CN111944333B - Continuous fluidized calcining system and method for pearlescent material - Google Patents

Continuous fluidized calcining system and method for pearlescent material Download PDF

Info

Publication number
CN111944333B
CN111944333B CN202010758740.7A CN202010758740A CN111944333B CN 111944333 B CN111944333 B CN 111944333B CN 202010758740 A CN202010758740 A CN 202010758740A CN 111944333 B CN111944333 B CN 111944333B
Authority
CN
China
Prior art keywords
water
fluidized bed
cyclone separator
air
enters
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN202010758740.7A
Other languages
Chinese (zh)
Other versions
CN111944333A (en
Inventor
吕鹏鹏
吴昌梓
朱庆山
邵国强
吴昌锦
吴昌在
吴万里
吴昊
吴俊�
吴万琛
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Ruicai Technology Co ltd
Institute of Process Engineering of CAS
Original Assignee
Ruicai Technology Co ltd
Institute of Process Engineering of CAS
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Ruicai Technology Co ltd, Institute of Process Engineering of CAS filed Critical Ruicai Technology Co ltd
Priority to CN202010758740.7A priority Critical patent/CN111944333B/en
Publication of CN111944333A publication Critical patent/CN111944333A/en
Application granted granted Critical
Publication of CN111944333B publication Critical patent/CN111944333B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK  ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
    • C09C3/00—Treatment in general of inorganic materials, other than fibrous fillers, to enhance their pigmenting or filling properties
    • C09C3/04—Physical treatment, e.g. grinding, treatment with ultrasonic vibrations
    • C09C3/043—Drying, calcination
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK  ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
    • C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
    • C09C1/0015—Pigments exhibiting interference colours, e.g. transparent platelets of appropriate thinness or flaky substrates, e.g. mica, bearing appropriate thin transparent coatings

Abstract

The invention belongs to the field of calcining heat treatment of a pearlescent material, and particularly relates to a fluidized continuous calcining system and method for the pearlescent material. The invention has the advantages of high continuous production efficiency, good calcination effect, low production energy consumption and the like, is suitable for the industrial calcination process section of the coated titanium mica pearlescent material, and has good economic and social benefits.

Description

Continuous fluidized calcining system and method for pearlescent material
Technical Field
The invention belongs to the fields of pearlescent materials and chemical industry, and particularly relates to a system and a method for a continuous fluidized calcining process of a pearlescent material.
Background
The pearlescent material is a novel decorative material, can show soft and dazzling pearlescent effects under the action of light, and is widely applied to the industries of coatings, printing ink, cosmetics, plastics, rubber, printing and the like. The mica titanium pearlescent material is one of the most representative materials, and is micropowder formed by coating one or more layers of titanium or other metal oxides on the surface of a flaky mica substrate serving as a core through a chemical coating process.
The calcination heat treatment of the pearlescent material precursor is an important process step in the production of the mica titanium pearlescent pigment. In the pearlescent material produced by the existing liquid phase process, hydrated titanium dioxide is arranged on the surface of a pearlescent material precursor and a mica sheet after the coating process, and crystal water is removed by calcination to become stable crystalline titanium dioxide and at the same time, anatase type titanium dioxide is converted into rutile type titanium dioxide. In addition, various acid radical ions (such as Cl) in the pearlescent material can be removed by the calcining heat treatment-、SO4 2-Etc.) to decompose and volatilize at high temperatures. The calcined pearlescent material can obviously improve whiteness and brightness, increase covering power, and endow higher adsorption capacity, pigment and other properties.
The traditional calcining device for producing the pearlescent material is a roller kiln, the pearlescent material is conveyed into a heating furnace through a conveyor belt to be calcined, the pearlescent material powder is accumulated on the conveyor belt and is static, the pearlescent material undergoes decomposition reaction at high temperature, the surface of the accumulated powder can be completely reacted, but the powder inside the accumulated powder is difficult to fully react, the calcining mode is very unstable for controlling the calcining quality of the pearlescent material, the efficiency is low, and the product quality of the pearlescent material is influenced. In addition, in order to prevent the powder from taking away heat, the moving speed of the conveyor belt needs to be reduced, the calcining time of the common pearlescent material is as long as several hours, so that the power consumption is greatly improved, and the calcining cost is directly increased.
Therefore, there is a need in the art for a system and method for rapid and efficient calcination of pearlescent materials.
Disclosure of Invention
The invention aims to provide a system and a method for continuous fluidized calcining process of pearlescent material, which have high continuous production efficiency, good calcining effect and low production energy consumption.
In order to achieve the purpose, the specific technical scheme of the invention is as follows:
a continuous fluidized calcining system for pearlescent materials comprises a raw material bin 1, a hot blast stove 2, a rotary dryer 3, a lifter 4, a top bin 5, a feeding screw 6, a feeding valve 7, a fluidized bed 8, a primary cyclone separator 9, a secondary cyclone separator 9-1, a primary return valve 10, a secondary return valve 11, a discharge valve 12, a water-cooling screw 13, a product bin 14, a bag-distribution dust collector 15, an induced draft fan 16, a chimney 17, an air fan 18, a natural gas fan 19, a combustion chamber 20, a water pump 21 and a cooling tower 22;
in the system, a discharge port of a raw material bin 1 is connected with a feed port of a rotary dryer 3, an air inlet of a hot blast stove 2 is connected with a natural gas fan 19 and an air outlet of a secondary cyclone separator 9-1, an air inlet of the rotary dryer 3 is connected with an air outlet of the hot blast stove 2, a discharge port of the rotary dryer 3 is connected with a feed port of a lifter 4, a discharge port of the lifter 4 is connected with a feed port of a top bin 5, a discharge port of the top bin 5 is connected with a feed port of a feed screw 6, a discharge port of the feed screw 6 is connected with a feed port of a feed valve 7, a discharge port of the feed valve 7 is connected with a feed port of a fluidized bed 8, an air inlet of the fluidized bed 8 is connected with an air outlet of a combustion chamber 20, a discharge port of the fluidized bed 8 is connected with a feed port of a discharge valve 12, an air inlet of a primary cyclone separator 9 is connected with an air outlet of the fluidized bed 8, a discharge port of the primary cyclone separator 9 is connected with a feed port of a feedback valve 10, an air inlet of a secondary cyclone separator 9-1 is connected with an air outlet of a primary cyclone separator 9, a discharge outlet of the secondary cyclone separator 9-1 is connected with a feed inlet of a two-part material returning valve 11, discharge outlets of a one-part material returning valve 10 and a two-part material returning valve 11 are connected with a fluidized bed 8, a discharge outlet of a discharge valve 12 is connected with a feed inlet of a water-cooling spiral 13, a discharge outlet of the water-cooling spiral 13 is connected with a product bin 14, an air inlet of a bag-distributing dust collector 15 is connected with an air outlet of a rotary dryer 3, an air inlet of an induced draft fan 16 is connected with an air outlet of the bag-distributing dust collector 15, an air outlet of the induced draft fan 16 is connected with a chimney 17, an air inlet of a combustion chamber 20 is connected with air outlets of an air fan 18 and a natural gas fan 19, a water outlet of a water pump 21 is connected with a water inlet of the water-cooling spiral 13, and a water outlet of the water-cooling spiral 13 is connected with a cooling tower 22.
In the invention, oxidizing hot air discharged from a fluidized bed 8 is dedusted by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters a hot blast stove 2 to recover sensible heat in the air.
The invention relates to a method for fluidizing and continuously calcining pearlescent pigment, which comprises the following steps:
1) the pearl material precursor powder enters a rotary dryer 3 through a raw material bin 1, sequentially enters a lifter 4, a top bin 5 and a feeding screw 6, and enters a fluidized bed 8 through a feeding valve 7; powder entrained in high-temperature tail gas (also called oxidizing hot air) discharged by the fluidized bed 8 is collected by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters the fluidized bed 8 through a first return valve 10 and a second return valve 11; discharging the fully calcined pearlescent material from a discharge port of the fluidized bed 8, cooling the pearlescent material by a water-cooling spiral 13 through a discharge valve 12, and finally piling the pearlescent material in a product bin 14;
2) fluidized air (also called as oxidizing hot flue gas) is generated by burning natural gas and air in a combustion chamber 20, the fluidized air generated by burning enters a fluidized bed through an air inlet of the fluidized bed 8 to fluidize and heat a pearlescent material precursor in the calcined fluidized bed, high-temperature tail gas discharged from the fluidized bed (8) enters a hot blast stove 2 for supplementary heating combustion after passing through a primary cyclone separator 9 and a secondary cyclone separator 9-1, then enters a rotary dryer 3 for drying the non-calcined pearlescent material precursor, flue gas of the rotary dryer (3) enters a bag collector 15 for dust removal and purification after passing through an air outlet of the rotary dryer 3, and the purified low-temperature flue gas is discharged from a chimney 17 through a draught fan 16;
3) the cooling water of the process water main is pressurized by the water pump 21, enters the water inlet of the water-cooling spiral 13 to exchange heat with the hot materials, and is cooled and recycled by the cooling tower 21 from the water outlet of the water-cooling spiral 13.
In the invention, the pearlescent material product comprises a silver white series pearlescent material, a magic color series pearlescent material or a coloring series pearlescent material.
In the invention, the water content of the pearlescent material precursor is 5-30 wt%.
In the invention, the calcination temperature is 550-850 ℃, and the calcination time is 10-60 min.
In the present invention, the discharge temperature of the rotary dryer 3 is 105 ℃.
Compared with the prior calcining technology based on a roller kiln, the method for the continuous calcining technology of the pearlescent material has the advantages that:
(1) the fluidized pearlescent material has sufficient gas-solid contact in the calcining process, good calcining effect, better dispersibility of the calcined powder and 10 percent improvement of the glossiness.
(2) The large-scale continuous calcination is realized by controlling the feeding and the discharging in the system, the production efficiency is high, the product quality can be improved by full calcination, and the stability of the calcination production is improved.
(3) The rapid and efficient calcination can greatly shorten the calcination time, realize the calcination with low energy consumption and reduce the calcination cost. The calcining energy consumption is only 50% of that of the roller kiln with the same equivalent weight.
Drawings
FIG. 1 is a schematic diagram of a continuous fluidized calcination process for pearlescent material provided by the present invention;
reference numerals:
1. a raw material bin; 2. a hot blast stove; 3. a rotary dryer; 4. a hoist; 5. a top bin; 6. a feed screw; 7. a feed valve; 8. a fluidized bed; 9. a primary cyclone separator; 9-1, a secondary cyclone separator; 10. a material dividing and returning valve; 11. a two-part material returning valve; 12. a discharge valve; 13. water-cooling the spiral; 14. a product bin; 15. a bag dust collector; 16. an induced draft fan; 17. a chimney; 18. an air blower; 19. a natural gas fan; 20. a combustion chamber; 21. a water pump; 22. and (5) cooling the tower.
Detailed Description
Any feature disclosed in this specification may be replaced by alternative features serving equivalent or similar purposes, unless expressly stated otherwise. Unless expressly stated otherwise, each feature is only an example of a generic series of equivalent or similar features. The description is only for the purpose of facilitating understanding of the present invention and should not be construed as specifically limiting the present invention.
In order to make the objects, technical solutions and advantages of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings of the present invention, but the present invention is not limited to the scope of the present invention.
Example 1
As shown in fig. 1, a system for a pearl material continuous fluidized calcination process comprises a raw material bin 1, a hot blast stove 2, a rotary dryer 3, a lifter 4, a top bin 5, a feeding screw 6, a feeding valve 7, a fluidized bed 8, a primary cyclone separator 9, a secondary cyclone separator 9-1, a primary return valve 10, a secondary return valve 11, a discharge valve 12, a water-cooling screw 13, a product bin 14, a bag-distribution dust collector 15, an induced draft fan 16, a chimney 17, an air fan 18, a natural gas fan 19, a combustion chamber 20, a water pump 21 and a cooling tower 22 which are connected in sequence;
in the system, a discharge port of a raw material bin 1 is connected with a feed port of a rotary dryer 3, an air inlet of a hot blast stove 2 is connected with a natural gas fan 19 and an air outlet of a secondary cyclone separator 9-1, an air inlet of the rotary dryer 3 is connected with an air outlet of the hot blast stove 2, a discharge port of the rotary dryer 3 is connected with a feed port of a lifter 4, a discharge port of the lifter 4 is connected with a feed port of a top bin 5, a discharge port of the top bin 5 is connected with a feed port of a feed screw 6, a discharge port of the feed screw 6 is connected with a feed port of a feed valve 7, a discharge port of the feed valve 7 is connected with a feed port of a fluidized bed 8, an air inlet of the fluidized bed 8 is connected with an air outlet of a combustion chamber 20, a discharge port of the fluidized bed 8 is connected with a feed port of a discharge valve 12, an air inlet of a primary cyclone separator 9 is connected with an air outlet of the fluidized bed 8, a discharge port of the primary cyclone separator 9 is connected with a feed port of a feedback valve 10, an air inlet of a secondary cyclone separator 9-1 is connected with an air outlet of a primary cyclone separator 9, a discharge outlet of the secondary cyclone separator 9-1 is connected with a feed inlet of a two-part material returning valve 11, discharge outlets of a one-part material returning valve 10 and a two-part material returning valve 11 are connected with a fluidized bed 8, a discharge outlet of a discharge valve 12 is connected with a feed inlet of a water-cooling spiral 13, a discharge outlet of the water-cooling spiral 13 is connected with a product bin 14, an air inlet of a bag-distributing dust collector 15 is connected with an air outlet of a rotary dryer 3, an air inlet of an induced draft fan 16 is connected with an air outlet of the bag-distributing dust collector 15, an air outlet of the induced draft fan 16 is connected with a chimney 17, an air inlet of a combustion chamber 20 is connected with air outlets of an air fan 18 and a natural gas fan 19, a water outlet of a water pump 21 is connected with a water inlet of the water-cooling spiral 13, and a water outlet of the water-cooling spiral 13 is connected with a cooling tower 22.
In the system, oxidizing hot air discharged from a fluidized bed 8 enters a hot blast stove 2 after being subjected to dust removal treatment by a primary cyclone separator 9 and a secondary cyclone separator 9-1, and sensible heat in the air is recovered.
Example 2
A method for continuous fluidized calcining process of pearlescent material comprises the following steps:
1) the pearl material precursor powder enters a rotary dryer 3 through a raw material bin 1, sequentially enters a lifter 4, a top bin 5 and a feeding screw 6, and enters a fluidized bed 8 through a feeding valve 7; powder entrained in high-temperature tail gas discharged by the fluidized bed 8 is collected by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters the fluidized bed 8 through a first return valve 10 and a second return valve 11; discharging the fully calcined pearlescent material from a discharge port of the fluidized bed 8, cooling the pearlescent material by a water-cooling spiral 13 through a discharge valve 12, and finally piling the pearlescent material in a product bin 14;
2) the fluidized air is generated by burning natural gas and air in a combustion chamber 20, oxidizing hot flue gas generated by burning enters a fluidized bed through an air inlet of the fluidized bed 8 and is used for fluidizing and heating pearlescent material precursors in the fluidized bed, high-temperature tail gas discharged from the fluidized bed (8) enters a hot blast stove 2 for supplementary heating combustion after passing through a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters a rotary dryer 3 for drying the non-calcined pearlescent material precursors, flue gas of the rotary dryer (3) enters a bag dust collector 15 for dust removal and purification after passing through an air outlet of the rotary dryer 3, and purified low-temperature flue gas is discharged from a chimney 17 through an induced draft fan 16;
3) the cooling water of the process water main is pressurized by the water pump 21, enters the water inlet of the water-cooling spiral 13 to exchange heat with the hot materials, is discharged from the water outlet of the water-cooling spiral 13, and is cooled by the cooling tower 21 for recycling.
The pearlescent material product comprises a silver white series pearlescent material, a fantasy color series pearlescent material or a coloring series pearlescent material.
The water content of the uncalcined pearlescent material precursor is 5-30%. The calcination temperature is 550-850 ℃, and the calcination time is 10-60 min. The discharge temperature of the rotary dryer 3 was 105 ℃.
Example 3
By adopting the method described in embodiment 2, silver white series pearlescent material precursor powder with the water content of 5 wt% enters a rotary dryer 3 through a raw material bin 1, sequentially enters a lifter 4, a top bin 5 and a feeding screw 6, and enters a fluidized bed 8 through a feeding valve 7; the fluidized air is generated by burning natural gas and air in the combustion chamber 20, and oxidizing hot flue gas generated by burning enters the fluidized bed through the air inlet of the fluidized bed 8 to fluidize and calcine the pearlescent material precursor in the fluidized bed, wherein the calcining temperature is 550 ℃ and the calcining time is 60 min; the pearl material is subjected to supplementary heat combustion in a hot blast stove 2 after passing through a primary cyclone separator 9 and a secondary cyclone separator 9-1, then enters a rotary dryer 3, dries the uncalcined pearl material precursor, enters a bag dust collector 15 through an air outlet of the rotary dryer 3 for dust removal and purification, and the purified low-temperature flue gas is discharged from a chimney 17 through an induced draft fan 16; the cooling water of the process water main is pressurized by the water pump 21, enters the water inlet of the water-cooling spiral 13 to exchange heat with the hot materials, and is cooled and recycled by the cooling tower 21 from the water outlet of the water-cooling spiral 13; powder entrained in high-temperature tail gas discharged by the fluidized bed 8 is collected by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters the fluidized bed 8 through a first return valve 10 and a second return valve 11; the pearl material which is fully calcined is discharged from a discharge hole of the fluidized bed 8, enters a water-cooling spiral 13 through a discharge valve 12 for cooling, and finally enters a product bin 14 for piling.
Example 4
By adopting the method described in the embodiment 2, the precursor powder of the glittering series pearlescent material with the water content of 30 wt% enters a rotary dryer 3 through a raw material bin 1, sequentially enters a lifter 4, a top bin 5 and a feeding screw 6, and enters a fluidized bed 8 through a feeding valve 7; the fluidized air is generated by burning natural gas and air in a combustion chamber 20, oxidizing hot flue gas generated by burning enters the fluidized bed through an air inlet of the fluidized bed 8 to fluidize and calcine the pearl material precursor in the fluidized bed, the calcining temperature is 850 ℃, and the calcining time is 10 min; the pearl material is subjected to supplementary heat combustion in a hot blast stove 2 after passing through a primary cyclone separator 9 and a secondary cyclone separator 9-1, then enters a rotary dryer 3, dries the uncalcined pearl material precursor, enters a bag dust collector 15 through an air outlet of the rotary dryer 3 for dust removal and purification, and the purified low-temperature flue gas is discharged from a chimney 17 through an induced draft fan 16; the cooling water of the process water main is pressurized by the water pump 21, enters the water inlet of the water-cooling spiral 13 to exchange heat with the hot materials, and is cooled and recycled by the cooling tower 21 from the water outlet of the water-cooling spiral 13; powder entrained in high-temperature tail gas discharged by the fluidized bed 8 is collected by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters the fluidized bed 8 through a first return valve 10 and a second return valve 11; the pearl material which is fully calcined is discharged from a discharge hole of the fluidized bed 8, enters a water-cooling spiral 13 through a discharge valve 12 for cooling, and finally enters a product bin 14 for piling.
Example 5
By adopting the method described in embodiment 2, coloring series pearlescent material precursor powder with the water content of 15 wt% enters a rotary dryer 3 through a raw material bin 1, sequentially enters a lifter 4, a top bin 5 and a feeding screw 6, and enters a fluidized bed 8 through a feeding valve 7; the fluidized air is generated by burning natural gas and air in a combustion chamber 20, oxidizing hot flue gas generated by burning enters a fluidized bed through an air inlet of the fluidized bed 8 to fluidize and calcine the pearlescent material precursor in the fluidized bed, the calcining temperature is 660 ℃, and the calcining time is 30 min; the pearl material is subjected to supplementary heat combustion in a hot blast stove 2 after passing through a primary cyclone separator 9 and a secondary cyclone separator 9-1, then enters a rotary dryer 3, dries the uncalcined pearl material precursor, enters a bag dust collector 15 through an air outlet of the rotary dryer 3 for dust removal and purification, and the purified low-temperature flue gas is discharged from a chimney 17 through an induced draft fan 16; the cooling water of the process water main is pressurized by the water pump 21, enters the water inlet of the water-cooling spiral 13 to exchange heat with the hot materials, and is cooled and recycled by the cooling tower 21 from the water outlet of the water-cooling spiral 13; powder entrained in high-temperature tail gas discharged by the fluidized bed 8 is collected by a primary cyclone separator 9 and a secondary cyclone separator 9-1 and then enters the fluidized bed 8 through a first return valve 10 and a second return valve 11; the pearl material which is fully calcined is discharged from a discharge hole of the fluidized bed 8, enters a water-cooling spiral 13 through a discharge valve 12 for cooling, and finally enters a product bin 14 for piling.
The method can be realized by upper and lower limit values and interval values of intervals of process parameters (such as temperature, time and the like), and embodiments are not listed.
Conventional technical knowledge in the art can be used for the details which are not described in the present invention.
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and are not limited. Although the present invention has been described in detail with reference to the embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the spirit and scope of the invention as defined in the appended claims.

Claims (7)

1. A fluidized continuous calcining system for pearlescent material is characterized by comprising a raw material bin (1), a hot blast stove (2), a rotary dryer (3), a lifter (4), a top bin (5), a feeding screw (6), a feeding valve (7), a fluidized bed (8), a primary cyclone separator (9), a secondary cyclone separator (9-1), a primary return valve (10), a secondary return valve (11), a discharge valve (12), a water-cooling screw (13), a product bin (14), a bag-distribution dust collector (15), a draught fan (16), a chimney (17), an air fan (18), a natural gas fan (19), a combustion chamber (20), a water pump (21) and a cooling tower (22);
in the system, the discharge hole of a raw material bin (1) is connected with the feed inlet of a rotary dryer (3), the air inlet of a hot blast stove (2) is connected with a natural gas fan (19) and the air outlet of a secondary cyclone separator (9-1), the air inlet of the rotary dryer (3) is connected with the air outlet of the hot blast stove (2), the discharge hole of the rotary dryer (3) is connected with the feed inlet of a lifter (4), the discharge hole of the lifter (4) is connected with the feed inlet of a top bin (5), the discharge hole of the top bin (5) is connected with the feed inlet of a feed screw (6), the discharge hole of the feed screw (6) is connected with the feed inlet of a feed valve (7), the discharge hole of the feed valve (7) is connected with the feed inlet of a fluidized bed (8), the air inlet of the fluidized bed (8) is connected with the air outlet of a combustion chamber (20), the discharge hole of the fluidized bed (8) is connected with the feed inlet of a discharge valve (12), the air inlet of a first-stage cyclone separator (9) is connected with the air outlet of a fluidized bed (8), the discharge outlet of the first-stage cyclone separator (9) is connected with the feed inlet of a first return valve (10), the air inlet of a second-stage cyclone separator (9-1) is connected with the air outlet of the first-stage cyclone separator (9), the discharge outlet of the second-stage cyclone separator (9-1) is connected with the feed inlet of a second return valve (11), the discharge outlets of the first return valve (10) and the second return valve (11) are connected with the fluidized bed (8), the discharge outlet of a discharge valve (12) is connected with the feed inlet of a water-cooling spiral (13), the discharge outlet of the water-cooling spiral (13) is connected with a product bin (14), the air inlet of a bag dust collector (15) is connected with the air outlet of a rotary dryer (3), the air inlet of a draught fan (16) is connected with the air outlet of the bag dust collector (15), the air outlet of the induced draft fan (16) is connected with the chimney (17), the air inlet of the combustion chamber (20) is connected with the air outlet of the air fan (18) and the natural gas fan (19), the water outlet of the water pump (21) is connected with the water inlet of the water-cooling spiral (13), and the water outlet of the water-cooling spiral (13) is connected with the cooling tower (22).
2. The pearly luster material fluidizing and continuous calcining system according to claim 1, wherein the oxidizing hot air discharged from the fluidized bed (8) enters the hot blast stove (2) after being dedusted by the primary cyclone separator (9) and the secondary cyclone separator (9-1), and the sensible heat in the air is recovered.
3. A method for fluidized continuous calcination of pearlescent material using the system of claim 1, comprising the steps of:
1) the pearl material precursor powder enters a rotary dryer (3) through a raw material bin (1), sequentially enters a lifter (4), a top bin (5) and a feeding screw (6), and enters a fluidized bed (8) through a feeding valve (7); powder entrained in high-temperature tail gas discharged by the fluidized bed (8) is collected by a primary cyclone separator (9) and a secondary cyclone separator (9-1) and then enters the fluidized bed (8) through a first material returning valve (10) and a second material returning valve (11); fully calcined pearlescent materials are discharged from a discharge hole of the fluidized bed (8), enter a water-cooling spiral (13) through a discharge valve (12) for cooling, and finally enter a product bin (14) for stockpiling;
2) the fluidized air is generated by burning natural gas and air in a combustion chamber (20), the fluidized air generated by burning enters a fluidized bed through an air inlet of the fluidized bed (8) and is used for fluidizing and calcining the pearl material precursor in the fluidized bed, high-temperature tail gas discharged from the fluidized bed (8) enters a hot blast stove (2) for heat supplementing combustion after passing through a primary cyclone separator (9) and a secondary cyclone separator (9-1) and then enters a rotary dryer (3) for drying the pearl material precursor, flue gas of the rotary dryer (3) enters a bag dust collector (15) for dust removal and purification through an air outlet of the rotary dryer (3), and the purified low-temperature flue gas is discharged from a chimney (17) through a draught fan (16);
3) the cooling water of the process water header pipe is pressurized by a water pump (21), enters the water inlet of the water-cooling spiral (13), exchanges heat with hot materials by the water-cooling spiral (13), and is cooled and recycled by a cooling tower (22) from the water outlet of the water-cooling spiral (13).
4. The method according to claim 3, wherein the pearlescent material comprises a silver white series pearlescent material, a fantasy color series pearlescent material, or a colored series pearlescent material.
5. The method according to claim 3, wherein the water content of the pearlescent material precursor is 5-30 wt%.
6. The method according to claim 3, wherein the calcination temperature in the fluidized bed (8) is 550 to 850 ℃ and the calcination time is 10 to 60 min.
7. A method according to claim 3, characterized in that the discharge temperature of the rotary dryer (3) is 105 ℃.
CN202010758740.7A 2020-07-31 2020-07-31 Continuous fluidized calcining system and method for pearlescent material Active CN111944333B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202010758740.7A CN111944333B (en) 2020-07-31 2020-07-31 Continuous fluidized calcining system and method for pearlescent material

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202010758740.7A CN111944333B (en) 2020-07-31 2020-07-31 Continuous fluidized calcining system and method for pearlescent material

Publications (2)

Publication Number Publication Date
CN111944333A CN111944333A (en) 2020-11-17
CN111944333B true CN111944333B (en) 2021-11-09

Family

ID=73339847

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202010758740.7A Active CN111944333B (en) 2020-07-31 2020-07-31 Continuous fluidized calcining system and method for pearlescent material

Country Status (1)

Country Link
CN (1) CN111944333B (en)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005005318A2 (en) * 2003-07-11 2005-01-20 Outokumpu Technology Oy Process and plant for producing metal oxide from metal hydroxide
CN1600687A (en) * 2003-09-28 2005-03-30 中国科学院过程工程研究所 Rapid cycled fluidized calcining procedure for superfine kaolin and equipment
CN1632436A (en) * 2005-01-18 2005-06-29 中国科学院过程工程研究所 Fast fluidized calcining process
CN108807884A (en) * 2018-05-31 2018-11-13 中国科学院过程工程研究所 A kind of system and method for lithium ion battery negative material carbon coating modification
CN109982775A (en) * 2016-11-22 2019-07-05 奥图泰(芬兰)公司 For heat-treating methods in fluidized-bed reactor and equipment

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005005318A2 (en) * 2003-07-11 2005-01-20 Outokumpu Technology Oy Process and plant for producing metal oxide from metal hydroxide
CN1600687A (en) * 2003-09-28 2005-03-30 中国科学院过程工程研究所 Rapid cycled fluidized calcining procedure for superfine kaolin and equipment
CN1632436A (en) * 2005-01-18 2005-06-29 中国科学院过程工程研究所 Fast fluidized calcining process
CN109982775A (en) * 2016-11-22 2019-07-05 奥图泰(芬兰)公司 For heat-treating methods in fluidized-bed reactor and equipment
CN108807884A (en) * 2018-05-31 2018-11-13 中国科学院过程工程研究所 A kind of system and method for lithium ion battery negative material carbon coating modification

Also Published As

Publication number Publication date
CN111944333A (en) 2020-11-17

Similar Documents

Publication Publication Date Title
WO1992014530A1 (en) Process and apparatus for producing concentrated aqueous slurries and spray dried particulate products
CN106007694B (en) High-grade daily-use talc ceramic produced by using low-price black talc and manufacturing method thereof
CN103193400A (en) Temperature-controlled suspension roaster
CN107758712A (en) The Processes and apparatus of nepheline preheating predecomposition dry sintering production alumina clinker
CN103708515A (en) Method for producing alpha-Al2O3 by employing predecomposition technology and taking aluminium hydrogen as raw material
CN111909538B (en) Continuous calcining system and method for pearlescent material
CN111944333B (en) Continuous fluidized calcining system and method for pearlescent material
CN112194181A (en) Method for preparing vanadium pentoxide by utilizing ammonium metavanadate
CN203212470U (en) Temperature-controllable suspension roaster
CN109110813B (en) Method for preparing multi-valence vanadium oxide by dynamic calcination
CN111847468B (en) Method for producing high-whiteness calcined kaolin by multi-stage suspension calcination of coal-series kaolin
CN212292841U (en) Equipment for producing lanthanum oxide by fluidized calcination
CN210292777U (en) Corrosion-resistant roasting system
CN209081442U (en) A kind of energy-saving titanium dioxide calciner
CN207247964U (en) Utilize the device of roasting oxidation aluminium waste-heat square position mother liquor
CN109982775B (en) Method and apparatus for heat treatment in a fluidized bed reactor
CN207943888U (en) The equipment that nepheline preheats predecomposition dry sintering production alumina clinker
CN206572938U (en) A kind of calcining kiln for titanium dioxide
US3105744A (en) Method for producing calcined titanium dioxide pigment material
CN114620726A (en) Calcination CO-production of high-purity CO from small-particle carbonate ore2Reactor and method
CN2818492Y (en) Producer for oxidation pelletizing
CN111892062A (en) System for producing high-whiteness calcined kaolin through multi-section suspension calcination of coal-series kaolin
CN215798531U (en) Coal series kaolin calcining device
CN111847469B (en) System for preparing multistage calcined kaolin by suspension calcination of coal-series kaolin
CN103090682B (en) Method and equipment of calcining and waste heat recovery

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant