie AG filed Critical Norddeutsche Affinerie AG
Publication of EP0177090A2 publication Critical patent/EP0177090A2/de
Publication of EP0177090A3 publication Critical patent/EP0177090A3/de
Application granted granted Critical
Publication of EP0177090B1 publication Critical patent/EP0177090B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Pre-Mixing And Non-Premixing Gas Burner (AREA)
  • Gas Burners (AREA)
EP85201500A 1984-10-05 1985-09-19 Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen Expired - Lifetime EP0177090B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19843436624 DE3436624A1 (de) 1984-10-05 1984-10-05 Vorrichtung zur erzeugung zuendfaehiger feststoff/gas-suspensionen
DE3436624 1984-10-05

Publications (3)

Publication Number Publication Date
EP0177090A2 EP0177090A2 (de) 1986-04-09
EP0177090A3 EP0177090A3 (en) 1987-08-19
EP0177090B1 true EP0177090B1 (de) 1990-06-13

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ID=6247218

Family Applications (1)

Application Number Title Priority Date Filing Date
EP85201500A Expired - Lifetime EP0177090B1 (de) 1984-10-05 1985-09-19 Vorrichtung zur Erzeugung zündfähiger Feststoff/Gas-Suspensionen

Country Status (17)

Country Link
US (1) US4665842A (zh)
EP (1) EP0177090B1 (zh)
JP (1) JPS6196044A (zh)
KR (1) KR860003354A (zh)
CN (1) CN1007923B (zh)
AU (1) AU582971B2 (zh)
BR (1) BR8504911A (zh)
CA (1) CA1264252A (zh)
DE (2) DE3436624A1 (zh)
ES (1) ES8605300A1 (zh)
FI (1) FI79348C (zh)
IN (1) IN160230B (zh)
PH (1) PH23693A (zh)
PL (1) PL148450B1 (zh)
PT (1) PT81259B (zh)
YU (1) YU44137B (zh)
ZA (1) ZA857675B (zh)

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CN104330519B (zh) * 2014-10-30 2016-05-18 西北工业大学 一种粒子气流悬浮激光点火实验装置
CN104634102B (zh) * 2015-02-13 2016-08-17 阳谷祥光铜业有限公司 一种反向旋浮熔炼方法、喷嘴和冶金设备
CN106521182B (zh) 2016-11-02 2019-05-21 阳谷祥光铜业有限公司 一种旋浮铜冶炼方法及旋浮铜冶炼装置
GB2575367B (en) * 2017-01-06 2022-08-10 Fenix Advanced Tech Limited Transportable combustible gaseous suspension of solid fuel particles
CN110081716B (zh) * 2018-01-26 2024-04-23 中国瑞林工程技术股份有限公司 用于电子废料冶炼装置的顶吹喷枪
DE102018220217A1 (de) * 2018-11-26 2020-05-28 Sms Group Gmbh Injektorvorrichtung zum Einblasen von Feststoffen in ein metallurgisches Aggregat
CN110346506A (zh) * 2019-08-13 2019-10-18 南京工业大学 一种气固混合物喷射火装置
CN112023740B (zh) * 2020-07-10 2022-03-01 湘潭大学 一种用于颗粒破碎的气固混合器
CN112138557A (zh) * 2020-10-21 2020-12-29 大庆德美特尔能源科技有限公司 一种固液混合射流器
CN113088715B (zh) * 2021-04-15 2022-05-31 攀钢集团攀枝花钢铁研究院有限公司 一种实现钒渣连续浸出系统
CN116067610B (zh) * 2023-04-06 2023-06-02 中国空气动力研究与发展中心空天技术研究所 一种低马赫数下宽范围调节气流温度的冷热气流掺混装置

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Also Published As

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

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