US20060230879A1 - Method and plant for the heat treatment of sulfidic ores using annular fluidized - Google Patents
Method and plant for the heat treatment of sulfidic ores using annular fluidized Download PDFInfo
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- US20060230879A1 US20060230879A1 US10/540,352 US54035203A US2006230879A1 US 20060230879 A1 US20060230879 A1 US 20060230879A1 US 54035203 A US54035203 A US 54035203A US 2006230879 A1 US2006230879 A1 US 2006230879A1
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- reactor
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- fluidized bed
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000010438 heat treatment Methods 0.000 title abstract description 14
- 239000007787 solid Substances 0.000 claims abstract description 95
- 239000000203 mixture Substances 0.000 claims abstract description 26
- 239000002245 particle Substances 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims description 183
- 238000001816 cooling Methods 0.000 claims description 27
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 16
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 238000004140 cleaning Methods 0.000 claims description 9
- 239000012717 electrostatic precipitator Substances 0.000 claims description 8
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims description 8
- 229910052737 gold Inorganic materials 0.000 claims description 8
- 239000010931 gold Substances 0.000 claims description 8
- 239000012528 membrane Substances 0.000 claims description 7
- 239000002918 waste heat Substances 0.000 claims description 6
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 2
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 claims description 2
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 2
- 229910052802 copper Inorganic materials 0.000 claims description 2
- 239000010949 copper Substances 0.000 claims description 2
- 229910052742 iron Inorganic materials 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 229910052709 silver Inorganic materials 0.000 claims description 2
- 239000004332 silver Substances 0.000 claims description 2
- 229910052725 zinc Inorganic materials 0.000 claims description 2
- 239000011701 zinc Substances 0.000 claims description 2
- 239000007858 starting material Substances 0.000 claims 1
- 230000014759 maintenance of location Effects 0.000 description 10
- WGPCGCOKHWGKJJ-UHFFFAOYSA-N sulfanylidenezinc Chemical compound [Zn]=S WGPCGCOKHWGKJJ-UHFFFAOYSA-N 0.000 description 9
- 229910052984 zinc sulfide Inorganic materials 0.000 description 9
- 239000000463 material Substances 0.000 description 6
- 239000000725 suspension Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 230000001105 regulatory effect Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005243 fluidization Methods 0.000 description 4
- 239000000428 dust Substances 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052960 marcasite Inorganic materials 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000011164 primary particle Substances 0.000 description 1
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 1
- 229910052683 pyrite Inorganic materials 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 239000011163 secondary particle Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- YALHCTUQSQRCSX-UHFFFAOYSA-N sulfane sulfuric acid Chemical compound S.OS(O)(=O)=O YALHCTUQSQRCSX-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0002—Preliminary treatment
- C22B15/001—Preliminary treatment with modification of the copper constituent
- C22B15/0013—Preliminary treatment with modification of the copper constituent by roasting
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1854—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement inside the reactor to form a loop
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
- B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
- C22B1/10—Roasting processes in fluidised form
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B15/00—Fluidised-bed furnaces; Other furnaces using or treating finely-divided materials in dispersion
- F27B15/02—Details, accessories, or equipment peculiar to furnaces of these types
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00725—Mathematical modelling
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B15/00—Fluidised-bed furnaces; Other furnaces using or treating finely-divided materials in dispersion
- F27B15/02—Details, accessories, or equipment peculiar to furnaces of these types
- F27B15/08—Arrangements of devices for charging
Abstract
The invention relates to a method and a plant for the heat treatment of sulfidic ores, in which solids are heated to a temperature of approximately 450 to 1500° C. in a fluidized bed reactor (1). In order to improve the energy utilization, it is proposed to introduce a first gas or gas mixture from below through a gas supply tube (3) into a mixing chamber (7) of the reactor (1), the gas supply tube (3) being at least partly surrounded by a stationary annular fluidized bed (35) which is fluidized by supplying fluidizing gas. The gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed (35) are adjusted such that the particle Froude numbers in the gas supply tube (3) are between 1 and 100, in the annular fluidized bed (35) between 0.02 and 2 and in the mixing chamber (7) between 0.3 and 30.
Description
- The present invention relates to a method for the heat treatment of in particular sulfidic ores, in which fine-grained solids are treated at a temperature of 450 to approximately 1500° C. in a first fluidized bed reactor, and to a corresponding plant.
- Such a method and a plant for the treatment of sulfidic ores containing gold are known for example from DE 196 09 286 A1. In that case, the ore is fluidized in a circulating fluidized bed of a roasting reactor by a gas containing oxygen, with metal sulfides being converted into metal oxides and an exhaust gas containing SO2 being obtained.
- It is further known to roast sulfidic ores, such as for example zinc blende, in a stationary fluidized bed furnace at temperatures between 500 and 1100° C. with air being supplied. In this roasting of zinc blende in a stationary fluidized bed furnace, up to 1000 metric tons of blende per day can be processed.
- The energy utilization of the heat treatment achieved when using a stationary fluidized bed is felt to be in need of improvement. One reason for this is that the mass and heat transfer is rather moderate on account of the comparatively low degree of fluidization. Furthermore, in the case of stationary fluidized beds, fine particles are discharged too quickly from the reactor, so that the retention time in the plant is not adequate for a complete reaction. This problem arises especially in the case of circulating fluidized beds due to the higher degree of fluidization, although better mass and heat transfer conditions prevail. Since the sulfidic ores used for the heat treatment, such as for example gold ore, zinc blende or concentrate, become increasingly fine, for example with a grain size fraction below 45 μm of 75%, an adequate roasting result can only be achieved with difficulty with the known methods and plants.
- Moreover, in the case of the known methods and plants, the temperature in the reactor can scarcely be regulated, further impairing the roasting result.
- Therefore, it is the object of the present invention to provide a method for the heat treatment of sulfidic ores which can be carried out more efficiently and is distinguished in particular by better roasting results along with good conditions for heat and mass transfer.
- In accordance with the invention, this object is achieved by a method as mentioned above in which a first gas or gas mixture is introduced from below through a preferably centrally arranged gas supply tube (central tube) into a mixing chamber region of the reactor, the central tube being at least partly surrounded by a stationary annular fluidized bed which is fluidized by supplying fluidizing gas, and in which the gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed are adjusted such that the particle Froude numbers in the central tube are between 1 and 100, in the annular fluidized bed between 0.02 and 2 and in the mixing chamber between 0.3 and 30.
- In the method of the invention, the advantages of a stationary fluidized bed, such as a longer solids retention time, and the advantages of a circulating fluidized bed, such as a good mass and heat transfer, can surprisingly be combined with each other during the heat treatment, such as for example the roasting of sulfidic ores, while the disadvantages of both systems are avoided. When passing through the upper region of the central tube, the first gas or gas mixture entrains solids from the annular stationary fluidized bed, which is referred to as the annular fluidized bed, into the mixing chamber, so that, due to the high speed differences between the solids and the first gas, an intensively mixed suspension is formed and an optimum heat and mass transfer between the two phases is achieved. By correspondingly adjusting the bed height in the annular fluidized bed as well as the gas velocities of the first gas or gas mixture and of the fluidizing gas, the solids load of the suspension above the orifice region of the central tube can be varied within wide ranges, so that the pressure loss of the first gas between the orifice region of the central tube and the upper outlet of the mixing chamber can be between 1 mbar and 100 mbar. In the case of high solids loading of the suspension in the mixing chamber, a large part of the solids will separate out from the suspension and fall back into the annular fluidized bed. In this way, the temperature in the annular fluidized bed can also be regulated by the amount of heated particles separating out. This recirculation is called internal solids recirculation, the stream of solids circulating in this internal circulation normally being significantly larger than the amount of solids supplied to the reactor from outside. The (smaller) amount of not precipitated solids is discharged from the mixing chamber together with the first gas or gas mixture. The retention time of the solids in the reactor can be varied within a wide range by the selection of the height and cross-sectional area of the annular fluidized bed and be adapted to the desired heat treatment. The amount of solids entrained from the reactor with the gas stream can be completely or at least partly recirculated to the reactor, with the recirculation expediently being fed into the stationary fluidized bed. The stream of solids thus recirculated to the annular fluidized bed normally lies in the same order of magnitude as the stream of solids supplied to the reactor from outside. With the method of the invention, on the one hand a high solids loading and at the same time a particularly good mass and heat transfer can consequently be achieved. Apart from the excellent utilization of energy, another advantage of the method in accordance with the invention consists in the possibility of quickly, easily and reliably adjusting the transfer of energy of the method and the mass transfer to the requirements by changing the flow velocities of the first gas or gas mixture and of the fluidizing gas.
- The heat transfer can be further intensified if the reactor is provided downstream with a second reactor, into which a gas mixture laden with solids is introduced from the first reactor. This preferably takes place from below through a, for example central, gas supply tube into a mixing chamber, the gas supply tube being surrounded at least partly by a stationary annular fluidized bed which is fluidized by supplying fluidizing gas. In principle, a single reactor is adequate for performing the method according to the invention. However, the combination of a reactor with a second reactor of a similar type of construction to form a reactor stage allows the overall retention time of the solids in the plant to be increased distinctly.
- To ensure a particularly effective heat transfer in the mixing chamber and a sufficient retention time in the reactors, the gas velocities of the first gas mixture and of the fluidizing gas are preferably adjusted for the fluidized bed such that the dimensionless particle Froude numbers (FrP) are 1.15 to 20, in particular between 3.95 and 11.6, in the central tube, 0.11 to 1.15, in particular between 0.11 and 0.52, in the annular fluidized bed, and/or 0.37 to 3.7, in particular between 0.53 and 1.32, in the mixing chamber. The particle Froude numbers are each defined by the following equation:
with -
- u=effective velocity of the gas flow in m/s
- pf=effective density of the fluidizing gas in kg/m3
- ps=density of a solid particle in kg/m3
- dp=mean diameter in m of the particles of the reactor inventory (or the particles forming) during operation of the reactor
- g=gravitational constant in m/s2.
- When using this equation it should be considered that dp does not indicate the mean diameter (d50) of the material used, but the mean diameter of the reactor inventory formed during the operation of the reactor, which can differ significantly in both directions from the mean diameter of the material used (primary particles). It is also possible for particles (secondary particles) with a mean diameter of 20 to 30 μm to be formed for instance during the heat treatment from very fine-grained material with a mean diameter of, for example, 3 to 10 μm. On the other hand, some materials, for example ores, are decrepitated during the heat treatment.
- In a development of the idea of the invention, it is proposed to adjust the bed height of solids in the reactor or the reactor stage such that the annular fluidized bed extends beyond the upper orifice end of the central tube by a few centimetres, and thus solids are constantly introduced into the first gas or gas mixture and entrained by the gas stream to the mixing chamber located above the orifice region of the central tube. In this way, there is achieved a particularly high solids loading of the suspension above the orifice region of the central tube.
- By means of the method in accordance with the invention, all kinds of sulfidic ores, in particular also those which contain gold, zinc, silver, nickel, copper and/or iron, can be effectively heat-treated. In particular, the method is suitable for the roasting of gold ore or zinc blende. The intensive mass and heat transfer and the adjustable retention time in the reactors allows a particularly high degree of conversion of the roasted material to be achieved.
- The generation of the amount of heat necessary for the operation of the reactor can be effected in any way known to the expert for this purpose. According to a preferred embodiment of the present invention, it is provided that, for the roasting, the reactors are supplied with oxygen-containing gas, for example with an oxygen content of approximately 20 vol-%, which is introduced into the annular fluidized beds of the reactors. The gas may be air, air enriched with oxygen or some other oxygen-containing gas. The oxygen-containing gas is preferably introduced into the reactor or the reactors with a temperature of approximately 25 to 50° C. The process of roasting sulfidic ores with excess of oxygen to form metal oxides is exothermal, so that usually no further heat has to be supplied to the reactor or the reactor stage.
- The energy utilization can be further improved in the case of the method in accordance with the invention by heat being supplied to or extracted from the first and/or second reactor in the annular fluidized bed and/or in the mixing chamber. Thus, in the case of an exothermal reaction, for example, the generated heat can be used in the reactor for steam generation for example.
- A cooling device is preferably provided downstream of the second reactor, in order to cool the solids-laden gas mixture emerging from the reactor to a temperature suitable for the further treatment of below 400° C., in particular to approximately 380° C. This cooling device may also be used for example for generating water vapour, whereby the energy utilization of the overall method is further improved.
- A separator, for example a cyclone or the like, may be provided downstream of the reactor stage. The solids separated from exhaust gases can be returned from the separator into the reactor stage, for example into the annular fluidized bed, from one or more reactors, or be passed on to a further cooling device.
- The retention time of the solids in the reactor stage can be varied in this way. In addition, the bed height of the solids in one or more reactors can be deliberately adapted to the requirements. The bed height in the annular fluidized bed in this case also influences the temperature established in the annular fluidized bed, since more particles are entrained into the mixing chamber and separated out from it in a heated state when there is a higher bed height. In this way, the temperature in the reactor can be deliberately regulated by the amount of solids recirculated from the separator.
- Preferably provided downstream of the separator is a gas cleaning stage with a hot-gas electrostatic precipitator and/or a wet-gas treatment, in which at least part of the exhaust gases separated from the solids in the separator is further cleaned. The cleaned exhaust gases can then be returned, for example as preheated fluidizing gas, into the annular fluidized bed of the first and/or second reactor. Part of the exhaust gas separated from the solids in the separator may also be supplied to a plant for producing sulfuric acid. The SO2-containing exhaust gases of the reactor stage can in this way be used for producing a byproduct.
- Coarse-grained solids and/or roasting residue are drawn off from the annular fluidized bed of the first and/or second reactor and passed on to a further cooling device, for example a fluidized bed cooler. The discharge of the solids or of the roasting residue may in this case take place discontinuously, whereby the amount of solids in the reactor stage can at the same time be regulated.
- A plant in accordance with the invention, which is in particular suited for performing the method described above, has a reactor constituting a fluidized bed reactor for the heat treatment of sulfidic ores, the reactor having a gas supply system which is formed such that gas flowing through the gas supply system entrains solids from a stationary annular fluidized bed, which at least partly surrounds the gas supply system, into the mixing chamber. Preferably, this gas supply system extends into the mixing chamber. It is, however, also possible to let the gas supply system end below the surface of the annular fluidized bed. The gas is then introduced into the annular fluidized bed for example via lateral apertures, entraining solids from the annular fluidized bed into the mixing chamber due to its flow velocity.
- In accordance with a preferred aspect of the invention, the gas supply system has a central tube extending upwards substantially vertically from the lower region of the reactor, which is at least partly surrounded in an annular manner by a chamber in which the stationary annular fluidized bed is formed. The annular fluidized bed does not have to be annular, but rather other forms of the annular fluidized bed are also possible, in dependence on the geometry of the central tube and the reactor, as long as the central tube is at least partly surrounded by the annular fluidized bed.
- Of course, two or more central tubes with different or identical dimensions or shapes may also be provided in the reactor. Preferably, however, at least one of the central tubes is arranged approximately centrally with reference to the cross-sectional area of the reactor.
- In accordance with a further embodiment of the present invention, the central tube has apertures on its shell surface, for example in the form of slots, so that during the operation of the reactor solids constantly get into the central tube through the apertures and are entrained by the first gas or gas mixture from the central tube into the mixing chamber.
- In order to increase the throughput of the plant or the solids retention time, instead of a single reactor there may also be a number of reactors, in particular two, connected to form a reactor stage. The reactors preferably have in each case an annular chamber for a stationary annular fluidized bed and a mixing chamber for the formation of a circulating fluidized bed, the central tube of a downstream reactor being connected to the exhaust-gas outlet of the reactor provided upstream of it.
- In accordance with a preferred embodiment, a separator, in particular a cyclone, is provided downstream of the reactor, or the reactor stage, for the separation of solids. The separator may have a solids conduit leading to the annular fluidized bed of the first reactor and/or a solids conduit leading to the annular fluidized bed of a second reactor possibly provided downstream.
- If a cooling device is provided downstream of the reactor stage, the solids-laden gas mixture discharged from the reactor stage can be cooled before further treatment to the temperature required for this. A waste-heat boiler provided with banks of cooling tubes may be used for example as the cooling device, it being possible for the banks of cooling tubes to serve at the same time for steam generation.
- Furthermore, the temperature required for the heat treatment may be exactly adjusted in the first and/or second reactor by means of temperature-control elements. For this purpose, the reactor may be provided as a natural circulation boiler with cooling elements and membrane walls.
- To provide for a reliable fluidization of the solids and the formation of a stationary fluidized bed, provided in the annular chamber of the first reactor and/or the further reactors is a gas distributor which divides the chamber into an upper fluidized bed region and a lower gas distributor chamber. The gas distributor chamber is connected to a supply conduit for fluidizing gas. Instead of the gas distributor chamber, a gas distributor composed of tubes may also be used.
- Preferably, the separator of the reactor or of the reactor stage is connected to a supply conduit leading into the annular chamber of a reactor, so that the exhaust gas, possibly further cleaned beforehand, can be used as a pre-heated fluidizing gas.
- As an alternative or in addition to this, a dedusting device and/or a plant for producing sulfuric acid may be provided downstream of the separator of the reactor or of the reactor stage.
- In the annular fluidized bed and/or the mixing chamber of the reactor, means for deflecting the solids and/or fluid flows may be provided in accordance with the invention. It is for instance possible to position an annular weir, whose diameter lies between that of the central tube and that of the reactor wall, in the annular fluidized bed such that the upper edge of the weir protrudes beyond the solids level obtained during operation, whereas the lower edge of the weir is arranged at a distance from the gas distributor or the like. Thus, solids raining out of the mixing chamber in the vicinity of the reactor wall must first pass by the weir at the lower edge thereof, before they can be entrained by the gas flow of the central tube back into the mixing chamber. In this way, an exchange of solids is enforced in the annular fluidized bed, so that a more uniform retention time of the solids in the annular fluidized bed is obtained.
- Developments, advantages and application possibilities of the invention also emerge from the following description of an exemplary embodiment and the drawing. All features described and/or illustrated in the drawing form the subject-matter of the invention per se or in any combination, independently of their inclusion in the claims or their back-reference.
- The single figure shows a process diagram of a method and a plant in accordance with an exemplary embodiment of the present invention.
- In the method shown in the figure, which is in particular suited for the heat treatment of sulfidic ores, solids are introduced into a first reactor 1 via a
supply conduit 2. The reactor 1, which is cylindrical for example, has acentral tube 3, which is arranged approximately coaxially with the longitudinal axis of the reactor and extends substantially vertically upwards from the bottom of the reactor 1. - Provided in the region of the bottom of the reactor 1 is an annular
gas distributor chamber 4, which is closed off at the top by agas distributor 5 having apertures. Asupply conduit 6 opens out into thegas distributor chamber 4. Arranged in the vertically upper region of the reactor 1, which forms a mixingchamber 7, is adischarge conduit 8, which opens out into asecond reactor 9. - The
second reactor 9 is largely similar in construction to the first reactor 1. Extending from the bottom of thereactor 9 substantially vertically upwards is acentral tube 10, which is connected to thedischarge conduit 8 of the first reactor 1 and is arranged approximately coaxially with the longitudinal axis of thereactor 9. - Provided in the region of the bottom of the
reactor 9 is an annulargas distributor chamber 11, which is closed off at the top by agas distributor 12 having apertures. Asupply conduit 13 opens out into thegas distributor chamber 11. Afurther supply conduit 14 is provided for introducing solids into thereactor 9 during the starting-up of the plant. - Temperature-
control elements gas distributors reactors 1 and 9 are formed asmembrane walls - Arranged in the vertically upper region of the
second reactor 9, which forms a mixingchamber 19, is a waste-heat boiler 21 provided with banks of coolingtubes 20. Via aconduit 22, the waste-heat boiler 21 is in connection with a separator, which is formed as acyclone 23. Asolids conduit 24 returns the solids from a floatingtank 25, provided downstream of thecyclone 23, into thereactors 1 or 9 or supplies the solids to afurther cooling device 26. Arranged above thegas distributors discharge conduits further cooling device 26. Thecooling device 26 is formed as a fluidized bed cooler, in which the stream of product is subjected to fluidizing air and cooled by acooling element 29. - Via a
conduit 30, the exhaust gas separated from the solids from thecyclone 23 is supplied to a gas cleaning stage, which has a hot-gaselectrostatic precipitator 31 and wet-gas cleaning 32. The dedusted exhaust gas can either be passed on to aplant 33 for the production of sulfuric acid and/or viaconduit 34 as fluidizing gas into thereactors 1 and 9 viaconduits - During operation of the plant, solids are introduced into the reactor 1 via the
supply conduit 2, so that a layer annularly surrounding thecentral tube 3, which is referred to as an annularfluidized bed 35, forms on thegas distributor 5. Fluidizing gas introduced into thegas distributor chamber 4 through thesupply conduit 6 flows through thegas distributor 5 and fluidizes the annularfluidized bed 35, so that a stationary fluidized bed is formed. The velocity of the gases supplied to the reactor 1 is adjusted such that the particle Froude number in the annularfluidized bed 35 is approximately 0.11 to 0.52. - By supplying further solids into the annular
fluidized bed 35, the level of the solids in the reactor 1 increases to the extent that solids enter the orifice of thecentral tube 3. At the same time, a gas or gas mixture is also introduced into the reactor 1 through thecentral tube 3. The velocity of the gas supplied to the reactor 1 is preferably adjusted such that the particle Froude number in thecentral tube 3 is approximately 3.95 to 11.6 and in the mixingchamber 7 approximately 0.53 to 1.32. Due to these high gas velocities, the gas flowing through thecentral tube 3 entrains solids from the stationary annularfluidized bed 35 into the mixingchamber 7 when passing through the upper orifice region. - Due to the banking of the level of the annular
fluidized bed 35 as compared to the upper edge of thecentral tube 3, solids flow over this edge into thecentral tube 3, whereby an intensively mixed suspension is formed. The upper edge of thecentral tube 3 may be straight, corrugated or indented or have lateral apertures. As a result of the reduction of the flow velocity by the expansion of the gas jet and/or by impingement on one of the reactor walls, the entrained solids in the mixingchamber 7 quickly lose speed and partly fall back again into the annularfluidized bed 35. The amount of not precipitated solids is discharged from the reactor 1 together with the gas stream via theconduit 8 and passed into thereactor 9. Between the reactor regions of the stationary annularfluidized bed 35 and the mixingchamber 7 there is thereby obtained a solids circulation which ensures a good heat transfer. - Before further processing, the solids discharged via the
conduit 8 are treated in thesecond reactor 9 in the way explained above with reference to reactor 1, so that a stationaryfluidized bed 36 is likewise formed above thegas distributor 12 in thereactor 9 by solids separating out from the mixingchamber 19. Moreover, the dust separated in the hot-gaselectrostatic precipitator 31 is returned via a recirculating conduit into the stationary annularfluidized bed 36 of thesecond reactor 9. The particle Froude numbers in thesecond reactor 9 correspond approximately to those of the first reactor 1. - The bed height of the solids in the
reactors 1 and 9 is regulated not only by the supply of solids viaconduit 2 but also firstly by means of the amount of solids returned from thecyclone 23 into the reactors and moreover by means of the amount of solids extracted from the reactors viaconduits - The solids removed from the
cyclone 23 and/or directly from thereactors 1 and 9 are cooled in the fluidized bed cooler 26 to a temperature suitable for the further processing. After cleaning in the hot-gaselectrostatic precipitator 31 and the wet-gas cleaning 32, the exhaust gas separated from the solids in thecyclone 23 can be partly supplied to the reactors as pre-heated fluidizing gas or to thesulfuric acid plant 33. - The invention will be described below with reference to two examples demonstrating the inventive idea, but not restricting the same.
- In a plant corresponding to the figure, 1200 kg/h of ground, dried and classified gold ore with a gold content of approximately 5 ppm, i.e. 5 g/t, and a maximum grain fraction of 50 μm, containing
-
- 1.05 wt-% organic carbon
- 19.3 wt-% CaCO3
- 12.44 wt-% Al2O3
- 2.75 wt-% FeS2
- 64.46 wt-% inert substances (for example SiO2),
were supplied in continuous operation to the reactor 1, the upper part of which had a diameter of 800 mm. Furthermore, 2500 Nm3/h of air with a temperature of 520° C. were introduced into the reactor 1 via thecentral tube 3 and viaconduit 6 as fluidizing gas. The particle Froude number was in this case between 3.95 and 6.25 in thecentral tube 3, between 0.84 and 1.32 in the mixingchamber 7 and between 0.32 and 0.52 in the annularfluidized bed 35.
- The retention time of the gold ore in the reactor 1 was between 5 and 10 minutes, with a temperature of between 600 and 780° C. being established in the reactor. 0.5 to 6.0 vol-% of residual oxygen were measured in the exhaust gas. The content of organic carbon in the product after the heat treatment was below 0.1%.
- In a plant corresponding to the figure, 42 t/h of zinc blende with a temperature of approximately 25° C. were supplied to the reactor 1 from a charging bunker with a capacity of about 200 m3 via
conduit 2 and a dosing device into the annularfluidized bed 35. At the same time, approximately 16,600 Nm3/h of air with a temperature of 47° C. and a pressure of approximately 1.2 bar, containing -
- 77.1 vol-% N
- 20.4 vol-% O2
- 2.5 vol-% H2O,
were introduced viaconduit 6 to the annular fluidized bed. Approximately 60,200 Nm3/h of air and additionally 3000 Nm3/h of exhaust cooler air from the fluidized bed cooler 26 with a temperature of 150° C. were passed through thecentral tube 3 to the reactor 1, so that the total amount of air passed to thecentral tube 3 was approximately 63,200 Nm3/h. The air had a temperature of 35° C. and a pressure of 1.07 bar and contained - 77.1 vol-% N
- 20.4 vol-% O2
- 2.5 vol-% H2O.
- The particle Froude number was in this case between 4.4 and 11.6 in the
central tube 3, between 0.53 and 1.15 in the mixingchamber 7 and between 0.11 and 0.3 in the annularfluidized bed 35. The reaction of the sulfidic zinc blende with the free oxygen of the fluidizing air to form metal oxide caused a temperature of 930° C. to be established in the reactor 1. At the same time, approximately 15.4 MW of heat were extracted from the reactor 1 via thecooling element 15 and themembrane wall 17 and used to generate saturated steam from cooling water. The temperature in the region of theconduit 8 at the outlet of the reactor 1 was thereby lowered to 800° C. To avoid an enrichment of coarse material in the reactor 1, approximately 0.16 t/h of product with a temperature of 901° C. were extracted from the annularfluidized bed 35 in discontinuous operation viaconduit 27 as coarse-grained run-off and passed to thefluidized bed cooler 26. - A solids-laden gas mixture with a pressure of 1.049 bar comprising 110.9 t/h of solids and approximately 79,600 Nm3/h of exhaust gas, containing
-
- 12.1 vol-% SO2
- 77.2 vol-% N
- 2.5 vol-% O2
- 8.2 vol-% H2O,
were passed to thecentral tube 10 of thesecond reactor 9 viaconduit 8. Furthermore, approximately 17,350 Nm3/h of air with a temperature of 43° C. at a pressure of approximately 1.18 bar, containing - 77.1 vol-% N
- 20.4 vol-% O2
- 2.5 vol-% H2O,
were supplied to thereactor 9 viaconduit 13 for fluidization. During start-up operation, 5 t/h of solids with a temperature of 25° C. were at the same time charged to thereactor 9 viaconduit 14. The solids-laden gas mixture was cooled to 480° C. in the mixingchamber 19 of thereactor 9, with a total of approximately 23.6 MW of heat being removed from thereactor 9 by thecooling element 16, themembrane wall 18 and the waste-heat boiler 21 and used to generate saturated steam from cooling water. Thecooling element 16 was in this case used as a steam superheater with a superheating temperature of 400° C.
- Approximately 96,200 Nm3/h of solids-laden gas mixture with a temperature of 380° C. and a pressure of 1.018 bar, which was laden with 213.5 t/h of solids and had the following composition:
-
- 9.4 vol-% SO2
- 77.8 vol-% N
- 5.5 vol-% O2
- 7.3 vol-% H2O
were removed from thereactor 9 viaconduit 22.
- In the
cyclone 23, the exhaust gas was separated from the solids to the extent that approximately 96,200 Nm3/h of air with a dust content of 50 g/Nm3 (4.81 t/h of solids) were passed on to the hot-gaselectrostatic precipitator 31 viaconduit 30. There, the exhaust gas was dedusted to a dust content of 50 mg/Nm3 and passed on to the wet-gas cleaning 32 and the downstreamsulfuric acid plant 33. - From the
cyclone 23, approximately 208 t/h of solids with a temperature of 380° C. were passed firstly to the floatingtank 25, serving as a buffer vessel, and divided in such a way that 76.2 t/h were passed into the annularfluidized bed 35 of the first reactor 1, approximately 100.9 t/h into the annularfluidized bed 36 of thesecond reactor 9 and 31 t/h into thefluidized bed cooler 26. - In this way it was possible for the bed height of the annular
fluidized beds reactors 1 and 9, to be adjusted to approximately 1 m. The solids were then cooled in the fluidized bed cooler 26 by thecooling element 29 to a temperature of below 150° C., with an amount of heat of approximately 1.7 MW being removed. As a result, a total of approximately 40.8 MW were removed from the plant and converted into 55.2 t/h of superheated steam with a pressure of 40 bar and a temperature of 400° C. - The product discharged from the fluidized bed cooler 26 was mixed with approximately 4.8 t/h of solids with a temperature of approximately 380° C., which were separated from the exhaust gas of the
cyclone 30 by the hot-gaselectrostatic precipitator 31. The stream of product discharged altogether from the plant was consequently approximately 36.54 t/h at a temperature of approximately 182° C. - In this way it was possible for even zinc blende or a zinc blende concentrate with a grain size fraction below 45 μm of 75% to be roasted in the plant in such a way that the end product contained 0.3 wt-% of sulfide sulfur and 1.8 wt-% of sulfate sulfur.
-
- 1 (first) reactor chamber
- 2 (solids) supply conduit
- 3 central tube (gas supply tube)
- 4 gas distributor chamber
- 5 gas distributor
- 6 (gas) supply conduit
- 7 mixing chamber
- 8 conduit
- 9 (second) reactor
- 10 central tube (gas supply tube)
- 11 gas distributor chamber
- 12 gas distributor
- 13 (gas) supply conduit
- 14 (solids) supply conduit
- 15 temperature-control element
- 16 temperature-control element
- 17 membrane wall
- 18 membrane wall
- 19 mixing chamber
- 20 bank of cooling tubes
- 21 waste-heat boiler
- 22 conduit
- 23 cyclone
- 24 conduit
- 25 floating tank
- 26 fluidized bed cooler
- 27 conduit
- 28 conduit
- 29 cooling element
- 30 conduit
- 31 hot-gas electrostatic precipitator
- 32 wet-gas cleaner
- 33 plant for producing sulfuric acid
- 34 conduit
- 35 annular fluidized bed
- 36 annular fluidized bed
Claims (35)
1. A method for heat treating sulfidic ores, comprising treating solids at a temperature of 450 to approximately 1500° C. in a fluidized bed reactor, introducing from below a first gas or gas mixture through a gas supply tube into a mixing chamber of the reactor, the gas supply tube being at least partly surrounded by a stationary annular fluidized bed which is fluidized by supplying fluidizing gas, and adjusting gas velocities of the first gas or gas mixture and the fluidizing gas for the annular fluidized bed wherein the gas velocities have a particle Froude number in the gas supply tube between 1 and 100, in the annular fluidized bed between 0.02 and 2, and in the mixing chamber between 0.3 and 30.
2. The method as claimed in claim 1 , wherein the fluidized bed reactor or first reactor is provided downstream with a second reactor, into which a gas mixture laden with solids is introduced from the first reactor from below through a gas supply tube into a mixing chamber, the gas supply tube being surrounded at least partly by a stationary annular fluidized bed which is fluidized by supplying fluidizing gas.
3. The method as claimed in claim 1 , wherein the particle Froude number in the gas supply tube is between 1.15 and 20.
4. The method as claimed in claim 1 , wherein the particle Froude number in the annular fluidized bed is between 0.11 and 1.15.
5. The method as claimed in claim 1 , wherein the particle Froude number in the mixing chamber is between 0.37 and 3.7.
6. The method as claimed in claim 1 , adjusting the solids in each reactor to have a bed height such that the annular fluidized bed extends beyond the upper orifice end of the gas supply tube and that solids are constantly introduced into the first gas or gas mixture and entrained by the gas stream to the mixing chamber located above the orifice region of the gas supply tube.
7. The method as claimed in claim 1 , wherein the sulfidic ore, comprises gold, zinc, silver, copper, nickel and/or iron, as starting material.
8. The method as claimed in claim 1 , wherein at least one reactor is supplied with oxygen-containing gas, through the gas supply tube and/or into the annular fluidized bed.
9. The method as claimed in claim 1 , wherein heat is supplied to or extracted from at least one reactor in the annular fluidized bed and/or in the mixing chamber.
10. The method as claimed in claim 1 , wherein provided downstream of at least one reactor is a cooling device, in which a solids-laden gas mixture from the reactor is cooled to a temperature of below 400° C.
11. The method as claimed in claim 1 , wherein provided downstream of at least one reactor is a separator, from which solids separated from exhaust gases are supplied to the first and/or second reactor or to a further cooling device.
12. The method as claimed in claim 11 , wherein at least part of the exhaust gases separated from the solids in the separator is supplied to the first and/or the second reactor as fluidizing gas, in particular after treatment in a downstream gas cleaning stage.
13. The method as claimed in claim 11 or wherein at least part of the exhaust gases separated from the solids in the separator is supplied to a plant for producing sulfuric acid.
14. The method as claimed in claim 11 , wherein the solids comprising coarse-grained solids and/or roasting residue are drawn off, discontinuously, from the annular fluidized bed of the first and/or second reactor and passed on to a further cooling device.
15. A plant for heat treating sulfidic ores, by the method as claimed in claim 1 , comprising a reactor constituting a fluidized bed reactor, wherein the reactor has a gas supply system which is formed such that gas flowing through the gas supply system entrains solids from a stationary annular fluidized bed, which at least partly surrounds the gas supply system, into the mixing chamber.
16. The plant as claimed in claim 15 , wherein the gas supply system has at least one gas supply tube extending upwards substantially vertically from the lower region of the reactor into a mixing chamber of the reactor, the gas supply tube being at least partly surrounded by an annular chamber in which the stationary annular fluidized bed is formed.
17. The plant as claimed in claim 16 , wherein the reactor is provided downstream with a second reactor, which has a gas supply tube, which is connected to a discharge conduit for solids-laden gas mixtures provided at the upper end of the first reactor and is formed such that gas flowing through the gas supply tube entrains solids from a stationary annular fluidized bed, which at least partly surrounds the gas supply tube, into the mixing chamber.
18. The plant as claimed in claim 16 wherein the gas supply tube is arranged approximately centrally with reference to the cross-sectional area of the reactor.
19. The plant as claimed in claim 18 , wherein a solids separator, is provided downstream of the second reactor, for the separation of solids, and that the solids separator has a solids conduit leading to the annular fluidized bed of the first and/or second reactor.
20. The plant as claimed in claim 18 wherein a cooling device, is provided downstream of the second reactor.
21. The plant as claimed in claim 18 , wherein temperature-control elements are provided in the first and/or second reactor.
22. The plant as claimed in claim 18 , wherein a gas distributor which divides the annular chamber into an upper fluidized bed region and a lower gas distributor chamber is provided in the first and/or second reactor, and that the gas distributor chamber is connected to a supply conduit for fluidizing gas.
23. The plant as claimed in claim 19 , wherein the first and/or second reactor has a supply conduit which leads to the annular chamber and is connected to an exhaust-gas conduit of the separator provided downstream of the second reactor.
24. The plant as claimed in claim 19 , wherein a dedusting device and/or a plant for producing sulfuric acid is provided downstream of the separator.
25. The method as claimed in claim 1 , wherein the gas supply tube is arranged approximately central.
26. The method as claimed in claim 3 , wherein the particle Froude number in the gas supply tube is between 3.95 and 11.6.
27. The method as claimed in claim 4 , wherein the particle Froude number in the annular fluidized bed is between 0.11 and 0.52.
28. The method as claimed in claim 5 , wherein the particle Froude number is between 0.53 and 1.32.
29. The method as claimed in claim 8 , wherein the oxygen-containing gas has an oxygen content of approximately 20 vol-%.
30. The method as claimed in claim 10 , wherein the solids-laden gas mixture is cooled to a temperature of approximately 380° C.
31. The method as claimed in claim 11 , wherein the separator is a cyclone.
32. The method as claimed in claim 12 , wherein gas cleaning stage is a hot-gas electrostatic precipitator and/or a wet-gas treatment.
33. The plant as claimed in claim 19 , wherein the solids separator is a cyclone.
34. The plant as claimed in claim 20 , wherein the cooling device is a waste-heat boiler with banks of cooling tubes.
35. The plant as claimed in claim 21 , wherein the temperature-control elements is a natural circulation boiler with cooling elements and membrane walls.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10260735.4 | 2002-12-23 | ||
DE10260735A DE10260735B4 (en) | 2002-12-23 | 2002-12-23 | Process and plant for heat treatment of sulfide ores |
PCT/EP2003/013984 WO2004057041A1 (en) | 2002-12-23 | 2003-12-10 | Method and plant for the heat treatment of sulfidic ores using annular fluidized |
Publications (1)
Publication Number | Publication Date |
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US20060230879A1 true US20060230879A1 (en) | 2006-10-19 |
Family
ID=32519334
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US10/540,352 Abandoned US20060230879A1 (en) | 2002-12-23 | 2003-12-10 | Method and plant for the heat treatment of sulfidic ores using annular fluidized |
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US (1) | US20060230879A1 (en) |
EP (1) | EP1583847B1 (en) |
JP (1) | JP2006511704A (en) |
KR (1) | KR20050093802A (en) |
CN (1) | CN100467630C (en) |
AT (1) | ATE410527T1 (en) |
AU (1) | AU2003296631B2 (en) |
BR (1) | BR0317707B1 (en) |
CA (1) | CA2510106A1 (en) |
DE (2) | DE10260735B4 (en) |
EA (2) | EA200800695A1 (en) |
ES (1) | ES2315570T3 (en) |
NO (1) | NO20053292L (en) |
PE (1) | PE20040633A1 (en) |
WO (1) | WO2004057041A1 (en) |
ZA (1) | ZA200505919B (en) |
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US20060162500A1 (en) * | 2002-12-23 | 2006-07-27 | Dirk Nuber | Fluidized bed method and plant for the heat treatment of solids containing titanium |
US20060230880A1 (en) * | 2002-12-23 | 2006-10-19 | Martin Hirsch | Method and plant for the heat treatment of solids containing iron oxide |
US20060231466A1 (en) * | 2002-12-23 | 2006-10-19 | Dirk Nuber | Method and apparatus for heat treatment in a fluidized bed |
US20060263292A1 (en) * | 2002-12-23 | 2006-11-23 | Martin Hirsch | Process and plant for producing metal oxide from metal compounds |
US20060278566A1 (en) * | 2002-12-23 | 2006-12-14 | Andreas Orth | Method and plant for producing low-temperature coke |
US20070137435A1 (en) * | 2002-12-23 | 2007-06-21 | Andreas Orth | Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor |
US20080124253A1 (en) * | 2004-08-31 | 2008-05-29 | Achim Schmidt | Fluidized-Bed Reactor For The Thermal Treatment Of Fluidizable Substances In A Microwave-Heated Fluidized Bed |
US7878156B2 (en) | 2002-12-23 | 2011-02-01 | Outotec Oyj | Method and plant for the conveyance of fine-grained solids |
US20110195016A1 (en) * | 2008-07-11 | 2011-08-11 | Outotec Oyj | Process and plant for producing calcine products |
WO2017129341A1 (en) * | 2016-01-26 | 2017-08-03 | Outotec (Finland) Oy | Method and apparatus for treating a leaching residue of a sulfur-containing metal concentrate |
WO2017162857A1 (en) * | 2016-03-24 | 2017-09-28 | Outotec (Finland) Oy | Process and facility for thermal treatment of a sulfur-containing ore |
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FI120556B (en) * | 2006-12-11 | 2009-11-30 | Foster Wheeler Energia Oy | A method and apparatus for controlling the temperature of a heat-binding fluidized bed reactor |
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2002
- 2002-12-23 DE DE10260735A patent/DE10260735B4/en not_active Expired - Fee Related
-
2003
- 2003-12-10 WO PCT/EP2003/013984 patent/WO2004057041A1/en active Application Filing
- 2003-12-10 US US10/540,352 patent/US20060230879A1/en not_active Abandoned
- 2003-12-10 AU AU2003296631A patent/AU2003296631B2/en not_active Ceased
- 2003-12-10 JP JP2004561262A patent/JP2006511704A/en not_active Withdrawn
- 2003-12-10 CN CNB2003801074375A patent/CN100467630C/en not_active Expired - Fee Related
- 2003-12-10 ZA ZA200505919A patent/ZA200505919B/en unknown
- 2003-12-10 KR KR1020057011924A patent/KR20050093802A/en not_active Application Discontinuation
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- 2003-12-10 EA EA200800695A patent/EA200800695A1/en unknown
- 2003-12-10 DE DE60324028T patent/DE60324028D1/en not_active Expired - Lifetime
- 2003-12-10 AT AT03813564T patent/ATE410527T1/en not_active IP Right Cessation
- 2003-12-10 BR BRPI0317707-6A patent/BR0317707B1/en not_active IP Right Cessation
- 2003-12-10 EA EA200501038A patent/EA010478B1/en not_active IP Right Cessation
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- 2003-12-10 ES ES03813564T patent/ES2315570T3/en not_active Expired - Lifetime
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DE10260735A1 (en) | 2004-07-15 |
BR0317707B1 (en) | 2012-01-24 |
KR20050093802A (en) | 2005-09-23 |
ZA200505919B (en) | 2006-12-27 |
EA010478B1 (en) | 2008-10-30 |
EP1583847A1 (en) | 2005-10-12 |
CA2510106A1 (en) | 2004-07-08 |
ES2315570T3 (en) | 2009-04-01 |
CN1732276A (en) | 2006-02-08 |
ATE410527T1 (en) | 2008-10-15 |
AU2003296631B2 (en) | 2009-07-23 |
NO20053292L (en) | 2005-09-14 |
PE20040633A1 (en) | 2004-11-05 |
WO2004057041A1 (en) | 2004-07-08 |
EP1583847B1 (en) | 2008-10-08 |
NO20053292D0 (en) | 2005-07-05 |
EA200501038A1 (en) | 2006-02-24 |
DE10260735B4 (en) | 2005-07-14 |
BR0317707A (en) | 2005-11-22 |
EA200800695A1 (en) | 2008-08-29 |
CN100467630C (en) | 2009-03-11 |
AU2003296631A1 (en) | 2004-07-14 |
DE60324028D1 (en) | 2008-11-20 |
JP2006511704A (en) | 2006-04-06 |
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