CN104550026B - Method for sorting limestone chips by utilizing fluidized bed - Google Patents
Method for sorting limestone chips by utilizing fluidized bed Download PDFInfo
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- CN104550026B CN104550026B CN201410792265.XA CN201410792265A CN104550026B CN 104550026 B CN104550026 B CN 104550026B CN 201410792265 A CN201410792265 A CN 201410792265A CN 104550026 B CN104550026 B CN 104550026B
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- 238000000034 method Methods 0.000 title claims abstract description 27
- 235000019738 Limestone Nutrition 0.000 title abstract description 18
- 239000006028 limestone Substances 0.000 title abstract description 18
- 239000000843 powder Substances 0.000 claims abstract description 38
- 239000000463 material Substances 0.000 claims abstract description 12
- 239000012530 fluid Substances 0.000 claims description 112
- 239000000839 emulsion Substances 0.000 claims description 65
- 239000008187 granular material Substances 0.000 claims description 32
- 238000009423 ventilation Methods 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 15
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 12
- 238000005243 fluidization Methods 0.000 claims description 7
- 239000000725 suspension Substances 0.000 claims description 6
- 239000002245 particle Substances 0.000 abstract description 14
- 235000008733 Citrus aurantifolia Nutrition 0.000 abstract description 5
- 235000011941 Tilia x europaea Nutrition 0.000 abstract description 5
- 239000004571 lime Substances 0.000 abstract description 5
- 235000019580 granularity Nutrition 0.000 description 32
- 238000012216 screening Methods 0.000 description 11
- 239000004575 stone Substances 0.000 description 10
- 238000001354 calcination Methods 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000004579 marble Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to the field of sorting limestone, in particular to a method for sorting limestone chips by utilizing a fluidized bed. The method comprises the following steps of a, feeding to-be-screened limestone chips into the fluidized bed, wherein the longitudinal section of a dense-phase zone, which is vertical to material flowing direction, of the fluidized bed is trapezoidal, a length-width ratio of the cross section of the fluidized bed is (4-20) : 1, the width of the surface of the trapezoidal dense-phase zone of the fluidized bed is 2-8 times as big as that of the bottom part of the dense-phase zone, and air is blown into the fluidized bed from the bottom part of the fluidized bed; b, controlling the standard state empty tower gas velocity of the bottom part of the fluidized bed to be 0.3-1.5m/s and the average residence time of the to-be-screened limestone chips in the dense-phase zone of the fluidized bed to be 6-20 minutes, and respectively obtaining coarse lime particles, fine lime particles and fine lime powder. Through the method, the limestone chips with different particle sizes in mixed limestone chips of which the particle sizes are smaller than 10mm can be efficiently classified to be sorted, and thus different industrial requirements can be met.
Description
Technical field
The present invention relates to limestone sorting field, in particular to a kind of side of utilization fluid bed separation race
Method.
Background technology
When the building stones such as stone field quarrying stone head, marble or slabstone, have the race that a large amount of granularities are less than 10mm
Thrown aside, not only waste of resource but also pollute environment.Numerous researchs show, in the 800-900 DEG C of Calx burning till because having very high ratio
Surface area and have very high activity.Therefore after circulation fluidized-bed combustion boiler in nineteen sixty, occur as soon as and use recirculating fluidized bed
The imagination of calcining furnace lime burning, raw material should be exactly the race that granularity is less than 10mm.
And current stone pit is after acquiring building stones, the waste limestone material that remaining granularity is less than 10mm is all size
The Calx building stones of the various granularities differing mix, and need granularity is less than the race of 10mm from good calcining angle
By the row screening again of finer grain size category, but need to spend substantial amounts of work with prior art.
Initially method is to use artificial screening, is specifically manually screened using screen cloth, so not only wastes time and energy, and sieves
Select efficiency low.Later with scientific and technological progress and development, using mechanical grading, its screening efficiency improves relatively, but still not
The market demand can be met, and screen limited precision, environmental pollution is serious, also has very big danger to the healthy of operating personnel
Evil.
Have evolved to quick strength screening at present, its screening efficiency is greatly improved, but equipment construction is multiple
Miscellaneous, one new equipment cost of manufacture is high, so that use cost is improved simultaneously, high energy consumption simultaneously, the electric power resource mistake of consumption
Height, finally makes the cost price of race too high, is unfavorable for that commercial production is applied.
In view of this, the special proposition present invention.
Content of the invention
It is an object of the invention to provide a kind of method of utilization fluid bed separation race, with it, can
By granularity be less than 10mm combined lime aggregate chips in varigrained race, efficiently classification and sorting out, with meet
Different industrial requirements.
In order to realize the above-mentioned purpose of the present invention, spy employs the following technical solutions：
A kind of method of utilization fluid bed separation race, comprises the following steps：
A, race to be sieved is sent in fluid bed, the emulsion zone perpendicular to Flow of Goods and Materials direction for this fluid bed is indulged
Section is trapezoidal, and the transverse section length-width ratio of fluid bed is (4-20)：1, the face width of the trapezoidal emulsion zone of described fluid bed
It is 2-8 times of its bottom width, wherein divulged information from the bottom of fluid bed；
B, the standard state empty tower gas velocity of the described fluidized-bed bottom of control are 0.3-1.5m/s, and described race to be sieved exists
The mean residence time of the emulsion zone of fluid bed is 6-20 minute, respectively obtains Calx coarse granule, Calx fine grained and Calx thin
Powder.
Circulating fluidized bed calcinator has three regions, an emulsion zone being in furnace bottom, its particle flow shape
State is bubbling bed, and wherein grain graininess is based on 1-5mm；Next to that being located at the suspension section on emulsion zone, its particle flow shape
State is air flow bed or fast bed, and wherein grain graininess is based on 0.1-1mm；It is finally high temperature cyclone separator, wherein air-flow is made
Strong rotation, can be separated more than 0.1mm granule and be sent back to burner hearth.Trizonal based on circulating fluidized bed calcinator presence
Characteristic, exactly for adapting to the difference requirement to granularity for the calcining furnace zones of different, for ensure good calcine, need by aggregate chips in addition
Screening, the present invention provides a kind of method of brand-new utilization fluid bed separation race：
Using the fluidization principle of fluid bed, granularity is less than the race of 10mm because its granularity is little, can be in fluid bed
Interior fluidized well.In up big and down small taper or trapezoidal fluid bed, varigrained race in fluid mapper process,
Can be layered because the upper and lower speed of service is different, especially thin stone powder can be left fluid bed emulsion zone by elutriation with carrying secretly, reaches close
In floating zone on phase region and cyclone separator, and coarse grained race can rest on emulsion zone bottom, fine grained
Emulsion zone surface can be distributed in, so, the little fine powder of granularity can directly be recovered in the air outlet of cyclone separator, and with
This simultaneously because layering, big particle can sink to the bottom first, and fine grained can stay coarse grained top, can be from the bottom of fluid bed
Portion first takes out coarse granule, takes out fine grained from emulsion zone surface, is finally reached and sorts varigrained race on demand
Effect.
Wherein, in order to race can be fluidized well and sorts, simultaneously need to the length-width ratio of setting fluid bed is big
In 4, the face width of the trapezoidal emulsion zone of described fluid bed is more than 2 times of its bottom width, and wherein length-width ratio is preferably
(4-20)：1, the face width of the preferably trapezoidal emulsion zone of described fluid bed is 2-8 times of its bottom width, only fluid bed
Length-width ratio and the face width of emulsion zone and bottom width when meeting aforementioned proportion and requiring, race could be by well
Fluidisation and sorting.
If Aspect Ratio is less than 4, race has little time layering it is difficult to reach the purpose of sorting in fluid bed.
And the face width of emulsion zone and when bottom width is equal or ratio is less than 2, in fluid mapper process, because upper and lower space size
Equal, do not have enough speed differences to allow race to go up lower leaf well, only the face width of emulsion zone is with relatively
When vast scale is more than bottom width, fine grained just more easily can float to top layer, and coarse granule can sink to bottom, is beneficial to
Fluidisation layering.
And when divulging information in fluid bed, the wind speed of its ventilation is closely related with quantity with the granularity of the powder body intending sorting,
And material is then closely related with sorting quality in the mean residence time of emulsion zone, and the present invention only need to control fluidized-bed bottom
Standard state empty tower gas velocity is 0.3-1.5m/s it is possible to sub-elect the powder that maximum particle size is 100-400 micron.To be sieved is described
The mean residence time of the emulsion zone in fluid bed for the race is more than 6 minutes, along with aforementioned fluid bed transverse section length-width ratio
With the condition of vertical section width ratio, then the race adding all can well be sorted.Preferably, race to be sieved
It is 6-20 minute in the mean residence time of the emulsion zone of fluid bed.
So, a kind of method of the utilization fluid bed separation race being provided by the present invention, granularity can be less than
The race of the combination grain of 10mm fluidizes well so as to classification more becomes more meticulous in fluid bed.And greatly improve
The speed of race screening and efficiency, energy saving simultaneously, more environmentally-friendly.And can sub-elect coarse granule is that granularity is
The granule of 1.5mm mass fraction of occupying on sieve is more than 70%, and fine powder is that fine powder that granularity the is 0.3mm part under sieve accounts for
Some mass fractions be more than 80%, fine grained be wherein more than 70% grain graininess be 0.3-1.5mm limestone particle.
Further, in step a, the length-width ratio arranging trapezoidal described fluid bed is (8-15)：1.It is highly preferred that setting
The length-width ratio of trapezoidal described fluid bed is 4：1 it is, arrange the length-width ratio minimum 4 of trapezoidal described fluid bed：1.
Further, in step a, the face width arranging the trapezoidal emulsion zone of described fluid bed is its bottom width
4-6 times, it is highly preferred that the face width of the trapezoidal emulsion zone of described fluid bed of setting is 2 times of its bottom width.Also
It is that the face width minimum arranging the trapezoidal emulsion zone of described fluid bed is 2 times of its bottom width.
Further, in step b, wherein said coarse granule is the mass parts that the granule that granularity is 1.5mm occupies on sieve
Number is more than 70%, and described fine powder is that the mass fraction that fine powder that granularity the is 0.3mm part under sieve is occupied is more than 80%, described
Fine grained be wherein more than 70% grain graininess be 0.3-1.5mm.
In step b, the mean residence time of the described race to be sieved emulsion zone in fluid bed is 6 minutes.?
It is exactly that the mean residence time the shortest of the described race to be sieved emulsion zone in fluid bed is 6 minutes.
Further, the minimum 8000Pa of blast in step a, during described ventilation.In order to meet the blast in fluid bed
Require, when divulging information from bottom is to fluid bed, its blast minimum should reach 8000Pa.
Further, the minimum 8000-8500Pa of blast in step a, during described ventilation.
Further, described ventilation includes being passed through First air in fluidized-bed bottom, is passed through secondary on emulsion zone surface simultaneously
Wind.
When needing the race of the fine-powder-grade collecting more amount from high temperature cyclone separator, because simply by stream
Change bed bottom to wind, wherein part fine powder can rest on suspension section it is impossible to rapidly enter in high temperature cyclone separator, so, this
When secondary wind wherein can be passed through by position more than emulsion zone surface, the powder that can accelerate fine-powder-grade enters high temperature
In cyclone separator.
Further, the blast of described secondary wind is 2000-2500Pa.
Further, during described ventilation, adjust the amount of feeding of described First air and secondary wind, obtain required thin
The demand of powder.
Meanwhile, as needed, part fine grained and oarse-grained race also can enter in high temperature cyclone separator, this
When only need to meet when the mass fraction that part under sieve for the fine powder that granularity is 0.3mm occupies is more than 80% and be believed that collection
To powder be fine powder race.Equally, when collecting coarse granule and fine grained, as long as meeting the granule that granularity is 1.5mm
The material that the mass fraction occupying on sieve is more than 70% is coarse granule, and wherein more than 70% grain graininess is 0.3-
The material of 1.5mm is fine grained.
Further, in step b, the standard state empty tower gas velocity of described fluidized-bed bottom is 0.8-1.2m/s, it is highly preferred that institute
The standard state empty tower gas velocity stating fluidized-bed bottom is 1m/s.
Compared with prior art, beneficial effects of the present invention are：
(1) using fluid bed, race can be sieved the material for different grain size grade.
(2) screening efficiency is high, and screening precision is high.
(3) it is beneficial to environmental protection.
Brief description
In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
The accompanying drawing having required use in technology description is briefly described.
The structural representation of the fluid bed of the race of the screening that Fig. 1 provides for the present invention；
The distribution schematic diagram of the race putting in fluid bed that Fig. 2 provides for the present invention；
1. fluid bed, 2. fine grained, 3. coarse granule, 4. suspension section, 5. emulsion zone, 6. high temperature cyclone separator.
Specific embodiment
Below in conjunction with embodiment, embodiment of the present invention is described in detail, but those skilled in the art will
Understand, the following example is merely to illustrate the present invention, and be not construed as limiting the scope of the present invention.Unreceipted concrete in embodiment
Condition person, the condition according to normal condition or manufacturer's suggestion is carried out.Agents useful for same or the unreceipted production firm person of instrument, are
Can be by the commercially available conventional products bought and obtain.
A kind of method of utilization fluid bed separation race, comprises the following steps：
A, race to be sieved is sent in fluid bed 1, this fluid bed is perpendicular to the emulsion zone in Flow of Goods and Materials direction
Vertical section is trapezoidal, and the transverse section length-width ratio of fluid bed is (4-20)：1, the surface width of the trapezoidal emulsion zone of described fluid bed
Degree is 2-8 times of its bottom width, is wherein divulged information from the bottom of fluid bed；
B, the standard state empty tower gas velocity controlling described fluid bed 1 bottom are 0.3-1.5m/s, described race to be sieved
It is 6-20 minute in the mean residence time of the emulsion zone 5 of fluid bed 1, respectively obtain Calx coarse granule, Calx fine grained and stone
Grey fine powder.
Fluidized bed calcination stove has three regions, an emulsion zone 5 being in furnace bottom, and its particle flow form is
Bubbling bed, wherein grain graininess is based on 1-5mm；Next to that being located at the suspension section 4 on emulsion zone 5, its particle flow form
It is air flow bed or fast bed, wherein grain graininess is based on 0.1-1mm；It is finally high temperature cyclone separator 6, wherein air-flow is made by force
Strong rotation, can be separated more than 0.1mm granule and be sent back to burner hearth.The trizonal spy being existed based on circulating fluidized bed calcinator
Property, exactly for adapting to the difference requirement to granularity for the calcining furnace zones of different, for ensureing well to calcine, need to be sieved aggregate chips
Point, the present invention provides a kind of method that brand-new utilization fluid bed 1 sorts race：
As depicted in figs. 1 and 2, using the fluidization principle of fluid bed 1, granularity is less than the race of 10mm because its granularity
Little, can be fluidized well in fluid bed 1.In up big and down small taper or trapezoidal fluid bed, varigrained Calx
Aggregate chips, in fluid mapper process, can be layered because the upper and lower speed of service is different, and especially thin stone powder can be left stream by elutriation with carrying secretly
Change bed 1 emulsion zone 5, reach in floating zone and the cyclone separator on emulsion zone 5, and the race of coarse granule 3 can stop
Stay emulsion zone 5 bottom, fine grained can be distributed in emulsion zone surface, so, the little fine powder of granularity can be directly in cyclonic separation
The air outlet of device is recovered, and meanwhile, because layering, big particle can sink to the bottom first, and fine grained 2 can stay coarse granule
3 top, can first take out coarse granule 3 from the bottom of fluid bed 1, from emulsion zone 5 surface take out fine grained 2, be finally reached by
The effect that varigrained race sorts on demand.
Wherein, in order to race can be fluidized well and sorts, simultaneously need to the length-width ratio of setting fluid bed 1 is big
In 4, the face width of the trapezoidal emulsion zone 5 of described fluid bed 1 is more than 2 times of its bottom width, and wherein length-width ratio is preferred
For (4-20)：1, the face width of the preferably trapezoidal emulsion zone 5 of described fluid bed 1 is 2-8 times of its bottom width, only flows
Change the face width of the length-width ratio of bed and emulsion zone 5 and when bottom width meets aforementioned proportion and requires, race could quilt
Fluidize well and sort.
If Aspect Ratio is less than 4, race has little time layering it is difficult to reach the purpose of sorting in fluid bed.
And the face width of emulsion zone 5 and when bottom width is equal or ratio is less than 2, in fluid mapper process, because upper and lower space is big
Little equal, do not have enough speed differences to make race go up lower leaf well, only the face width of emulsion zone 5 is with larger
When ratio is more than bottom width, fine grained 2 just more easily can float to top layer, and coarse granule 3 can sink to bottom, is beneficial to
Fluidisation layering.
And when divulging information in fluid bed 1, the wind speed of its ventilation is closely related with quantity with the granularity of the powder body intending sorting,
And material is then closely related with sorting quality in the mean residence time of emulsion zone, and the present invention only need to control fluid bed 1 bottom
Standard state empty tower gas velocity be 0.3-1.5m/s it is possible to sub-elect maximum particle size be 100-400 micron powder.Institute to be sieved
The mean residence time stating the emulsion zone 5 in fluid bed 1 for the race is more than 6 minutes, along with aforementioned fluid bed transverse section is long
The wide condition with vertical section width ratio for the ratio, then the race adding all can be by active fluidization.Preferably, Calx to be sieved
The mean residence time of the emulsion zone 5 in fluid bed 1 for the aggregate chips is 6-20 minute.
So, the method that race is sorted by a kind of utilization fluid bed 1 that the present invention provides, granularity can be less than
The race of 10mm fluidizes well so as to classification more becomes more meticulous in fluid bed 1.And substantially increase race
The speed of screening and efficiency, energy saving simultaneously, more environmentally-friendly.And the granule that coarse granule is that granularity is 1.5mm can be sub-elected
On sieve, the mass fraction that occupies is more than 70%, and fine powder is the mass parts that fine powder that granularity the is 0.3mm part under sieve is occupied
Number be more than 80%, fine grained be wherein more than 70% grain graininess be 0.3-1.5mm limestone particle.
Preferably, in step a, the length-width ratio arranging trapezoidal described fluid bed is (8-15)：1.It is highly preferred that setting ladder
The length-width ratio of the described fluid bed of shape is 4：1 it is, arrange the length-width ratio minimum 4 of trapezoidal described fluid bed：1.
Preferably, in step a, the face width arranging the trapezoidal emulsion zone of described fluid bed is the 4- of its bottom width
6 times, it is highly preferred that the face width of the trapezoidal emulsion zone of described fluid bed of setting is 2 times of its bottom width.It is,
The face width minimum arranging the trapezoidal emulsion zone of described fluid bed is 2 times of its bottom width.
Preferably, in step b, wherein said coarse granule is the mass fraction that the granule that granularity is 1.5mm occupies on sieve
More than 70%, described fine powder is that the mass fraction that fine powder that granularity the is 0.3mm part under sieve is occupied is more than 80%, described thin
Granule be wherein more than 70% grain graininess be 0.3-1.5mm.
Preferably, in step b, the mean residence time of the described race to be sieved emulsion zone 5 in fluid bed 1 is
6 minutes.It is, the mean residence time the shortest of the described race to be sieved emulsion zone 5 in fluid bed 1 is 6 minutes.
Preferably, the minimum 8000Pa of blast in step a, during described ventilation.Will in order to meet the blast in fluid bed 1
Ask, when divulging information from bottom is to fluid bed, its blast minimum should reach 8000Pa.
Preferably, the minimum 8000-8500Pa of blast in step a, during described ventilation.
Preferably, described ventilation includes being passed through First air in fluidized-bed bottom, is passed through secondary on emulsion zone 5 surface simultaneously
Wind.
When needing the race of the fine-powder-grade collecting more amount from high temperature cyclone separator 6, because simply by
Fluidized-bed bottom can rest on suspension section 4 it is impossible to rapidly enter in high temperature cyclone separator 6 to wind, wherein part fine powder, institute
Now can be given by the position more than emulsion zone 5 surface and to be wherein passed through secondary wind, the powder that can accelerate fine-powder-grade enters
Enter in high temperature cyclone separator 6.
Preferably, the blast of described secondary wind is 2000-2500Pa.
Preferably, during described ventilation, adjust the amount of feeding of described First air and secondary wind, obtain required fine powder
Demand.
Meanwhile, as needed, part fine grained 2 and oarse-grained race also can enter in high temperature cyclone separator 6,
Now only need to meet when the mass fraction that part under sieve for the fine powder that granularity is 0.3mm occupies is more than 80% and be believed that receipts
The powder collecting is fine powder race.Equally, when collecting coarse granule 3 and fine grained 2, as long as meeting granularity is 1.5mm's
The material that the mass fraction that granule occupies on sieve is more than 70% is coarse granule 3, and wherein more than 70% grain graininess is
The material of 0.3-1.5mm is fine grained 2.
Preferably, in step b, the standard state empty tower gas velocity of described fluidized-bed bottom is 0.8-1.2m/s, it is highly preferred that described
The standard state empty tower gas velocity of fluidized-bed bottom is 1m/s.
Embodiment 1
A kind of method that utilization fluid bed 1 sorts race, comprises the following steps：
A, race to be sieved is sent into arrange the length-width ratio of trapezoidal described fluid bed 1 in fluid bed 1 be 4：1,
The face width of the emulsion zone 5 of trapezoidal described fluid bed 1 is 2 times of its bottom width, gives wherein logical from the bottom of fluid bed 1
Wind；
B, the standard state empty tower gas velocity of described fluid bed 1 bottom of control are 0.6m/s, and described race to be sieved is in stream
The mean residence time changing the emulsion zone 5 of bed 1 is 6 minutes.
Embodiment 2
A kind of method that utilization fluid bed 1 sorts race, comprises the following steps：
A, race to be sieved is sent into arrange the length-width ratio of trapezoidal described fluid bed 1 in fluid bed 1 be 20：
1, the face width of the trapezoidal emulsion zone 5 of described fluid bed 1 is 8 times of its bottom width, gives wherein from the bottom of fluid bed 1
It is passed through First air, the blast of ventilation is 8000Pa, is passed through secondary wind on emulsion zone 5 surface simultaneously, blast is 2000Pa；
B, the standard state empty tower gas velocity of described fluid bed 1 bottom of control are 1.5m/s, and the amount according to required fine powder is adjusted once
Wind and the intake of secondary wind, the mean residence time of the described race to be sieved emulsion zone 5 in fluid bed 1 is 20 points
Clock.
C, collect limestone fines from the air outlet of high temperature cyclone separator 6, collect limestone from fluidized-bed bottom big
Granule, from emulsion zone 5 surface collection limestone fine grained 2.
Experimental example 1
By 1 ton/when race to be sieved send into that to arrange the length-width ratio of trapezoidal fluid bed in fluid bed be 8：1, ladder
The face width of the emulsion zone of described fluid bed of shape is 6 times of its bottom width, gives from the bottom of fluid bed and is wherein passed through one
Secondary wind, the blast of ventilation is 8000Pa, is passed through secondary wind on emulsion zone surface simultaneously, and blast is 2000Pa；Control fluid bed bottom
The standard state empty tower gas velocity in portion is 1m/s, adjusts the intake of First air and secondary wind according to the amount of required fine powder, stone to be sieved
The mean residence time of the emulsion zone in fluid bed for the limestone chips is 10 minutes.Finally respectively from the air outlet of high temperature cyclone separator
Limestone fines 0.1-0.2 that the mass fraction that part under sieve for the fine powder for 0.3mm for place's collection granularity is occupied is more than 80%
Ton, the granularity of collection is that to be more than 70% limestone coarse granule be 0.2-0.3 for the mass fraction that occupies on sieve of granule of 1.5mm
Ton, the grain graininess of collection more than 70% is the limestone fine grained 0.5-0.7 ton of 0.3-1.5mm.
Although illustrate and describing the present invention with specific embodiment, but it will be appreciated that without departing substantially from the present invention's
Many other changes can be made in the case of spirit and scope and change.It is, therefore, intended that in the following claims
Including all such changes and modifications belonging in the scope of the invention.
Claims (7)
1. a kind of method using fluid bed separation race is it is characterised in that comprise the following steps：
A, race to be sieved is sent in fluid bed, this fluid bed is perpendicular to the emulsion zone vertical section in Flow of Goods and Materials direction
For trapezoidal, the transverse section length-width ratio of fluid bed is（4-20）：1, the surface width of the trapezoidal emulsion zone vertical section of described fluid bed
Degree is 2-8 times of its bottom width, divulges information to it from the bottom of fluid bed；
B, the standard state empty tower gas velocity of the described fluidized-bed bottom of control are 0.3-1.5m/s, and described race to be sieved is in fluidisation
The mean residence time of the emulsion zone of bed is 6-20 minute, and combines at the suspension section on high temperature cyclone separator and emulsion zone
Reason, respectively obtains Calx coarse granule, Calx fine grained and Calx fine powder；
Wherein, described ventilation includes being passed through First air in fluidized-bed bottom, is passed through secondary wind on emulsion zone surface simultaneously；Described
During ventilation, adjust the amount of feeding of described First air and secondary wind, obtain the demand of required fine powder；
In described step b, described coarse granule is that the mass fraction that the granule that granularity is 1.5mm occupies on sieve is more than 70%, institute
The mass fraction that to state fine powder be that fine powder that granularity the is 0.3mm part under sieve is occupied is more than 80%, and described fine grained is wherein
More than 70% grain graininess is 0.3-1.5mm.
2. a kind of utilization fluid bed separation race according to claim 1 method it is characterised in that
In step a, the length-width ratio arranging described fluid bed transverse section is（8-15）：1.
3. a kind of utilization fluid bed separation race according to claim 1 method it is characterised in that
In step a, the face width arranging the trapezoidal emulsion zone vertical section of described fluid bed is 4-6 times of its bottom width.
4. a kind of utilization fluid bed separation race according to claim 1 method it is characterised in that
The minimum 8000Pa of blast in step a, during described ventilation.
5. a kind of utilization fluid bed separation race according to claim 4 method it is characterised in that
In step a, blast during described ventilation is 8000-8500Pa.
6. a kind of utilization fluid bed separation race according to claim 1 method it is characterised in that
The blast of described secondary wind is 2000-2500Pa.
7. a kind of utilization fluid bed separation race according to claim 1 method it is characterised in that
In step b, the standard state empty tower gas velocity of described fluidized-bed bottom is 0.8-1.2m/s.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410792265.XA CN104550026B (en) | 2014-12-18 | 2014-12-18 | Method for sorting limestone chips by utilizing fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410792265.XA CN104550026B (en) | 2014-12-18 | 2014-12-18 | Method for sorting limestone chips by utilizing fluidized bed |
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| Publication Number | Publication Date |
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| CN104550026A CN104550026A (en) | 2015-04-29 |
| CN104550026B true CN104550026B (en) | 2017-02-22 |
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| CN104858137B (en) * | 2015-06-04 | 2016-08-24 | 中国矿业大学 | A kind of based on secondary bed arrange semi-automatic carry material device fluid bed separation experimental machine |
| CN108465563B (en) * | 2017-02-23 | 2020-06-09 | 中国石油化工股份有限公司 | Dry sorting device and method for solid materials |
| CN107185837A (en) * | 2017-05-03 | 2017-09-22 | 大连理工大学 | A kind of particle grading device and its method |
| CN109401794B (en) * | 2017-08-17 | 2021-02-09 | 中国石油化工股份有限公司 | Staged conversion combined fluidized bed reaction device and reaction method |
| CN110314772B (en) * | 2019-07-10 | 2021-02-26 | 河南神马尼龙化工有限责任公司 | Method for improving quality of dried adipic acid product by utilizing particle size screening |
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| CN1063830A (en) * | 1991-02-01 | 1992-08-26 | 中南工业大学 | The method and apparatus of tungsten powder or tungsten carbide powder dry classification |
| CN1060236A (en) * | 1991-10-22 | 1992-04-15 | 国家建筑材料工业局咸阳非金属矿研究所 | Method with sort asbestos with fluidized bed |
| JP2812917B2 (en) * | 1996-04-18 | 1998-10-22 | 川崎重工業株式会社 | Fluidized bed classifier |
| JP4530965B2 (en) * | 2005-10-05 | 2010-08-25 | 中国電力株式会社 | Recovery method of valuable materials from bed material ash |
| CN201454851U (en) * | 2009-09-04 | 2010-05-12 | 中国矿业大学 | Large-scale vibration counterflow fluidized bed dry sorting machine |
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Effective date of registration: 20190110 Address after: 065200 South Side of North Outer Ring Road, Siyang Town, Sanhe City, Langfang City, Hebei Province Patentee after: Hebei Fuhao Machinery Manufacturing Co., Ltd. Address before: 065200 Lao Xinzhuang Village 333, Loess Tuzhuang Town, Sanhe City, Hebei Province Patentee before: Yang Lianming |