CN1129313A - Coal drying and grading device using fluidization-layer - Google Patents
Coal drying and grading device using fluidization-layer Download PDFInfo
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- CN1129313A CN1129313A CN95118676A CN95118676A CN1129313A CN 1129313 A CN1129313 A CN 1129313A CN 95118676 A CN95118676 A CN 95118676A CN 95118676 A CN95118676 A CN 95118676A CN 1129313 A CN1129313 A CN 1129313A
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- WWXKPYPTLSRBFP-UHFFFAOYSA-N C[N+](C1)=C2C1CCC2 Chemical compound C[N+](C1)=C2C1CCC2 WWXKPYPTLSRBFP-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
- C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
- F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B3/00—Drying solid materials or objects by processes involving the application of heat
- F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
- F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried
- F26B3/08—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried so as to loosen them, e.g. to form a fluidised bed
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Dispersion Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Drying Of Solid Materials (AREA)
- Combined Means For Separation Of Solids (AREA)
Abstract
Gas is sprayed from a spray orifice 21 which is arranged on a dispersion plate 2 to the upper inclined direction of the coal conveying direction which is relative to the dispersion plate 2, coal C flows and is conveyed simultaneously to form a fluidized layer 3 which is arranged on the conveying direction of the coal C so as to continuously constitute a first fluidized layer part 8 and a second fluidized layer part 9. The gas ejection speed at the second fluidized layer part 9 is higher than the gas ejection speed at the first fluidized layer part 8 and is set within the range of 60 to 80 m/s. A vertical filling layer 24 is arranged at the exhaust part of the fluidized layer 3. The invention can effectively dry the loaded coal C, obtain dry coal with very small water content and actually remove the components of fine powder in the dry coal by grading, and the residual rate can be reduced to be less than 1 percent.
Description
The invention relates to the coal dry classification device that utilizes fluosolids, particularly the coal in the coke-fired furnace of packing into is carried out drying, then fine powder in the coal is carried out the dry classification device that classification is removed.
As drying device for coal in the dry this coke-fired furnace of packing into, the general rotary drier that heating tube is installed that uses of past.Yet using this rotary drier that heating tube is installed, can not be the degree that the coal of about 12-13% is dried to about 4-6% with moisture content.And, in the coal that drying is crossed, contain the fine powder of a large amount of particle diameters below 105 μ m.Therefore, coal is being sent in the process of coke-fired furnace, these fine powders can produce a large amount of dust, in order to remove these dust, need deduster etc., thereby bring the increase of expense, simultaneously, the steam that residual moisture produces can condense in deduster, and its result need spend very big strength to take care of.
Therefore, present inventors propose to be provided with the scheme of fluosolids in the flat 3-181349 of spy number patents such as (spy open flat 5-71875 communique), make it from being located at the emission direction of the jet pipe ejection gas on the dispersion plate, and the direction along carrying object being treated is inclined upwardly.; adopt the coal drying device of this fluosolids; the coal particle that particle diameter is thick is from the speed ejection of nozzle with the 40-50 meter per second, because the effect of ejection gas; and in the fluosolids bottom near dispersion plate; be transferred drying while rotating, the coal particle that size ratio is less is owing to the effect of above-mentioned ejection gas obtains suitable mobile acceleration; be dried while flowing, superficial linear velocity in a column at this moment is the 2.0-4.5 meter per second.And then, handled by classification than the fine powder that this particle diameter is littler, be discharged from simultaneously with exhaust, thereby can obtain effective dry and remove fine powder.For example, the moisture content maximum can reach 2-3%, and the fine powder residual rate can be reduced to about below 2%.
Yet, above-mentioned fluosolids, coal there is not particular determination, about be mixed with the object being treated of oversize grain in having the particle that normal particle sizes distributes, the particle that normal particle sizes distributes can flow, on one side and thick particle rotates, be transferred on one side, can obtain satisfactory tangible processing, as purpose, and also keep room for improvement about the processing of fine powder with this.For example, about the coal in the coke-fired furnace of packing into, wish that particle diameter is that the following fine powder residual rate of 105 μ m can remain on below 1%, people wish to handle like this coal treating apparatus in the cards consumingly.
The present invention under this background, with this end in view, provides a kind of feasible coal dry classification device just, to use fluosolids, the fine powder composition that contains in the coal particle is carried out effective classification handle, and can obtain the few moisture-free coal of fine powder residual rate.
In order to solve above-mentioned problem, to reach this purpose, the dry classification device of being put down in writing in the claim 1 of the present invention, it is characterized in that having the gas that sprays the jet pipe on being located at dispersion plate coal is flowed, Yi Bian the fluosolids of carrying, will be from the emission direction of above-mentioned jet pipe ejection gas, throughput direction towards coal, with respect to above-mentioned dispersion plate, be set in the obliquity of oblique upper one side, the spouting velocity with above-mentioned gas is set in the scope of 60-80 meter per second simultaneously.
The dry classification device of being put down in writing in the claim 4 of the present invention, it is characterized in that having by the gas that sprays the jet pipe on being located at dispersion plate while the fluosolids that makes coal flow and carry, will be from the emission direction of above-mentioned jet pipe ejection gas, towards the throughput direction of coal and with respect to above-mentioned dispersion plate, be set in the obliquity of oblique upper one side, and with above-mentioned fluosolids towards above-mentioned coal throughput direction, the first class layer and second fluosolids are constituted continuously, will be set at bigger in the above-mentioned gas spouting velocity in above-mentioned second fluosolids than the gas spouting velocity in above-mentioned first class layer.
The dry classification device of being put down in writing in the claim 1, be preferably disposed on the rotary dryer that heating tube is installed in the past and the back segment of fluosolids drier, mainly be with the fine powder composition that removes in the moisture-free coal, the jet pipe on being arranged on dispersion plate, ejection gas with the high-speed ejection of 60-80m/ second, remove again and remain in the moisture that drops in the coal, simultaneously effectively with the fine powder of particle diameter below 105 μ m from greater than classification the coal particle of this particle diameter, discharge simultaneously with exhaust.
At this, when this spouting velocity is lower than 60 meter per seconds, the classification effectively of fine powder composition, the fine powder residual rate of discharging in the moisture-free coal still surpasses 1%, otherwise, spouting velocity substantially exceeds 80m/ during second, and the ratio regular meeting of the above particle of particle diameter 105 μ m of discharging with fine powder increases, and the fine powder classification becomes invalid.
In addition, according to same reason, hope is set in the superficial linear velocity in a column in this fluosolids in the scope of 3.5-4.5 meter per second.When the emission direction of above-mentioned gas is excessive with respect to the angle of inclination of above-mentioned dispersion plate, it is excessive that the composition of the vertical direction of flowing velocity also can become, the same existence greater than the particle of 105 μ m discharged the danger that ratio also will increase, and the horizontal direction speed of ejection gas can diminish on the contrary, owing to rotate the conveying that can hinder oversize grain.For this reason, wish emission direction, tilt to be set in 30 ° with respect to dispersion plate with above-mentioned gas.
In addition, the dry classification device of record is suitable for carrying out drying from coal until the classification of fine powder in the claim 4, in the gas spouting velocity is set in low relatively first class layer, the coal that is dried and handles, be transported in the second high relatively fluosolids of gas spouting velocity once more dryly, remove contained fine powder composition with time stage.
Therefore, in this dry classification device, change by gas spouting velocity in these 2 fluosolids, make the classification of fine powder become possibility, but in order to want more effective removal fine powder, require the dry classification device of record in 1 same with aforesaid right, be classified to make in second fluosolids gas spouting velocity preferably to be set in the scope of 60-80 meter per second mainly carrying out fine powder.
In addition, in these dry classification devices, for so remove fine powder, the discharge position of coal preferably is provided with by discharging coal and is formed the perpendicular type packed layer that sprays gas in the packed layer in above-mentioned fluosolids.
Below referring to figs. 1 through Fig. 8 the embodiment of the dry classification device of claim 4 of the present invention is described.
In addition, the dry classification device of claim 1 of the present invention, the independent sector of second fluosolids is roughly the same in the device of its formation and claim 4, so saved the detailed description to it.
Among Fig. 1, the device body of symbol 1 expression present embodiment dry classification device, this device body 1 roughly makes the casing shape, and its inside is installed dispersion plate 2 in the horizontal direction.Like this, on the dispersion plate 2 of this device body 1 inside, form fluosolids 3, simultaneously, the bottom of dispersion plate 2 got make gas and import compression chamber 4.
In addition, be provided with on an end top of this device body 1 to carry out the position 5 of packing into of the coal C that dry classification handles, simultaneously, at the other end discharge position 6 that moisture-free coal that implement to handle is discharged is set, the coal C that packs into white arrow direction in dispersion plate 2 upper edge figure is carried.
Inside at device body 1, its vertical middle part is provided with dividing plate 7 dispersion plate 2 is separated in two, above-mentioned fluosolids 3 is clamped dividing plate 7, a side that is divided into the above-mentioned position 5 of packing into, be first class layer 8 He of coal C throughput direction rear side, above-mentioned discharge portion 6 one sides, i.e. second fluosolids 9 of coal C throughput direction one side.Gap 10 between aforementioned barriers 7 and the dispersion plate 2 as the discharge position of first fluidized bed 8, also is the position of packing into of the 2nd fluosolids 9 simultaneously not only.
Have, the top 11 of device body 1 makes it the top 11a more highland formation of the top 11b of second fluosolids 9 than first class layer 8, and at each top 11a, exhaust outlet 12,13 is set respectively on the 11b again.
In addition, in the compression chamber 4 that the bottom of dispersion plate 2 forms, also be provided with and the corresponding dividing plate 14 in position of aforementioned barriers 7, the compression chamber 4 that forms of dividing plate 14 thus is divided into first compression chamber 15 under the first class layer and second compression chamber 16 under second fluosolids 9.And then, in the first, the second compression chamber 15,16, air supply opening 17,18 is set respectively, separate air feed.By dispersion plate 2, gas is sprayed onto in each fluidized bed 8,9.
Fig. 2 is the section amplification figure of above-mentioned dispersion plate 2, as shown in the figure, many air introducing ports 19 are arranged on the dispersion plate 2 ... on the direction vertical, extend respectively with above-mentioned throughput direction, and on this throughput direction, form mutual gap, simultaneously, at each air introducing port 19 ... first cover 20 cylindraceous of loam cake makes on same vertical with the throughput direction direction of this cover to be arranged on the dispersion plate 2.On these covers 20, along it direction being set there are a plurality of spray orifices 21 with proper spacing ..., respectively towards above-mentioned throughput direction one side, and make it tiltangle for dispersion plate 2 below 30 °, form the direction of inclination towards oblique upper.
And then, tabular transport platform 22 is set between the cover 20 that adjoins each other on the above-mentioned throughput direction, make it to be located at above dispersion plate 2 above throughput direction rear side cover 20, tilt obliquely upward with above-mentioned tiltangle angle same.
In addition, the shape of above-mentioned spray orifice 21, its section can be circular, or along above-mentioned oval shape and the ellipticity that direction is extended is set, or rectangular-shaped and platform shape.And then, can change the section configuration of the spray orifice 21 in the first class layer 8 and second fluosolids 9, for example, when section is circular in the first class layer 8, can adopt ellipticity in second fluosolids 9.
Can utilize as shown in Figure 3 formation spray orifice 21 and transport platform 22, section is that the plate cover 23 of " ヘ " type replaces the cover 20 of semicircle tubulars and tabular transport platform 22, is arranged on the dispersion plate 2.Perhaps the dispersion plate 2 that is provided with as shown in Figure 4 self forms stair-stepping spray orifice 21 and transport platform 22.
But these spray orifices 21 are preferably in the plane and look when seeing dispersion plate 2, and decentralized configuration forms staggeredly etc. equably, and self forms when stepped as above-mentioned dispersion plate 2, makes transport platform 22 also can disperse equably to form equally.
And then for the area of dispersion plate 2, the ratio of the aperture area of spray orifice 21 promptly on the aperture efficiency of spray orifice 21, the particularly dispersion plate in second fluosolids 2, preferably is set in 3-6%.When this aperture efficiency is reduced to less than 3% the time, can seem not enough to the gas supply of fluosolids 3, otherwise when surpassing 6% and when excessive, must increase the gas supply for obtaining desirable spouting velocity, this is not too economical again.
, be fed to the gas in the first, the second compression chamber 15,16, from the spray orifice 21 of the dispersion plate 2 of such formation ... ejection is fed to respectively in the first, two the fluosolids 8,9.
In the present embodiment, wherein be sprayed onto the gas spouting velocity in the 2nd fluosolids 9, be set in the 60-80m/ scope of second from second compression chamber 16.And the gas spouting velocity that is sprayed onto the 1st fluosolids 8 from first compression chamber 15 is littler than these, is set in the 40-50m/ scope of second.
Moreover, be sprayed onto the gas in the 1st fluosolids portion 8, be heated into hot blast for the drying of coal C, ejection is fed in first compression chamber 15.To this, be sprayed onto the gas the 2nd fluosolids portion 9 from second compression chamber 16, according to the moisture content of coal C in the 2nd fluosolids 9 of packing into etc., preferably elect the gas of hot blast or normal temperature as.And, heating tube can be installed in fluosolids 3 in order to carry out the drying aid processing.
And then, in the present embodiment, discharge 6 places, position in the end of above-mentioned throughput direction one side that is positioned at fluosolids 3, perpendicular shape packed layer 24 is set, the gas that is formed in the packed layer by the coal C that discharges position 6 discharges can spray.
This perpendicular shape packed layer 24, attenuate downwards in the perpendicular shape silo 25 that extends from discharging position 6, conical dispersion umbrella 26 is set, simultaneously, be blown into tube 27 in the setting of the bottom of silo 25, and employing is fed to these dispersion umbrellas 26 and the gas that is blown in the case 27, the structure of the spray pattern quiescent layer clasfficiator that can spray.In addition, be provided with outlet 28 in the lower end of silo 25.
At this, as above-mentioned dispersion umbrella 26, for example can be suitable for, the scheme that inventors of the present invention propose in the past has been documented in the special dispersion umbrella in (special fair 1-23711 communique) patent of being willing to clear 59-95983 number, promptly, preferably make it to constitute as shown in Figure 5, disperseing to form the same generally gas dispersion hole 26b on the ramp 26a of umbrella 26, and on the 26b of these gas dispersion holes, forming at least with horizontal direction or blow out the shield 26c of gas separately downwards.
In addition, the above-mentioned case 27 that is blown into can dispense according to classification efficiency of 3 pairs of fine powders of fluosolids etc.
In the present embodiment dry classification device of this formation, be encased in the coal C of fluosolids from the position 5 of packing into, at first in first class layer 8, be subjected to passing through the hot blast gas drying of spray orifice 21 ejections of dispersion plate 2 from the 1st compression chamber 15 while moving, make moisture content reach dry limit, 2-3% limit and carry, pack second fluosolids 9 into from the gap 10 of 7 on dividing plate in.In addition, in this first class layer 8, the coal particle that size ratio is bigger is subjected to from the effect of spray orifice 21 ejection gases and rotates, and takes advantage of transport platform 22 all to move bottom at fluosolids 3.In addition, show the smaller coal particle that normal grain distributes, be subjected to disperseing the effect of ejection gas, and produce suitable flowing velocity, move while flowing by big particle diameter coal particle.Infeed the gas in the first class layer portion 8, after having captured the moisture that is contained among the coal C, discharge from the exhaust outlet 12 of top 11a.
Equally, the coal C in second fluosolids 9 of packing into, here, by spray orifice 21, from the gas of the 2nd compression chamber 16 with the high-speed ejection of 60-80 meter per second, the fine powder composition of particle diameter less than 105 μ m removed in classification.Wherein discharged from the exhaust outlet 13 that is located at top 11b simultaneously by the fine powder composition of classification and exhaust, suitable capture means capture processing to utilize bag hose and cyclone separator etc.
In addition, the coal particle that particle diameter is big is subjected to the action edge rotation limit of above-mentioned ejection gas and moves in the bottom of fluosolids 3, in addition, shows that between these oversize grains and fine powder the particle that normal particle sizes distributes moves while flowing.
Fig. 6 is the raw material with size distribution shown in Figure 7, pack in the 2nd fluosolids 9 of present embodiment dry classification device, in the fluosolids different with the spray orifice direction, when changing the spouting velocity of spray orifice gas, particle diameter is less than the residual rate investigation of 105 μ m fine powders in the coal of discharge.But, situation when the chain-dotted line among the figure represents that gas sprays to oblique upper in the present embodiment, perhaps, solid line represents that from diameter be the situation of 3mm spray orifice vertical up-spray when going out gas, and then dotted line represents that from diameter be the situation of 6mm spray orifice vertical up-spray when going out gas.At this moment the particle holdup time is 15 seconds in the fluosolids, and floor height is 300mm, and superficial linear velocity in a column is 3.6 meter per seconds.
Yet, result according to Fig. 6, gas is from spray orifice sprays vertically upward, no matter adopt which kind of spouting velocity, residual fine powder all can surpass 2%, otherwise, if adopt the device of present embodiment, when spouting velocity was higher than 60 meter per seconds, the fine powder residual rate can be reduced to 1%, also can keep this situation even spouting velocity reaches about 90 meter per seconds.
Fig. 8 packs the feed coal of size distribution shown in Fig. 7 in the 2nd fluosolids 9 of present embodiment structure equally, aspect the spouting velocity of setting changing gas, and when changing in the fluosolids 9 superficial linear velocity in a column, the investigation of fine powder residual rate.But, the situation when solid line represents that spouting velocity is 50 meter per seconds among the figure, the situation when dotted line represents that spouting velocity is 100 meter per seconds in the present embodiment, and the situation of the triangulation point among the figure when representing that spouting velocity is 150 meter per seconds.At this moment holdup time and the height of fluosolids were respectively 15 seconds and 300mm with above-mentioned identical.
Yet, result according to Fig. 8, at first, exceed about the gas spouting velocity under the situation of above-mentioned scope, which kind of situation no matter, the fine powder residual rate can not be reduced to 1%, otherwise, when spouting velocity was 75 meter per seconds in above-mentioned scope, even superficial linear velocity in a column is higher than 3.5 meter per seconds, the fine powder residual rate also can be reduced to below 1%.
But when the gas spouting velocity surpassed 80 meter per seconds or superficial linear velocity in a column and substantially exceeds 4.5 meter per seconds, fine powder and particle diameter surpass the particle of 105 μ m discharged with exhaust, and the fine powder residual rate increases on the contrary and becomes invalid.For this reason,, make the gas spouting velocity in 60-80 meter per second scope, or superficial linear velocity in a column is set in the scope of 3.5-4.5 meter per second respectively as above-mentioned.In addition, can carry out according to the adiabatic drying method about the mensuration of these fine powder residual rates.
And then, carrying out drying through first class layer 8 handles, in the 2nd fluosolids 9, carry out classification and remove the coal C of fine powder composition, in perpendicular shape packed layer 24 pack into from the discharge position 6 of fluosolids 3, by disperseing umbrella 26 and blowing out the remaining fine powder composition of the further classification removal of gas that case 27 sprays, discharge from outlet 28 subsequently.In addition, in perpendicular shape packed layer 24 by the fine powder of classification, with in the 2nd fluosolids 9 by the fine powder of classification from exhaust outlet 13 discharges.
In the present embodiment, the first class layer 8 and second fluosolids 9 are by dividing plate 7 separately, and because respectively at fluosolids 8,9 places are provided with exhaust outlet 12,13, thus as mainly to moisture content are high in the withering first class layer 8 of loading coal C exhaust with as the high exhausts of fine powder containing ratio in the 2nd fluosolids 9 that mainly carries out the fine powder classification, discharge respectively, and can suitably handle respectively, can obtain the pump-down process of different efficient.
But in the fluosolids 3 of present embodiment, by the gas that the spray orifice 21 from above-mentioned dispersion plate 2 sprays, thick coal particle is rotating mobile.Therefore, in fluosolids 3, usually form very strong deflection stream along above-mentioned throughput direction, particularly this dry classification device begins starting or when stopping, when particle flow is insufficient, only in fluidized bed 3, even in above-mentioned the 2nd fluosolids 9, fine powder can not obtain abundant classification, and the harm that brings residual rate to increase.
At this situation, at the discharge position 6 of fluosolids 3 perpendicular shape packed layer 24 is set, this structure can suppress starting for this reason, the increase of fine powder residual rate when stopping, and simultaneously, can obtaining significantly when normally turning round continuously, the fine powder residual rate reduces.
Two kinds of situations compare below the table 1 pair, the feed coal of the above-mentioned size distribution shown in Figure 7 of packing into, at the present embodiment dry classification device that is provided with perpendicular shape packed layer 24 with only with the dry classification device of the structure of present embodiment fluosolids 3, beginning starting or when stopping and the fine powder residual rate when turning round continuously.
Table 1
| Operating condition | The fine powder residual rate | |
| Embodiment ( |
The starting, when stopping | ????1.2％ |
| When turning round continuously | ????0.7％ | |
| Has only |
The starting, when stopping | ????3.0％ |
| When turning round continuously | ????1.0％ |
As can be known from the results of Table 1, have only in the structure of fluosolids 3, the fine powder residual rate can be reduced to 1% when turning round continuously, starts, is 3% o'clock when stopping, and is extremely unstable.But in contrast, in the present embodiment dry classification device that is provided with perpendicular shape packed layer 24, in starting, when stopping, the fine powder residual rate can reduce significantly, is 1.2%, and when the particle flow stable continuous turned round, residual rate can be reduced to 0.7%.
In addition, illustrated as described above in the present embodiment, about by fluosolids 3, promptly by the 1st and the 2nd fluosolids position 8,9, the dry classification device of the claim 4 of the present invention of formation, for example as shown in Figure 9, only be fluosolids position 9 with this embodiment the 2nd separately as dry classification device 31, can be equipped with the back of the rotary drier that heating tube is installed 32 in the past.But among Fig. 9, shown in the symbol 33 is the position of packing into that the rotary dryer 32 of heating tube is installed, the 34th, discharge the position, the 35th, the position of packing into of above-mentioned dry classification device 31, the 36th, discharge the position, the 37th, the bag hose that is connected with the exhaust outlet 38 of this dry classification machine 31.Other and the common part of embodiment shown in Figure 1 are furnished with same symbol, omit its explanation.
Yet in this dry classification device 31, from the gas of spray orifice 21 ejection of dispersion plate 2, its spouting velocity is the 60-80 meter per second, in view of the above, can carry out effective fine powder classification.Be fed to compression chamber 4 and the gas of ejection is heated as hot blast, be dried to a certain degree moisture-free coal by the rotary dryer 32 that heating tube is installed, can further carry out drying, its result can obtain fine powder and residual moisture moisture-free coal seldom.By be provided with perpendicular shape packed layer 24 at above-mentioned discharge position 36, can obtain reduction fine powder residual rate with the foregoing description same effect.
As described above, according to the present invention, can carry out drying to loading coal effectively, obtain moisture content moisture-free coal seldom, the fine powder composition in this moisture-free coal can be removed by classification indeed simultaneously, and its residual rate can be reduced to below 1%.Therefore, can prevent from course of conveying such as coke-fired furnace, to produce dust in advance, and the environment around polluting perhaps spends a large amount of expenses in order to tackle dust.These cover end and can be inhibited.
Fig. 1 is the overall structure figure of one embodiment of the invention.
Fig. 2 is the amplification profile diagram of the dispersion plate 2 of embodiment shown in Fig. 1.
Fig. 3 is the amplification profile diagram of expression dispersion plate 2 another form examples shown in Figure 2.
Fig. 4 is the amplification profile diagram of the third form example of dispersion plate 2 shown in Figure 2.
Fig. 5 is the sectional drawing that disperses umbrella 26 in the perpendicular shape packed layer 24 embodiment illustrated in fig. 1.
Fig. 6 is the graph of a relation of gas spouting velocity and fine powder residual rate in the second fluosolids position 9 embodiment illustrated in fig. 1.
Fig. 7 is a particle size distribution figure of measuring used coal shown in Fig. 6 and Fig. 8.
Fig. 8 is the graph of a relation of superficial linear velocity in a column and fine powder residual rate in the 2nd fluosolids position 9 of embodiment shown in Fig. 1.
Fig. 9 is the structure chart of other embodiment of the present invention.
Symbol description
1 ... device body 2. ... dispersion plate
3 ... fluosolids 4 ... the compression chamber
Positions are discharged at 5,35 pack into positions 6 36
7,14 dividing plates 8 the 1st fluosolids position
9 the 2nd fluosolids positions, 12,13 exhaust outlets
21 spray orifices, 22 transport platform
24 perpendicular shape packed layers 26 disperse umbrella
32 install the rotary dryer C coal of heating tube
Claims (6)
1. coal dry classification device that utilizes fluosolids, it is characterized in that: have the fluosolids that coal is carried from the gas that is arranged on the spray orifice ejection on the dispersion plate while flowing, and will be from the direction of above-mentioned spray orifice ejection gas, be set in throughput direction along coal, and oblique upper with respect to above-mentioned dispersion plate inclination, simultaneously, the above-mentioned gas spouting velocity is set in the scope of 60-80 meter per second.
2. according to the coal dry classification device of claim 1, it is characterized in that: the superficial linear velocity in a column in the above-mentioned fluosolids is set in the scope of 3.5-4.5 meter per second.
3. according to the coal dry classification device of claim 1 or 2, it is characterized in that: the emission direction of above-mentioned gas is located at below 30 ° with respect to the inclination angle of above-mentioned dispersion plate.
4. coal dry classification device that utilizes fluosolids, it is characterized in that: have the fluosolids that coal is carried from the gas that is arranged on the spray orifice ejection on the dispersion plate while flowing, and will spray the direction setting of gas at throughput direction from above-mentioned spray orifice along coal, and oblique upper with respect to above-mentioned dispersion plate inclination, above-mentioned fluosolids, on the throughput direction of above-mentioned coal, constituting the 1st fluosolids position and the 2nd fluosolids position continuously, bigger than the gas spouting velocity at above-mentioned the 1st fluosolids position in the gas spouting velocity at above-mentioned the 2nd fluosolids position.
5. according to the coal dry classification device of claim 4, it is characterized in that: the gas spouting velocity at above-mentioned the 2nd fluosolids position is set in the scope of 60-80 meter per second.
6. according to each coal dry classification device among the claim 1-5, it is characterized in that: the discharge position of coal in above-mentioned fluosolids is provided with by the perpendicular shape filling position of discharging the packed layer ejection gas that coal forms.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP022144/1995 | 1995-02-09 | ||
| JP022144/95 | 1995-02-09 | ||
| JP02214495A JP3342595B2 (en) | 1995-02-09 | 1995-02-09 | Dry classifier for coal using fluidized bed |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1129313A true CN1129313A (en) | 1996-08-21 |
| CN1053038C CN1053038C (en) | 2000-05-31 |
Family
ID=12074681
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95118676A Expired - Lifetime CN1053038C (en) | 1995-02-09 | 1995-09-29 | Coal drying and grading device using fluidization-layer |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP3342595B2 (en) |
| KR (1) | KR0180346B1 (en) |
| CN (1) | CN1053038C (en) |
| TW (1) | TW272149B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102230717A (en) * | 2011-08-01 | 2011-11-02 | 长沙通发高新技术开发有限公司 | Body structure of boiling rotating fluidized bed |
| CN101724422B (en) * | 2009-12-11 | 2013-01-02 | 本溪鹤腾高科技研发（中心）有限公司 | Device for drying and sieving coal by wind power |
| CN104101179A (en) * | 2013-04-10 | 2014-10-15 | 长沙通发高新技术开发有限公司 | Bubbling fluidized bed body structure capable of simultaneously realizing winnowing and drying |
| CN108686956A (en) * | 2018-05-16 | 2018-10-23 | 华东理工大学 | A kind of powder granule sorting unit and method for separating |
| CN109514755A (en) * | 2018-12-24 | 2019-03-26 | 青岛海诺中天科技股份有限公司 | A kind of drying system for plastic foam particle overlay film |
| CN110546446A (en) * | 2016-09-21 | 2019-12-06 | 日铁工程技术株式会社 | drying method and drying apparatus |
| CN111097693A (en) * | 2019-12-27 | 2020-05-05 | 河南理工大学 | Continuous drying and sorting integrated equipment and method for wet fine coal |
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| KR100509001B1 (en) * | 2000-12-13 | 2005-08-18 | 주식회사 포스코 | apparatus for separating wet coal in surge bin hopper |
| JP4741545B2 (en) * | 2007-04-19 | 2011-08-03 | 新日本製鐵株式会社 | Fluidized bed drying classifier |
| KR101118308B1 (en) * | 2009-09-28 | 2012-03-20 | 주식회사 포스코 | Device for covering blending bin |
| CN103571513B (en) * | 2013-10-15 | 2016-12-07 | 长沙通发高新技术开发有限公司 | The process system of UTILIZATION OF VESIDUAL HEAT IN is carried out in coking coal preparation technique |
| KR101497565B1 (en) * | 2014-06-17 | 2015-03-02 | 주식회사 한국테크놀로지 | Device for Flattening of Transportation Coal in System for Drying Coal |
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-
1995
- 1995-02-09 JP JP02214495A patent/JP3342595B2/en not_active Expired - Lifetime
- 1995-09-02 KR KR1019950028685A patent/KR0180346B1/en not_active IP Right Cessation
- 1995-09-06 TW TW084109318A patent/TW272149B/en not_active IP Right Cessation
- 1995-09-29 CN CN95118676A patent/CN1053038C/en not_active Expired - Lifetime
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101724422B (en) * | 2009-12-11 | 2013-01-02 | 本溪鹤腾高科技研发（中心）有限公司 | Device for drying and sieving coal by wind power |
| CN102230717A (en) * | 2011-08-01 | 2011-11-02 | 长沙通发高新技术开发有限公司 | Body structure of boiling rotating fluidized bed |
| CN102230717B (en) * | 2011-08-01 | 2014-10-29 | 长沙通发高新技术开发有限公司 | Body structure of boiling rotating fluidized bed |
| CN104101179A (en) * | 2013-04-10 | 2014-10-15 | 长沙通发高新技术开发有限公司 | Bubbling fluidized bed body structure capable of simultaneously realizing winnowing and drying |
| CN104101179B (en) * | 2013-04-10 | 2016-01-06 | 长沙通发高新技术开发有限公司 | Selection by winnowing and dry fluidizing fluid-bed bed structure can be carried out simultaneously |
| CN110546446A (en) * | 2016-09-21 | 2019-12-06 | 日铁工程技术株式会社 | drying method and drying apparatus |
| CN110546446B (en) * | 2016-09-21 | 2020-11-10 | 日铁工程技术株式会社 | Drying method and drying apparatus |
| CN108686956A (en) * | 2018-05-16 | 2018-10-23 | 华东理工大学 | A kind of powder granule sorting unit and method for separating |
| CN108686956B (en) * | 2018-05-16 | 2024-05-03 | 华东理工大学 | Powder particle sorting device and sorting method |
| CN109514755A (en) * | 2018-12-24 | 2019-03-26 | 青岛海诺中天科技股份有限公司 | A kind of drying system for plastic foam particle overlay film |
| CN111097693A (en) * | 2019-12-27 | 2020-05-05 | 河南理工大学 | Continuous drying and sorting integrated equipment and method for wet fine coal |
Also Published As
| Publication number | Publication date |
|---|---|
| KR0180346B1 (en) | 1999-02-18 |
| KR960031576A (en) | 1996-09-17 |
| CN1053038C (en) | 2000-05-31 |
| JPH08219655A (en) | 1996-08-30 |
| TW272149B (en) | 1996-03-11 |
| JP3342595B2 (en) | 2002-11-11 |
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