CN106673463A - Production method of high-activity lime - Google Patents
Production method of high-activity lime Download PDFInfo
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- CN106673463A CN106673463A CN201611236721.8A CN201611236721A CN106673463A CN 106673463 A CN106673463 A CN 106673463A CN 201611236721 A CN201611236721 A CN 201611236721A CN 106673463 A CN106673463 A CN 106673463A
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- decompression
- storehouse
- decompression storehouse
- rotary kiln
- production method
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B2/00—Lime, magnesia or dolomite
- C04B2/10—Preheating, burning calcining or cooling
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Furnace Details (AREA)
- Muffle Furnaces And Rotary Kilns (AREA)
Abstract
The invention discloses a production method of high-activity lime, and belongs to the field of lime preparation. The production method comprises the following steps of pretreating and preheating: sequentially sending limestone powder in a material bin into a preheater, a first pressure relief bin and a second pressure relief bin, heating the surface and interior of the limestone powder to 820+/-10 DEG C by the preheater, sending into the first pressure relief bin, closing a connecting passage with the preheater after the first pressure relief bin is filled with the limestone powder, and sucking vacuum to 1E0 to 1E2Pa; after the vacuum sucking of the first pressure relief bin is completed, sending all limestone material into the second pressure relief bin; closing the passage between the first pressure relief bin and the second pressure relief bin, and sucking vacuum to 1E-1 to 1E-2Pa; calcining, and cooling, so as to obtain the limestone with activity higher than 360ml. The production method has the advantages that the continuous calcining is realized in the vacuum atmosphere, the calcining temperature is lower than the common calcining temperature, and the relationship between activity of limestone and decomposing speed of limestone is solved.
Description
Technical field
The present invention relates to Calx preparation field, particularly a kind of active lime production method.
Background technology
Active lime has the distinguishing features such as specific surface area is big, bulk density is little, the porosity is high, crystal grain is tiny.By activity
Calx is applied in steelmaking process, can make that slag making slugging accelerates, the duration of heat shortens, and desulfurization dephosphorization effect also can be more preferable.
Production practices are proved:Made steel using active lime, dephosphorization rate and desulfurization degree are respectively increased 10%~60%, and lime consumption is reduced
10%~35%, calcium fluoride consumption reduces by 30%, and the quantity of slag reduces 10%~12%, and duration of blast shortens 10%.And traditional handicraft
During calcined limestone, the grain size intervals of limestone are larger, in calcination process, because the rate of heat transfer of Calx is much smaller than limestone
Rate of heat transfer, with the lkd layer increasingly thickness of outer layer after, cause the rate of heat transfer of inner layer limestone particle can be increasingly slower,
Calcination time is longer, and long-time high temperature can make limestone surfaces burning " porcelain ", and then makes the CO2 gases produced in calcining
It is difficult to discharge, decarburization not exclusively, forms raw burn.The energy is not only wasted, and affects the quality of low-carbon (LC) active lime.
In prior art, there is contradiction in the activity degree and decomposition of limestone speed of Calx：Calcining heat is high, decomposition of limestone
Speed is fast, but activity of lime is low, in addition burning and lose activity；And calcining heat is low, although activity of lime is high, but Calx
Stone decomposition rate is slow, and calcination time is long；And calcining heat is low, it is also possible to cause raw burn, can equally reduce the activity degree of Calx.
And the activity of lime that existing most process is obtained is generally less than 360ml, and generally forge at a temperature of 950-1150 DEG C
Burn, power consumption is big, is susceptible to burning.
The content of the invention
The goal of the invention of the present invention is, for the problems referred to above, there is provided a kind of active lime production method, by vacuum
In realize continuous calcining, and calcining heat is less than usual calcining heat, solve activity of lime and decomposition of limestone speed it
Between relation, the activity degree of more than 360ml can be obtained under less energy consumption.
To reach above-mentioned purpose, the technical solution adopted in the present invention is：
A kind of active lime production method, comprises the following steps：
Pretreatment, will collect limestone raw ore and sequentially passes through broken, and cleaning is desilted, and staged care obtains granule size and is
The limestone powder of 40-50mm, sends limestone powder into feed bin storage；
The pre-heat treatment, by the limestone powder in feed bin preheater, the first decompression storehouse and the second decompression storehouse, institute are sequentially sent to
State preheater limestone powder surface and internal temperature is heated to into 850 ± 10 DEG C and the first decompression storehouse is sent into, the first decompression storehouse
Fill up after limestone powder and close with preheater interface channel and carry out being evacuated to 1E0~1E2pa；Taking out true in the first decompression storehouse
Limestone powder whole is sent into into the second decompression storehouse after the completion of idle job；Second decompression storehouse is closed and is gone forward side by side with the first decompression warehouse channel
Row is evacuated to 1E-1~1E-2pa；
Limestone powder is sent in the rotary kiln isobaric with the second decompression storehouse and is carried out in calcination processing, the second decompression storehouse
Calcination processing, obtains high-temperature lime, and calcining heat is 850-950 DEG C, and calcination time is 90-130min；
High-temperature lime is sequentially sent to the 3rd decompression storehouse, the 4th decompression storehouse and cooling chamber, institute by cooling treatment, the rotary kiln
State the rotary kiln to send into high-temperature lime and the 3rd of its equipressure decompression storehouse, the 3rd decompression storehouse fill up after high-temperature lime close with
Rotary kiln passage, and high-temperature lime is sent into into the 4th decompression storehouse；4th decompression storehouse is filled up after high-temperature lime and is closed and the 3rd decompression
Warehouse channel, and high-temperature lime feeding cooling chamber is carried out into cold front heavy rain.
Kiln tail in the rotary kiln is reduced pressure storehouse by the first valve connection second, and its kiln hood is by the second valve connection the
Three decompression storehouses；Rotary kiln is provided with heater and vacuum extractor, and the heater includes burner, the burner edge
Rotary kiln central axis is arranged；Multiple burner noz(zle)s for connecting fuel-device are evenly equipped with burner, burner is near
Aerator of the two decompression storehouse one end connections outside rotary kiln, burner is near the 3rd decompression storehouse one end connection preheater；It is described
Vacuum extractor includes check valve, exhaustor and vacuum pump, and the exhaustor is arranged in rotary kiln, and exhaustor is located at turn around kiln
Central axis top and with rotary kiln centerline axis parallel；The check valve is uniformly arranged on exhaustor and check valve is by outward extremely
Interior conducting, the vacuum pump is located at turn around outside kiln and connects with exhaustor；The outlet side connection preheater of the vacuum pump.
Realize that raw limestone, to the conveying of rotary kiln, its role is to by many by multi-step pressure reduction storehouse in such scheme
Level decompression is adjusted, and raw limestone is sent into and reduce the impact to rotary kiln during rotary kiln so as to which be maintained at needs for a long time
Under the vacuum state wanted, to realize continuous production.In prior art, although also have and calcine in a vacuum, but its is more
Segment section is to maintain for vacuum state, such as kiln hood；Or it is fixed to change vacuum, feeds intake be required for opening calcining again every time
Stove；The unnecessary energy is so not only expended, and is intermittent production, it does not have continuous production, can only be adapted to little
The generation demand of batch.Simultaneously it will be appreciated that large-scale its volume of rotary kiln is very huge, its evacuation extremely consumes energy, because
And need to save the energy loss of each step.
Preferably, the preheater is connected with emission-control equipment.Arranging emission-control equipment can effectively be reduced to big
Discharge pollutants between gas, it is possible to reduce the pressure to environment.
Preferably, the rotary kiln is followed successively by from the inside to the outside shell, external thermal insulation, intermediate interlayer, inner thermal insulating layer and inner shell,
The burner combustion device arranges intermediate interlayer temperature at 800-850 DEG C near the 3rd decompression storehouse one end connection intermediate interlayer,
Pressure is 3E5-6E5pa；The intermediate interlayer of the rotary kiln is near second decompression storehouse one end connection preheater.Here with burning
The flue gas of generation carries out post bake to rotary kiln, it is ensured that the temperature of rotary kiln is uniform so that decomposition of limestone is uniform, and
Reduce the loss of fuel.
Preferably, it is described first decompression position in storehouse in second decompression storehouse directly over and between arrange connection valve, described second
Decompression storehouse is more than the first decompression storehouse, a quarter of the connection valve diameter not less than the first decompression storehouse diameter.This
Sample arranges the limestone powder enabled in the first decompression storehouse and rapidly enters the second decompression storehouse, and the second decompression storage capacity is more
The limestone powder that the first decompression storehouse falls can be conveniently housed greatly, while reserved certain space gives evacuation operation, it is to avoid stone
Lime stone powder is blocked to pipeline, affecting parameters adjustment.
Preferably, it is described 3rd decompression position in storehouse in the 4th decompression storehouse directly over and between arrange connection valve, the described 4th
Decompression storehouse is more than the 3rd decompression storehouse, a quarter of the connection valve diameter not less than the 4th decompression storehouse diameter.This
Sample arranges the limestone powder enabled in the 3rd decompression storehouse and rapidly enters the 4th decompression storehouse, and the 4th decompression storage capacity is more
The limestone powder that the 3rd decompression storehouse falls can be conveniently housed greatly；Reduce by the 3rd decompression storehouse evacuation operation.
Preferably, the second decompression orlop portion is provided with the spiral feeder of rotary kiln, and spiral feeder is just
To the first valve.Material straight line conveying can be carried out by spiral feeder, while structure setting can be reduced and optimized.
Preferably, the 3rd decompression position in storehouse is in the kiln hood lower section of rotary kiln.High-temperature lime so in rotary kiln can be with
It is convenient and swift in falling directly into the 3rd decompression storehouse, reduce unnecessary conveying arrangement.
Preferably, the first decompression storehouse and the second decompression storehouse include successively from the inside to the outside shell, external thermal insulation, centre
Interlayer and inner shell；The intermediate interlayer of the rotary kiln sequentially passes through the middle interval in the second decompression storehouse near second decompression storehouse one end
Preheater is connected after layer, the intermediate interlayer in the first decompression storehouse.Limestone powder after preheating is through the first decompression storehouse and second
Can there is the situation of temperature drop behind decompression storehouse, not reach the due effect of preheating, and flue gas is discharged to first by burner
Decompression storehouse and the second decompression storehouse are heated, and can form soak layer on the first decompression storehouse and the second decompression storehouse, maximum
Reduce or cause the limestone powder after preheating there is no heat behind the first decompression storehouse and the second decompression storehouse in degree
The problem of loss.Burner can be made full use of simultaneously to discharge the preheating of flue gas, reduce thermal losses.
Preferably, the upper end in the first decompression storehouse, the second decompression storehouse and the 3rd decompression storehouse is mounted on for evacuation
Vacuum pump.
Due to adopting above-mentioned technical proposal, the invention has the advantages that：
1. the present invention allows rotary kiln continuous under 1E-1~1E-2pa vacuum environments by arranging multi-step pressure reduction storehouse
Unbroken production, it has calcining heat low, and fuel is burned low, obtain activity of lime it is high the characteristics of.Wherein, Activity of Lime
Degree is in more than 360ml.
Description of the drawings
Fig. 1 is illustrative view of functional configuration of the present invention.
In accompanying drawing, 1- feed bins, 2- preheaters, the decompressions of 3- first storehouse, the decompressions of 4- second storehouse, 5- rotary kilns, 6- the 3rd reduce pressure
Storehouse, the decompressions of 7- the 4th storehouse.
Specific embodiment
Below in conjunction with accompanying drawing to invention be embodied as further illustrate.
As shown in figure 1, a kind of active lime production method, comprises the following steps：
Pretreatment, will collect limestone raw ore and sequentially passes through broken, and cleaning is desilted, and staged care obtains granule size and is
The limestone powder of 45mm, limestone powder feeding feed bin 1 is stored.
The pre-heat treatment, by the limestone powder in feed bin 1 decompression of preheater 2, first storehouse 3 and second decompression storehouse is sequentially sent to
4, limestone powder surface and internal temperature is heated to 850 DEG C and sends into the first decompression storehouse 3 by the preheater 2, the first decompression
Storehouse 3 is filled up after limestone powder and closes with the interface channel of preheater 2 and carry out being evacuated to 1E2pa.Preheater 2 is connected with waste gas
Processing meanss.First decompression storehouse 3 is all sent into the second decompression storehouse 4 by limestone powder after the completion of evacuation operation.Second subtracts
Pressure storehouse 4 is closed with the first decompression passage of storehouse 3 and carries out being evacuated to 1E-2pa.
First decompression storehouse 3 be located at directly over the second decompression storehouse 4 and between connection valve is set, the second decompression storehouse 4 is more than the
One decompression storehouse 3, a quarter of the connection valve diameter not less than the first decompression diameter of storehouse 3.So arranging can
So that the limestone powder in the first decompression storehouse 3 rapidly enters the second decompression storehouse 4, and the second decompression volume of storehouse 4 more greatly can be with
It is convenient to house the limestone powder that the first decompression storehouse 3 falls, while reserved certain space gives evacuation operation, it is to avoid agstone
Material is blocked to pipeline, affecting parameters adjustment.First decompression storehouse 3 and second decompression storehouse 4 from the inside to the outside successively include shell,
External thermal insulation, intermediate interlayer and inner shell.The upper end in the first decompression storehouse 3, second decompression storehouse 4 is mounted on the vacuum for evacuation
Pump.The second decompression bottom of storehouse 4 is provided with the spiral feeder of rotary kiln 5, and spiral feeder is just to the first valve.Pass through
Spiral feeder can carry out material straight line conveying, while structure setting can be reduced and optimized.
Calcination processing, the second decompression storehouse 4 is carried out in the rotary kiln 5 by limestone powder feeding with the second decompression equipressure of storehouse 4
Calcination processing, obtains high-temperature lime, and calcining heat is 870 DEG C, and calcination time is 110min.Kiln tail in rotary kiln 5 is by the
The second decompression of one valve connection storehouse 4, its kiln hood is by the decompression storehouse 6 of the second valve connection the 3rd.Rotary kiln 5 is provided with heater
And vacuum extractor, heater include burner, burner along the central axis of rotary kiln 5 arrange.It is evenly equipped with burner many
The individual burner noz(zle) for connecting fuel-device, air blast of the burner near second decompression one end of storehouse 4 connection outside rotary kiln 5
Machine.Vacuum extractor includes check valve, exhaustor and vacuum pump, and exhaustor is arranged in rotary kiln 5, and exhaustor is located at turn around kiln
5 central axis top and with the centerline axis parallel of rotary kiln 5.Check valve be uniformly arranged on exhaustor and check valve from outside to inside
Conducting, vacuum pump is located at turn around outside kiln 5 and connects with exhaustor.The outlet side connection preheater 2 of vacuum pump.
Rotary kiln 5 is followed successively by from the inside to the outside shell, external thermal insulation, intermediate interlayer, inner thermal insulating layer and inner shell, burner combustion
Device arranges intermediate interlayer temperature at 820 DEG C near the 3rd decompression one end of storehouse 6 connection intermediate interlayer, and pressure is 3E5Pa；Revolution
Intermediate interlayer of the intermediate interlayer of kiln 5 near second the second decompression of decompression one end of storehouse 4 connection storehouse 4.Produce here with burning
Flue gas carries out post bake to rotary kiln 5, it is ensured that the temperature of rotary kiln 5 is uniform so that decomposition of limestone is uniform, and reduces
The loss of fuel.
The intermediate interlayer of rotary kiln 5 near second decompression one end of storehouse 4 sequentially pass through the intermediate interlayer in the second decompression storehouse 4, the
Preheater 2 is connected after the intermediate interlayer in one decompression storehouse 3.Limestone powder after preheating is subtracting through the first decompression storehouse 3 and second
Can there is the situation of temperature drop behind pressure storehouse 4, not reach the due effect of preheating, and flue gas be discharged by burner and is subtracted to first
Pressure storehouse 3 and second decompression storehouse 4 is heated, and can form soak layer on the first decompression storehouse 3 and second decompression storehouse 4, most
Reduce or cause the limestone powder after preheating not exist behind the first decompression storehouse 3 and second decompression storehouse 4 in big degree
The problem of thermal losses.Burner can be made full use of simultaneously to discharge the preheating of flue gas, reduce thermal losses.
High-temperature lime is sequentially sent to the 3rd decompression storehouse the 6, the 4th decompression storehouse 7 and cooling chamber by cooling treatment, rotary kiln 5, is returned
Rotary kiln 5 is sent into the 3rd decompression storehouse 6 with its equipressure by high-temperature lime, and the 3rd decompression storehouse 6 is filled up after high-temperature lime and closed and revolution
The passage of kiln 5, and high-temperature lime is sent into into the 4th decompression storehouse 7.4th decompression storehouse 7 is filled up after high-temperature lime and is closed and the 3rd decompression storehouse
6 passages, and high-temperature lime feeding cooling chamber is carried out into cold front heavy rain.Finally obtain the Calx that activity degree is 376ml.
3rd decompression storehouse 6 be located at directly over the 4th decompression storehouse 7 and between connection valve is set, the 4th decompression storehouse 7 is more than the
Three decompression storehouses 6, a quarter of the connection valve diameter not less than the 4th decompression diameter of storehouse 7.So arranging can
So that the limestone powder in the 3rd decompression storehouse 6 rapidly enters the 4th decompression storehouse 7, and the 4th decompression volume of storehouse 7 more greatly can be with
It is convenient to house the limestone powder that the 3rd decompression storehouse 6 falls；Reduce by the 3rd decompression evacuation operation of storehouse 6.3rd decompression storehouse 6 it is upper
End is provided with the vacuum pump for evacuation.3rd decompression storehouse 6 is located at turn around the kiln hood lower section of kiln 5.Height so in rotary kiln 5
Fire stons ash can be fallen directly in the 3rd decompression storehouse 6, convenient and swift, reduce unnecessary conveying arrangement.
Realize that raw limestone, to the conveying of rotary kiln 5, its role is to pass through by multi-step pressure reduction storehouse in such scheme
Multi-step pressure reduction is adjusted, and raw limestone is sent into the impact reduced during rotary kiln 5 to rotary kiln 5 so as to keep for a long time
Under the vacuum state for needing, to realize continuous production.In prior art, although also have and calcine in a vacuum, but its
It is more to be to maintain segment section for vacuum state, such as kiln hood；Or it is fixed to change vacuum, feeds intake to be required for opening again every time and forge
The stove of burning；The unnecessary energy is so not only expended, and is intermittent production, it does not have continuous production, Zhi Nengshi
Close the generation demand of small lot.Simultaneously it will be appreciated that large-scale its volume of rotary kiln 5 is very huge, its evacuation is extremely to consume energy
, so that saving the energy loss of each step.
Described above is the detailed description for the present invention preferably possible embodiments, but embodiment is not limited to this
Bright patent claim, the equal change completed under the technical spirit suggested by all present invention or modification change, all should belong to
Cover the scope of the claims in the present invention.
Claims (9)
1. a kind of active lime production method, it is characterised in that comprise the following steps：
Pretreatment, will collect limestone raw ore and sequentially passes through broken, and cleaning is desilted, and staged care obtains granule size for 40-
The limestone powder of 50mm, sends limestone powder into feed bin storage；
The pre-heat treatment, by the limestone powder in feed bin preheater, the first decompression storehouse and the second decompression storehouse are sequentially sent to, described pre-
Limestone powder surface and internal temperature is heated to 850 ± 10 DEG C and sends into the first decompression storehouse by hot device, and the first decompression storehouse is filled up
Close with preheater interface channel after limestone powder and carry out being evacuated to 1E0~1E2pa；Make in evacuation in the first decompression storehouse
Limestone powder whole is sent into into the second decompression storehouse after the completion of industry；Second decompression storehouse is closed with the first decompression warehouse channel and is taken out
Vacuum is to 1E-1~1E-2pa；
Limestone powder is sent in the rotary kiln isobaric with the second decompression storehouse and is calcined in calcination processing, the second decompression storehouse
Process, obtain high-temperature lime, calcining heat is 850-950 DEG C, and calcination time is 90-140min；
High-temperature lime is sequentially sent to the 3rd decompression storehouse, the 4th decompression storehouse and cooling chamber, the institute by cooling treatment, the rotary kiln
Rotary kiln is stated by high-temperature lime feeding and the 3rd decompression storehouse of its equipressure, the 3rd decompression storehouse is filled up after high-temperature lime and closes and turn round
Kiln passage, and high-temperature lime is sent into into the 4th decompression storehouse；4th decompression storehouse is filled up after high-temperature lime to close and is led to the 3rd decompression storehouse
Road, and high-temperature lime feeding cooling chamber is carried out into cold front heavy rain；
Kiln tail in the rotary kiln is subtracted by the second decompression of the first valve connection storehouse, its kiln hood by the second valve connection the 3rd
Pressure storehouse；Rotary kiln is provided with heater and vacuum extractor, and the heater includes burner, and the burner is along revolution
Kiln central axis is arranged；Multiple burner noz(zle)s for connecting fuel-device are evenly equipped with burner, burner subtracts near second
Aerator of pressure storehouse one end connection outside rotary kiln, burner is near the 3rd decompression storehouse one end connection preheater；It is described to take out true
Empty device includes check valve, exhaustor and vacuum pump, and the exhaustor is arranged in rotary kiln, and exhaustor is located at turn around kiln center
Axis top and with rotary kiln centerline axis parallel；The check valve is uniformly arranged on exhaustor and check valve is led from outside to inside
Logical, the vacuum pump is located at turn around outside kiln and connects with exhaustor；The outlet side connection preheater of the vacuum pump.
2. a kind of active lime production method according to claim 1, it is characterised in that：The preheater is connected with useless
Flash Gas Compression Skid System.
3. a kind of active lime production method according to claim 1, it is characterised in that：The rotary kiln is from the inside to the outside
Shell, external thermal insulation, intermediate interlayer, inner thermal insulating layer and inner shell are followed successively by, the burner combustion device is near the 3rd decompression storehouse one
End connection intermediate interlayer, and intermediate interlayer temperature is set at 800-850 DEG C, pressure is 3E5-6E5pa；The centre of the rotary kiln
Interlayer is near second decompression storehouse one end connection preheater.
4. a kind of active lime production method according to claim 1, it is characterised in that：It is described first decompression position in storehouse in
Directly over second decompression storehouse and between connection valve is set, the second decompression storehouse is more than the first decompression storehouse, and the connection valve is straight
A quarter of the footpath size not less than the first decompression storehouse diameter.
5. a kind of active lime production method according to claim 1, it is characterised in that：It is described 3rd decompression position in storehouse in
Directly over 4th decompression storehouse and between connection valve is set, the 4th decompression storehouse is more than the 3rd decompression storehouse, and the connection valve is straight
A quarter of the footpath size not less than the 4th decompression storehouse diameter.
6. a kind of active lime production method according to claim 1, it is characterised in that：The second decompression orlop portion
The spiral feeder of rotary kiln is provided with, spiral feeder is just to the first valve.
7. a kind of active lime production method according to claim 1, it is characterised in that：It is described 3rd decompression position in storehouse in
The kiln hood lower section of rotary kiln.
8. a kind of active lime production method according to claim 3, it is characterised in that：The first decompression storehouse and the
Two decompression storehouses include successively from the inside to the outside shell, external thermal insulation, intermediate interlayer and inner shell；The intermediate interlayer of the rotary kiln is leaned on
Nearly second decompression storehouse one end sequentially passes through connection preheating after the intermediate interlayer in the second decompression storehouse, the intermediate interlayer in the first decompression storehouse
Device.
9. a kind of active lime production method according to claim 1, it is characterised in that：The first decompression storehouse, the
The upper end in two decompression storehouses and the 3rd decompression storehouse is mounted on the vacuum pump for evacuation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611236721.8A CN106673463B (en) | 2016-12-28 | 2016-12-28 | A kind of active lime production method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611236721.8A CN106673463B (en) | 2016-12-28 | 2016-12-28 | A kind of active lime production method |
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| Publication Number | Publication Date |
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| CN106673463A true CN106673463A (en) | 2017-05-17 |
| CN106673463B CN106673463B (en) | 2019-05-03 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1830863A (en) * | 2006-03-31 | 2006-09-13 | 河北理工大学 | Method and device of obtaining active lime by vacuum calcining limestone |
| CN101921073A (en) * | 2010-08-31 | 2010-12-22 | 贾会平 | Method and machine for producing lime |
| CN103387347A (en) * | 2013-07-30 | 2013-11-13 | 天津水泥工业设计研究院有限公司 | Method and device for producing active lime powder from calcined limestone |
| CN104496206A (en) * | 2014-06-19 | 2015-04-08 | 谢英健 | Method for preparation of high activity lime from calcite and comprehensive application of product |
-
2016
- 2016-12-28 CN CN201611236721.8A patent/CN106673463B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1830863A (en) * | 2006-03-31 | 2006-09-13 | 河北理工大学 | Method and device of obtaining active lime by vacuum calcining limestone |
| CN101921073A (en) * | 2010-08-31 | 2010-12-22 | 贾会平 | Method and machine for producing lime |
| CN103387347A (en) * | 2013-07-30 | 2013-11-13 | 天津水泥工业设计研究院有限公司 | Method and device for producing active lime powder from calcined limestone |
| CN104496206A (en) * | 2014-06-19 | 2015-04-08 | 谢英健 | Method for preparation of high activity lime from calcite and comprehensive application of product |
Non-Patent Citations (1)
| Title |
|---|
| 宋延辉等: "活性石灰的生产及在冶金中的应用", 《河北理工学院学报》 * |
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| CN106673463B (en) | 2019-05-03 |
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Effective date of registration: 20200713 Address after: 537811 Xinrong Village, Kuiyang Town, Xingye County, Yulin City, Guangxi Zhuang Autonomous Region Patentee after: Xingye Chenggang calcium comprehensive utilization Co., Ltd Address before: 545001, No. 1, No. 1-20, hang long Plaza, 20 North Bird Road, Liu Bei District, the Guangxi Zhuang Autonomous Region, Liuzhou Patentee before: LIUZHOU CHANGQUAN TRADE Co.,Ltd. |