CN210419773U - Equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale - Google Patents
Equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale Download PDFInfo
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- CN210419773U CN210419773U CN201920982420.2U CN201920982420U CN210419773U CN 210419773 U CN210419773 U CN 210419773U CN 201920982420 U CN201920982420 U CN 201920982420U CN 210419773 U CN210419773 U CN 210419773U
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Abstract
The equipment system for preparing the anhydrite powder from the industrial waste residue phosphogypsum in a large scale comprises a material distribution device, a vertical mill dust collection device, a raw powder conveying device, a raw powder warehouse, a raw powder metering, feeding and conveying device, a combined cyclone preheater, a fluidized bed furnace, a hot blast furnace, a heat exchange conveyor, a cooked powder conveying device and a cooked powder warehouse. Utilize the utility model discloses equipment system to industrial waste residue ardealite is raw materials system anhydrite powder, can directly absorb hydrous ardealite in a large number, carries out synchronous modification, drying, grinding to hydrous ardealite to can accomplish "dehydration + calcination" process fast, and easily effective control calcination quality, the energy consumption is low.
Description
Technical Field
The utility model relates to an anhydrite cementing material makes technical field, concretely relates to equipment system of anhydrite powder is made with industrial waste residue ardealite to scale.
Background
The existing anhydrite cementing material is generally prepared by grinding natural anhydrite and adding an activating agent, or calcining dihydrate gypsum in a rotary kiln to convert the dihydrate gypsum into the anhydrite and then grinding the anhydrite and the compound activating additive.
In the method for preparing anhydrite powder by utilizing various industrial waste gypsums, in particular industrial waste residue phosphogypsum, the prior advanced technology and equipment adopt a three-rotary kiln three-stage combined process, wherein a first-stage rotary kiln in the combined process equipment is a drying rotary kiln (namely a rotary drum type dryer), a second-stage rotary kiln for calcining (preparing anhydrite) (namely a directly-heated rotary roasting furnace) and a third-stage rotary kiln for cooling powder (namely a rotary drum type cooler), and the calcined and cooled anhydrite powder is ground to prepare the anhydrite powder.
The traditional equipment system of calcining in the rotary kiln and grinding or the current advanced equipment system of combining the three-stage rotary kiln and grinding have the problems of over-burning or under-burning in the roasting quality, and have high energy consumption and low productivity.
The limitation of the prior advanced process and the equipment system thereof in the technical aspect leads the production scale to be mostly in the productivity range of 10-30 t/a. The consumption and treatment capacity of the productivity of 10-30 t/a is obviously insufficient for the scale of phosphogypsum with the stockpiling amount of hundreds of millions of tons and the emission total amount of nearly 5000 ten thousand tons newly increased in the year.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is, overcome prior art's not enough, provide one kind and be convenient for directly absorb aqueous phosphogypsum in a large number, the dry grinding of synchronous modification to can accomplish "dehydration + calcination" process fast, and easily effective control calcination quality, the equipment system of making anhydrite powder with industrial waste residue phosphogypsum that the energy consumption is low.
The utility model provides a technical scheme that its technical problem adopted is, the equipment system of industrial waste residue ardealite system anhydrite powder is used to the scale, mainly includes: the combined cyclone preheater is formed by combining at least two stages of cyclone preheaters which are sequentially connected from bottom to top, namely at least a first cyclone preheater and a second cyclone preheater, each stage of cyclone preheater comprises an upper air outlet ascending pipeline at the upper part, a bottom discharging pipeline with an air locking flap valve and an air material inlet at the upper part of the side part, and an air outlet ascending pipeline of the next stage of cyclone preheater is connected with the air material inlet of the previous stage of cyclone preheater; the material distributing device is connected with a feed inlet of a vertical mill, an air outlet of the vertical mill is connected with an air inlet of a dust collecting device of the vertical mill, a powder outlet of the dust collecting device of the vertical mill is connected with a feed inlet of a raw powder conveying device, a discharge outlet of the raw powder conveying device is connected with a feed inlet of a raw powder warehouse, a warehouse bottom discharge port of the raw powder warehouse is connected with a feed inlet of a raw powder meter feeding conveying device, a discharge outlet of the raw powder meter feeding conveying device is connected with a feed inlet of a second cyclone preheater, a discharge pipeline of the second cyclone preheater of a combined cyclone preheater is connected with a feed inlet of a fluidized bed furnace, an air outlet of the upper part of the fluidized bed furnace is connected with an air inlet of a first cyclone preheater of the cyclone combined preheater, a discharge pipeline of the first cyclone preheater of the cyclone combined preheater is connected with a feed inlet of a heat exchange conveyor, a discharge outlet of the heat exchange conveyor is, the outlet of the cooked powder conveying device is connected with the inlet of the cooked powder warehouse, the hot air outlet of the heat exchange conveyor is connected with the air inlet pipeline of the hot blast stove, the hot air outlet of the hot blast stove is respectively connected with the hot air inlets of the vertical mill and the fluidized bed furnace through pipelines, and the waste gas outlet of the top cyclone preheater of the combined cyclone preheater is connected with the hot air inlet of the vertical mill through a pipeline.
Further, the combined type cyclone preheater further comprises a third cyclone preheater, or further comprises a fourth cyclone preheater, or further comprises a fifth cyclone preheater.
It can be seen that the combined type cyclone preheater may be formed by combining two to five stages of cyclone preheaters.
Further, the lower part or the middle lower part of the fluidized bed furnace is also provided with a fuel combustion device, and the fuel combustion device can provide all or part of the heat energy required by the fluidized bed furnace.
Further, a vertical mill hot air furnace is also arranged, and the vertical mill hot air furnace is connected with a hot air inlet of the vertical mill through a pipeline.
Further, a fluidized bed furnace hot blast stove is also arranged, and the fluidized bed furnace hot blast stove is connected with a hot blast inlet of the fluidized bed furnace through a pipeline.
Further, the proportioning device is a phosphogypsum feeding device.
Further, the material distribution and feeding device further comprises a modifier feeding device and/or an additive feeding device.
Furthermore, the dust collecting device of the vertical mill is composed of a cyclone separator, a fan and a dust collector which are connected in sequence.
The utility model discloses the usable current dry process rotary kiln cement production line's of equipment system raw material vertical mill system, the dore furnace and the five-stage preheater system transformation of kiln tail form with industrial waste residue ardealite system anhydrite powder for the scale, as the equipment system of a large amount of ardealite system anhydrite powder that dissolves.
The utility model discloses the basic process flow who equips the system does: the method comprises the following steps that (1) water-containing phosphogypsum (bulk material or block material) and a modification additive are continuously fed into a vertical mill through a dosing device, hot air is supplied to the vertical mill by a hot air furnace at the beginning, under the normal operation condition, heat energy can be supplied by waste gas waste heat at an outlet of a combined cyclone preheater, the phosphogypsum entering the vertical mill is modified, dried and ground, then enters a dust collecting device of the vertical mill along with waste gas flow, raw powder collected by the dust collecting device of the vertical mill is conveyed into a raw powder warehouse, the raw powder is continuously conveyed into the combined cyclone preheater and a fluidized bed furnace through metering to rapidly complete dehydration roasting to form anhydrite powder, and the continuously discharged heat anhydrite powder is conveyed into a calcined powder (anhydrite powder) warehouse after the waste heat; the recovered waste heat is recycled by the fluidized bed furnace.
The technical principle and the technical advantages of the utility model: 1) The energy-saving vertical mill system can be used for drying and grinding the industrial waste residue water-containing phosphogypsum into dry powder by utilizing the characteristics of low energy consumption, high capacity and strong adaptability to materials of the energy-saving vertical mill system which is mature and applied in other industries such as cement and other production industries, stripping impurities on phosphogypsum crystal particles and organic impurities wrapped in cluster gypsum crystals to purify the gypsum crystals, and is easy to synchronously implement modification, drying and grinding of the phosphogypsum so as to create conditions for quick roasting of the phosphogypsum and full ablation of the organic impurities; 2) the combined cyclone preheater and fluidized bed furnace, namely the 'dehydration and roasting' of the 'second-to-fifth-stage cyclone preheater and fluidized bed furnace', are utilized to prepare a anhydrite powder system by hot air flow and powder, so that the efficiency is high, the energy is saved, the traditional ardealite roasting control concept is broken through, the dry powder of ardealite is rapidly dehydrated and preheated within 8-40 seconds, then, the ardealite is roasted within 5-15 seconds within the temperature range of 700-950 ℃ in the fluidized bed furnace, organic impurities are ablated, the densification of anhydrite crystals can be inhibited, and the under-burning and the over-burning are easily prevented; meanwhile, the waste heat of the anhydrite powder is recycled by the heat exchange type conveyor device and is recycled by a fluidized bed furnace system, and the waste heat of the waste gas at the outlet of the combined cyclone preheater of the dehydration roasting system is used as a main heat source of a vertical grinding dry powder system, so that the energy consumption is saved to the maximum extent; 3) the scale of the consumed phosphogypsum is easy to reach 3000-10000 tons/day, the automatic control is easy to realize, and the product quality is stable.
Drawings
Fig. 1 is a schematic structural view of an embodiment 1 of the utility model equipment system;
FIG. 2 is a schematic structural view of embodiment 2 of the equipment system of the present invention;
fig. 3 is a schematic structural diagram of embodiment 3 of the utility model equipment system.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
Example 1
As shown in fig. 1, the present embodiment mainly includes a material preparing and feeding device 1, a vertical mill 2, a vertical mill dust collecting device 3, a raw powder conveying device 4, a raw powder warehouse 5, a raw powder metering, feeding and conveying device 6, a two-stage combined cyclone preheater 7, a fluidized bed furnace 8, a hot blast furnace 9, a heat exchange conveyor 10, a cooked powder conveying device 11, and a cooked powder warehouse 12, the feeding and proportioning device 1 comprises a phosphogypsum feeding device 101 and a modifier feeding device 102, the vertical mill dust collecting device 3 comprises a cyclone separator 301, a fan 302 and a dust collector 303 which are connected in sequence, the two-stage combined type cyclone preheater 7 is formed by combining a first cyclone preheater 7A and a second cyclone preheater 7B which are sequentially connected from bottom to top, each stage of cyclone preheater comprises an air outlet ascending pipeline at the upper part, a discharge pipeline at the bottom part and provided with an air-locking flap valve, and an air material inlet at the lateral upper part, and the air outlet ascending pipeline of the next stage of cyclone preheater is connected with the air material inlet of the previous stage of cyclone preheater; the phosphogypsum feeding device 101 and the modifier feeding device 102 of the phosphogypsum feeding device 1 are connected with a feeding hole of a vertical mill 2, a hot air outlet of a hot air furnace 9 is connected with a hot air inlet of the vertical mill 2 by a pipeline, an air material outlet of the vertical mill 2 is connected with an air material inlet of a cyclone separator 301 by a pipeline, a dust-containing air outflow air inlet of the cyclone separator 301 is connected with an air inlet of a fan 302 by a pipeline, an air outlet of the fan 302 is connected with an air inlet of a dust collector 303 by a pipeline, a feeding hole of a raw powder conveying device 4 is connected with powder outlets of the cyclone separator 301 and the dust collector 303, a discharging hole of a raw powder conveying device 4 is connected with a feeding hole of a raw powder warehouse 5, a feeding hole of a raw powder metering and feeding conveying device 6 is connected with a discharging hole at the bottom of the raw powder warehouse 5, a discharging hole at the tail end of the raw powder metering and feeding conveying device 6 is connected with, a discharge pipeline of a second cyclone preheater 7B in the second-stage combined preheater 7 is connected with a feed inlet of a fluidized bed furnace 8, an air outlet at the top of the fluidized bed furnace 8 is connected with an air inlet of a first cyclone preheater 7A of the second-stage combined preheater 7, a discharge pipeline of the first cyclone preheater 7A of the second-stage combined cyclone preheater 7 is connected with a feed inlet of a heat exchange conveyor 10, a discharge outlet of the heat exchange conveyor 10 is connected with a feed inlet of a cooked powder conveying device 11, a discharge outlet of the cooked powder conveying device 11 is connected with a feed inlet of a cooked powder warehouse 12, residual hot air of the heat exchange conveyor 10 is connected with an air inlet of a hot blast stove 9 through a pipeline, hot air outlets of the hot blast stove 9 are respectively connected with hot air inlets of the vertical mill 2 and the fluidized bed furnace 8 through pipelines, and a waste gas outlet of the top cyclone preheater (i.e. the second cyclone preheater) 7B of the second-stage combined cyclone preheater 7 is.
The working process is as follows: the hot blast stove 9 provides mill-entering hot blast from the vertical mill 2 through a hot blast pipeline (in the initial operation stage, the hot blast required by the vertical mill 2 is supplied by the hot blast stove 9), the phosphogypsum is continuously fed into the vertical mill 2 from a feed inlet of the vertical mill 2 by the phosphogypsum feeding device 1 (a proper amount of modifier can be added if necessary, the modifier is fed into the vertical mill 2 through the modifier feeding device 102), the water-containing phosphogypsum material entering the vertical mill 2 is simultaneously and efficiently modified, dried and ground, the ground material is discharged from an upper air material outlet of the vertical mill 2 along with wet hot air flow and directly enters the cyclone separator 301 through a connecting pipeline, coarse particle powder separated and collected by the cyclone separator 301 is discharged through a powder outlet and is sent into the raw powder warehouse 5 through the raw powder conveying device 4, dust-containing air flow of the cyclone separator 301 is discharged from an air outlet of the cyclone separator 301 and is induced into the dust collector 303 through a fan 302 through the connecting pipeline, the wet waste gas is purified by the dust collector 303 and then is discharged from the waste gas outlet of the dust collector 303, the fine particle powder collected by the dust collector 303 is discharged from the powder outlet of the dust collector 303, the raw meal is conveyed into a raw meal bin 5 through a raw meal conveying device 4, the raw meal in the raw meal bin 5 is conveyed into a feed inlet of a second cyclone preheater 7B of a two-stage combined cyclone preheater 7 through a bin bottom raw meal metering, feeding and conveying device 6 and is preheated by the second cyclone preheater 7B, discharging the mixture into a fluidized bed furnace 8 through a discharge pipeline, controlling the temperature of a dense phase zone at the bottom of the fluidized bed furnace 8 to be 800-950 ℃, the temperature of a dilute phase zone to be 820-860 ℃ and the temperature of a hearth outlet to be 810-850 ℃, roasting to anhydrite at the temperature of 800-950 ℃ in the fluidized bed furnace region within the time range of 9-11 seconds of passing through the fluidized bed furnace 8, ablating organic impurities and simultaneously inhibiting the densification of anhydrous gypsum crystals; the hot anhydrite powder continuously discharged from the fluidized bed furnace 8 is conveyed into a calcined powder (namely anhydrite powder) warehouse 12 through a calcined powder conveying device 11 after waste heat is recovered through a heat exchange conveyor 10, and the waste heat recovered by the heat exchange conveyor 10 is supplied to a hot blast stove 9 for cyclic utilization so as to save energy consumption.
Example 2
As shown in fig. 2, the embodiment mainly includes a feeding device 1, a vertical mill 2, a dust collecting device 3 of the vertical mill, a raw powder conveying device 4, a raw powder warehouse 5, a raw powder metering, feeding and conveying device 6, a three-stage combined cyclone preheater 7, a fluidized bed furnace 8, a hot blast furnace 9a of the vertical mill, a heat exchange conveyor 10, a cooked powder conveying device 11 and a cooked powder warehouse 12, wherein the feeding device 1 includes a phosphogypsum feeding device 101, the vertical mill dust collecting device 3 includes a cyclone separator 301, a fan 302 and a dust collector 303 which are sequentially connected, the three-stage combined cyclone preheater 7 is composed of a first cyclone preheater 7A, a second cyclone preheater 7B and a third cyclone preheater 7C which are sequentially connected from bottom to top, each stage of cyclone preheater includes an upper air outlet pipeline at the upper part, a discharge pipeline with an air-locking flap valve at the bottom part and an air inlet at the upper part of a side part, the upper air outlet pipeline of the next stage of the cyclone preheater is connected with the air, the phosphogypsum feeding device 101 of the phosphogypsum feeding device 1 is connected with a feeding hole of a vertical mill 2, a hot air outlet of a hot air furnace 9a of the vertical mill is connected with a hot air inlet of the vertical mill 2 by a pipeline, an air outlet of the vertical mill 2 is connected with an air inlet of a cyclone separator 301 by a pipeline, a dust-containing air outflow air inlet of the cyclone separator 301 is connected with an air inlet of a fan 302 by a pipeline, an air outlet of the fan 302 is connected with an air inlet of a dust collector 303 by a pipeline, a feeding hole of a raw powder conveying device 4 is connected with powder outlets of the cyclone separator 301 and the dust collector 303, a discharging hole of the raw powder conveying device 4 is connected with a feeding hole of a raw powder warehouse 5, a feeding hole of the raw powder metering, feeding and conveying device 6 is connected with a discharging hole of the raw powder warehouse 5, a discharging hole at the tail end of the raw powder metering, feeding and conveying device 6 is connected with, a discharge pipeline of a second cyclone preheater 7B in the three-stage preheater 7 is connected with a feed inlet of a fluidized bed furnace 8, a fuel combustion device 801 is arranged at the middle lower part of the fluidized bed furnace 8, an air outlet at the top of the fluidized bed furnace 8 is connected with an air inlet of a first cyclone preheater 7A of the three-stage preheater 7, a discharge pipeline of the first cyclone preheater 7A of the three-stage combined cyclone preheater 7 is connected with a feed inlet of a heat exchange conveyor 10, a discharge outlet of the heat exchange conveyor 10 is connected with a feed inlet of a cooked powder conveying device 11, a discharge outlet of the cooked powder conveying device 11 is connected with a feed inlet of a cooked powder warehouse 12, a waste heat air outlet of the heat exchange conveyor 10 is connected with the fuel combustion device 801 at the middle lower part of the fluidized bed furnace 8 and an air inlet at the bottom through pipelines, a waste gas outlet of a third cyclone preheater 7C of the three-stage combined cyclone preheater 7 is connected with a, the fuel combustion device 801 arranged at the middle lower part of the fluidized bed furnace 8 can provide all heat energy required by the fluidized bed furnace 8.
The working process is as follows: the vertical mill hot-blast stove 9a provides mill-entering hot air for the vertical mill 2 through a hot-blast pipeline (at the beginning, the hot air required by the vertical mill 2 is supplied by the hot-blast stove), the phosphogypsum feeding device 101 of the phosphogypsum feeding device 1 continuously feeds water-containing phosphogypsum into the vertical mill 2 from a feeding hole of the vertical mill 2, the water-containing phosphogypsum material entering the vertical mill 2 is simultaneously dried and ground efficiently, the ground material is discharged from an upper air material outlet of the vertical mill 2 along with wet hot air flow and directly enters the cyclone separator 301 through a connecting pipeline, coarse particle powder separated and collected by the cyclone separator 301 is discharged from a powder outlet and is sent to the raw powder warehouse 5 through the raw powder conveying device 4, the dust-containing air flow of the cyclone separator 301 is discharged from an air outlet of the cyclone separator 301, is induced by a connecting pipeline through a fan 302, enters the dust collector 303 from an air inlet of the dust collector 303, the wet waste gas is discharged from a waste gas outlet of the dust, discharging fine particle powder collected by a dust collector 303 through a powder outlet, conveying the fine particle powder into a raw powder warehouse 5 through a raw powder conveying device 4, preheating raw powder in the raw powder warehouse 5 through a raw powder meter feeding and conveying device 6 at the bottom of the warehouse, conveying the raw powder into a feed inlet of a third cyclone preheater 7C of a three-level combined type cyclone preheater 7, discharging the raw powder into a fluidized bed furnace 8 through a discharge pipeline after preheating through the third cyclone preheater 7C and a second cyclone preheater 7B, controlling the temperature of a dense phase region at the bottom of the fluidized bed furnace to 860-980 ℃, the temperature of a dilute phase region to 810-920 ℃ and the temperature of a hearth outlet to 800-910 ℃, roasting the calcined gypsum into anhydrite within 8-10 seconds within the temperature range of 810-980 ℃ in the fluidized bed furnace, ablating organic impurities and simultaneously inhibiting the densification of anhydrite crystals, recovering waste heat from the anhydrite powder continuously discharged from the fluidized bed furnace 8 through a heat exchange conveyor 10, conveying the calcined gypsum powder into a calcined powder (anhydrite powder) warehouse 12 through a, the waste heat recovered by the heat exchange conveyor 10 is supplied to the fluidized bed furnace 8 for cyclic utilization, so that the energy consumption is saved.
Example 3
As shown in fig. 3, the present embodiment mainly includes a raw powder feeding device 1, a vertical mill 2, a vertical mill dust collecting device 3, a raw powder conveying device 4, a raw powder warehouse 5, a raw powder meter feeding and conveying device 6, a five-stage combined cyclone preheater 7, a fluidized bed furnace 8, a vertical mill hot air furnace 9a, a fluidized bed furnace hot air furnace 9B, a heat exchange conveyor 10, a cooked powder conveying device 11, and a cooked powder warehouse 12, wherein the raw powder feeding device 1 includes a phosphogypsum feeding device 101, a modifier feeding device 102, and an additive feeding device 103, the vertical mill dust collecting device 3 includes a cyclone separator 301, a fan 302, and a dust collector 303 connected in sequence, the five-stage combined cyclone preheater 7 is formed by combining a first cyclone preheater 7A, a second cyclone preheater 7B, a third cyclone preheater 7C, a fourth cyclone preheater 7D, and a fifth cyclone preheater 7E connected in sequence from bottom to top, each stage of cyclone preheater comprises an air outlet ascending pipeline at the upper part, a discharge pipeline with an air-locking flap valve at the bottom and an air inlet at the upper part on the side, the air outlet ascending pipeline of the next stage of cyclone preheater is connected with the air inlet of the previous stage of cyclone preheater, the phosphogypsum feeding device 101, the modifier feeding device 102 and the additive feeding device 103 of the phosphogypsum feeding device 1 are connected with the feed inlet of the vertical mill 2, the hot air outlet of the hot air furnace 9a of the vertical mill is connected with the hot air inlet of the vertical mill 2 through a pipeline, the air outlet of the vertical mill 2 is connected with the air inlet of the cyclone separator 301 through a pipeline, the dust-containing air outflow port of the cyclone separator 301 is connected with the air inlet of the fan 302 through a pipeline, the air outlet of the fan 302 is connected with the air inlet of the dust collector 303 through a pipeline, the feed inlet of the raw powder conveying device 4 is connected with the powder, the discharge port of the raw powder conveying device 4 is connected with the feed port of the raw powder warehouse 5, the feed port of the raw powder metering, feeding and conveying device 6 is connected with the discharge port of the raw powder warehouse 5, the discharge port of the raw powder metering, feeding and conveying device 6 is connected with the feed port of the fifth cyclone preheater 7E of the five-stage combined cyclone preheater 7, the discharge pipeline of the second cyclone preheater 7B in the five-stage combined cyclone preheater 7 is connected with the feed port of the fluidized bed furnace 8, the air outlet at the top of the fluidized bed furnace 8 is connected with the air inlet of the first cyclone preheater 7A of the five-stage combined cyclone preheater 7, the discharge pipeline of the first cyclone preheater 7A of the five-stage combined cyclone preheater 7 is connected with the feed port of the heat exchange conveyer 10, the discharge port of the heat exchange conveyer 10 is connected with the feed port of the cooked powder conveying device 11, the discharge port of the cooked powder conveying device 11 is connected with the feed, the residual heat gas outflow port of the heat exchange conveyor 10 is connected with the air inlet of the fluidized bed furnace hot blast stove 9b through a pipeline, the hot air outlet of the fluidized bed furnace hot blast stove 9b is connected with the hot air inlet of the fluidized bed furnace 8 through a pipeline, and the waste gas outlet of the top cyclone preheater 7E (namely, the fifth cyclone preheater 7E) of the five-stage combined cyclone preheater 7 is connected with the hot air inlet of the vertical mill 2 through a pipeline.
The working process is as follows: the vertical mill hot-blast stove 9a provides mill hot-blast air for the vertical mill 2 through a hot-blast pipeline (at the beginning, the hot-blast air required by the vertical mill 2 is supplied by the hot-blast stove 9 a), the phosphogypsum feeding device 101, the modifier feeding device 102 and the additive feeding device 103 of the phosphogypsum matched feeding device 1 respectively continuously feed water-containing phosphogypsum, a modifier and an additive into the vertical mill 2 from a feeding hole of the vertical mill 2 according to a preset proportion, the water-containing phosphogypsum material entering the vertical mill 2 is simultaneously and efficiently modified, dried and ground, the ground material is discharged from an air material outlet at the upper part of the vertical mill 2 along with wet hot air flow and directly enters a cyclone separator 301 through a connecting pipeline, coarse particle powder separated and collected by the cyclone separator 301 is discharged through a powder outlet and is sent to a raw powder warehouse 5 through a raw powder conveying device 4, dust-containing air flow of the cyclone separator 301 is discharged from an air outlet of the cyclone separator 301 and is induced by a fan 302 through the connecting, the wet waste gas is purified by the dust collector 303 and then is discharged from the waste gas outlet of the dust collector 303, the fine particle powder collected by the dust collector 303 is discharged from the powder outlet, the powder is conveyed into the raw powder warehouse 5 by the raw powder conveying device 4, the raw powder in the raw powder warehouse 5 is conveyed into the feed inlet of the fifth cyclone preheater 7E of the five-stage combined cyclone preheater 7 by the raw powder metering, feeding and conveying device 6 at the bottom of the warehouse, is preheated by the fifth cyclone preheater 7E, the fourth cyclone preheater 7D, the third cyclone preheater 7C and the second cyclone preheater 7B, is discharged into the fluidized bed furnace 8 by a discharge pipeline, controls the temperature of the dense-phase zone at the bottom of the fluidized bed furnace to be 900-1050 ℃, the temperature of the dilute-phase zone to be 860-980 ℃, the temperature of the hearth outlet to be 850 ℃ and is calcined into the anhydrite within the temperature range of 850 ℃ to 1050 ℃ in the fluidized bed furnace for 6-8 seconds, ablates organic impurities and simultaneously inhibits the densification of, the hot anhydrite powder continuously discharged from the fluidized bed furnace 8 is conveyed into a calcined powder (namely anhydrite powder) warehouse 12 through a calcined powder conveying device 11 after waste heat is recovered through a heat exchange conveyor 10, and the waste heat recovered by the heat exchange conveyor 10 is supplied to a fluidized bed furnace hot blast stove 9b for cyclic utilization so as to save energy consumption.
Claims (10)
1. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale is characterized by mainly comprising the following components: the device comprises a material distribution and feeding device (1), a vertical mill (2), a vertical mill dust collection device (3), a raw powder conveying device (4), a raw powder warehouse (5), a raw powder metering and feeding conveying device (6), a combined cyclone preheater (7), a fluidized bed furnace (8), a hot blast stove (9), a heat exchange conveyor (10), a cooked powder conveying device (11) and a cooked powder warehouse (12), wherein the combined cyclone preheater (7) is formed by combining at least two stages of cyclone preheaters which are sequentially connected from bottom to top, namely at least a first cyclone preheater (7A) and a second cyclone preheater (7B), each stage of cyclone preheater comprises an upper air outlet ascending pipeline at the upper part, a discharge pipeline with an air-locking flap valve at the bottom and an air material inlet at the upper part at the side, and an air outlet ascending pipeline of a next stage of cyclone preheater is connected with the air material inlet of the previous stage of; the feed proportioning device (1) is connected with the feed inlet of a vertical mill (2), the air outlet of the vertical mill (2) is connected with the air inlet of a dust collecting device (3) of the vertical mill, the powder outlet of the dust collecting device (3) of the vertical mill is connected with the feed inlet of a raw powder conveying device (4), the discharge outlet of the raw powder conveying device (4) is connected with the feed inlet of a raw powder warehouse (5), the warehouse bottom discharge outlet of the raw powder warehouse (5) is connected with the feed inlet of a raw powder metering and feeding conveying device (6), the discharge outlet of the raw powder metering and feeding conveying device (6) is connected with the feed inlet of a cyclone (7), the discharge pipeline of a second cyclone preheater (7B) of a cyclone combined preheater (7) is connected with the feed inlet of a fluidized bed furnace (8), the air outlet at the upper part of the fluidized bed furnace (8) is connected with the air inlet of a first cyclone preheater (7A) of the combined cyclone preheater (7), the discharge pipeline of the first cyclone preheater (7A) of the combined cyclone preheater (7) is connected with the feed inlet of the heat exchange conveyor (10), the discharge port of the heat exchange conveyor (10) is connected with the inlet of the cooked powder conveying device (11), the outlet of the cooked powder conveying device (11) is connected with the inlet of the cooked powder warehouse (12), the hot air outlet of the heat exchange conveyor (10) is connected with the air inlet pipeline of the hot air furnace (9), the hot air outlet of the hot air furnace (9) is respectively connected with the vertical mill (2), the hot air inlet of the fluidized bed furnace (8) is connected with the pipeline, and the waste gas outlet of the top cyclone preheater of the combined cyclone preheater (7) is connected with the hot air inlet of the vertical mill (2) by the pipeline.
2. The equipment system for large-scale production of anhydrite powder from industrial waste residue phosphogypsum as claimed in claim 1, wherein the combined cyclone preheater (7) further comprises a third cyclone preheater (7C), or further comprises a fourth cyclone preheater (7D), or further comprises a fifth cyclone preheater (7E).
3. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale according to claim 1 or 2, characterized in that a fuel combustion device (801) is arranged at the lower part or the middle lower part of the fluidized bed furnace (8).
4. The equipment system for preparing the anhydrite powder from the industrial waste residue phosphogypsum in a large scale according to the claim 1 or the claim 2, and is characterized by further comprising a vertical mill hot air furnace (9 a), wherein the vertical mill hot air furnace (9 a) is connected with a hot air inlet of the vertical mill (2) through a pipeline.
5. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale according to claim 1 or 2, characterized by further comprising a fluidized bed furnace hot blast stove (9 b), wherein the fluidized bed furnace hot blast stove (9 b) is connected with a hot blast inlet of a fluidized bed furnace (8) through a pipeline.
6. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale according to claim 3, which is characterized by further comprising a fluidized bed furnace hot blast stove (9 b), wherein the fluidized bed furnace hot blast stove (9 b) is connected with a hot blast inlet of a fluidized bed furnace (8) through a pipeline.
7. The equipment system for preparing the anhydrite powder from the industrial waste residue phosphogypsum in a large scale according to claim 4, which is characterized by further comprising a fluidized bed furnace hot blast stove (9 b), wherein the fluidized bed furnace hot blast stove (9 b) is connected with a hot blast inlet of a fluidized bed furnace (8) through a pipeline.
8. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale according to claim 1 or 2, characterized in that the material distribution and feeding device (1) is a phosphogypsum feeding device (101).
9. The equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale according to claim 8, wherein the material distribution and feeding device (1) further comprises a modifier feeding device (102) and/or an additive feeding device (103).
10. The equipment system for preparing the anhydrite powder from the industrial waste residue phosphogypsum in a large scale according to the claim 1 or the claim 2, characterized in that the vertical mill dust collecting device (3) is composed of a cyclone separator (301), a fan (302) and a dust collector (303) which are connected in sequence.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920982420.2U CN210419773U (en) | 2019-06-27 | 2019-06-27 | Equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale |
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| CN201920982420.2U CN210419773U (en) | 2019-06-27 | 2019-06-27 | Equipment system for preparing anhydrite powder from industrial waste residue phosphogypsum in large scale |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110128040A (en) * | 2019-06-27 | 2019-08-16 | 长沙紫宸科技开发有限公司 | A kind of change system of scale consumption ardealite anhydrite powder |
| CN111662022A (en) * | 2020-07-01 | 2020-09-15 | 长沙紫宸科技开发有限公司 | Method for producing silicate clinker by using stone coal instead of tail coal and siliceous raw material |
-
2019
- 2019-06-27 CN CN201920982420.2U patent/CN210419773U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110128040A (en) * | 2019-06-27 | 2019-08-16 | 长沙紫宸科技开发有限公司 | A kind of change system of scale consumption ardealite anhydrite powder |
| CN110128040B (en) * | 2019-06-27 | 2023-10-20 | 长沙紫宸科技开发有限公司 | Equipment system for preparing anhydrite powder by large-scale phosphogypsum digestion |
| CN111662022A (en) * | 2020-07-01 | 2020-09-15 | 长沙紫宸科技开发有限公司 | Method for producing silicate clinker by using stone coal instead of tail coal and siliceous raw material |
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