WO2005028978A1 - Method and apparatus for heat treatment of particulates in an electrothermal fluidized bed furnace and resultant products - Google Patents
Method and apparatus for heat treatment of particulates in an electrothermal fluidized bed furnace and resultant products Download PDFInfo
- Publication number
- WO2005028978A1 WO2005028978A1 PCT/US2004/029814 US2004029814W WO2005028978A1 WO 2005028978 A1 WO2005028978 A1 WO 2005028978A1 US 2004029814 W US2004029814 W US 2004029814W WO 2005028978 A1 WO2005028978 A1 WO 2005028978A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fluidized bed
- furnace
- cylindrical portion
- nozzles
- conical
- Prior art date
Links
Classifications
-
- 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
-
- 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
- F27B15/10—Arrangements of air or gas supply devices
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/20—Graphite
- C01B32/21—After-treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L9/00—Treating solid fuels to improve their combustion
- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
-
- 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
- F27B15/14—Arrangements of heating devices
Definitions
- the present invention relates to a method and apparatus for the continuous high-temperature treatment in an electrothermally heated fluidized bed of carbonaceous particles comprising fine or irregularly shaped particles having a wide range of particle size distribution and the products resulting from such treatment. More particularly, the invention relates to, in one aspect, the use of a fountain-type fluidized bed for the high temperature treatment of carbonaceous particles that cannot be effectively treated in a bubble-type fluidized bed due to their fine sizes, range of size distribution, and shape.
- bubble EFB furnaces to treat and/or synthesize polydispersed materials has resulted in the entrainment of particles smaller than 106 ⁇ m (140 mesh) . That is, the particles are entrained by the fluidizing gas outside of the active area of the EFB furnace. This results in a low recovery rate of treated product as a percent of raw material. This has proven to be especially the case in bubble EFB furnaces where the raw materials are introduced at the top of the fluidized bed and the treated particles are discharged from the bottom of the furnace.
- the plate gas distributor and its plurality of vertically oriented gas nozzles create a number of local circulating zones that have an upward flow of particle/gas mixture and a downward flow of particles, with each zone being formed around a single nozzle or group of nozzles on the distribution plate.
- an object of the present invention to provide a method for treating of fine, irregularly shaped and/or polydispersed particulate matter in an electrothermal fluidized bed furnace. It is a related object to provide a furnace for performing the method.
- SUMMARY OF THE INVENTION [0009]
- the furnace includes at least one electrode extending through the upper and lower cylindrical portions and a treated material discharge pipe at the lower end of the conical portion.
- a feed pipe is provided for introducing raw material into the lower cylindrical portion, and at least one gas flue is provided at the top of the furnace body for discharging fluidizing gas.
- a plurality of nozzles is disposed in the conical section for introducing fluidizing gas into the furnace, with the nozzles being arranged in a generally horizontal plan and orientated so that the streams of the fluidizing gas introduced therethrough cross and form an upward flow in the central portion furnace body.
- Such an electrothermal fluidized bed furnace ' is adapted to be used in a process for continuously heat treating particulate matter by continuously introducing a non-reactive fluidizing gas through the nozzles of the furnace at predetermined rate, continuously introducing untreated particulate matter through the feed pipe of the furnace at a predetermined rate so that it forms a fluidized bed, energizing the electrode so as to heat the fluidized bed, and continuously collecting the treated particulate matter from the discharge pipe.
- Fig. 1 is a vertical cross-sectional view of a fountain EFB furnace according to the present invention.
- Fig. 2 is a top view of the fountain EFB furnace of Fig. 1.
- FIG. 3 is a cross-sectional view of the EFB furnace taken along line 3-3 of Fig. 1, showing the fluidizing gas distribution nozzles.
- Fig. 4 is similar to Fig. 3, except that it shows an alternative arrangement for the fluidizing gas distribution nozzles .
- DESCRIPTION OF THE PREFERRED EMOBODIMENT [00015]
- a fountain fluidized bed also known as a "spout” or “jetting” fluidized bed
- the principal characteristic of a fountain fluidized bed is that it has a strong circulating contour with a central upward flow of particle-gas mixture in the center of the fluidized bed and an outer downward flow of particles along the furnace walls .
- the high speed central upward flow draws in and carries along the solid particles .
- the formation of fine particle clusters and gas channels in the fluidized bed is avoided.
- the vertical velocity gradient provides for a thorough fluidization of all fractions of poly-dispersed grain materials .
- the furnace 10 includes a furnace shell 11, typically made of steel that encases a furnace body 12. If the operation temperature of the furnace is greater than 1500 °C, made of graphite and constitutes the return electrode.
- the furnace body may be made of other materials if the operation temperature is less than 1500 °C.
- An insulating material 14 is disposed between the shell 11 and body 12.
- the furnace body 12 comprises a lower cylindrical portion 16, an upper cylindrical portion 18 disposed above the lower cylindrical portion and having a larger diameter than the central cylindrical portion 16.
- a conical gas distributor 20 is disposed below the central cylindrical portion 16, and has a plurality of fluidizing gas distribution nozzles 22.
- the nozzles 22 are in fluid communication with a plenum 24 into which the fluidizing gas is introduced through an inlet 26.
- the conical gas distributor 20 defines a central angle ⁇ (alpha) of from 30° to 90°, and preferably of from 40° to 60°.
- ⁇ alpha
- the space above the fluidized bed zone, coinciding generally with the upper cylindrical portion 18, is known as the overbed space or free board zone 30.
- the operational height H FB of the fluidized bed area 28 generally coincides with the distance between the nozzles 22 and the upper end of the lower cylindrical portion 18.
- H FB is preferably less than or equal to one and one-half to twice the inside diameter ID F B of the lower cylindrical portion 16.
- the minimal height of the free board or overbed space Hov.s s preferably one and one-half times the height of the fluidized bed H fb to ensure that any entrained particles are separated from the gas flow and returned to the fluidized bed space of the furnace.
- each of the cylindrical portions 16, 18 and the conical gas distributor 20 has a circular or an elliptical cross-section.
- Other shaped cross-sections may exhibit satisfactory hydro-dynamic characteristics. However, such shapes are practically unworkable due to the amount of thermal expansion encountered by the furnace during use.
- An elongated electrode 32 extends into the furnace body 12 from the top 34 through the upper and lower cylindrical portions 18, 16, respectively.
- the electrode 32 is preferably fabricated from an electrically conductive, heat-resistant material such as graphite and must be electrically isolated from furnace body 12. When a single electrode is used, it must be located centrally within the furnace body and aligned with a vertical axis Y thereof. Alternatively, a plurality of electrodes may be used, in which case the electrodes are arranged symmetrically about the central axis Y.
- a feed pipe 38 is provided for continuously supplying raw material into the fluidized bed zone 28 of the furnace body 12.
- the feed pipe 38 is vertically orientated and extends through the top 34 of the furnace body 12, down through the upper cylindrical portion 18, and has its outlet adjacent to the wall either at or below the top of the lower cylindrical portion 16.
- raw material is introduced from the feed pipe 38 into the fluidized bed, or at least at the top surface thereof, in the area of the downward flow of solid particles being circulated in the fluidized bed. This results in easier loading of raw material into the fluidized bed, reduces the likelihood of the untreated particles being entrained by the upward flow of fluidizing gas and carried into the overbed space, and provides better mixing of the treated and raw materials .
- the bottom of the furnace body includes a discharge port 40 through which effluent solids may be continuously withdrawn by gravity flow.
- the discharge port 40 depends from the conical gas distributor 20, with the inlet to the discharge port 40 generally coinciding with the apex of the conical gas distributor 20.
- Gaseous effluent can be withdrawn through one or more exhaust pipes or gas flues 42 in the top 34 of the furnace body 12. This effluent gas can be readily cleaned and treated to control particulate and gaseous pollutants as required.
- the conical gas distributor 20 includes a plurality of fluidizing gas inlet nozzles 22 (eight shown) , through which fluidizing gas is introduced into the furnace body 12.
- the nozzles 22 are orientated radially to the center of the conical distributor 20 so that fluidizing gas forms crossing sprays, with a strong uniform upward flow.
- the velocity at which the fluidizing gas exits the nozzles and the average gas velocity in the fluidized bed portion 16 depend on the particle size, density, and shape of the material being fluidized.
- the fluidizing gas is typically nitrogen, argon or other non- reactive gas .
- the nozzles 22 are arranged so that their axes X are aligned radially, with the fluidizing gas being directed toward the center of the conical gas distributor 20.
- the nozzles 22 maybe orientated so that their axes X form an angle ⁇ of from 10 to 20° with respect to a tangent to the conical gas distributor 20 at the location of the nozzle, as best seen in Fig. 4.
- the arrangement of the nozzles 22 so that their axes X are generally tangential to nozzle circle provides for a rotation of the fluidized bed, making it more stable and less sensitive to any deviation of the elongated electrode 32 from the central axis Y.
- the nozzles 22 are preferably disposed at a height H H above the conjunction of the gas distributor 20 and the inlet to the discharge port 40.
- H N is from 0.5 to 0.75 of the total height H ⁇ c of the conical gas distributor 20, and more preferably from 0.6 to 0.65 H ⁇ c .
- Each of the nozzles 22 has preferably a ring cross section perpendicular to its X axis at which is defined a free cross-sectional area.
- the cross-sectional shape can be circular or can have another shape such as rectangular, oval etc.
- the sum of the free cross-sectional areas of the nozzles 22 should be from 0.15 to 0.5% of the cross-sectional area of the cylindrical portion of the fluidized bed, that is the cross- sectional area of the lower cylindrical portion 16.
- the free cross-sectional area of the nozzles 22 should be between 0.25 and 0.4% of the cross-sectional area of .the fluidized bed.
- untreated particulate material is continuously fed by gravity through the feed pipe 38 into the reaction zone of the EFB furnace 10.
- the untreated particulate material may comprise fine, irregularly shaped or polydispersed materials.
- the polydispersed material has comprised particles sized from between 1.7mm (12 mesh), and as small as 5 ⁇ m.
- the untreated particulate may be an electroconductive or semiconductive material, such as carbonaceous materials like carbon black, coke (fluid coke, flexi-coke, delayed coke, needle coke, pitch coke, etc.), and graphite (flake graphite, synthetic graphite, vein graphite, amorphous graphite, etc.).
- the various cokes may be either green or calcined, petroleum or metallurgical, and are widely available from various sources.
- the graphites are available from Superior Graphite Co. of Chicago, Illinois, the assignee of the present application.
- the untreated particulate matter is discharged from the feed pipe 38 at the top of, or just inside, the fluidizing zone in the downward flow of particles.
- the material from the feed pipe is maintained in a fluidized state in the region of the furnace corresponding approximately to the lower cylindrical portion 16, and electric current is passed through the fluidized bed to uniformly heat the material to a high temperature, typically from 2,200- 2,400°C.
- Treated particulate material is continuously withdrawn by gravity through the discharge pipe 40. The discharge rate is such that the treatment time of the particulate material within, the fluidized bed is sufficient to result in the desired heat treatment or chemical reaction. In the use of the present EFB furnace, there is no need for mechanical devices or moving parts within the furnace 10.
- the treated material After being discharged through the pipe 40, the treated material may be cooled in a cooling chamber (not shown) .
- Gaseous effluent can be withdrawn through the gas flue 42 at the top 34 of the furnace body 12. This gaseous effluent can be readily cleaned and treated to control pollutants to the extent required.
- inventive EFB furnace and the heat treatment fine particles significantly better recovery rates (of 90.3% in pilot runs) for treated particulate have resulted, in contrast to the recovery rates when using the prior art, bubble-type EFB's, (in which the recovery rate is typically less than 64%) .
- the critical velocity of fluidization has been reduced over that of a bubble-type EFB furnace by 10- 15%, for example from approximately 0.30 ft. /sec. to approximately 0.25 ft. /sec. in the inventive EFB furnace.
- Table I below compares purity characteristics for several different graphite and coke materials both prior to and after heat treatment according to the present invention. The purity characteristics compared are percentage (wt.) of ash and sulfur. TABLE I
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP04783869A EP1678453A1 (en) | 2003-09-18 | 2004-09-10 | Method and apparatus for heat treatment of particulates in an electrothermal fluidized bed furnace and resultant products |
BRPI0414560-7A BRPI0414560A (en) | 2003-09-18 | 2004-09-10 | fluid-based electro-thermal furnace, method for continuous treatment of particulate matter, product resulting from the treatment of particulate coke and product resulting from the treatment of particulate graphite |
JP2006526956A JP2007506065A (en) | 2003-09-18 | 2004-09-10 | Method and apparatus for heat treatment of particles in an electrothermal fluidized bed furnace and the resulting product |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/666,614 US20050062205A1 (en) | 2003-09-18 | 2003-09-18 | Method and apparatus for heat treatment of particulates in an electrothermal fluidized bed furnace and resultant products |
US10/666,614 | 2003-09-18 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2005028978A1 true WO2005028978A1 (en) | 2005-03-31 |
Family
ID=34313156
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2004/029814 WO2005028978A1 (en) | 2003-09-18 | 2004-09-10 | Method and apparatus for heat treatment of particulates in an electrothermal fluidized bed furnace and resultant products |
Country Status (7)
Country | Link |
---|---|
US (1) | US20050062205A1 (en) |
EP (1) | EP1678453A1 (en) |
JP (1) | JP2007506065A (en) |
KR (1) | KR20060116799A (en) |
CN (1) | CN1871487A (en) |
BR (1) | BRPI0414560A (en) |
WO (1) | WO2005028978A1 (en) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2005028569A2 (en) * | 2003-09-18 | 2005-03-31 | Columbian Chemicals Company | Thermally modified carbon blacks for various type applications and a process for producing same |
DE102007060307A1 (en) | 2007-12-12 | 2009-06-18 | Evonik Degussa Gmbh | Process for the aftertreatment of carbon black |
US8236274B2 (en) | 2006-08-07 | 2012-08-07 | Evonik Carbon Black Gmbh | Carbon black, method of producing carbon black, and device for implementing the method |
US8372191B2 (en) | 2008-12-12 | 2013-02-12 | Evonik Carbon Black Gmbh | Ink jet ink |
US8852739B2 (en) | 2010-02-23 | 2014-10-07 | Evonik Carbon Black Gmbh | Carbon black, method for the production thereof, and use thereof |
US8915998B2 (en) | 2008-11-27 | 2014-12-23 | Evonik Carbon Black Gmbh | Pigment granulate, method for producing the same and use thereof |
WO2022226654A1 (en) * | 2021-04-29 | 2022-11-03 | Hatch Ltd. | Process and reactor for removing impurities from carbon material |
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DE102005009321A1 (en) * | 2005-03-01 | 2006-09-07 | Degussa Ag | Suspension, useful for coloring antistatic equipments, comprises water insoluble coloring agents, a heterocyclic compound and water and/or polyvalent alcohol |
DE102005037336A1 (en) * | 2005-08-04 | 2007-02-08 | Degussa Ag | Carbon material |
DE102007018181A1 (en) | 2007-04-18 | 2008-10-23 | Continental Aktiengesellschaft | Rubber compound, preferably for treads of tires |
JP2009079794A (en) * | 2007-09-25 | 2009-04-16 | Babcock Hitachi Kk | Solid fuel burner, combustion device using the same, and its operation method |
CN101817523B (en) * | 2009-03-19 | 2011-09-28 | 株洲弗拉德科技有限公司 | Graphite purification and graphitizable high temperature vertical continuous induction heating furnace |
CN102530923B (en) * | 2010-12-08 | 2013-08-14 | 沈阳铝镁设计研究院有限公司 | High-temperature electric calcining system and method of carbon raw material |
CN103990422A (en) * | 2013-02-16 | 2014-08-20 | 江苏中能硅业科技发展有限公司 | Fluidized bed reactor and method for preparing granular polysilicon and trichlorosilane by employing same |
EP3011617B1 (en) * | 2013-06-21 | 2017-08-09 | Cabot Corporation | Conductive carbons for lithium ion batteries |
CN107899520B (en) * | 2017-12-12 | 2023-11-21 | 中国科学院金属研究所 | High-temperature fluidized bed reaction device |
DE102019126394A1 (en) * | 2019-09-30 | 2021-04-01 | Onejoon Gmbh | Process for the production of graphite and vertical graphitization furnace |
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US4160813A (en) * | 1975-07-01 | 1979-07-10 | Graphite Synthesis Company | Method for heat treating carbonaceous material in a fluidized bed |
US4177742A (en) * | 1978-04-05 | 1979-12-11 | Babcock-Hitachi Kabushiki Kaisha | Incinerator for burning waste and a method of utilizing same |
JPS55818A (en) * | 1978-06-19 | 1980-01-07 | Babcock Hitachi Kk | Incinerating method by medium turning ascending current |
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US3448234A (en) * | 1966-08-31 | 1969-06-03 | Battelle Development Corp | Electrical resistivity control of fluidized beds |
US3684446A (en) * | 1970-02-24 | 1972-08-15 | Superior Graphite Co | Method for high-temperature treatment of petroleum coke |
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US4288407A (en) * | 1975-07-01 | 1981-09-08 | Markel Richard F | Method and apparatus for treating material in a fluidized bed |
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US4178170A (en) * | 1976-08-04 | 1979-12-11 | Istituto Di Ricerca Finsider Per La Riduzione Diretta S.P.A. | Process for the production of carburized sponge iron briquettes |
JPS54152615A (en) * | 1978-05-24 | 1979-12-01 | Ishikawajima Harima Heavy Ind Co Ltd | Suspended layer type direct reduction iron making process |
US4543240A (en) * | 1980-02-08 | 1985-09-24 | Superior Graphite Co. | Method for the continuous production of carbides |
US4435444A (en) * | 1981-11-10 | 1984-03-06 | Superior Graphite Co. | Method of making ultra-microcrystallite silicon carbide product |
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JP2727436B2 (en) * | 1995-05-31 | 1998-03-11 | 川崎重工業株式会社 | Method and apparatus for manufacturing iron carbide |
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2003
- 2003-09-18 US US10/666,614 patent/US20050062205A1/en not_active Abandoned
-
2004
- 2004-09-10 EP EP04783869A patent/EP1678453A1/en not_active Withdrawn
- 2004-09-10 JP JP2006526956A patent/JP2007506065A/en active Pending
- 2004-09-10 CN CNA2004800307071A patent/CN1871487A/en active Pending
- 2004-09-10 BR BRPI0414560-7A patent/BRPI0414560A/en not_active Application Discontinuation
- 2004-09-10 KR KR1020067005348A patent/KR20060116799A/en not_active Application Discontinuation
- 2004-09-10 WO PCT/US2004/029814 patent/WO2005028978A1/en not_active Application Discontinuation
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US4177742A (en) * | 1978-04-05 | 1979-12-11 | Babcock-Hitachi Kabushiki Kaisha | Incinerator for burning waste and a method of utilizing same |
JPS55818A (en) * | 1978-06-19 | 1980-01-07 | Babcock Hitachi Kk | Incinerating method by medium turning ascending current |
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PATENT ABSTRACTS OF JAPAN vol. 004, no. 025 (M - 001) 5 March 1980 (1980-03-05) * |
Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2005028569A2 (en) * | 2003-09-18 | 2005-03-31 | Columbian Chemicals Company | Thermally modified carbon blacks for various type applications and a process for producing same |
WO2005028569A3 (en) * | 2003-09-18 | 2006-03-09 | Columbian Chem | Thermally modified carbon blacks for various type applications and a process for producing same |
US8236274B2 (en) | 2006-08-07 | 2012-08-07 | Evonik Carbon Black Gmbh | Carbon black, method of producing carbon black, and device for implementing the method |
DE102007060307A1 (en) | 2007-12-12 | 2009-06-18 | Evonik Degussa Gmbh | Process for the aftertreatment of carbon black |
US8574527B2 (en) | 2007-12-12 | 2013-11-05 | Evonik Carbon Black Gmbh | Process for aftertreating carbon black |
US8915998B2 (en) | 2008-11-27 | 2014-12-23 | Evonik Carbon Black Gmbh | Pigment granulate, method for producing the same and use thereof |
US8372191B2 (en) | 2008-12-12 | 2013-02-12 | Evonik Carbon Black Gmbh | Ink jet ink |
US8852739B2 (en) | 2010-02-23 | 2014-10-07 | Evonik Carbon Black Gmbh | Carbon black, method for the production thereof, and use thereof |
WO2022226654A1 (en) * | 2021-04-29 | 2022-11-03 | Hatch Ltd. | Process and reactor for removing impurities from carbon material |
Also Published As
Publication number | Publication date |
---|---|
BRPI0414560A (en) | 2006-11-07 |
EP1678453A1 (en) | 2006-07-12 |
KR20060116799A (en) | 2006-11-15 |
US20050062205A1 (en) | 2005-03-24 |
JP2007506065A (en) | 2007-03-15 |
CN1871487A (en) | 2006-11-29 |
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