Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
  • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
  • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
  • B04C5/22—Apparatus in which the axial direction of the vortex is reversed with cleaning means
• • C—CHEMISTRY; METALLURGY
  • C21—METALLURGY OF IRON
  • C21B—MANUFACTURE OF IRON OR STEEL
  • C21B13/00—Making spongy iron or liquid steel, by direct processes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
  • B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
  • B04C5/00—Apparatus in which the axial direction of the vortex is reversed
• • C—CHEMISTRY; METALLURGY
  • C21—METALLURGY OF IRON
  • C21B—MANUFACTURE OF IRON OR STEEL
  • C21B13/00—Making spongy iron or liquid steel, by direct processes
  • C21B13/0033—In fluidised bed furnaces or apparatus containing a dispersion of the material
• • 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
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P10/00—Technologies related to metal processing
  • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
  • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

• the invention relates to a method for treating, preferably for reducing, particulate material in at least one fluidization zone at elevated temperature, in particular for reducing fine ore, the particulate material being held in the fluidization zone by a treatment gas flowing from the bottom up and being out with the treatment gas fine particle material discharged from the fluidization zone is separated from the treatment gas in a separation zone, the following steps being carried out in the separation zone: supplying the stream of treatment gas and discharged fine particle material to a separating device, separating the fine particle material from the treatment gas, the treatment gas being the waste gas is withdrawn from the separating device, and discharging the separated fine-particulate material from the separating device, and a device for carrying out the method.
• Fine dust has poor flow properties, particularly when hot, and tends to block and cake in cyclone outlets and inlets. In extreme cases, blockages of fine dust return lines can even occur.
• the flow properties of the fine dust are improved by adding coarse-grained material to the separation zone, i.e. whose tendency to stick to is reduced. Existing caking can even be reduced due to a cleaning effect that occurs when the coarse-grained material is added.
• coarse-grained material is used, the temperature of which is at least 200 ° C. below the temperature of the treatment gas and that of the fine-particle material.
• the temperature of the coarse-grained material is substantially below the temperature of the fine-particulate material.
• the temperature of the coarse-grained material is essentially ambient.
• the coarse-grained material is introduced into the stream of the treatment gas to be fed to the separation device.
• coarse-grained material is added to the fine-particulate material discharged from the separating device. This has proven to be particularly advantageous if the separated fine-particulate material is fed to a further fluidization zone.
• the location of the addition of the coarse material can be varied depending on the requirements of the method, but a simultaneous addition of coarse material at all of the above positions is also possible.
• the coarse-grained material is added pneumatically with the aid of a carrier gas.
• the carrier gas is chemically inert to the treatment gas, or is largely or completely identical to it.
• the treatment gas is a reducing gas containing CO and H 2
• the carrier gas is preferably also such a reducing gas containing CO and H 2 , particularly preferably one with the same composition.
• the pneumatic addition of the coarse-grained material has a particularly pronounced abrasive effect, so that it is not necessary to continuously add coarse-grained material and a periodic addition, for example pulsating, is sufficient.
• the coarse-grained material is added gravitationally.
• the coarse-grained material is, for example, introduced into a solids lock and introduced into the separating device under the influence of gravity.
• the coarse-grained material has a composition which is largely similar to that of the particulate material treated in the fluidization zone, or if the coarse-grained material has a composition which allows the coarse-grained material together with the particulate material to be located in a downstream of the fluidization zone Process step to process further.
• the coarse-grained material of ore and / or of additives such as lime, dolomite or MgO is therefore advantageously formed.
• the invention also relates to a device with at least one fluidized bed reactor with a lower part receiving the fluidization zone and with an upper part connected to a separating device, the separating device being separable from a separating device, preferably a cyclone, in which fine-particulate material from the treatment gas , a means for supplying treatment gas and fine-particulate material into the separation device, a treatment gas discharge line originating from the separation device and a solids discharge line starting from the separation device is formed.
• a separating device preferably a cyclone
• this object is achieved in that the separating device is provided with a means for feeding coarse-grained material into the separating device.
• the means for supplying treatment gas and fine-particulate material to the separating device is designed depending on the spatial arrangement of the fluidized bed reactor and the separating device, as well as on their spatial distance, and includes, for example, an inlet opening (in the case of an inner cyclone), a pipe (in the case of a slightly spaced one) external cyclone) or a pneumatic delivery line (if there is a greater distance between the fluidized bed reactor and the cyclone).
• the separating device is preferably designed as a cyclone, since this is by far the most frequently occurring application.
• the means for feeding coarse-grained material is designed as a lance which opens into the interior of the separating device in such a way that coarse-grained material can be introduced into the interior of the separating device.
• the means for supplying coarse-grained material is connected to the means for supplying treatment gas in such a way that coarse-grained material can be introduced into the stream of the fine-particulate material carried with the treatment gas.
• a further possibility of making coarse-grained material insertable into the separating device is that at least one additional inlet opening is provided on the separating device, through which the coarse-grained material can be introduced into the separating device with the means for feeding coarse-grained material.
• an additional inlet opening is advantageously arranged in such a way that coarse-grained material can be introduced into the cyclone essentially tangentially with the means for supplying coarse-grained material.
• the separation efficiency of the cyclone is least affected by a tangential feed of the coarse-grained material.
• an additional inlet opening is arranged such that coarse-grained material can be introduced into the separating device from above with the means for feeding coarse-grained material.
• Another embodiment of the device according to the invention is that the means for supplying coarse-grained material is connected to the solids discharge in such a way that coarse-grained material can be introduced into the stream of the fine-particulate material separated in the separating device.
• the device according to the invention can in principle be equipped with both internal and external separating devices, the solids discharge of an external separating device either being returned to the same fluidized bed reactor (circulating fluidized bed) or opening into a further fluidized bed reactor.
• the separating device is on the inside, the treatment gas discharge line is guided outside the fluidized bed reactor and the solids discharge line opens into the fluidization zone of the same fluidized bed reactor.
• the means for feeding coarse-grained material is designed as a pneumatic feeding device.
• the invention further relates to a device and a method for cleaning dust-laden gas in a separation chamber, in particular a cyclone, preferably by means of centrifugal force separation, the dust-laden gas flowing into the separation chamber via an opening and the at least partially cleaned gas via a line, for example via a Dip tube, again derived from the separation chamber, preferably flows out.
• the invention further relates to a method for reducing the gas flow from a separation chamber, in particular a cyclone, in which solid is separated from a gas, preferably by means of centrifugal force separation and the at least partially cleaned gas is discharged via at least one line for discharge, and the separation chamber, as a result of an at least partial blockage by the separated solid, shows a reduced separation performance, in particular compared to normal operation.
• Centrifugal separators generally refer to apparatuses in which the centrifugal force is used to separate solids, for example dust, from gases.
• the occurrence of caking in the cyclone must be taken into account, especially at high operating temperatures, i.e. cleaning hot, dust-containing exhaust gas.
• caking especially on the underflow of the centrifugal separator, cannot always be completely prevented, which is why suitable measures must be taken when the caking occurs and the subsequent impairment of operation.
• shut-off devices are susceptible to failure, especially at high temperatures, and require regular and intensive maintenance.
• corresponding functional designs of such shut-off devices are also very expensive to purchase.
• the present invention is therefore based on the object of overcoming the disadvantages of the prior art, and a simple and economical method according to the preamble of claims 20 and 24, and a suitable device, preferably for carrying out the method mentioned, according to claim 27 develop.
• the explanations for the invention are mostly based on a centrifugal separator, in particular a cyclone, for example, but in no way limit the use of the methods according to the invention, such as the device according to the invention, to these.
• caking and / or deposits which form in the separation chamber and / or in the region of the separation chamber are prevented or reduced , and / or caking already formed effectively, at least partially, removed.
• the caking is removed and / or blasted off, in particular by mechanical action.
• coarse bulk material in a predetermined grain size, composition and / or amount is fed into the separation chamber, in which the occurrence of caking in the separation chamber is reduced and / or caking already formed is at least partially removed.
• the coarse bulk material is preferably introduced via the line for discharging the at least partially cleaned gas.
• the coarse bulk material is introduced directly into the separation chamber.
• the coarse bulk material is fed into the separation chamber together with the dust-laden gas to be cleaned.
• Adequate kinetic energy of the bulk material particles is essential for the cleaning action of the bulk material, in particular in the separation chamber and / or on the material discharge line. Accordingly, for example when the bulk material is fed together with the dust-laden gas in the centrifugal separator, there must be a corresponding possibility for absorbing kinetic energy, preferably a corresponding head.
• the coarse bulk material has an average grain diameter, which at least partially prevents undesired discharge of the coarse bulk material from the separation chamber, in particular via the line for discharging the at least partially cleaned gas.
• the coarse bulk material is processed before it is introduced into the separation chamber in such a way that the coarse bulk material has an average grain diameter which reduces, in particular prevents, the discharge of the bulk material via the line for discharging the at least partially cleaned gas.
• the grain size required depends on the design of the separation chamber and on the flow conditions in the separation chamber and / or the line for discharging the at least partially cleaned gas.
• the material drain is laid in a separation chamber, in particular a cyclone, this is filled with the separated solid to just below the line for discharging the at least partially treated gas, in particular the immersion tube, so that the solids-laden gas can flow from the inlet to the immersion tube, and the solid to be separated through the line, in particular the dip tube, transported away.
• a separation chamber in particular a cyclone
• the undedusted gas flow does not come to a standstill and can even increase, depending on the flow resistances, in comparison to, for example, functioning separation chambers connected in parallel.
• this problem can be solved in a much more elegant manner in that a material filler neck, for example with a nominal diameter of approximately 200 mm, is preferably arranged in the gas line leading away and is preferably closed off with a ball valve.
• This ball valve can be designed for low temperatures due to a slight flushing flow and generally works without problems.
• a container with a crane is placed on the ball valve and flanged on.
• This container is with coarser bulk material - e.g. screened ore-filled.
• the ball valve is then opened and the bulk material fills the space left up to the dip tube and part of the dip tube.
• the dust-laden gas should now flow through this bed, whereupon the flow comes to a standstill.
• the initial flow of the dust-laden gas through the flow fills the interstices of the coarse bulk material with the transported fine dust, which ultimately results in an at least partial sealing of the bulk material. The cyclone is thus effectively shut off.
• the gas in the separation chamber is at least partially prevented from being discharged from the separation chamber via the line for discharging the at least partially treated gas, caused by the introduction of the coarse bulk material.
• the coarse bulk material has an average grain diameter which at least partially prevents discharge via the gas flow from the separation chamber, preferably from the separation chamber itself, in particular via the line for discharging the at least partially cleaned gas.
• the coarse bulk material is processed before it is introduced into the separation chamber in such a way that the coarse bulk material has an average grain diameter which reduces, in particular prevents, the discharge of the bulk material via the line for discharging the at least partially cleaned gas.
• the grain size required depends on the design of the separation chamber and on the flow conditions in the separation chamber and / or the line for discharging the at least partially cleaned gas.
• the invention is further characterized by a device according to claim 27, preferably for carrying out a method according to one or more of claims 20 to 23 and / or 24 to 26.
• a filler neck is preferably a device through which the coarse bulk material can be introduced into the line for discharging the gas which is at least partially cleaned in normal operation in the separation chamber.
• a filter and / or a grate is provided downstream of the separation chamber, in particular below the separation chamber, through which the coarse bulk material can be separated from the separated dusts.
• a device for removing the coarse bulk material is arranged downstream of the separation chamber, in particular below the separation chamber.
• the coarse bulk material can be recycled and, for example, again introduced into the separation chamber and / or into the line for discharging the at least partially cleaned gas in the manner described.
• the filler neck is provided as part of a device for the metered supply of the coarse bulk material, the device further comprising a controllable sluice or a controllable cellular wheel or another component for the metered supply of the bulk material.
• the device for the controlled supply has a container which can be coupled to the filler neck.
• the following devices are provided for the, in particular controlled, supply of coarse bulk material:
• Container which is either fixed or variable (can be coupled and uncoupled), again equipped with a corresponding lock, in particular a cellular wheel
• the method according to the invention and the device according to the invention are particularly preferably suitable for use in metallurgy technology, since dust-laden, hot gases which often require cleaning are often used here.
• the methods described and the device according to the invention for cleaning the reducing gas, in particular a fluidized bed process, preferably the metallurgical reduction technique, are particularly preferably used.
• the methods according to the invention and the device according to the invention are also particularly suitable for use in plants and methods in the non-ferrous metal industry or the non-metal industry, for example in cement production and / or cement processing.
• 1 shows an embodiment of the method according to the invention for treating, preferably for reducing, particulate material, and also a suitable device for carrying out the method
• FIG. 2 shows a further embodiment of the method according to the invention for treating, preferably for reducing, particulate material, as well as a device suitable for carrying out the method
• Fig. 3 shows a vertical cross section of a separator
• 4A and 4B show a separating device in vertical and horizontal cross section
• FIG. 5 shows an exemplary embodiment of a method and a device for cleaning a dust-laden gas
• FIG. 6 shows an exemplary embodiment of a method and a device for cleaning a dust-laden gas, as well as a way of introducing the coarse bulk material
• FIG. 7 shows a method for minimizing the gas flow from a separation chamber for separating solids from gases
• the fluidized bed reactor 1 shows a fluidized bed reactor 1, the lower part of which contains a fluidization zone 2.
• the fluidized bed reactor 1 is supplied with treatment gas from below through a treatment gas supply line 3.
• the treatment gas is evenly distributed via a gas distribution base 4, which can be designed, for example, as a nozzle grate, the particulate material in the fluidization zone 2 also being fluidized.
• the reactor 1 is provided with feed and discharge lines 5, 6 for particulate material, and with a discharge line 7 which at the same time forms the means 7 for supplying treatment gas and fine particulate material into the separating device.
• the separating device 8 is designed as a cyclone and has a treatment gas discharge line 9 and a solids discharge line 10.
• the solids discharge 10 opens into the fluidized bed reactor 1 or into the fluidization zone 2.
• Arrows 11, 12, 13, 14, 15 schematically represent several means for feeding coarse-grained material into the separating device, or the locations where these means can be arranged.
• Coarse-grained material is introduced into the treatment gas feed 7 by the means 11, and coarse-grained material is introduced into the cyclone through the means 12, 13, 14, the means 12 partially passing through the treatment gas discharge line 9 and opening into the interior of the cyclone.
• Coarse-grained material is introduced directly into the interior of the cyclone via the means 13, 14, specifically at 13 from above through an additional insertion opening (not shown) and at 14 essentially tangentially - in relation to the cyclone 8.
• Coarse-grained material is introduced into the solid discharge 10 leading away from the cyclone 8 by means 15.
• Each of the means 11, 12, 13, 14, 15 is preferably designed as a pneumatic feed device, although gravitational addition is equally possible.
• the fluidized bed reactor V 3 is supplied with treatment gas from below through a treatment gas feed line.
• the treatment gas is evenly distributed via a gas distribution base 4, which can be designed, for example, as a nozzle grate, the particulate material in the fluidization zone 2 also being fluidized.
• the reactor 1 is equipped with feed and discharge lines 5, 6 for particulate material.
• the fluidized bed reactor 1 ' is equipped with an internal cyclone 16, in which the means 17 for supplying treatment gas is formed by an inlet opening 17 and from which a solids discharge line 18 leads, which opens into the fluidization zone 2.
• a treatment gas discharge line 19 leads away from the cyclone 16, through which treatment gas is led away from the fluidized bed reactor 1 '.
• Arrows 12, 13 schematically represent means 12, 13 for feeding coarse-grained material into the cyclone 16, the means 12 partially passing through the treatment gas discharge line 19 or the means 13 from above through an additional introduction opening (not shown) into the The inside of the cyclone opens.
• Both the treatment gas supply 7 and the means 14 for supplying coarse material open approximately tangentially and horizontally with respect to the cyclone 8.
• FIG. 4A shows a vertical cross section through a cyclone 8 with treatment gas discharge line 9 and solids discharge line 10.
• a means 17 for supplying treatment gas is designed as an inlet opening arranged on the side.
• a means 13 for supplying coarse-grained material is guided through the cyclone cover at an angle from above.
• Fig. 4B shows the same cyclone 8 as Fig. 4A in a horizontal cross section. It can be seen that both the treatment gas supply 7 and the means 13 for supplying coarse-grained material open substantially tangentially into the cyclone 8.
• dust-laden gas is introduced via an inlet 20 into a cyclone 21, and in this cyclone is at least partially freed of dust.
• the cleaned gas is discharged from the separation chamber via an immersion tube 22.
• the separated residues, especially the separated dust are discharged via an outlet pipe 23 for further use.
• the separated dust tends to caking 24, which, according to one embodiment of the method according to the invention, are removed by coarse bulk material 25, which is introduced, for example, via the immersion tube.
• the introduction of the coarse bulk material into the immersion tube 22 is shown in detail. Accordingly, the cleaned gas is discharged from the separation chamber 21 via a gas line 26. Opens above the separation chamber a nozzle 27 into the gas line 26 through which the coarse bulk material is introduced, in particular via a ball valve 28.
• FIG. 7 shows the case in which the separation chamber 21 is blocked by the hot dust 24 ', and no more significant removal of the dust can take place.
• now uncleaned gas could flow from the separation chamber into the immersion tube 22 and interfere with the further process.

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• Engineering & Computer Science (AREA)
• Chemical & Material Sciences (AREA)
• Dispersion Chemistry (AREA)
• Manufacturing & Machinery (AREA)
• Materials Engineering (AREA)
• Metallurgy (AREA)
• Organic Chemistry (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Cyclones (AREA)
• Manufacture And Refinement Of Metals (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

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• 2002
  • 2002-05-28 US US10/481,619 patent/US7144447B2/en not_active Expired - Fee Related
  • 2002-05-28 RU RU2004101037/02A patent/RU2289633C2/ru not_active IP Right Cessation
  • 2002-05-28 CA CA002450688A patent/CA2450688A1/en not_active Abandoned
  • 2002-05-28 JP JP2003505383A patent/JP4647206B2/ja not_active Expired - Fee Related
  • 2002-05-28 BR BRPI0210455-5A patent/BR0210455B1/pt not_active IP Right Cessation
  • 2002-05-28 KR KR1020037016553A patent/KR100877007B1/ko not_active IP Right Cessation
  • 2002-05-28 EP EP02743123A patent/EP1397521A2/de not_active Withdrawn
  • 2002-05-28 WO PCT/EP2002/005856 patent/WO2002103063A2/de active Application Filing

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