CN207881502U - Powder dynamic calcining system - Google Patents
Powder dynamic calcining system Download PDFInfo
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- CN207881502U CN207881502U CN201820182027.0U CN201820182027U CN207881502U CN 207881502 U CN207881502 U CN 207881502U CN 201820182027 U CN201820182027 U CN 201820182027U CN 207881502 U CN207881502 U CN 207881502U
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- 238000001354 calcination Methods 0.000 title claims abstract description 56
- 239000000843 powder Substances 0.000 title claims abstract description 27
- 239000000463 material Substances 0.000 claims abstract description 59
- 239000007789 gas Substances 0.000 claims abstract description 39
- 238000001816 cooling Methods 0.000 claims abstract description 27
- 239000011229 interlayer Substances 0.000 claims abstract description 20
- 238000001035 drying Methods 0.000 claims abstract description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 24
- 239000003546 flue gas Substances 0.000 claims description 24
- 239000000498 cooling water Substances 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 8
- 238000012545 processing Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000000203 mixture Substances 0.000 abstract description 3
- 239000002245 particle Substances 0.000 abstract description 3
- 239000003517 fume Substances 0.000 abstract 1
- 238000000034 method Methods 0.000 description 9
- 239000012530 fluid Substances 0.000 description 8
- 239000002893 slag Substances 0.000 description 5
- 235000019738 Limestone Nutrition 0.000 description 4
- 239000006028 limestone Substances 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000010410 layer Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000012937 correction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- JQJCSZOEVBFDKO-UHFFFAOYSA-N lead zinc Chemical compound [Zn].[Pb] JQJCSZOEVBFDKO-UHFFFAOYSA-N 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Landscapes
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
The utility model provides a kind of powder dynamic calcining system, including drying unit, blanking unit, Geldart-D particle unit, calcine unit, cooling unit, and material collection and fume treatment unit, blanking unit includes feed bin, the rotary feeder and venturi loader of frequency control, Geldart-D particle unit is arranged to provide the conveying gas that high temperature compressed air and superheated vapour arbitrary proportion mix to venturi loader, it includes inner cylinder to calcine unit, upper interlayer, spiral flow deflector is provided in inner cylinder, upper interlayer is configured to have lower hot wind inlet and upper hot-blast outlet and for transmitting the source space of heat to dried material in inner cylinder.The utility model has the characteristics that ensure product purity, the conveying of precise and stable material, high operation ratio and low comprehensive energy consumption.
Description
The technical field is as follows:
the utility model relates to a powder calcines technical field, in particular to powder developments system of calcining.
Background art:
the calcination is used for the technological processes of purification, decomposition, reduction and modification. The small materials produced in the mining process and the slag produced in the production process, such as slag after lead-zinc ore flotation, carbide slag produced by a carbide furnace, ammonium sulfate slag produced during secondary utilization of phosphogypsum produced during phosphoric acid production and the like, can not be used for calcination in the traditional process because the particle size of the materials cannot meet the requirement, can only be used for paving roads, and a small part of the materials are used for cement calcination, so that the great resource waste exists. The dynamic calcination of the powder is widely applied to the fields of metallurgy, chemical industry, mining and the like, is also a novel treatment mode for recycling the solid waste of the powder slag, and has wide prospect and market. The dynamic calcination of the powder relates to a plurality of fields of materials, heat transfer, mass transfer and fluid, and realizes the resource recycling by the calcination of the powder, thereby reducing the burden of the environment.
Compared with the traditional block calcination mode, the powder dynamic calcination method has the advantages of short calcination time, large heat exchange coefficient, high product quality and the like, but has close relation with material conveying, calcination temperature, material-gas ratio, conveying gas components, device structure and the like. The calcination time of the powder is in the second level, how to accurately control each process parameter, reduce the comprehensive energy consumption, avoid the over-burning of the product, ensure the purity of the finished product and the equipment operation rate, and is the difficult point of the current powder dynamic calcination industry.
The utility model has the following contents:
in order to solve the above problems, the utility model provides a powder dynamic calcining system which helps to ensure the product purity, accurately stabilize the material transportation, has high operation rate and low comprehensive energy consumption.
Therefore, the utility model provides a powder developments system of calcining, it includes drying unit, the unloading unit, the pneumatic conveyor unit, calcine the unit, the cooling unit, and material collection and flue gas processing unit, the unloading unit includes the feed bin that receives dry material from drying unit, top-down installs the rotatory feeder and the venturi feeder of frequency conversion control below the feed bin, the pneumatic conveyor unit sets up to provide the conveying gas that high temperature compressed air and superheated steam mix in arbitrary proportion to the venturi feeder so that this conveying gas can send the dry material that comes out from the venturi feeder into and calcine the unit, it includes the inner tube that is used for the tangential receipt by the dry material of conveying gas transport to calcine the unit, be located the upper interlayer outside the inner tube, wherein, a spiral flow deflector is arranged in the inner cylinder, and the upper interlayer is a heat source space which is provided with a lower hot air inlet and an upper hot air outlet and is used for transferring heat to the drying material in the inner cylinder.
In the utility model, because the heat source (namely hot air) in the heat source space is not in direct contact with the material in the inner cylinder during drying and calcining, the product is ensured not to be polluted by the heat source, is suitable for fine processing of the product and is helpful for ensuring the purity of the product; the superheated gas is used as a gas source, the injection capacity of the venturi feeder is increased, the powder supply stability of the combined feeder of the rotary feeder and the venturi feeder is further ensured, the gas-material ratio and the calcination time can be changed by changing the flow rate and the blanking amount of the gas source, and overburning is avoided; the material is tangentially conveyed into the calcining space (namely the inner cylinder) by the conveying gas, and the spiral flow deflector is arranged in the inner cylinder, so that compared with a straight tube type calcining space, the structure can reduce the occupied calcining space resources to a great extent (because the spiral flow deflector lengthens the calcining path, the calcining space can be reduced), and meanwhile, the gas-solid two-phase flow formed by the material and the conveying gas flows in the inner cylinder to greatly damage a boundary layer, thereby enhancing the heat exchange effect,the energy consumption is reduced, and simultaneously, the overburning is avoided; the pneumatic transmission can select air sources with different atmospheres (different atmospheres refer to different proportions of compressed air and steam) according to requirements, for example, superheated steam is selected as a carrier in the limestone calcining process, the decomposition temperature of limestone can be reduced, the aim of catalysis is fulfilled, and when materials in an inner cylinder of a calcining unit are decomposed to generate CO2And CaO finished product, wherein the gas in the inner cylinder is CO2And steam, for extracting high purity CO2The difficulty is reduced, and a product with extremely high added value is produced; because the utility model discloses the feed is stable, heat exchange efficiency is high and do not have the overburning to the probability greatly reduced that the system shut down the correction makes entire system have high operating rate.
Further, the pneumatic conveying unit comprises a compressed air tank, a steam generator, a gas heater and a conveying gas pipeline, wherein the venturi feeder is communicated with the conveying gas pipeline at the inlet end of the venturi feeder, is communicated with the inner cylinder at the outlet end of the venturi feeder through a feeding pipeline, and the part of the feeding pipeline, which is connected with the inner cylinder, is arranged to be tangent to the inner cylinder and has a downward inclination angle of 5-10 degrees in the height direction.
Further, the drying unit comprises a hopper, a dryer which is communicated with the hopper and is provided with a heat exchange pipeline, and a chute, wherein one end of the chute is communicated with the dryer, and the other end of the chute is communicated with the storage bin.
Through the arrangement of the structure, the raw materials which are not dried can enter the bin of the discharging unit through the hopper, the dryer and the chute in sequence.
Further, the cooling unit comprises a lower interlayer positioned at the outer side of the bottom of the inner cylinder, and a lower cooling air inlet and an upper cooling air outlet which are connected with the lower interlayer.
Through the structure, external cooling air can enter the lower interlayer through the lower cooling air inlet, and the calcined material in the inner cylinder is cooled and then discharged through the upper cooling air outlet.
Further, the material collecting and flue gas processing unit comprises a cyclone communicated with the inner cylinder, a finished product ash hopper communicated with the cyclone, a flue gas pipeline communicated with the cyclone and penetrating through a shell-and-tube heat exchanger with a cooling water inlet and a cooling water outlet, and a bag-type dust collector communicated with the flue gas pipeline, wherein a cold air valve is further arranged on the flue gas pipeline to control the temperature of discharged smoke.
Through the structure, calcined materials enter the cyclone to complete the collection of powdery materials, the powdery materials enter the finished product ash hopper after being collected, flue gas enters the shell-and-tube heat exchanger to be cooled by cooling water, the opening degree of the cold air valve is adjusted to control the exhaust temperature, and finally the flue gas is discharged to the atmosphere after passing through the bag-type dust collector.
These and other aspects of the invention will be apparent from and elucidated with reference to the embodiments described hereinafter.
Description of the drawings:
the structure of the invention, together with further objects and advantages thereof, will best be understood from the following description taken in conjunction with the accompanying drawings, in which like reference characters identify like elements:
FIG. 1 is a schematic diagram of a powder dynamic calcination system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of the calcining unit and the cooling unit of the dynamic powder calcining system shown in FIG. 1;
fig. 3 is a schematic diagram of a part of the structure of a blanking unit of the powder dynamic calcining system shown in fig. 1.
The specific implementation mode is as follows:
the following description of the embodiments of the present invention will be made with reference to the accompanying drawings.
As shown in fig. 1 to 3, the dynamic powder calcining system according to an embodiment of the present invention includes a drying unit 100, a blanking unit 200, a pneumatic conveying unit 300, a calcining unit 400, a cooling unit 500, and a material collecting and flue gas processing unit 600. Wherein,
the drying unit 100 comprises a hopper 4, a dryer 102 communicated with the hopper 4 and provided with a heat exchange pipeline 101, and a chute 7, wherein one end of the chute 7 is communicated with the dryer 102, and the other end of the chute is communicated with the blanking unit 200, and the heat exchange pipeline 101 is provided with a hot fluid inlet 5 and a hot fluid outlet 6;
the blanking unit 200 comprises a bin 8 for receiving dry materials from a chute 7 of the drying unit 100, and a rotary feeder 9 and a venturi feeder 10 which are controlled by frequency conversion, wherein the rotary feeder 9 and the venturi feeder 10 are arranged below the bin 8 from top to bottom;
the pneumatic conveying unit 300 is arranged to supply a conveying gas to the venturi feeder 10, the conveying gas being high-temperature compressed air and superheated steam mixed in any proportion, and it is capable of feeding the dry material from the venturi feeder 10 to the calcining unit 400, in this embodiment, the pneumatic conveying unit 300 comprises a compressed air tank 1, a steam generator 2, a gas heater 3, and a conveying gas pipeline 301;
the calcining unit 400 comprises an inner cylinder 13 and an upper interlayer 14 positioned outside the inner cylinder 13, wherein a spiral flow deflector 130 is arranged in the inner cylinder 13, and the upper interlayer 14 is a heat source space which is provided with a lower hot air inlet 15 and an upper hot air outlet 16 and is used for drying the dry materials in the inner cylinder 13;
the venturi feeder 10 in the blanking unit 200 is communicated with the conveying gas pipeline 301 at the inlet end thereof, and is communicated with the inner cylinder 13 at the outlet end thereof through a supply pipeline 302, and a part 11 of the supply pipeline 302, which is connected with the inner cylinder 13, is arranged to be perpendicular to the inner cylinder 13, so that the inner cylinder 13 can switchably receive the dry material conveyed by the conveying gas;
the cooling unit 500 comprises a lower interlayer 17 positioned at the outer side of the bottom of the inner cylinder 13, and a lower cooling air inlet 18 and an upper cooling air outlet 19 which are connected with the lower interlayer 17, and through the structural arrangement, external cooling air can enter the lower interlayer 17 through the lower cooling air inlet 18, cool calcined materials in the inner cylinder 13 and then be discharged through the upper cooling air outlet 19;
the material collecting and flue gas processing unit 600 comprises a cyclone 20 communicated with an inner cylinder 13 through a material collecting pipe 12, a finished product ash hopper 21 communicated with the cyclone 20, a flue gas pipeline 601 communicated with the cyclone 20 and passing through a shell-and-tube heat exchanger 22 with a cooling water inlet 23 and a cooling water outlet 24, and a bag-type dust collector 26 communicated with the flue gas pipeline 601, wherein a cold air valve 25 is further arranged on the flue gas pipeline 601 to control the exhaust gas temperature. Through the structure, calcined materials can enter the cyclone cylinder 20 to complete the collection of the powdery materials, the powdery materials enter the finished product ash hopper 21 after being collected, the flue gas enters the shell-and-tube heat exchanger 22 to be cooled by cooling water, the exhaust temperature is controlled by adjusting the opening degree of the cold air valve 25, and finally the flue gas is exhausted to the atmosphere after passing through the bag-type dust collector.
The following describes a specific process flow for performing dynamic calcination of powder by using the dynamic powder calcination system of the present embodiment with reference to fig. 1 to 3:
1) drying materials: raw materials which are not dried enter a dryer 102 through a hopper 4 in a drying unit 100, a heat exchange pipeline 101 serves as a heat source to dry the raw materials, wherein the heat exchange pipeline 101 is provided with a hot fluid inlet 5 and a hot fluid outlet 6, the hot fluid inlet 5 serves as a heat source inlet, the hot fluid outlet 6 serves as a heat source outlet, and the dried materials enter a bin 8 in a blanking unit 200 through a chute 7;
2) material conveying: the dry materials in the bin 8 enter a venturi feeder 10 through a rotary feeder 9 controlled by frequency conversion, and the materials are sent to the calcining unit 400 through a combined feeder consisting of the rotary feeder 9 and the venturi feeder 10;
3) conveying gas: the compressed air and the water vapor are used as air sources which are communicated with the Venturi feeder 10, namely, the compressed air and the water vapor are used as conveying gas for conveying materials, wherein the compressed air is sourced from the compressed air tank 1, and the water vapor is sourced from saturated water vapor generated by the steam generator 2 and is heated by the gas heater 3 to become superheated water vapor;
4) calcining the materials: the material tangentially enters an inner cylinder 13 in the calcining unit 400 through pneumatic conveying of conveying gas and spirally moves along the wall surface of the inner cylinder 13, wherein a spiral flow deflector 130 is arranged in the inner cylinder 13, an upper interlayer 14 is used as a heat source space, and hot air enters the upper interlayer 14 from a lower hot air inlet 15 and is discharged from an upper hot air outlet 16;
5) cooling materials: the lower interlayer 17 in the cooling unit 500 is used as a material cooling space, and cooling air enters from a lower cooling air inlet 18 and is discharged from an upper cooling air outlet 19;
6) material collection and flue gas treatment: flue gas (namely a mixture of calcined material and conveying gas) from the calcining unit 400 enters a cyclone 20 of a material collecting and flue gas processing unit 600 to complete material collection, the collected material enters a finished product ash hopper 21, the flue gas then enters a shell-and-tube heat exchanger 22, cooling water enters the shell-and-tube heat exchanger 22 through a cooling water inlet 23, then flows out through a cooling water outlet 24 to be used for cooling the flue gas, the exhaust temperature is controlled by adjusting the opening degree of a cold air valve 25, and finally the flue gas is exhausted to the atmosphere after passing through a bag-type dust collector 26.
The utility model discloses advantage and effect lie in following several aspects:
1) during drying, heat source fluid is not contacted with the raw materials in the drying unit, and meanwhile, a heat source (hot air) is not directly contacted with the materials in the inner barrel 13 in the upper interlayer 14 during calcination, so that the product is not polluted by the heat source, the purity of the product is ensured, and the method is suitable for fine processing of the product;
2) the spiral flow deflector 130 is arranged in the calcining space, namely the inner cylinder 13, compared with the calcining space of a straight pipe, the structure can reduce the calcining space to a great extent because the calcining path is lengthened by the spiral flow deflector 130, and meanwhile, the boundary layer is greatly damaged because the gas-solid two-phase flow formed by the material and the conveying gas flows in the pipe, the heat exchange effect is enhanced, and the local over-burning phenomenon is avoided;
3) the air source of different atmospheres can be selected according to the requirements in pneumatic transmission, and the different atmospheres mean that compressed air and steam can be mixed according to different proportions to be used as the air source, for example, superheated steam is selected as a carrier in the limestone calcining process, so that the decomposition temperature of limestone can be reduced, and the aim of catalysis is fulfilled; meanwhile, the smoke in the inner cylinder is CO decomposed from materials2CaO finished products and water vapor, the CaO finished products are subjected to secondary separation through cyclone dust collection and cloth bag dust removal, and the water vapor can be separated out in a condensation mode, so that the extraction of high-purity CO is reduced2The difficulty of (2) can produce extremely high value-added products;
4) the superheated gas is used as the gas source, the injection capacity of the venturi feeder 10 can be increased, the powder supply stability of the combined feeder of the rotary feeder and the venturi feeder is further ensured, and the gas ratio and the calcination time can be changed by changing the flow rate and the blanking amount of the gas source. While the invention has been described with reference to the above embodiments, it will be understood by those skilled in the art that various changes and modifications may be made to the above-described arrangements, including combinations of features disclosed herein either individually or in any combination as is evident from the below disclosure. These variants and/or combinations fall within the technical field of the present invention and are intended to be protected by the following claims.
Claims (5)
1. A dynamic powder calcining system is characterized by comprising a drying unit, a blanking unit, a pneumatic conveying unit, a calcining unit, a cooling unit and a material collecting and smoke processing unit, wherein the blanking unit comprises a bin for receiving dry materials from the drying unit, a frequency-conversion-controlled rotary feeder and a Venturi feeder which are arranged below the bin from top to bottom, the pneumatic conveying unit is arranged to provide conveying gas for the Venturi feeder, the conveying gas is mixed by high-temperature compressed air and superheated water vapor in any proportion, so that the conveying gas can convey the dry materials from the Venturi feeder into the calcining unit, the calcining unit comprises an inner cylinder for tangentially receiving the dry materials conveyed by the conveying gas and an upper interlayer positioned outside the inner cylinder, wherein, a spiral flow deflector is arranged in the inner cylinder, and the upper interlayer is a heat source space which is provided with a lower hot air inlet and an upper hot air outlet and is used for transferring heat to the drying material in the inner cylinder.
2. The dynamic powder calcining system of claim 1, wherein the pneumatic conveying unit comprises a compressed air tank, a steam generator, a gas heater, and a conveying gas pipeline, wherein the venturi feeder is communicated with the conveying gas pipeline at an inlet end thereof, and is communicated with the inner cylinder at an outlet end thereof through a feeding pipeline, and a part of the feeding pipeline connected with the inner cylinder is arranged to be tangent to the inner cylinder and has a downward inclination angle of 5-10 degrees in a height direction.
3. The dynamic powder calcination system of claim 1, wherein the drying unit comprises a hopper, a dryer with a heat exchange pipeline communicated with the hopper, and a chute with one end communicated with the dryer and the other end communicated with the silo.
4. The dynamic powder calcining system as claimed in claim 1, wherein the cooling unit comprises a lower interlayer positioned at the outer side of the bottom of the inner barrel, and a lower cooling air inlet and an upper cooling air outlet connected with the lower interlayer.
5. The dynamic powder calcination system of claim 1, wherein the material collection and flue gas treatment unit comprises a cyclone in communication with the inner cylinder, a finished product ash hopper in communication with the cyclone, a flue gas duct in communication with the cyclone and passing through a shell-and-tube heat exchanger having a cooling water inlet and a cooling water outlet, and a bag-type dust collector in communication with the flue gas duct, wherein a cold air valve is further disposed on the flue gas duct to control the exhaust temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820182027.0U CN207881502U (en) | 2018-02-02 | 2018-02-02 | Powder dynamic calcining system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820182027.0U CN207881502U (en) | 2018-02-02 | 2018-02-02 | Powder dynamic calcining system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207881502U true CN207881502U (en) | 2018-09-18 |
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ID=63510760
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820182027.0U Active CN207881502U (en) | 2018-02-02 | 2018-02-02 | Powder dynamic calcining system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN207881502U (en) |
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2018
- 2018-02-02 CN CN201820182027.0U patent/CN207881502U/en active Active
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