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WO2003064950A1 - Procedes et dispositifs permettant de chauffer un flux continu de matiere solide - Google Patents

Procedes et dispositifs permettant de chauffer un flux continu de matiere solide Download PDF

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Publication number
WO2003064950A1
WO2003064950A1 PCT/EP2003/050003 EP0350003W WO03064950A1 WO 2003064950 A1 WO2003064950 A1 WO 2003064950A1 EP 0350003 W EP0350003 W EP 0350003W WO 03064950 A1 WO03064950 A1 WO 03064950A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized bed
gas
solid
pressure vessel
heat exchanger
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.)
Ceased
Application number
PCT/EP2003/050003
Other languages
German (de)
English (en)
Inventor
Yvan Kroemmer
Paul Goedert
Louis Schmit
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.)
Paul Wurth SA
Original Assignee
Paul Wurth SA
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 Paul Wurth SA filed Critical Paul Wurth SA
Priority to AU2003209752A priority Critical patent/AU2003209752B2/en
Priority to JP2003564503A priority patent/JP4098247B2/ja
Priority to DE50302535T priority patent/DE50302535D1/de
Priority to KR10-2004-7007330A priority patent/KR20040077659A/ko
Priority to EP03734728A priority patent/EP1470379B1/fr
Publication of WO2003064950A1 publication Critical patent/WO2003064950A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C21B5/003—Injection of pulverulent coal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D13/00—Heat-exchange apparatus using a fluidised bed
    • 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 specially adapted for furnaces of these types

Definitions

  • the present invention relates to a method for heating a continuous flow of solids and devices for carrying out this method.
  • Pneumatically conveyable solids such as e.g. Coal dust to be heated in a fluidized bed heat exchanger.
  • Fluidized bed heat exchangers comprise a columnar pressure vessel in which a bed of solid particles is flowed through from below by a loosening gas. In the bed, the solid particles are carried by the upward loosening gas, so that a so-called fluidized bed is maintained.
  • the fluidized bed is heated by heat exchangers which are immersed in or surround the fluidized bed.
  • Such a fluidized bed heat exchanger is described in WO 99/24773.
  • the solid to be heated is transported to the heat exchanger in a pneumatic conveyor line and continuously fed into the fluidized bed at the lower end of the heat exchanger.
  • the fluidized bed flows into a discharge device for the solid.
  • the latter includes a rotary valve that continuously discharges the solid.
  • the gas that accumulates at the upper end of the heat exchanger is drawn off in such a way that there is a constant overpressure in the heat exchanger.
  • the extracted gas is cleaned in a cyclone.
  • the coal dust is then discharged from this degassing container into a fluidization device, which feeds it into a pneumatic conveying line, the mass flow rate of the coal dust in the pneumatic conveying line being regulated.
  • the degassing tank with entry lock, the fluidization device and the mass flow control device naturally cause the plant to become significantly more expensive.
  • a pneumatically conveyable solid stream is continuously fed into one Pressure vessel entered, in which a fluidized bed is maintained by adding a loosening gas, which is heated by heat exchange with a heat transfer medium.
  • a solid / gas mixture is continuously removed from the fluidized bed and divided into a weakly laden gas phase and a highly compressed solid / gas mixture by gravity or centrifugal separation.
  • the highly compressed solid / gas mixture is then continuously discharged into a pneumatic conveying line and pneumatically conveyed there.
  • the solids content of the pressure vessel is continuously monitored.
  • the continuously discharging of the highly compressed solid / gas mixture into the pneumatic conveying line is regulated in such a way that the solids content of the pressure vessel always remains largely constant via a regulated gas discharge from the weakly laden gas phase.
  • the proposed method is suitable e.g. Excellent for heating and drying a pneumatically conveyable solid that has bound water to it due to hygroscopicity.
  • the solid in the fluidized bed is heated such that a large part of this water evaporates in the fluidized bed and passes into the gas phase. It should be noted that the proposed method makes it possible to subsequently convey the heated solid immediately pneumatically, while ensuring good stability of the pneumatic conveyance, which was previously considered impossible.
  • the proposed method can advantageously be applied to coal dust that has been dehumidified in front of the pressure vessel at a temperature of less than 100 ° C., so that its surface moisture is negligible when it enters the fluidized bed, but its pore moisture is still relatively high.
  • This coal dust loses most of its pore moisture in the fluidized bed at temperatures between 150 ° C and 250 ° C.
  • the proposed method makes it possible for the strongly heated Transporting coal dust directly pneumatically, whereby a good stability of the pneumatic conveying is guaranteed, which was previously considered impossible.
  • the pressure vessel comprises a fluidized bed heat exchanger and a degassing column.
  • the solid stream is continuously introduced into the fluidized bed heat exchanger at the lower end.
  • a fluidized bed is maintained by adding a loosening gas, which is heated by heat exchange with a heat transfer medium.
  • a heated solid / gas mixture flows from the fluidized bed into the degassing column.
  • the overflowed solid / gas mixture forms a fluidized bed which is highly compressed under the influence of gravity, the separated gas phase accumulating in the upper end of the degassing column.
  • the highly compressed fluidized bed is continuously discharged into the pneumatic delivery line at the lower end of the degassing column.
  • This continuous discharge of the highly compressed fluidized bed into the pneumatic delivery line is controlled via a regulated gas outlet at the upper end of the degassing column.
  • the highly compressed fluidized bed can be loosened at the lower end of the degassing column by adding a gas before it is discharged into the pneumatic delivery line.
  • a change in the solids content is advantageously detected by a change in the height of the highly compressed fluidized bed in the degassing column.
  • the pressure vessel only comprises a fluidized bed heat exchanger.
  • the solid stream is continuously introduced into the fluidized bed heat exchanger at the lower end.
  • a fluidized bed is maintained by adding a loosening gas, which is heated by heat exchange with a heat transfer medium.
  • a heated solid / gas mixture is removed from the top of the fluidized bed via a cyclone, the cyclone removing the removed solid / gas mixture by centrifugal force into a weakly laden gas phase and a highly compressed solid / gas mixture divides.
  • the highly compressed solid / gas mixture is continuously fed into the pneumatic delivery line.
  • the throughput of the solid / gas mixture into the pneumatic delivery line is controlled via a regulated gas discharge in the cyclone.
  • a change in the solids content is advantageously detected by a change in the height of the fluidized bed in the fluidized bed heat exchanger.
  • FIG. 1 a simplified system diagram of a coal dust injection for a blast furnace, with a first embodiment of a device according to the invention for heating the pneumatically conveyed coal dust;
  • FIG. 2 an enlarged detail from FIG. 1, which shows the structure of the device for heating a pneumatically conveyed solid in a schematic longitudinal section;
  • FIG. 3 shows a schematic longitudinal section through a second embodiment of a device according to the invention for heating a pneumatically conveyed solid; 4 shows a cross section along the section line 4-4 'of FIG. 3; and
  • Fig. 1 shows a highly simplified scheme of a
  • Reference numeral 12 designates a plant for the processing of coal dust globally.
  • This system 12 comprises, in a known manner, one
  • each pneumatic delivery line 22 ⁇ , 22 2 , 22 3 , 22, ... comprises a control device 26 ⁇ .
  • this control device 26 ⁇ is shown in the pneumatic delivery line 22i by a mass flow meter 28 and a flow control valve 30. It should also be emphasized that the coal dust in the pneumatic conveying lines 22 ⁇ , 22 2 , 22 3 , 22 4 , ... is preferably transported in a dense stream, so that gas and energy consumption and wear are minimized. Dense phase conveying is understood to mean a solids loading of at least 20 kg of solids per kg of conveying gas.
  • the reference numeral 40 shows a device for heating the pneumatically conveyed coal dust, which is built into the pneumatic conveying lines 22 ⁇ (the section of the pneumatic conveying line 22 ⁇ downstream of the device 40 is provided with the reference number 22' ⁇ ).
  • This device 40 is intended to heat the coal dust, which is conveyed in the pneumatic delivery line 22 ⁇ , 22' ⁇ , to temperatures between 150 ° C. and 300 ° C. before blowing into the blast furnace 10.
  • the device 40 from FIG. 1 will now be described in more detail with reference to FIG. 2. It comprises two columnar pressure vessels 42, 44, the first pressure vessel 42 forming a fluidized bed heat exchanger and the second pressure vessel 42 forming a degassing column. It should be emphasized that each of the two columnar pressure vessels 42, 44 has a height of several meters.
  • the fluidized bed heat exchanger 42 has in its lower end a fluidization device 46 with a gas connection 48 for
  • Such a fluidization device 46 includes, for example a porous fluidization tray 50 known per se, via which the loosening gas (in the case of coal dust it is preferably an inert gas such as nitrogen) is distributed uniformly over the entire cross section of the columnar pressure vessel 42.
  • the loosening gas in the case of coal dust it is preferably an inert gas such as nitrogen
  • the coal dust is introduced from the pneumatic delivery line 22 ⁇ directly above the fluidization tray 50 into the pressure vessel 42.
  • the loosening gas flowing in via the porous fluidization base 50 carries the solid particles upwards.
  • a fluidized bed 54 is formed in the columnar pressure vessel 42, which has liquid-like properties. This fluidized bed 54 extends from the fluidization base 50 to a cross connection 56 which connects the two columnar pressure vessels 42, 44 at their head ends.
  • the solid / gas mixture flows from the fluidized bed 54 into the second pressure vessel 44.
  • the solids mass throughput in the cross connection 56 corresponds to the solids mass throughput in the pneumatic conveying line 22.
  • a fluidized bed 54 of several meters in height is therefore maintained in the first pressure vessel 42, in which the coal dust particles slowly move from bottom to top ,
  • This fluidized bed 54 is heated by a heat exchanger, which is formed by a double-walled jacket 58 in FIG. 2.
  • This jacket heat exchanger 58 surrounds the fluidized bed 54 over most of its height and is flowed through from top to bottom by a heat transfer medium, normally a heat transfer oil.
  • the fluidized bed heat exchanger 42 is preferably designed such that
  • Temperatures and dwell times in the fluidized bed 54 are achieved, which ensure that the majority of the pore moisture of the coal dust in the fluidized bed 54 evaporates. This is normally achieved at temperatures of 150 ° C to 250 ° C, residence times of 2 to 4 minutes and a pressure in the pressure vessel of approximately 6 to 8 bar. It can be assumed that between 0.05 and 0.1 kg of water vapor is released per kg of coal dust, which is at a pressure of 8 bar and a temperature of 200 ° C corresponds to a gas volume between 0.012 to 0.024 m 3 per kg of coal dust.
  • the solid / gas mixture overflowing from the fluidized bed 54 through the cross-connection 56 is strongly compressed under the influence of gravity.
  • a strongly compressed fluidized bed 60 is formed in the degassing column 44, the separated gas phase accumulating in the upper end 62 of the degassing column 44.
  • the degassing column 44 has a discharge device 64 for the continuous discharge of the highly compressed fluidized bed 60 into the pneumatic delivery line 22 '.
  • This discharge device 64 advantageously comprises a gas-loosening device 66 which loosens the highly compressed fluidized bed 60 before it is discharged into the pneumatic conveying line 22 '.
  • the continuous discharge of the highly compressed fluidized bed 60 from the degassing column 44 into the pneumatic delivery line 22 1 ! is regulated here via a regulated gas vent 68 at the upper end 62 of the degassing column 44 such that the solids content of the device 40 remains largely constant.
  • the regulated gas outlet 68 has a regulating valve 70, a regulator 72 and a measuring probe 74.
  • the measuring probe 74 detects a change in the height of the strongly compressed fluidized bed 60 in the degassing column 44. Capacitive level meters or microwave level meters are suitable as measuring probe 74, for example. As the height of the highly compressed fluidized bed 60 increases, the controller 72 causes less gas to be drawn off via the control valve 70.
  • the gas pressure in the degassing column 44 increases, and the discharge device 64 discharges more coal dust into the pneumatic delivery line 22 ′.
  • the controller 72 causes more gas to be drawn off via the control valve 70.
  • the gas pressure in the degassing column 44 drops and the discharge device 64 discharges less coal dust into the pneumatic delivery line 22.
  • This regulation thus ensures that the solids flow of the is continuously discharged from the device 40, corresponds to the solid flow which is continuously introduced into the device 40. In this way, a stable dense phase flow of the coal dust can be achieved in the pneumatic delivery line 22 ′ downstream of the device 40.
  • the gas drawn from the upper end 62 of the degassing column 44 can, as shown in FIG. 1, be returned via a line 76 to the storage bunker, where it contributes to preheating the coal dust before it is discharged into the atmosphere via a filter device 78.
  • a device 140 for heating a pneumatically conveyed solid is now described with reference to FIGS. 3 to 5, which represents an interesting alternative to the device 40 from FIG. 1, since it only comprises a columnar pressure vessel 142.
  • the latter also has a height of several meters and forms a fluidized bed heat exchanger.
  • the columnar pressure vessel 142 like the columnar pressure vessel 42, has a fluidization device 146 with a gas connection 148 for a loosening gas in its lower end.
  • a fluidization device 146 comprises, for example, a porous fluidization base 150 known per se, via which the loosening gas, in the case of coal dust, is preferably an inert gas, such as nitrogen, is uniformly distributed over the entire cross section of the columnar pressure vessel 142.
  • the coal dust from the pneumatic conveying line 22- ⁇ which comes from the system 12 for the processing of the coal dust, is introduced into the pressure vessel 142 immediately above the fluidization tray 150.
  • the loosening gas flowing in through the porous fluidization base 150 carries the solid particles upwards.
  • a fluidized bed 154 is formed, which extends in the columnar pressure vessel 142 from the fluidization base 150 to the upper end of the pressure vessel 142. Accordingly, a fluidized bed 154 with a height of several meters is maintained in the pressure vessel 142, in which the coal dust particles slowly move from bottom to top.
  • This fluidized bed 154 is heated by a heat exchanger, which is formed by a double-walled jacket 158 in FIG. 3 becomes.
  • This jacket heat exchanger 158 surrounds the fluidized bed 154 over most of its height and is flowed through from top to bottom by a heat transfer medium, normally a heat transfer oil.
  • a heat transfer medium normally a heat transfer oil.
  • the fluidized bed heat exchanger 142 is preferably designed in such a way that temperatures and residence times are achieved in the fluidized bed 154, which ensure that the majority of the hygroscopically bound water evaporates in the fluidized bed 154.
  • a heated solid / gas mixture is withdrawn from the fluidized bed 154 via a cyclone 161, the removed solid / gas mixture being divided by centrifugal force into a weakly laden gas phase and a highly compressed solid / gas mixture ,
  • the cyclone 161 is advantageously arranged within the columnar pressure vessel 142, wherein it has an inlet 163 for the removal of a solid / gas mixture from the fluidized bed 154, a first outlet 165 for a compressed solid / gas stream and a second outlet 167 for the weakly laden gas stream.
  • the first outlet 165 and the second outlet 167 are led out of the columnar pressure vessel 142 in a pressure-tight manner.
  • the cyclone 161 due to its arrangement within the pressure vessel 142, does not itself have to be designed as a pressure vessel.
  • the first outlet 165 of the cyclone 161 opens directly into the pneumatic conveying line 22 ′ leading to the blast furnace 10. A strongly compressed solid / gas mixture is thus continuously introduced into the pneumatic delivery line 22 ′ via this first outlet 165.
  • the throughput of the highly compressed solid / gas mixture into the pneumatic delivery line 22 ′ is regulated here via a regulated gas discharge through the second outlet 167 of the cyclone 161 in such a way that the total solid content of the device 140 remains largely constant.
  • the second outlet 167 has a control element 170 designed as a throttle device for the controlled removal of a weakly laden gas stream from the cyclone 161.
  • This regulator 170 forms with a regulator 172 and a measuring probe 174 a control loop.
  • the measuring probe 174 detects a change in the height of the fluidized bed 154. As this height increases, the controller 172 throttles the second outlet 167 via the throttling device 170, so that less gas is drawn off above the cyclone 161. This increases the gas pressure, which causes an increase in the mass flow rate in the first outlet 165 of the cyclone 161. When the height of the fluidized bed 154 decreases, the controller 172 reduces the throttling of the second outlet 167 via the throttle device 170, so that more gas is drawn off above the cyclone 161. As a result, the gas pressure in the cyclone 161 drops, which causes a reduction in the mass flow rate in the first outlet 165 of the cyclone 161.
  • This regulation thus ensures that the solid stream that is continuously discharged from the device 140 corresponds to the solid stream that is continuously fed into the device 140. In this way, a stable pneumatic conveying of the coal dust can be achieved in the pneumatic conveying line 22 ′, ie downstream of the device 140.
  • the latter comprises a separation chamber 180 with a tangential inlet chamber 182, which forms the inlet 163 in the fluidized bed 152.
  • the separation chamber 180 tapers conically downwards and merges into the first outlet 165. It is connected via a pipe 184 to a flange 186 which is fastened in a gas-tight manner on a counter flange 188 of the pressure vessel 142.
  • the second outlet 167 is arranged centrally in the deposition chamber 180. It is formed by a vertically displaceable inlet connector 200 which extends through the pipe 184 and is led out of the pressure vessel 142 in a sealed manner.
  • Reference number 204 denotes a fixed closure body which projects centrally into the lower outlet of the inlet connector 200. Here it interacts with a reduced through opening 206 of the inlet connector 200 such that, depending on the vertical position of the inlet connector 200, the Closure body 204 more or less constricts the through-opening 206, ie more or less throttles the second outlet 167.
  • the height measurement of the fluidized bed 54, 154 described herein is most likely the easiest way to determine a change in the solids content in the devices 40 and 140. If necessary, it can be refined by one or more density measurements of the fluidized bed 54, 154. However, it is not outside the scope of the present invention to change the solids content of the devices 40 and 140 by other measurement methods, such as e.g. a weight measurement.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Dispersion Chemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Drying Of Solid Materials (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Blast Furnaces (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • General Preparation And Processing Of Foods (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Apparatuses For Bulk Treatment Of Fruits And Vegetables And Apparatuses For Preparing Feeds (AREA)
  • Resistance Heating (AREA)

Abstract

Un flux de matière solide transportable par voie pneumatique est introduit en continu dans un contenant à pression (42) dans lequel on entretient un lit fluidisé par apport d'un gaz fluidisant, ce lit fluidisé étant chauffé par un échange de chaleur avec un agent caloporteur (58). Un mélange matière solide/gaz est prélevé en continu du lit fluidisé et divisé en une phase gazeuse faiblement chargée et en un mélange matière solide/gaz fortement comprimé par séparation par gravité ou par force centrifuge. Le mélange matière solide/gaz fortement comprimé est ensuite déversé en continu dans une conduite de transport pneumatique (221) dans laquelle le mélange est emporté par voie pneumatique. Le contenu de matière solide du contenant à pression (42) est surveillé en continu. Le déversement continu du mélange matière solide/gaz fortement comprimé, séparé de la phase gazeuse faiblement chargée, dans la conduite de transport pneumatique (221) par un carneau à gaz (68) est réglé de telle manière que le contenu de matière solide du contenant à pression (42) soit toujours largement constant.
PCT/EP2003/050003 2002-02-01 2003-01-27 Procedes et dispositifs permettant de chauffer un flux continu de matiere solide Ceased WO2003064950A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
AU2003209752A AU2003209752B2 (en) 2002-02-01 2003-01-27 Methods and devices for heating a continuous flow of solids
JP2003564503A JP4098247B2 (ja) 2002-02-01 2003-01-27 固体の連続流を加熱するための方法と装置
DE50302535T DE50302535D1 (de) 2002-02-01 2003-01-27 sERFAHREN UND VORRICHTUNGEN ZUM ERWÄRMEN EINES KONTINUIERLICHEN FESTSTOFFSTROMS
KR10-2004-7007330A KR20040077659A (ko) 2002-02-01 2003-01-27 연속적인 고체 흐름을 가열시키는 방법 및 장치
EP03734728A EP1470379B1 (fr) 2002-02-01 2003-01-27 Procedes et dispositifs permettant de chauffer un flux continu de matiere solide

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
LU90888A LU90888B1 (de) 2002-02-01 2002-02-01 Verfahren und Vorrichtungen zum Erwaermen eines kontinuierlichen Feststoffstroms
LU90888 2002-02-01

Publications (1)

Publication Number Publication Date
WO2003064950A1 true WO2003064950A1 (fr) 2003-08-07

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2003/050003 Ceased WO2003064950A1 (fr) 2002-02-01 2003-01-27 Procedes et dispositifs permettant de chauffer un flux continu de matiere solide

Country Status (8)

Country Link
EP (1) EP1470379B1 (fr)
JP (1) JP4098247B2 (fr)
KR (1) KR20040077659A (fr)
AT (1) ATE319064T1 (fr)
AU (1) AU2003209752B2 (fr)
DE (1) DE50302535D1 (fr)
LU (1) LU90888B1 (fr)
WO (1) WO2003064950A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115807142A (zh) * 2022-12-06 2023-03-17 付光明 一种高效竖式煤粉加热装置和方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115354097B (zh) * 2022-08-25 2023-10-31 付光明 一种节能型高炉煤气多级加热竖式煤粉加热装置和方法

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1179572A (fr) * 1957-07-11 1959-05-26 Pechiney Procédé et appareil pour le chauffage et le refroidissement des poudres
WO1999024773A1 (fr) * 1997-11-12 1999-05-20 Paul Wurth S.A. Dispositif destine a l'echange de chaleur entre un fluide porteur de chaleur et une matiere solide

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1179572A (fr) * 1957-07-11 1959-05-26 Pechiney Procédé et appareil pour le chauffage et le refroidissement des poudres
WO1999024773A1 (fr) * 1997-11-12 1999-05-20 Paul Wurth S.A. Dispositif destine a l'echange de chaleur entre un fluide porteur de chaleur et une matiere solide

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115807142A (zh) * 2022-12-06 2023-03-17 付光明 一种高效竖式煤粉加热装置和方法

Also Published As

Publication number Publication date
JP2005525525A (ja) 2005-08-25
EP1470379B1 (fr) 2006-03-01
JP4098247B2 (ja) 2008-06-11
AU2003209752B2 (en) 2007-03-29
KR20040077659A (ko) 2004-09-06
LU90888B1 (de) 2003-08-04
DE50302535D1 (de) 2006-04-27
ATE319064T1 (de) 2006-03-15
EP1470379A1 (fr) 2004-10-27

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