CN112209392A - A deacidification stove for producing fumed silica - Google Patents
A deacidification stove for producing fumed silica Download PDFInfo
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- CN112209392A CN112209392A CN202011172872.8A CN202011172872A CN112209392A CN 112209392 A CN112209392 A CN 112209392A CN 202011172872 A CN202011172872 A CN 202011172872A CN 112209392 A CN112209392 A CN 112209392A
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- fumed silica
- rotary kiln
- tail gas
- heating
- kiln cylinder
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
- C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
- C01B33/18—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof
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- Inorganic Chemistry (AREA)
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- Muffle Furnaces And Rotary Kilns (AREA)
Abstract
The invention discloses a deacidification furnace for producing fumed silica, which comprises a fumed silica feeding pipeline, a heating section shell, a rotary kiln cylinder, a fumed silica collector, a heating burner and a process burner, wherein the fumed silica collector is designed at the tail of the rotary kiln cylinder, the middle lower section of the fumed silica collector is connected with high-temperature airflow of the burner, the high-temperature airflow enters the tangential direction of the fumed silica collector, the materials in the fumed silica collector are stirred and fluidized, then the high-temperature airflow enters the rotary kiln cylinder from the tail of the rotary kiln cylinder and passes through the rotary kiln cylinder, and the fumed silica stirred in the rotary kiln cylinder is contacted with the high-temperature airflow to heat the materials and remove hydrogen chloride and chlorine on the surface of the fumed silica. The device has the advantages of simple structure, simplified operation, improved deacidification capacity, high heat utilization rate, improved productivity, reduced power consumption, improved product qualification rate, improved work efficiency, and good popularization and application value.
Description
Technical Field
The invention relates to a fumed silica production device, in particular to a deacidification furnace for producing fumed silica.
Background
The fumed silica is one of the most important nano-scale inorganic raw materials, and has the characteristics of large specific surface area, strong surface adsorption, large surface energy, high chemical purity, good dispersion performance, thermal resistance, electric resistance and the like due to small particle size, excellent stability, reinforcement, thickening property and thixotropy, unique characteristics in various subjects and fields and irreplaceable effect. In the prior art, processing equipment for fumed silica is generally of a multi-stage series vertical cylindrical fluidized bed structure, a single horizontal fluidized bed structure is provided individually, the outer wall of the fluidized bed is mostly in an electric heating heat supply mode, the multi-stage vertical fluidized bed has more equipment, the operation is complex, and the capacity of a device with poor deacidification capability is small; the multistage vertical fluidized bed needs additional conveying power for materials to enter and exit the fluidized bed for multiple times, so that the tail gas load of a production device is increased, and the energy consumption for production is higher due to repeated heating for the materials to enter and exit; the horizontal fluidized bed has high energy consumption and gas consumption when the device is used for producing small energy, and has small operation elasticity and is not economical; because the horizontal fluidized bed is of a cuboid structure, the wall surface of the box body is easy to deform when electric heating is used, and thicker materials are needed for preventing equipment from deforming, so that the equipment investment is increased; the horizontal fluidized bed needs larger deacidification air and steam to meet the basic requirement of maintaining the bed height of the fluidized bed, and if the gas velocity is low, the fluidized bed has the abnormal local bed collapse accumulation, so that the product quality is unqualified.
Disclosure of Invention
The invention aims to provide a deacidification furnace for producing fumed silica.
In order to achieve the purpose, the invention is implemented according to the following technical scheme:
the invention comprises a fumed silica feeding pipeline, a heating section shell, a rotary kiln cylinder, a fumed silica collector, a heating burner and a process burner, wherein the outer shell is arranged outside the fumed silica feeding pipeline, the outer shell of the fumed silica feeding pipeline is in rotary sealing connection with one end of the rotary kiln cylinder through a process section sealing rotating shaft, the heating section shell is arranged at the periphery of the rotary kiln cylinder, the two ends of the heating section shell are in rotary sealing connection with the rotary kiln cylinder through the heating section sealing rotating shaft, the other end of the rotary kiln cylinder is in rotary sealing connection with the fumed silica collector through the process section sealing rotating shaft, the lower end of the heating section shell is connected with the heating burner, the upper end of the heating section shell is provided with a heating tail gas outlet, one side of the fumed silica collector is provided with the process burner, and a tail gas outlet is formed in the shell outside the fumed silica feeding pipeline, a gear ring is arranged on the excircle of one end of the rotary kiln cylinder, and the rotary kiln cylinder is connected with a driving device through the gear ring to rotate.
As an improvement, the tail gas discharge port is provided with a tail gas separation treatment device.
Specifically, the tail gas separation treatment device comprises a tail gas cyclone separator, a reclaimed material unloader and a process tail gas pipe, wherein one end of the process tail gas pipe is connected with the tail gas discharge port, the other end of the process tail gas pipe is connected with an air inlet of the tail gas cyclone separator, the upper end of the tail gas cyclone separator is a process tail gas outlet, the lower end of the tail gas cyclone separator is provided with the reclaimed material unloader, and an outlet of the reclaimed material unloader is connected into the rotary kiln cylinder through a pipeline.
Preferably, a heating section guide plate is arranged on the inner wall of the heating section shell. And the inner wall of the rotary kiln barrel is provided with a barrel internal spiral belt.
Preferably, rolling rings are arranged at two ends of the rotary kiln cylinder body and are positioned on the support.
Further, the lower end of the fumed silica collector is connected with one end of a product unloading machine, and the other end of the product unloading machine is a fumed silica outlet.
Specifically, be provided with heating combustor primary air and heating combustor secondary air on the heating combustor, the inlet end access of heating combustor fuel gas. The process burner is provided with secondary air of the process burner and primary air of the process burner, and the air inlet end of the process burner is connected with fuel gas of the process burner.
Preferably, the process section sealing rotating shaft and the heating section sealing rotating shaft are both provided with a sealing air inlet.
The invention has the beneficial effects that:
the device has the advantages of simple structure, simplified operation and improved deacidification capacity, and has high heat utilization rate, capacity of improving the capacity, reduced power consumption, improved product qualification rate and improved working efficiency, and has popularization and application values.
Drawings
FIG. 1 is a schematic structural view of the present invention;
fig. 2 is a partially enlarged view of a portion a in fig. 1.
Detailed Description
The invention will be further described with reference to the drawings and specific embodiments, which are illustrative of the invention and are not to be construed as limiting the invention.
As shown in fig. 1: the invention comprises a fumed silica feeding pipeline 6, a heating section shell 7, a rotary kiln cylinder 8, a fumed silica collector 11, a heating burner 13 and a process burner 14, wherein the outer shell is arranged outside the fumed silica feeding pipeline 6, the outer shell of the fumed silica feeding pipeline 6 is in rotary sealing connection with one end of the rotary kiln cylinder 8 through a process section sealing rotating shaft 4, the heating section shell 7 is arranged at the periphery of the rotary kiln cylinder 8, the connection part of the two ends of the heating section shell 7 and the rotary kiln cylinder 8 is in rotary sealing connection through a heating section sealing rotating shaft 5, the other end of the rotary kiln cylinder 8 is in rotary sealing connection with the fumed silica collector 11 through the process section sealing rotating shaft 4, the lower end of the heating section shell 7 is connected with the heating burner 13, the upper end of the heating section shell 7 is provided with a heating tail gas outlet 26, the process burner 14 is arranged on one side of the fumed silica collector 11, a tail gas discharge port is formed in the shell outside the fumed silica feeding pipeline 6, a gear ring 16 is arranged on the excircle of one end of the rotary kiln cylinder 8, and the rotary kiln cylinder 8 is connected with a driving device through the gear ring 16 to rotate.
The deacidification furnace is of a rotary kiln type structure, the bed body is kept to rotate by external force, the gas and the materials can be kept to be fully contacted under any yield, the product quality cannot be influenced due to capacity change, high-temperature airflow and fumed silica move in a countercurrent mode in the kiln, the fumed silica moves from the head to the tail of the kiln, and the high-temperature airflow moves from the tail to the head of the kiln after passing through the fumed silica collector.
A fumed silica collector is arranged at the tail of a rotary kiln cylinder body 8, high-temperature airflow of a burner is connected to the middle lower section of the fumed silica collector, the high-temperature airflow enters the fumed silica collector in the tangential direction, materials in the fumed silica collector are stirred and fluidized, then the high-temperature airflow enters the rotary kiln cylinder body from the tail of the rotary kiln cylinder body and penetrates through the rotary kiln cylinder body, the fumed silica stirred in the rotary kiln cylinder body is contacted with the high-temperature airflow, and the materials are heated and hydrogen chloride and chlorine on the surface of the fumed silica are removed.
As an improvement, the tail gas discharge port is provided with a tail gas separation treatment device.
Specifically, the tail gas separation treatment device comprises a tail gas cyclone separator 1, a reclaimed material unloading machine 2 and a process tail gas pipe 3, wherein one end of the process tail gas pipe 3 is connected with the tail gas outlet, the other end of the process tail gas pipe 3 is connected with the gas inlet of the tail gas cyclone separator 1, the upper end of the tail gas cyclone separator 1 is a process tail gas outlet 18, the reclaimed material unloading machine 2 is arranged at the lower end of the tail gas cyclone separator 1, and the outlet of the reclaimed material unloading machine 2 is connected in the rotary kiln cylinder 8 through a pipeline.
A gas-phase white carbon black semi-finished product feeding hole and a tail gas outlet are designed at the 8 ends of the rotary kiln barrel, white carbon black is separated from the tail gas of the deacidification furnace through a tail gas cyclone separator and is returned to the rotary kiln barrel 8 by a reclaimed material unloading machine, and the tail gas of the tail gas cyclone separator enters a tail gas system or a separation system of the gas-phase white carbon black production device.
Preferably, a heating section flow guide plate 10 is arranged on the inner wall of the heating section shell 7. And the inner wall of the rotary kiln cylinder body 8 is provided with a cylinder body inner spiral belt 9.
The rotary kiln body of the deacidification furnace is internally and externally heated in a bidirectional mode, a fixed heating section shell is designed on the outer side of a rotary kiln cylinder, a heating section guide plate is designed in the heating section shell, and hot gas generated by a combustion engine is in countercurrent with the direction of materials in the rotary kiln cylinder under the action of the heating section guide plate and rotates around the rotary kiln cylinder to be heated. The inner wall of the rotary kiln cylinder 8 is provided with a cylinder inner screw belt, the cylinder inner screw belt can turn over the gaseous phase white carbon black in the kiln along with the rotation of the kiln body and can move to the kiln tail along the spiral direction.
Preferably, rolling rings 15 are arranged at two ends of the rotary kiln cylinder 8, and the rolling rings 15 are positioned on the support.
The rotary kiln comprises a rotary kiln barrel body, wherein rolling rings are arranged at two ends of the rotary kiln barrel body and fixed with the rotary kiln barrel body, the rolling rings are placed on two groups of rolling wheels, the rolling wheels are arranged on a support and can roll freely, a gear ring is arranged in front of the rolling rings and connected with a gear of a speed reducer, and the speed reducer can rotate the rotary kiln barrel body at a certain speed through the gear ring.
Further, the lower end of the fumed silica collector 11 is connected with one end of the product unloader 12, the other end of the product unloader 12 is a fumed silica outlet 19, and the material layer height in the fumed silica collector is controlled by the rotating speed of the product unloader.
Specifically, the heating burner 13 is provided with heating burner primary air 23 and heating burner secondary air 25, and the air inlet end of the heating burner 13 is connected to heating burner fuel gas 21. The process combustor 14 is provided with process combustor secondary air 24 and process combustor primary air 22, and the air inlet end of the process combustor 14 is connected with process combustor fuel gas 20.
The heating burner and the process burner are both provided with a fuel inlet, a primary air inlet and a secondary air inlet, natural gas or hydrogen is used as fuel, primary air is combustion air, the temperature of high-temperature airflow is adjusted by adjusting the consumption of the fuel and the primary air, and the flow rate of the high-temperature airflow in the kiln is adjusted by adjusting the secondary air.
Preferably, the process section seal rotating shaft 4 and the heating section seal rotating shaft 5 are both provided with a seal air inlet 27.
A process section sealing rotating shaft is designed at the kiln head and the kiln tail of the rotary kiln cylinder body 8, the process section sealing rotating shaft adopts two mixed sealing structures of a labyrinth and a packing, the packing is sealed at the side close to the atmosphere, a hot air interface is also designed between the labyrinth seal and the packing seal, and hot air is introduced to block the leakage of hydrogen chloride and chlorine, as shown in figure 2.
A heating section sealing rotating shaft is arranged between the outer wall of the rotary kiln barrel and the heating section shell, the heating section sealing adopts a labyrinth and packing mixed sealing structure, the packing is sealed on the side close to the atmosphere, a normal-temperature air interface is designed between the labyrinth and the packing, and normal-temperature air is introduced to prevent hot air in the heating section from spraying out to hurt people.
Example (b):
the yield of the fumed silica treated by the deacidification furnace is 500 to 10000 tons per year, and the specific surface area of the fumed silica can be 30 to 450 square meters per gram.
The diameter of the rotary kiln cylinder of the deacidification furnace is as follows: 800mm to 2000mm, the length-diameter ratio of 6:1 to 30:1, the height of an internal spiral belt of 30 to 300mm, the diameter of a fumed silica collector of 1200 to 3000mm, the height of 2400 to 5000mm, and the diameter of a heating section shell of the deacidification furnace: 810-2600 mm.
The diameter of a feed inlet of the deacidification furnace is 100-400 mm, the diameter of a discharge outlet of the deacidification furnace is 200-500 mm, the diameter of a tail gas pipe is 200-400 mm, the diameter of a shell of a tail gas cyclone separator is 400-1000 mm, the height of a cylinder of the cyclone separator is 600-2500 mm, and the diameter of a recycling unloader of the cyclone separator is 150-350 mm.
The process section seal and the heating section seal of the deacidification furnace are sealed by 5 labyrinth seals and 1 graphite packing.
The rotating speed of the rotary kiln cylinder of the deacidification furnace is 0.5-5 r/min.
The gradient of the rotary kiln of the deacidification furnace is 0-3.5%.
The heating burner natural gas flow of the rotary kiln of the invention is as follows: 10 to 50Nm3H, primary air flow rate: 100 to 750Nm30-750 Nm secondary air3/h。
The natural gas flow of the process burner of the rotary kiln is 25-150 Nm3H, primary air flow rate: 250 to 2000Nm30-2000 Nm of secondary air3/h。
When the deacidification furnace is in full load, the PH value of the fumed silica aqueous dispersion with the specific surface area of 150 square meters per gram is more than or equal to 4.30;
when the deacidification furnace is in full load, the PH value of the fumed silica aqueous dispersion with the specific surface area of 200 square meters per gram is more than or equal to 4.20;
when the deacidification furnace is in full load, the PH value of the fumed silica aqueous dispersion with the specific surface area of 300 square meters per gram is more than or equal to 4.15;
the PH value of the fumed silica aqueous dispersion with the specific surface area of 380 square meters per gram is more than or equal to 4.10 when the deacidification furnace is fully loaded.
The technical solution of the present invention is not limited to the limitations of the above specific embodiments, and all technical modifications made according to the technical solution of the present invention fall within the protection scope of the present invention.
Claims (10)
1. The utility model provides a deacidification stove for producing fumed silica which characterized in that: comprises a fumed silica feeding pipeline (6), a heating section shell (7), a rotary kiln cylinder body (8), a fumed silica collector (11), a heating burner (13) and a process burner (14), wherein the outer shell is arranged outside the fumed silica feeding pipeline (6), the outer shell of the fumed silica feeding pipeline (6) is in rotary seal connection with one end of the rotary kiln cylinder body (8) through a process section sealing rotating shaft (4), the heating section shell (7) is arranged at the periphery of the rotary kiln cylinder body (8), the two ends of the heating section shell (7) and the joint of the rotary kiln cylinder body (8) are in rotary seal connection through a heating section sealing rotating shaft (5), the other end of the rotary kiln cylinder body (8) is in rotary seal connection with the fumed silica collector (11) through the process section sealing rotating shaft (4), the lower extreme of heating section casing (7) is connected heating combustor (13), the upper end of heating section casing (7) is provided with heating tail gas export (26), one side of fumed silica aggregate ware (11) sets up technology combustor (14), the installation be provided with the tail gas discharge port on the outer casing of fumed silica charge-in pipeline (6), be provided with ring gear (16) on the one end excircle of rotary kiln barrel (8), rotary kiln barrel (8) are passed through drive arrangement is connected in ring gear (16) and is rotated.
2. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: and the tail gas discharge port is provided with a tail gas separation treatment device.
3. The deacidification furnace for producing fumed silica according to claim 2, characterized in that: the tail gas separation treatment device is composed of a tail gas cyclone separator (1), a reclaimed material unloading machine (2) and a process tail gas pipe (3), one end of the process tail gas pipe (3) is connected with a tail gas discharge port, the other end of the process tail gas pipe (3) is connected with a gas inlet of the tail gas cyclone separator (1), the upper end of the tail gas cyclone separator (1) is a process tail gas outlet (18), the lower end of the tail gas cyclone separator (1) is provided with the reclaimed material unloading machine (2), and an outlet of the reclaimed material unloading machine (2) is connected into the rotary kiln cylinder body (8) through a pipeline.
4. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: and a heating section guide plate (10) is arranged on the inner wall of the heating section shell (7).
5. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: and an inner barrel spiral belt (9) is arranged on the inner wall of the rotary kiln barrel (8).
6. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: and rolling rings (15) are arranged at two ends of the rotary kiln cylinder (8), and the rolling rings (15) are positioned on the support.
7. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: the lower end of the fumed silica collector (11) is connected with one end of a product unloader (12), and the other end of the product unloader (12) is a fumed silica outlet (19).
8. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: the heating burner (13) is provided with primary air (23) and secondary air (25) of the heating burner, and the air inlet end of the heating burner (13) is connected with fuel gas (21) of the heating burner.
9. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: the process combustor (14) is provided with process combustor secondary air (24) and process combustor primary air (22), and the air inlet end of the process combustor (14) is connected with process combustor fuel gas (20).
10. The deacidification furnace for producing fumed silica according to claim 1, characterized in that: and the process section sealing rotating shaft (4) and the heating section sealing rotating shaft (5) are both provided with a sealing air inlet (27).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011172872.8A CN112209392A (en) | 2020-10-28 | 2020-10-28 | A deacidification stove for producing fumed silica |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011172872.8A CN112209392A (en) | 2020-10-28 | 2020-10-28 | A deacidification stove for producing fumed silica |
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| Publication Number | Publication Date |
|---|---|
| CN112209392A true CN112209392A (en) | 2021-01-12 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202011172872.8A Withdrawn CN112209392A (en) | 2020-10-28 | 2020-10-28 | A deacidification stove for producing fumed silica |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116081631A (en) * | 2022-12-30 | 2023-05-09 | 浙江工程设计有限公司 | Deacidification method for gas-phase white carbon black |
-
2020
- 2020-10-28 CN CN202011172872.8A patent/CN112209392A/en not_active Withdrawn
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116081631A (en) * | 2022-12-30 | 2023-05-09 | 浙江工程设计有限公司 | Deacidification method for gas-phase white carbon black |
| CN116081631B (en) * | 2022-12-30 | 2024-05-31 | 浙江工程设计有限公司 | Deacidification method for gas-phase white carbon black |
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Application publication date: 20210112 |
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| WW01 | Invention patent application withdrawn after publication |