CN113828429B - System and process for deacidifying ultrafine powder - Google Patents
System and process for deacidifying ultrafine powder Download PDFInfo
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- CN113828429B CN113828429B CN202111110719.7A CN202111110719A CN113828429B CN 113828429 B CN113828429 B CN 113828429B CN 202111110719 A CN202111110719 A CN 202111110719A CN 113828429 B CN113828429 B CN 113828429B
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- 239000000843 powder Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 16
- 239000007787 solid Substances 0.000 claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 23
- 238000011084 recovery Methods 0.000 claims abstract description 10
- 239000002912 waste gas Substances 0.000 claims abstract description 8
- 239000004744 fabric Substances 0.000 claims description 30
- 238000000926 separation method Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 238000005485 electric heating Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 2
- 239000012467 final product Substances 0.000 claims description 2
- 239000012071 phase Substances 0.000 abstract description 5
- 239000007790 solid phase Substances 0.000 abstract description 3
- 238000005054 agglomeration Methods 0.000 abstract description 2
- 230000002776 aggregation Effects 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 abstract description 2
- 230000007547 defect Effects 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 22
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 11
- 238000002474 experimental method Methods 0.000 description 11
- 239000000047 product Substances 0.000 description 9
- 239000011295 pitch Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000003584 silencer Effects 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 229910010413 TiO 2 Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000005389 magnetism Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/08—Vortex chamber constructions
- B04C5/081—Shapes or dimensions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/20—Apparatus in which the axial direction of the vortex is reversed with heating or cooling, e.g. quenching, means
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
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- Physics & Mathematics (AREA)
- Engineering & Computer Science (AREA)
- Geometry (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Cyclones (AREA)
Abstract
The invention discloses a system and a process for deacidifying ultrafine powder, wherein the system comprises an ultrafine powder feeder, an air inlet system, a primary deacidification system, a multistage gas-solid countercurrent deacidification module and an energy recovery system, the primary deacidification system is circularly connected with the multistage gas-solid countercurrent deacidification module to form a loop, the ultrafine powder feeder is arranged on a feeding pipeline of the primary deacidification system, the air inlet system is connected with the multistage gas-solid countercurrent deacidification module, the energy recovery system is used for recovering heat of circulated waste gas, the gas-solid countercurrent deacidification module comprises cyclones and cyclone separators, an inner rotational flow plate and an outer rotational flow plate are alternately arranged in each cyclone, each rotational flow plate is divided into a plurality of areas, and rotational flow sheets are obliquely arranged in each area. The invention increases the turbulence degree between the gas phase and the solid phase, reduces the agglomeration of the ultrafine powder, can strengthen the heat and mass transfer between the gas phase and the solid phase, improves the deacidification rate and the energy utilization rate, and solves the defects of low deacidification efficiency, high energy consumption and the like in the traditional deacidification process.
Description
Technical Field
The invention belongs to the technical field of deacidification processes, and particularly relates to a system and a process for deacidifying ultrafine powder.
Background
Currently, the high and new technology and the material industry are rapidly developed, and the superfine powder industry is very different day by day. The superfine powder has the characteristics of good specific dispersibility, strong magnetism, good activity, good thermal conductivity and the like, and becomes a hot spot for research in various countries, but the prepared superfine powder is generally obtained by gas-phase combustion and hydrolysis of chloride, and the generation of target products is accompanied by the generation of HCl, and the superfine powder can adsorb trace HCl due to the fact that the superfine powder has a large specific surface area. In the application occasion of the superfine powder, the HCl amount adsorbed by the superfine powder is strictly required, wherein the pH value is an important index for measuring the quality of the product. In order to meet the requirements of various applications, the HCl contained therein needs to be removed to meet the specified product quality standards.
Regarding ultra-fine powder deacidification, in the gas phase nano TiO 2 Fluidized bed deacidification and mechanism research (Liu Jie, li Chunzhong, hu Yanjie, etc.; chinese powder technology; 2007.); nanometer alumina powder deacidification process research (Shijin, yan Weiwei, liu Guodong; chemical working hours and periodical; 2020) and other documents teach that the traditional deacidification mode is dry hot air deacidification and wet hot air deacidification. The temperature in the traditional parallel flow deacidification process is required to be controlled to be more than 500 ℃, the energy consumption is high, the residence time is too long, and ultrafine powder is easy to agglomerate. The deacidification device is also mostly a fluidized bed or a deacidification furnace, the occupied area of equipment is relatively large, and the pH after deacidification is basically about 4 or even below 4.
Disclosure of Invention
In order to solve the above problems, the present invention aims to provide a system and a process for deacidifying ultrafine powder.
In order to achieve the above purpose, the following technical scheme is provided:
a system for superfine powder deacidification comprises a superfine powder feeder, an air inlet system, a primary deacidification system, a multistage gas-solid countercurrent deacidification module and an energy recovery system, wherein the primary deacidification system is circularly connected with the multistage gas-solid countercurrent deacidification module to form a loop, the superfine powder feeder is arranged on a feeding pipeline of the primary deacidification system, the air inlet system is connected with the multistage gas-solid countercurrent deacidification module, and the energy recovery system is used for recycling waste gas heat.
Further, the primary deacidification system comprises a cyclone, a cloth bag separator, a star-shaped discharger and a venturi conveyor, wherein the top outlet of the cyclone is connected with the side inlet of the cloth bag separator, the star-shaped discharger and the venturi conveyor are sequentially arranged at the lower discharge port of the cloth bag separator, the multistage gas-solid countercurrent deacidification module is connected with the cloth bag separator to form a loop, and the multistage gas-solid countercurrent deacidification module is sequentially connected with the cyclone and the cloth bag separator to form a loop; the gas-solid countercurrent deacidification module comprises a cyclone, a cyclone separator, a star-shaped discharger and a venturi conveyor, wherein the top outlet of the cyclone is connected with the side inlet of the cyclone separator, the star-shaped discharger and the venturi conveyor or the discharging device are sequentially arranged below the cyclone separator, N gas-solid countercurrent deacidification modules are sequentially connected to form a loop, and the value of N is 1-5.
Further, the air inlet system comprises a filter, an electric heating device and an air blower, wherein the filter, the air blower and the electric heating device are connected through pipelines in sequence, and the electric heating pipeline is connected with the multistage gas-solid countercurrent deacidification module.
Further, the superfine powder feeder comprises a hopper and a venturi conveyor, and the venturi conveyor is arranged on a pipeline of the primary deacidification system, which is circularly connected with the multistage gas-solid countercurrent deacidification module.
Further, the energy recovery system comprises a preheater, a cooler, a circulating pump and a heat exchange medium circulating tank, wherein the preheater is arranged at the front end of the electric heating inlet, the cooler is arranged on an air outlet pipeline above the cloth bag separator, the preheater and the cooler are connected into a loop to realize heat exchange, and the heat exchange medium circulating tank and the circulating pump are arranged on the loop.
Further, 2-20 cyclone plates are arranged in the cyclone, each cyclone plate comprises an inner cyclone plate and an outer cyclone plate, the inner cyclone plates and the outer cyclone plates are distributed up and down alternately, the cyclone plates are divided into multiple areas by the multiple separation plates, cyclone sheets are obliquely arranged in each area, the cyclone sheets of the outer cyclone plates are inclined downwards towards the central point, and the cyclone sheets of the inner cyclone plates are inclined upwards towards the central point.
Further, the swirl plates are in a shutter type regular arrangement, the inclination angle range of the swirl plates of the outer swirl plate is 10-30 degrees, the inclination angle range of the swirl plates of the inner swirl plate is 35-70 degrees, and the distance e between the swirl plates is set asD is the diameter of the cyclone plate, D is the thickness of the cyclone sheets, M is the total number of the cyclone sheets of each cyclone plate, and θ is the inclination angle of the cyclone sheets.
Further, a discharging device below the Nth cyclone separator is a double-butterfly-valve discharging device and is used for collecting the final product; the outside of the cloth bag separator is also provided with a vibrator.
A process for deacidifying ultrafine powder, comprising the following steps:
1) Starting a blower, an electric heating and circulating pump, enabling hot air to sequentially pass through a multistage gas-solid countercurrent deacidification module and a primary deacidification system, and adding a heat exchange medium into a heat exchange medium circulating tank to enable an energy recovery system to circulate;
2) After the temperature is stable, adding the superfine powder material into a cyclone of a primary deacidification system through a superfine powder feeder for primary deacidification, then entering a cloth bag separator for gas-solid separation, cooling gas from the upper part of the cloth bag separator, blowing out the gas, and enabling solids to enter a multistage gas-solid countercurrent deacidification module for multistage deacidification, and collecting after deacidification is completed.
Further, when the temperature of the hot air after primary deacidification is less than 100 ℃, the heat exchange medium in the heat exchange medium circulation tank is water, when the temperature of the hot air after primary deacidification is greater than 100 ℃, the heat exchange medium in the heat exchange medium circulation tank is heat conduction oil, the temperature of the waste gas cooled by the cooler is about 50-80 ℃, and then the waste gas is discharged out of the system by the induced draft fan.
The invention has the beneficial effects that:
1) The cyclone plates in the cyclone are alternately arranged up and down in an internal and external rotation mode, and each part of cyclone sheets separated by the separation plates are orderly distributed by adopting a louver type arrangement method, so that the crushing among particles is enhanced, the formation of agglomerates is reduced, and the heat and mass transfer of the superfine powder is better;
2) When the superfine powder rotates on the cyclone sheets along with the airflow, if the distance between the cyclone sheets is too large, the heat transfer effect may not be good, the distance between the cyclone sheets is too small, the fluid resistance is too large, the powder can be gathered together when rotating on the cyclone sheets, the calculation of the distance between the cyclone sheets is accurately set, the proper distance enables better heat and mass transfer between gas and solid, the agglomeration and powder accumulation of the superfine powder are reduced, and the cyclone plate achieves the best beneficial effect;
3) The process is provided with a heat energy recycling system, and is characterized in that heat is recycled based on a heat exchange medium circulation tank, a circulation pump, a cooler and a preheater, cold air of the preheater enters the heat exchange medium circulation tank, the heat exchange medium enters the cooler through the circulation pump to exchange heat with hot air, the temperature of the heat exchanged hot air is reduced through heat exchange between the preheater and the cold air, and the cooled hot air enters the heat exchange medium circulation tank to recycle, so that the heat is effectively utilized;
4) The process adopts a multistage cyclone deacidification device to carry out multistage gas-solid countercurrent deacidification to obtain a deacidification product, and the deacidification effect of the superfine powder is effectively improved through multistage deacidification.
Drawings
FIG. 1 is a schematic flow chart of the present invention;
FIG. 2 is a schematic perspective view of an outer spin plate;
FIG. 3 is a schematic perspective view of an inner rotational flow plate;
FIG. 4 shows the pH values of the gas-solid countercurrent deacidification modules with different stages;
FIG. 5 shows the pH values when different angles of inclination of the cyclone plate of the inner cyclone plate are used;
FIG. 6 shows the pH values when different angles of inclination of the swirl plates of the outer swirl plate are used;
FIG. 7 is a graph showing pH values for different distances between cyclone plates;
FIG. 8 shows the pH values when different distances between cyclone plates of the outer cyclone plate are used.
In the figure: 1. a cyclone; 2. a cloth bag separator; 3. a cyclone separator; 4. electrically heating; 5. a preheater; 6. a swirl plate; 7. a cooler; 8. a circulation pump; 9. a heat exchange medium circulation tank; 10. a hopper; 11. a venturi conveyor; 12. a double butterfly valve discharger; 13. a vibrator; 14. a filter; 15. a star-shaped discharger; 61. a partition plate; 62. swirl plate.
Detailed Description
The invention will be further described with reference to the drawings and examples of the specification, but the scope of the invention is not limited thereto.
As shown in fig. 1, a system for deacidifying ultrafine powder when the value of N is 3 comprises 4 cyclones 1, 1 cloth bag separator 2, 3 cyclone separators 3, electric heater 4, preheater 5, cooler 7, circulating pump 8, heat exchange medium circulating tank 9, hopper 10, 4 venturi conveyors 11, double butterfly valve discharger 12, vibrator 13, filter 14 and 3 star-shaped discharger 15; the first cyclone 1 is used as a primary deacidification device, the top outlet of the first cyclone 1 is connected with the side inlet of the cloth bag separator 2, the discharge port below the cloth bag separator 2 is sequentially provided with a star-shaped discharge device 15 and a venturi conveyor 11, one end of the venturi conveyor 11 is connected with the feed inlet of the second cyclone 1 through a pipeline, the top outlet of the second cyclone 1 is connected with the side inlet of the first cyclone 3, the discharge port below the first cyclone 3 is sequentially provided with the star-shaped discharge device 15 and the venturi conveyor 11, one end of the venturi conveyor 11 is connected with the feed inlet of the second cyclone 1 through a pipeline, the third cyclone 1, the second cyclone 3, the fourth cyclone 1 and the third cyclone 3 are sequentially connected through the same connecting mode as the prior, the discharge port below the third cyclone 3 is provided with a double butterfly valve discharge device 12, the upper air outlet of the first cyclone separator 3 is connected with the feed inlet of the first cyclone separator 1 through a pipeline to form a loop, a venturi conveyer 11 is arranged on the connected pipeline, a hopper 10 is arranged above the venturi conveyer 11, the upper air outlet of the second cyclone separator 3 is connected with the other end of the venturi conveyer 11 below the cloth bag separator 2 through a pipeline to form a loop, the upper air outlet of the third cyclone separator 3 is connected with the other end of the venturi conveyer 11 below the first cyclone separator 3 through a pipeline to form a loop, a filter 14 is sequentially connected with a blower, a preheater 5 and an electric heater 4, the preheater 5 is arranged at the inlet end of the electric heater 4, the electric heater 4 is connected with the venturi conveyer 11 below the second cyclone separator 3 through a pipeline, a cooler 7 is arranged on the pipeline of the upper air outlet of the cloth bag separator 2, the cooler 7 is connected with the preheater 5 through a pipeline to form a circulation loop, and a circulation pump 8 and a heat exchange medium circulation tank 9 are arranged on the circulation loop.
The cyclone 1 is internally provided with a cyclone plate 6, the cyclone plate 6 comprises an outer cyclone plate shown in fig. 2 and an inner cyclone plate shown in fig. 3, the outer cyclone plate and the inner cyclone plate are alternately arranged up and down, the cyclone plate 6 is divided into a plurality of areas by a plurality of separation plates 61, each area is internally provided with a cyclone sheet 62 which is obliquely arranged, the cyclone sheets 62 of the outer cyclone plate incline downwards towards a central point, the cyclone sheets 62 of the inner cyclone plate incline upwards towards the central point, the inclination angle range of the cyclone sheets 62 of the outer cyclone plate is 10-30 degrees, and the inclination angle range of the cyclone sheets 62 of the inner cyclone plate is 35-70 degrees; the air outlet of the cooler 7 is sequentially connected with an induced draft fan and a silencer, and a vibrator 13 is arranged outside the cloth bag separator 2.
Example 1
The scheme adopted by the embodiment is as follows: the cyclone plate comprises an inner cyclone plate, an outer cyclone plate, a separation plate 61, a cyclone plate 6 and a cyclone plate 6, wherein the inclination angle is 45 degrees, the inclination angle is 15 degrees, the diameter of the cyclone plate 6 is 1m, the thickness of the cyclone plate 62 is about 0.5mm, the inner cyclone plate is divided into four areas by the separation plate 61, the cyclone plate 62 in each area is 11, the separation distance between every two cyclone plates 62 of the inner cyclone plate is about 5 cm, the separation distance between every two cyclone plates 62 of the outer cyclone plate is about 3 cm, the experimental control total cyclone deacidification time is about 30 minutes, when three-stage countercurrent deacidification is adopted, namely, when N is 3, the number of cyclone plates 6 in the cyclone 1 in the primary deacidification place is 2, the number of the cyclone plates 6 in the second cyclone 1 is 3, the number of the cyclone plates 6 in the third cyclone 1 is 3, the number of the cyclone plates 6 in the fourth cyclone 1 is 3, and the total number of cyclone plates 6 is 11.
The specific process is as follows: before the experiment, checking whether equipment, a control valve, a switch and the like normally operate, checking the heat exchange medium circulation tank 9, and ensuring that the volume of the heat conduction oil occupies the volume of the heat exchange medium circulation tank 9After the inspection, a filter 14, a blower, a preheater 5 and an electric heater 4 are started, the temperature of the electric heater 4 is set to 500 ℃, heat preservation cotton is arranged on heating pipelines to preserve heat, heat dissipation is prevented, the temperature rises to a stable state, a cooler 7 and a circulating pump 8 are started to switch for recycling energy, a compressed air control valve, a vibrator 13, an induced draft fan, a silencer and a shut-off fan are started after the system is stable, the frequency of the shut-off fan is adjusted to 15 Hz, the materials are ultrafine alumina with an initial pH value of about 2.8, the feeding amount is about 125 kg/h, the air speed is set to 0.5m/s, after 2 minutes, the ultrafine alumina is poured into a hopper 10, enters a venturi conveyor 11 through the shut-off fan, enters a cyclone 1 with hot air to be deacidified, and when the ultrafine alumina enters the cyclone 1, under the action of the bottom guide plate, cyclone flows in different directions on the cyclone plate 6 along with the gas, heat and mass transfer are maximized, superfine alumina enters the cloth bag separator 2 after passing through the first cyclone 1 of primary deacidification, then sequentially enters the three-stage gas-solid countercurrent deacidification module for multistage deacidification, heated fresh air directly enters the cyclone 1 along with the superfine alumina to carry out high Wen Tuosuan, the inlet temperature of the second cyclone 1 is measured to be about 376 ℃, the outlet temperature of the separator is about 325 ℃, the inlet temperature of the third cyclone 1 is measured to be about 428 ℃, the outlet temperature of the separator is about 388 ℃, the inlet temperature of the fourth cyclone 1 is about 490 ℃, the outlet temperature of the separator is about 440 ℃, and deacidified materials are discharged by a double-butterfly-valve discharger12 discharge system, collecting 99.8% of the product; the gas subjected to primary deacidification is discharged through an induced draft fan and a silencer after heat exchange, and finally the hot air subjected to deacidification enters a third cyclone 1 to be continuously utilized, and the hot air subjected to deacidification by the second cyclone 1 enters a venturi conveyor 11 below a hopper 10 to be recycled; the heat conduction oil in the heat exchange medium circulation tank 9 enters the cooler 7 through the circulation pump 8 to exchange heat air, and the final exhaust temperature is measured to be 90 ℃. Finally, 1g of superfine alumina is fully dispersed in 24 g of deionized water to prepare suspension with the mass fraction of 4%, and the pH value of the deacidified superfine alumina is about 5.50 after detection by a pH meter, so that the product requirement is met.
Examples 2 to 4
The number of stages of the multistage gas-solid countercurrent deacidification module is changed, N is 1,2 and 4 respectively, other conditions are the same as those of the embodiment 1, experiments are carried out, when the superfine alumina is subjected to primary deacidification, namely, when N is 1, the total number of the cyclone plates 6 is 14, the number of the cyclone plates 6 in the cyclone 1 at the primary deacidification position is 6, the number of the cyclone plates 6 in the second cyclone 1 is 8, when N is 1, the outlet of the cyclone 1 of the primary deacidification is connected with the cloth bag separator 2, a star-shaped discharger 15 and a venturi conveyor 11 are arranged below the cloth bag separator 2, and the venturi conveyor 11 is connected with the inlet of the primary cyclone 1 through a pipeline; the outlet of the primary cyclone 1 is connected with the cyclone 3, fresh gas heated by the preheater 5 and the electric heater 4 enters the primary deacidification module to deacidify the superfine powder, the deacidified hot air is recycled to the primary deacidification system by the primary cyclone 3 through a pipeline to be continuously utilized, the waste gas discharged by the primary deacidification enters the cooler 7 to recover heat and then is emptied, and the superfine powder enters the primary deacidification system and the primary deacidification module from the hopper 10 through the off-fan to obtain deacidification products; when the superfine alumina is subjected to secondary countercurrent deacidification, namely N is 2, the total number of cyclone plates 6 is 13, the number of cyclone plates 6 in a cyclone 1 at a primary deacidification position is 3, the number of cyclone plates 6 in the second cyclone 1 is 5, when the number of cyclone plates 6 in a third cyclone 1 is 5,N, a cloth bag separator 2 of a primary deacidification system is connected with the primary gas-solid countercurrent deacidification cyclone 1, a star-shaped discharger 15 and a venturi conveyor 11 are arranged below the primary cyclone 3, the venturi conveyor 11 is connected with an inlet of the secondary cyclone 1 through a pipeline, an outlet of the secondary cyclone 1 is connected with the cyclone 3, fresh gas heated by a preheater 5 and an electric heater 4 enters a secondary deacidification module, deacidification is carried out on superfine powder, hot air after deacidification is recovered to the primary deacidification module through a pipeline by the secondary cyclone 3, the hot air after the primary deacidification is continuously utilized, waste gas discharged by the primary deacidification enters a cooler 7 to recover heat, and the exhaust is emptied body enters a primary deacidification system from a fan 10 through a fan to obtain superfine powder product; when four-stage countercurrent deacidification is adopted for superfine alumina, the total number of the cyclone plates 6 is 10, the number of the cyclone plates 6 in the cyclone 1 at the primary deacidification position is 2, the number of the cyclone plates 6 in the second cyclone 1 is 2, the number of the cyclone plates 6 in the third cyclone 1 is 2, the number of the cyclone plates 6 in the fourth cyclone 1 is 2, and when the number of the cyclone plates 6 in the fifth cyclone 1 is 2 and N is 4, the cloth bag separator 2 of the primary deacidification system is connected with the cyclone 1 of the primary deacidification module, the venturi conveyor 11 below the cyclone separator 3 of the primary deacidification module is connected with the cyclone 1 of the secondary deacidification module, the venturi conveyor 11 below the cyclone separator 3 of the secondary deacidification module is connected with the cyclone 1 of the tertiary deacidification module, the outlet of the tertiary gas-solid countercurrent deacidification module 1 is connected with the cyclone 3, the cyclone separator 3 below is equipped with star type discharger 15 and venturi conveyer 11, venturi conveyer 11 links to each other with level four swirler 1 entry through the pipeline, fresh gas after the heating of pre-heater 5 and electrical heating 4 gets into level four deacidification module, carry out the deacidification to the superfine powder, the hot air after the deacidification is retrieved to level three deacidification module in proper order by level four cyclone separator 3 through the pipeline, the level two deacidification module, the level one deacidification module, the hot air after the level one then gets into the primary deacidification system and continues to utilize, the exhaust waste gas of primary deacidification then gets into the cooling ware 7 and retrieves the heat and emptys, and the superfine powder gets into primary deacidification system from hopper 10 through closing the fan, the level one deacidification module, the level two deacidification module, the level three deacidification module, level four deacidification module obtains deacidification product.
The experiment gave the pH values at different levels as shown in fig. 4, leading to the following conclusion: under the experimental operation conditions of example 1, as the number of stages of the multistage gas-solid countercurrent deacidification module increases, the deacidification effect increases continuously, and then tends to be stable, that is, the deacidification effect is optimal when N is 3.
Examples 5 to 8
The experiment was performed under the same conditions as in example 1 except that the inclination angles of the inner rotational flow plate were changed to 35 °, 50 °, 65 °, and 70 °, respectively.
The experiment shows that the pH value of the cyclone plate is shown in the figure 5 under different inclination angles, and the following conclusion is drawn: in the range of 35 degrees to 45 degrees of inclination angle, the deacidification effect is gradually enhanced along with the increase of the inclination angle, in the range of 45 degrees to 70 degrees, the deacidification effect is gradually weakened along with the increase of the inclination angle, the inclination angle mainly influences the heat and mass transfer between the gas and the solid, when the inclination angle is between 35 degrees and 45 degrees, the contact area of the gas and the solid on the cyclone plate 6 is increased along with the increase of the angle, the residence time is prolonged, the deacidification effect is better and better, when the inclination angle is between 45 degrees and 70 degrees, the contact area of the gas and the solid on the cyclone plate 6 is excessively enlarged, the heat and mass transfer effect is weakened, and the deacidification effect is also reduced to some extent.
Examples 8 to 11
The experiment was performed under the same conditions as in example 1 except that the inclination angles of the outer spin plates were changed to 10 °, 20 °, 25 °, and 30 °, respectively.
The experiment shows that the PH values of the external rotation whirl plates are shown in the figure 6 under different inclination angles, and the following conclusion is obtained: in the range of 10 degrees to 15 degrees of inclination, the deacidification effect is gradually enhanced along with the increase of the inclination, in the range of 15 degrees to 30 degrees of inclination, the deacidification effect is gradually weakened along with the increase of the inclination, the inclination mainly influences the heat and mass transfer between gas and solid, when the inclination is between 10 degrees and 15 degrees, the contact area of the gas and solid on the cyclone plate 6 is increased along with the increase of the angle, the residence time is prolonged, the deacidification effect is better and better, when the inclination is between 15 degrees and 30 degrees, the angle is increased for the inner cyclone plate, the rotation intensity of airflow is influenced, the energy of unit gas loss is more, the heat and mass transfer effect is weakened, and the deacidification effect is also reduced to some extent.
Examples 12 to 15
The pitch of the swirling sheets 62 of the internal rotation swirling plates is changed to be 4.5, 5.5, 6.5 and 7 respectively, and the number of the swirling sheets 62 in each swirling plate 6 is changed according to the formulaThe pitch was determined and the experiment was performed under the same conditions as in example 1.
Experiments were conducted to obtain the pH values shown in fig. 7 under the condition of the pitches of the cyclone sheets 62 of different internal rotation cyclone plates, and the following conclusion was obtained: the deacidification effect is gradually increased along with the increase of the spacing in the range of 4.5-5.0 cm between the swirling sheets 62 of the inner swirling flow plate, and is gradually weakened along with the increase of the spacing in the range of 5.0-7.0 cm between the swirling sheets 62 of the inner swirling flow plate. In the range of 4.5-5.0 cm, the resistance is smaller when the gas-solid phase passes through the cyclone plate 6 to do internal rotation movement along with the increase of the interval gap, the gas-phase turbulence is increased, and the deacidification effect of the powder on the cyclone plate 6 is gradually enhanced. When the space between the cyclone sheets is 5.0-7.0 cm. Under the same operation condition, as the interval gap is increased, the powder back mixing phenomenon is aggravated, the mass transfer area is reduced, and the deacidification effect of the powder on the cyclone plate 6 is gradually weakened.
Examples 16 to 19
The spacing of the swirling sheets 62 of the outer swirling plates is changed to be 2.0, 2.5, 4.0 and 5.0 respectively, and the number of the swirling sheets 62 in each swirling plate 6 is changed according to the formulaThe pitch was determined and the experiment was performed under the same conditions as in example 1.
Experiments were conducted to obtain the pH values shown in fig. 8 under the condition of the pitches of the cyclone sheets 62 of different external cyclone plates, and the following conclusion was reached: in the range of 2.0-3.0 of the interval between the swirling sheets 62 of the external swirling plate, the deacidification effect is gradually enhanced along with the increase of the interval, in the range of 3.0-5.0, the deacidification effect is gradually weakened along with the increase of the interval, in the range of 2.0-3.0 cm, the resistance of the gas in the swirling plate 6 during external swirling motion is smaller along with the increase of the interval gap, the external swirling strength of the gas flow is larger, the deacidification effect of the powder on the swirling plate 6 is gradually enhanced, and when the interval of the swirling sheets 62 is 3.0-5.0 cm, the gas resistance is relatively larger for the external swirling plate along with the increase of the interval gap, the powder back mixing phenomenon is aggravated, the energy loss of the gas per unit volume is larger, and the deacidification effect of the powder on the swirling plate 6 is gradually weakened.
Claims (9)
1. The system for deacidifying the superfine powder is characterized by comprising a superfine powder feeder, an air inlet system, a primary deacidification system, a multistage gas-solid countercurrent deacidification module and an energy recovery system, wherein the primary deacidification system is circularly connected with the multistage gas-solid countercurrent deacidification module to form a loop, the superfine powder feeder is arranged on a feeding pipeline of the primary deacidification system, the air inlet system is connected with the multistage gas-solid countercurrent deacidification module, and the energy recovery system is used for recycling waste gas heat;
the primary deacidification system comprises a cyclone (1), a cloth bag separator (2), a star-shaped discharger (15) and a venturi conveyor (11), wherein the top outlet of the cyclone (1) is connected with the side inlet of the cloth bag separator (2), the star-shaped discharger (15) and the venturi conveyor (11) are sequentially arranged at the lower discharge outlet of the cloth bag separator (2), the multistage gas-solid countercurrent deacidification module is connected with the cloth bag separator (2) to form a loop, and the multistage gas-solid countercurrent deacidification module is sequentially connected with the cyclone (1) and the cloth bag separator (2) to form a loop; the gas-solid countercurrent deacidification module comprises a cyclone (1), a cyclone separator (3), a star-shaped discharging device (15) and a venturi conveyor (11), wherein the top outlet of the cyclone (1) is connected with the side inlet of the cyclone separator (3), the star-shaped discharging device (15) and the venturi conveyor (11) or a discharging device are sequentially arranged below the cyclone separator (3), N gas-solid countercurrent deacidification modules are sequentially connected to form a loop, and the value of N is 1-5.
2. The system for deacidifying ultrafine powder according to claim 1, wherein the air inlet system comprises a filter (14), an electric heater (4) and a blower, the filter (14), the blower and the electric heater (4) are connected in sequence through pipelines, and the electric heater (4) is connected with the multistage gas-solid countercurrent deacidification module through a pipeline.
3. The system for deacidifying ultrafine powder according to claim 1, wherein the ultrafine powder feeder comprises a hopper (10) and a venturi conveyor (11), and the venturi conveyor (11) is arranged on a pipeline of the primary deacidification system, which is circularly connected with the multistage gas-solid countercurrent deacidification module.
4. The system for deacidifying ultrafine powder according to claim 2, wherein the energy recovery system comprises a preheater (5), a cooler (7), a circulating pump (8) and a heat exchange medium circulating tank (9), wherein the preheater (5) is arranged at the front end of an inlet of the electric heater (4), the cooler (7) is arranged on an air outlet pipeline above the cloth bag separator (2), the preheater (5) and the cooler (7) are connected into a loop to realize heat exchange, and the heat exchange medium circulating tank (9) and the circulating pump (8) are arranged on the loop.
5. A system for deacidification of ultrafine powder according to claim 1, characterized in that 2-20 cyclone plates (6) are arranged in the cyclone (1), the cyclone plates (6) comprise an inner cyclone plate and an outer cyclone plate, the inner cyclone plate and the outer cyclone plate are alternately distributed up and down, the cyclone plates (6) are divided into a plurality of areas by a plurality of separating plates (61), cyclone plates (62) are obliquely arranged in each area, the cyclone plates (62) of the outer cyclone plate are obliquely inclined downwards towards the central point, and the cyclone plates (62) of the inner cyclone plate are obliquely inclined upwards towards the central point.
6. The system for deacidification of ultrafine powder as set forth in claim 5, wherein the swirling sheets (62) are arranged in a louver type, the swirling sheets (62) of the outer swirling plate are inclined at an angle ranging from 10 to 30 °, the swirling sheets (62) of the inner swirling plate are inclined at an angle ranging from 35 to 70 °, and the distance e between the swirling sheets (62) is set to
D is the diameter of the cyclone plate (6), D is the thickness of the cyclone sheet (62), M is the total number of the cyclone sheets (62) of each cyclone plate (6), and θ is the inclination angle of the cyclone sheet (62).
7. A system for the deacidification of ultrafine powders as claimed in claim 1, characterized in that the discharge means below the cyclone (3) of the nth stage is a double butterfly valve discharge (12) for the collection of the final product; the outside of the cloth bag separator (2) is also provided with a vibrator (13).
8. A process for deacidifying ultra-fine powder using the system of claim 4, comprising the steps of:
1) Starting a blower, an electric heating device (4) and a circulating pump (8) to enable hot air to sequentially pass through a multistage gas-solid countercurrent deacidification module and a primary deacidification system, and adding a heat exchange medium into a heat exchange medium circulating tank (9) to enable an energy recovery system to circulate;
2) After the temperature is stable, adding the superfine powder material into a cyclone (1) of a primary deacidification system through a superfine powder feeder for primary deacidification, allowing the deacidified material to enter a cloth bag separator (2) for gas-solid separation, cooling and blowing out gas from the upper part of the cloth bag separator (2), allowing solids to enter a multistage gas-solid countercurrent deacidification module for multistage deacidification, and collecting the deacidified materials after deacidification is completed.
9. The process according to claim 8, wherein the heat exchange medium in the heat exchange medium circulation tank (9) is water when the temperature of the hot air after primary deacidification is less than 100 ℃, the heat exchange medium in the heat exchange medium circulation tank (9) is heat transfer oil when the temperature of the hot air after primary deacidification is greater than 100 ℃, the temperature of the exhaust gas after cooling by the cooler (7) is 50 ℃ to 80 ℃, and then the exhaust gas is discharged from the system by the induced draft fan.
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