CN1871487A - 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
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- CN1871487A CN1871487A CNA2004800307071A CN200480030707A CN1871487A CN 1871487 A CN1871487 A CN 1871487A CN A2004800307071 A CNA2004800307071 A CN A2004800307071A CN 200480030707 A CN200480030707 A CN 200480030707A CN 1871487 A CN1871487 A CN 1871487A
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- conical portion
- fluidized bed
- spout
- cylindrical part
- bed furnace
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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
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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
- F27B15/10—Arrangements of air or gas supply devices
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- 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
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- 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
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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
- F27B15/14—Arrangements of heating devices
Abstract
An electrothermal fluidized bed furnace is disclosed in which the furnace body has upper and lower cylindrical portions with the upper cylindrical portion having a diameter larger than that of the lower cylindrical portion. A conical portion is disposed below the lower cylindrical portion so that the conical portion and the lower cylindrical portion define a fluidizing zone while the upper cylindrical portion defines an overbed zone. 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 that the streams of the fluidizing gas introduced there through 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 continuous process for continuously heat treating of fine particulate matter.
Description
Technical field
The present invention relates to a kind of being used for carries out method and apparatus that continuous high temperature handles and the product that is obtained by above-mentioned processing to the carbonaceous particles in the electrothermal heated fluidized bed, and described carbonaceous particles comprises the tiny or erose particle of the particle size distribution range with broad.More particularly, one aspect of the present invention relates to the purposes that is used for carbonaceous particles is carried out the spray pattern fluid bed of high-temperature process, and described carbonaceous particles is because its tiny particle size, particle size distribution range and shape former thereby can not effectively be handled in foaming formula (bubble-type) fluid bed.
Background technology
Adopting electrothermal fluid bed (EFB) stove to be used for carbonaceous material is carried out high temperature purification and is used for high temeperature chemistry synthetic is known (respectively referring to U.S. Patent No. 4,160,813 and No.4,547,430).
These technologies such as U.S. Patent No. 4,543, adopt fluid bed furnace shown in 240, wherein, a plurality of gas spouts that the cross section of the fluid bed part (or " fluidization regions ") of EFB stove is constant highly substantially along it and fluidizing gas passes through vertically to locate basically import in the stoves, and described gas spout extends through board-like distributor at furnace bottom.Such EFB stove is commonly called " foaming formula " EFB stove.
Employing foaming formula EFB stove is purified and the method for chemical synthesis is applicable to the little particle of 106 μ m (140mesh) very much.But foaming formula EFB stove but can not be handled well for littler particle especially those particles less than 75 μ m (200mesh).In addition, this stove can not be used for for example laminar or elongated piece of erose particle effectively, can not be used to have the particle of broad particle size distribution (polydisperse) scope, especially material comprise high level (greater than 30%), under the situation of particle diameter less than the fine particle of 106 μ m (140mesh).
Adopt foaming formula EFB stove processing and/or synthetic polydisperse material to cause the loss of the little particle of 106 μ m (140mesh).That is to say that these particles are fluidized the outside that gas takes effective district of EFB stove to.Caused as the rate of recovery of the processing afterproduct of raw material percentage lower like this.Verified: as especially to have this situation in the foaming formula EFB stove that the particle of raw material after the fluid bed top is introduced into and handles is discharged from from the bottom of stove.
For fine particle, especially those are less than particle and those the erose particles of 45 μ m (325mesh), verified: because the gas circuit of fluidizing gas, these particles of fluidisation are very difficult or are impossible sometimes equably in foaming formula EFB stove.This is considered to owing to have higher bonding force, this higher bonding force between granule is to be caused by the relatively large surface area of fine particle, and owing to is formed with the cause of stagnant wake in the bottom of fluid bed.
These defectives result from the special hydrodynamic characteristics of foaming formula EFB stove.The gas spout of especially board-like gas distributor and its a plurality of vertical location has formed has a plurality of local flow district that particle/admixture of gas upwards flows and particle flows downward, and each district forms around single spout or spout group on dispenser panel.
Therefore, an object of the present invention is to provide a kind of method of in electrothermal fluidized bed furnace, handling tiny, erose and/or polydisperse particulate matter.A relative purpose provides a kind of stove of implementing described method.
Summary of the invention
Will be well understood to these purposes and other purpose with reference to following detailed description and drawings, realize described purpose by a kind of electrothermal fluidized bed furnace, wherein body of heater has last cylindrical part and following cylindrical part, and last cylindrical part has the diameter bigger than following cylindrical part.Below following cylindrical part, be provided with conical portion, make conical portion and following cylindrical part define fluidization regions and go up cylindrical part and defined bed and distinguish (overbedzone).Described stove comprises at least one electrode of extending through cylindrical part and following cylindrical part and the discharge nozzle of material after the processing of conical portion lower end.Feed pipe is provided to be used for raw material is imported cylindrical part down, and at described body of heater top at least one air flue is set and is used for the discharge stream oxidizing gases.A plurality of spouts are arranged on and are used on the conical portion fluidizing gas is imported stove, and spout is arranged on the plane of level substantially and is positioned such that the fluidizing gas stream that is imported into by spout intersects and forms flowing upwards at the core of body of heater.
This electrothermal fluidized bed furnace is suitable for being used in continuously in the particulate matter heat-treating process, in this technology, spout with predetermined amount of flow (rate) thereby by stove imports the inertia fluidizing gas continuously and imports untreated particulate matter continuously with the feed pipe of predetermined amount of flow by stove and forms fluid bed, give electrifying electrodes with heated fluidized bed, and from the discharge nozzle particulate matter after the collection and treatment continuously.The raw material that are used for this technology advantageously comprise various types of coke (for example fluid coke, flexible coke (flexi-coke), pitch coke, delay coke and needle coke (neddle coke)) and graphite material (for example flake graphite, Delanium, amorphous graphite and vein graphite (vein graphite)).
Description of drawings
Fig. 1 is the vertical cross section according to jet flow EFB stove of the present invention.
Fig. 2 is the top view of jet flow EFB stove shown in Figure 1.
Fig. 3 is along the profile of the EFB stove of line 3-3 intercepting shown in Figure 1, shows the fluidization gas distribution spout.
Fig. 4 and Fig. 3 are similar, and just it shows the alternative construction that is used for the fluidization gas distribution spout.
The specific embodiment
By means of accompanying drawing as seen according to of the present invention, totally by the jet flow EFB stoves of 10 expressions.The principal character of jet flow fluid bed (being also referred to as " nozzle type " or " injecting type " fluid bed) is that it has strong flow profile, and this flow profile has at the center of the particle-admixture of gas at fluid bed center and upwards flows and outside that particle carries out along the furnace wall flows downward.Make progress flow draws and take away solid particle of center at a high speed.Fine particle family and gas circuit have been avoided in this fluid bed, forming.Vertical velocity gradient makes the complete fluidisation of all parts of polydisperse particulate matter.
With reference to Fig. 1, stove 10 comprises furnace shell 11, and it is made by the steel that accommodates body of heater 12 usually.If the operating temperature of stove is higher than 1500 ℃, then body of heater is made by graphite and has been constituted feedback electrode.If operating temperature is less than 1500 ℃, then body of heater can be made by other material.Insulating materials 14 is arranged between furnace shell 11 and the body of heater 12.Body of heater 12 comprises following cylindrical part 16, be arranged on down above the cylindrical part and have last cylindrical part 18 than intermediate cylindrical part 16 larger diameters.(in order to describe stove 10, term " cylindrical " meaning is to have vertical wall body and constant cross section on its height.) conical gas distributor 20 is arranged on the below of intermediate cylindrical part 16, and has a plurality of fluidization gas distribution spouts 22.Spout 22 is communicated with plenum chamber 24 fluids, and fluidizing gas imports in the plenum chamber 24 by air inlet 26.Conical gas distributor 20 defines 30 °-90 ° preferably 40 °-60 ° central angle alpha (alpha).In this body of heater 12, gas distribution nozzles 22 defines fluidized bed region 28 basically with the space at cylindrical part 16 tops top to bottm.Fluidized bed region is above to be called as bed space (overbed space) or freeboard region (free board zone) 30 with last cylindrical part 18 corresponding to spaces substantially.In stove of the present invention, the operation height H of fluidized bed region 28
FBSubstantially with the upper end of spout 22 and following barrel portion 18 between distance consistent.In order to prevent to form foaming fluidization regions, H at the top of fluidized bed region 28
FBPreferably be less than or equal to cylindrical part 16 inner diameter, ID down
FB1.5 times to twice.A freeboard region or a mistake bed Space H
OV.SMinimum constructive height fluidized bed height H preferably
Fb1.5 times to guarantee any particle that is pulled away and flow separation and the fluidized bed space of getting back to stove.
Preferably, each in cylindrical part 16,18 and the conical gas distributor 20 all has circle or oval cross section.The cross section of other shape (for example square, rectangle, octagon etc.) also can have the hydrodynamic characteristics that meets the requirements.But because in use stove will suffer a certain amount of thermal expansion, so these shapes are difficult to work in practice.
Slender electrode 32 passes upper and lower cylindrical part 18,16 respectively and extends in the body of heater 12 from top 34.Electrode 32 preferably by the conduction heat proof material for example graphite make and must with body of heater 12 electric insulations.When adopting single electrode, electrode 32 must be located in body of heater and align with the vertical axis Y of body of heater between two parties.Selectively be, can adopt a plurality of electrodes, in this case, described electrode retaining collar is around central axis Y symmetric arrangement.
The bottom of body of heater comprises discharging opening 40, and the solid of outflow passes described discharging opening 40 by the gravity effect and is discharged from continuously.Discharging opening 40 is sagging from conical gas distributor 20, and the inlet of discharging opening 40 overlaps with the summit of conical gas distributor 20 usually.
Gaseous emission can be discharged from by one or more blast pipes on the top 34 of body of heater 12 or air flue 42.The gas of this discharge is easy to be cleaned and handles to control particle and gas pollutant on demand.
According to the present invention, conical gas distributor 20 comprises a plurality of fluidizing gas inlet nozzles 22 (being depicted as 8), and fluidizing gas imports body of heater 12 by described inlet nozzle 22.Spout 22 makes fluidizing gas form and has the crosswise jet that upwards flows extremely uniformly radially towards the center of conical distributor 20.Can recognize that fluidizing gas discharges that the speed of spout and the average gas speed in fluid bed part 16 depend on particle size, density and the shape of the material that is fluidized.In the content of the method for the invention, fluidizing gas is nitrogen, argon gas or other inert gas normally.
In one embodiment, illustrate best in Fig. 3, it is radially relative that spout 22 is arranged to their axis X, thereby fluidizing gas directly is guided the center to conical gas distributor 20.Selectively, as being clearly shown that among Fig. 4, the axis X that spout 22 can be oriented to them becomes 10-20 ° of angle β with respect to conical gas distributor 20 at the tangent line of nozzle exit area.The layout of spout 22 makes their axis X and spout circumference tangent substantially, and fluid bed can be rotated, thereby makes any influence that departs from that fluid bed is more stable and produced with respect to central axis Y by slender electrode 32.This angle helps to prevent that fluidized particles from contacting with conical gas distributor 20 under high speed, this contact has caused wall excessive wear owing to swipe of gas distributor 20.
In order to prevent that fluidizing gas from disturbing or hindering the particle after handling to discharge from stove 10, spout 22 preferably is set at the tie point height H of gas distributor 20 and discharging opening 40 inlets
NThe place.Preferably, H
NIt is the overall height H of conical gas distributor 20
TC0.5-0.75 doubly, more preferably be H
TC0.6-0.65 doubly.
Each spout 22 preferably has the annular cross section vertical with its axis X, and the free cross-section area is limited at the axis X place.Shape of cross section can be circular or have other shape for example rectangle, ellipse etc.Spout 22 total free cross-section areas should be the 0.15%-0.5% that the cross-sectional area of fluid bed cylindrical part just descends the cross-sectional area of cylindrical part 16.Preferably, the free cross-sectional area of spout 22 the fluid bed cross-sectional area 0.25% to 0.4% between.
According to above description, the method that is used for processing fine particulate materials in EFB stove of the present invention should be conspicuous.At first, untreated granular materials passes under the gravity effect in the reaction zone that feed pipe 38 is fed to EFB stove 10 continuously.Untreated granular materials can comprise tiny, erose or polydisperse material.In trial run, the polydispersion material comprise particle size at 1.7mm (12mesh) to the particle between the 5 μ m.In addition, untreated particle can be conduction or semiconductive material, for example the carbonaceous material as carbon black, coke (fluid coke, flexible coke (flexi-coke), delay coke, needle coke, pitch coke etc.) and graphite (flake graphite, Delanium, vein graphite, amorphous graphite etc.).Various coke can be undressed or baked, can be petroleum coke or metallurgical coke, widely from various Jiao Yuan.Graphite can obtain from the Superior Graphite company in Chicago, assignee Illinois (Chicago Illinois) of the application.Untreated particulate matter is discharged from feed pipe 38 at the top end of the fluidization regions of the particle that flows downward or the just inner place of this fluidization regions.
The material of discharging from feed pipe is held in stove and the roughly corresponding zone of following cylindrical part 16 and is in fluidized state, and electric current by fluid bed equably described material is heated to common 2,200 ℃-2,400 ℃ high temperature.
Granular materials after the processing is discharged from from discharging opening 40 under the gravity effect continuously.Emission flow is configured such that the processing time of granular materials in fluid bed is enough to carry out required heat treatment or chemical reaction.In the use of EFB stove of the present invention, need in stove 10, not be provided with mechanical device or moving-member.
By manage 40 be discharged from after, the material after the processing is cooled in the cooling chamber (not shown).Gaseous emission passes air flue 42 at the top 34 of body of heater 12 and is discharged from.This gaseous emission is easy to be cleaned and handles pollutant is controlled at desired degree.
By utilizing EFB furnace treatment of the present invention reason fine particle, caused significantly improving (being 90.3%) in trial run with the rate of recovery of particle after the rate of recovery (the wherein said rate of recovery is less than 64% usually) of the foaming formula EFB stove of employing prior art is compared processing.In addition, the critical speed of fluidisation has reduced 10%-15% with respect to foaming formula EFB stove, for example in EFB stove of the present invention from about 0.30 feet per second to about 0.25 feet per second.
Following table 1 has compared several different graphite and coke material before according to heat treatment of the present invention and purity feature afterwards.The purity feature that is compared is the percentage (weight) of ash content and sulphur.
Table 1
| The purity of the heat treatment material of various carbon containings and graphite heat treatment material | |||
| Material is described | Content of ashes % | Sulphur content % | |
| Flake graphite (coarse) | After charging is handled | 0.9-1. 150 | - - |
| Flake graphite (tiny) | After charging is handled | 1.5-1.65 0 | 0.03-0.04 0.0012 |
| Fluid coke | After charging is handled | 0.6-0.7 0 | 1.9-2.0 0.007 |
| Carbon (particle) | After charging is handled | - - | 0.48 0.004 |
Therefore, a kind of improved EFB stove and processing method that fine particle is handled that be used for proposed.Although described the present invention according to preferred implementation and method, its purpose is not will limit the present invention in these embodiments and the method.For example, described stove and method are applicable to the chemical treatment of fine particle equally well, and fluidizing gas can be a reducibility gas in this case, for example carbon monoxide, hydrogen, methane etc.On the contrary, the present invention is limited by the scope of additional claim.
Claims (34)
1. electrothermal fluidized bed furnace comprises:
Body of heater with first cylindrical part, second cylindrical part and conical portion, described first cylindrical part has a height, described second cylindrical part is arranged on described first cylindrical part top and has the diameter bigger than first cylindrical part, described conical portion is arranged on described first cylindrical part below, described first cylindrical part and conical portion define fluidization regions, and described second cylindrical part defined the bed district;
Be arranged in the described body of heater and extend through at least one electrodes of described first and second cylindrical parts;
The discharge nozzle of material after the processing of described conical portion lower end;
Be used for raw material is imported the material feeding tube of described first cylindrical part;
At least one air flue that is used for the discharge stream oxidizing gases at described body of heater top; And
Be arranged on a plurality of spouts that are used for described fluidizing gas is imported described stove on the described conical portion, described spout is arranged on the plane of basic horizontal and described spout is positioned such that passing fluidizing gas stream that spout is imported into intersects and form flowing upwards at the core of described body of heater.
2. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that described electrode has end, and described end is positioned at first cylindrical part of described body of heater.
3. electrothermal fluidized bed furnace as claimed in claim 1, the center of being included in extend through the single electrode of described body of heater.
4. electrothermal fluidized bed furnace as claimed in claim 1 comprises extending through described body of heater and around a plurality of electrodes of the central axis symmetric arrangement of described body of heater.
5. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, described conical portion defines 30 °-90 ° central angle.
6. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, described conical portion defines 40 °-60 ° central angle.
7. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, each spout is arranged such that fluidizing gas stream acutangulates with respect to the tangent line of the wall of described conical portion and enters described conical portion.
8. electrothermal fluidized bed furnace as claimed in claim 1, it is characterized in that, described spout has central axis, and described spout is positioned such that with respect to the wall of described conical portion the described axis of each spout and the wall of described conical portion define 10 °-20 ° angle at the tangent line of described nozzle exit area.
9. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that described conical portion has overall height H
TC, and described spout is arranged on top, described conical portion bottom 0.5H
TC-0.75H
TCOn the described conical portion of distance.
10. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, described spout is arranged on top, described conical portion bottom 0.6H
TC-0.6H
TCOn the described conical portion of distance.
11. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, the height of described fluidised bed zones is less than or equal to 2 times of height of described first cylindrical part.
12. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, each spout has the 0.15%-0.5% of cross-sectional area that annular cross section area and the total annular cross section area of described spout are first cylindrical parts of described body of heater.
13. electrothermal fluidized bed furnace as claimed in claim 1 is characterized in that, each spout has the 0.25%-0.4% of cross-sectional area that annular cross section area and the total annular cross section area of described spout are first cylindrical parts of described body of heater.
14. electrothermal fluidized bed furnace, comprise body of heater with first cylindrical part, second cylindrical part and conical portion, described first cylindrical part has a height, described second cylindrical part is arranged on described first cylindrical part top and has the diameter bigger than first cylindrical part, described conical portion is arranged on described first cylindrical part below, described first cylindrical part and conical portion define fluidization regions, and described second cylindrical part defined the bed district; Be arranged in the described body of heater and extend through at least one electrodes of described first and second cylindrical parts; The discharge nozzle of material after the processing of described conical portion lower end; Be used for raw material is imported the material feeding tube of described first cylindrical part; At least one air flue that is used for the discharge stream oxidizing gases at described body of heater top; Improvement comprises:
Be arranged on a plurality of spouts that are used for described fluidizing gas is imported described stove on the described conical portion, described spout is arranged on the plane of basic horizontal and described spout is positioned such that the fluidizing gas stream that is imported into by spout intersects and forms flowing upwards at the core of described body of heater.
15. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, described electrode has end, and described end is positioned at first cylindrical part of described body of heater.
16. electrothermal fluidized bed furnace as claimed in claim 14, the center of being included in extend through the single electrode of described body of heater.
17. electrothermal fluidized bed furnace as claimed in claim 14 comprises extending through described body of heater and around a plurality of electrodes of the central axis symmetric arrangement of described body of heater.
18. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, described conical portion defines 30 °-90 ° central angle.
19. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, described conical portion defines 40 °-60 ° central angle.
20. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, each spout is arranged such that fluidizing gas stream acutangulates with respect to the tangent line of the wall of described conical portion and enters described conical portion.
21. electrothermal fluidized bed furnace as claimed in claim 14, it is characterized in that described spout has central axis and described spout and is positioned such that with respect to the wall of described conical portion the described axis of each spout and the wall of described conical portion define 10 °-20 ° angle at the tangent line of described nozzle exit area.
22. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, described conical portion has overall height H
TC, and described spout is arranged on top, described conical portion bottom 0.5H
TC-0.75H
TCOn the described conical portion of distance.
23. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, described spout is arranged on top, described conical portion bottom 0.6H
TC-0.6H
TCOn the described conical portion of distance.
24. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, the height of described fluidised bed zones is less than or equal to 2 times of height of described first cylindrical part.
25. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, each spout has the 0.15%-0.5% of cross-sectional area that annular cross section area and the total annular cross section area of described spout are first cylindrical parts of described body of heater.
26. electrothermal fluidized bed furnace as claimed in claim 14 is characterized in that, each spout has the 0.25%-0.4% of cross-sectional area that annular cross section area and the total annular cross section area of described spout are first cylindrical parts of described body of heater.
27. the method for a continuous treatment of particulate material comprises:
Electrothermal fluidized bed furnace as claimed in claim 1 is provided;
The spout that passes described stove with predetermined amount of flow imports fluidizing gas continuously;
The feed pipe that passes described stove with predetermined amount of flow imports untreated particulate matter continuously, makes described particulate matter mainly form fluid bed in first cylindrical part of described stove;
Give described electrifying electrodes to heat described fluid bed; And
From the discharge nozzle of the described stove particulate matter after the collection and treatment continuously.
28. method as claimed in claim 27 is characterized in that, described untreated particulate matter has the particle size less than 180 μ m (80mesh).
29. method as claimed in claim 27 is characterized in that, described untreated particulate matter comprises carbonaceous material.
30. method as claimed in claim 27 is characterized in that, described untreated particulate matter comprises the graphite of selecting from the group of being made up of flake graphite, Delanium, amorphous graphite and vein graphite.
31. method as claimed in claim 27 is characterized in that, described untreated particulate matter comprises the coke of selecting from the group of being made up of fluid coke, flexible coke, pitch coke, delay coke and needle coke.
32. method as claimed in claim 27 is characterized in that, described untreated particulate matter comprises conduction or semiconductive material.
33. a method according to claim 27 is handled resulting product to the granular coke of selecting from the group of being made of fluid coke, flexible coke, pitch coke, delay coke and needle coke.
34. a method according to claim 27 is handled resulting product to the granular graphite of selecting from the group of being made of flake graphite, Delanium, amorphous graphite and vein graphite.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US10/666,614 | 2003-09-18 | ||
| 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 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1871487A true CN1871487A (en) | 2006-11-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2004800307071A Pending CN1871487A (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) |
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| DE102010002244A1 (en) * | 2010-02-23 | 2011-08-25 | Evonik Carbon Black GmbH, 63457 | Carbon black, process for its preparation and its use |
| KR101956971B1 (en) * | 2013-06-21 | 2019-03-11 | 캐보트 코포레이션 | Conductive carbons for lithium ion batteries |
| DE102019126394A1 (en) * | 2019-09-30 | 2021-04-01 | Onejoon Gmbh | Process for the production of graphite and vertical graphitization furnace |
| AU2022264859A1 (en) * | 2021-04-29 | 2023-10-26 | Hatch Ltd. | Process and reactor for removing impurities from carbon material |
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| JPS54152615A (en) * | 1978-05-24 | 1979-12-01 | Ishikawajima Harima Heavy Ind Co Ltd | Suspended layer type direct reduction iron making process |
| JPS55818A (en) * | 1978-06-19 | 1980-01-07 | Babcock Hitachi Kk | Incinerating method by medium turning ascending current |
| 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 |
| US4547430A (en) * | 1981-11-10 | 1985-10-15 | Superior Graphite Company | Ultra-microcrystallite silicon carbide product |
| JP2727436B2 (en) * | 1995-05-31 | 1998-03-11 | 川崎重工業株式会社 | Method and apparatus for manufacturing iron carbide |
| US20050063892A1 (en) * | 2003-09-18 | 2005-03-24 | Deepak Tandon | Thermally modified carbon blacks for various type applications and a process for producing same |
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2003
- 2003-09-18 US US10/666,614 patent/US20050062205A1/en not_active Abandoned
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2004
- 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 WO PCT/US2004/029814 patent/WO2005028978A1/en not_active Application Discontinuation
- 2004-09-10 KR KR1020067005348A patent/KR20060116799A/en not_active Application Discontinuation
- 2004-09-10 JP JP2006526956A patent/JP2007506065A/en active Pending
- 2004-09-10 EP EP04783869A patent/EP1678453A1/en not_active Withdrawn
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102530923A (en) * | 2010-12-08 | 2012-07-04 | 沈阳铝镁设计研究院有限公司 | High-temperature electric calcining system and method of carbon raw material |
| 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 |
| CN107899520A (en) * | 2017-12-12 | 2018-04-13 | 中国科学院金属研究所 | A kind of high-temperature fluidized bed device |
| CN107899520B (en) * | 2017-12-12 | 2023-11-21 | 中国科学院金属研究所 | High-temperature fluidized bed reaction device |
Also Published As
| Publication number | Publication date |
|---|---|
| US20050062205A1 (en) | 2005-03-24 |
| JP2007506065A (en) | 2007-03-15 |
| KR20060116799A (en) | 2006-11-15 |
| WO2005028978A1 (en) | 2005-03-31 |
| EP1678453A1 (en) | 2006-07-12 |
| BRPI0414560A (en) | 2006-11-07 |
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