CN115477558A - Rotary kiln internal circulation granular bed reactor and using method thereof - Google Patents
Rotary kiln internal circulation granular bed reactor and using method thereof Download PDFInfo
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- 238000000034 method Methods 0.000 title claims description 39
- 239000002994 raw material Substances 0.000 claims abstract description 45
- 239000002245 particle Substances 0.000 claims abstract description 33
- 239000012265 solid product Substances 0.000 claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 13
- 239000000376 reactant Substances 0.000 claims abstract description 12
- 238000000197 pyrolysis Methods 0.000 claims description 24
- 238000001035 drying Methods 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 21
- 238000000855 fermentation Methods 0.000 claims description 11
- 230000004151 fermentation Effects 0.000 claims description 11
- 238000001354 calcination Methods 0.000 claims description 10
- 239000000047 product Substances 0.000 claims description 10
- 238000000354 decomposition reaction Methods 0.000 claims description 7
- 238000007789 sealing Methods 0.000 claims description 7
- 239000007790 solid phase Substances 0.000 claims description 7
- 239000002912 waste gas Substances 0.000 claims description 7
- 238000009264 composting Methods 0.000 claims description 6
- 239000007787 solid Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 5
- 239000004568 cement Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 238000005266 casting Methods 0.000 claims description 3
- 239000003546 flue gas Substances 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 238000010304 firing Methods 0.000 claims description 2
- 230000001580 bacterial effect Effects 0.000 claims 1
- 238000009413 insulation Methods 0.000 abstract description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001603 reducing effect Effects 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
- C05F17/90—Apparatus therefor
- C05F17/921—Devices in which the material is conveyed essentially horizontally between inlet and discharge means
- C05F17/929—Cylinders or drums
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- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
- C05F17/90—Apparatus therefor
- C05F17/964—Constructional parts, e.g. floors, covers or doors
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- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
- C05F17/90—Apparatus therefor
- C05F17/964—Constructional parts, e.g. floors, covers or doors
- C05F17/971—Constructional parts, e.g. floors, covers or doors for feeding or discharging materials to be treated; for feeding or discharging other material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
- F27B7/32—Arrangement of devices for charging
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
- F27B7/33—Arrangement of devices for discharging
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
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- Mechanical Engineering (AREA)
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- Processing Of Solid Wastes (AREA)
Abstract
Compared with the traditional rotary kiln reactor, the rotary kiln internal circulation particle bed reactor is provided with the particle internal circulation device in the middle section of the kiln, partial particles at the tail end of the reaction can be returned to the head end of the reaction along the internal circulation pipeline, the raw materials and the tail end solid products can be fully and uniformly mixed along with the circumferential movement of the rotary kiln, the tail end solid products can provide various media for different reactions, a pouring material layer and an outer heat insulation layer are respectively arranged inside and outside the middle section of the kiln according to the friction performance and the application temperature among particles, and in order to control the residence time of reactants, baffles are arranged at the head end and the tail end of the middle section of the kiln.
Description
Technical Field
The invention belongs to the field of environmental protection, and particularly relates to a circulating granular bed reactor in a rotary kiln and a using method thereof.
Background
Biological drying and composting are commonly used in the recycling treatment process of high-moisture-content organic materials, but the traditional biological drying and composting technology has the problems that the material mixing and fermentation processes are carried out in different reactors, and the equipment investment is high; and the fermentation period is long, the water reducing effect in the drying process is not obvious, the decomposition degree in the composting process is not enough, and the like.
The problem of too long reaction time also exists in the organic matter pyrolysis and cement calcination process taking high-temperature gas as a heat source, and the problem can be solved at the cost of improving the length of the cylinder in the rotary kiln, so that the overall cost of the reactor is greatly increased, and a large economic burden is increased for the operation of related enterprises.
Disclosure of Invention
In order to overcome the defects of the existing production process, the invention provides the rotary kiln internal circulation granular bed reactor and the use method thereof.
The technical scheme of the invention is as follows:
a rotary kiln internal circulation granular bed reactor is formed by connecting a kiln head section 1, a kiln middle section 2 and a kiln tail section 3 in sequence;
the kiln head section 1 is provided with a feeding bin 4, a sealed feeding valve 5, a buffering bin 6, a feeding device 7 and a preheating device 8; the feeding bin 4 is arranged between two stages of sealed feeding valves 5, the outlet of the sealed feeding valve 5 at the bottom is connected with a buffer bin 6, feeding devices 7 are distributed at the bottom of the buffer bin 6, preheating devices 8 are distributed outside the buffer bin 6, gas outlets 9 are arranged on the preheating devices 8, and the gas inlets of the preheating devices 8 and the feeding devices 7 are communicated with the reaction bin of the middle section 2 of the kiln;
more than one group of particle internal circulation devices 10 are arranged in a reaction bin arranged at the middle section 2 of the kiln, the particle internal circulation devices 10 are provided with a conical inlet 11, a circulation pipeline 12 and a circulation material outlet 13 which are sequentially arranged from the tail end to the head end of the middle section 2 of the kiln, and a filter screen 14 can be additionally arranged at the front end of the conical inlet 11 according to different treatment raw materials; according to the difference of the friction performance and the application temperature among the particles, a casting material layer 15 and an outer heat-insulating layer 16 are respectively arranged inside and outside the middle section 2 of the kiln, in order to control the residence time of reactants, baffles 17 are locally arranged at the lower parts of the head end and the tail end of the middle section 2 of the kiln, and the baffles 17 do not rotate along with the middle section 2 of the kiln;
the kiln tail section 3 is provided with a solid-phase product outlet 18 and an air inlet 19.
The reactor has the following three use methods:
i, biological drying and composting process: raw materials to be processed are sent into a buffer bin 6 through a feeding bin 4 and a two-stage sealing feeding valve 5, are pushed to the head end of a kiln middle section 2 by a feeding device 7, along with the circumferential movement of a rotary kiln reactor, partial solid products at the tail end of the kiln middle section 2 enter a circulating pipeline 12 through a tapered inlet 11 of a particle internal circulating device 10 and return to the head end of the kiln middle section 2 through a circulating material outlet 13 in a counter-current mode, so that the raw materials and the solid products are fully and uniformly mixed, the water content and the number of florae of initial reactants are adjusted, the reaction starting time can be effectively shortened, and the temperature rise of the materials is promoted; meanwhile, high-temperature air is fed into the rotary kiln reactor through the air inlet 19, so that oxygen and a high-temperature background environment are provided for the fermentation process, and the total reaction time is further shortened; waste gas generated in the drying process is sent into a preheating device 8, is heated as an initial reactant in an indirect heat exchange mode and then is discharged from a gas outlet 9, after the fermentation process is finished, part of solid particles return to the head end of the middle section 2 of the kiln to be used as the raw material again in the fermentation process, so that the water content and the number of flora are adjusted, and the rest solid product is discharged from a solid product outlet 18;
II, pyrolysis process: the sealed feed valve 5 at the top of the device is opened, the sealed feed valve 5 at the bottom is closed, raw materials to be processed are sent into the feed bin 4, the sealed feed valve 5 at the top is closed after the raw materials reach a certain quantity, the sealed feed valve 5 at the bottom is opened, the raw materials are sent into the buffer bin 6 and pushed to the head end of the kiln middle section 2 by the feed device 7, along with the circumferential movement of the rotary kiln reactor, partial solid products at the tail end of the kiln middle section 2 enter the circulating pipeline 12 through the conical inlet 11 of the particle internal circulating device 10 and return to the head end of the kiln middle section 2 through the circulating material outlet 13 in a countercurrent mode, so that the raw materials and the solid products are fully and uniformly mixed, and the high-temperature solid products provide energy for the quick drying and pyrolysis of the raw materials; meanwhile, high-temperature inert gas is sent into the rotary kiln reactor through the gas inlet 19, so that energy and a high-temperature background environment are further provided for the pyrolysis process; pyrolysis volatile products generated in the pyrolysis process are sent into a preheating device 8, initial reactants are heated in an indirect heat exchange mode and then discharged from a gas outlet 9 to be condensed and collected, after the pyrolysis process is finished, partial solid particles return to the head end of the middle section 2 of the kiln to provide energy for quick drying and pyrolysis of the raw materials again, and residual solid products are discharged from a solid product outlet 18;
III cement calcination process: raw materials are fed into a buffer bin 6 through a feeding bin 4 and a two-stage sealing feeding valve 5 and pushed to the head end of the middle section 2 of the kiln by a feeding device 7, along with the circumferential movement of the rotary kiln reactor, partial clinker at the tail end of the middle section 2 of the kiln enters a circulating pipeline 12 through a conical inlet 11 of an in-particle circulating device 10 and returns to the head end of the middle section 2 of the kiln through a circulating material outlet 13 in a counter-current mode, so that the raw materials and the clinker are fully and uniformly mixed, and the high-temperature clinker provides energy for quick drying and preheating decomposition of the raw materials; meanwhile, high-temperature flue gas is sent into the rotary kiln reactor through the gas inlet 19 to further provide energy and a high-temperature background environment for the subsequent firing process; high-temperature waste gas generated in the calcining process is sent into a preheating device 8, secondary waste heat recovery is carried out after raw materials are heated and discharged from a gas outlet 9 in an indirect heat exchange mode, after the calcining process is finished, partial clinker is returned to the head end of the middle section 2 of the kiln to provide energy for quick drying and preheating decomposition of the raw materials again, and the residual clinker is discharged from a solid-phase product outlet 18.
The inclination angle of the whole set of device of the circulating granular bed reactor in the rotary kiln and the horizontal plane is 3-15 degrees, and the device is arranged in a way that the kiln head section 1 is higher than the kiln tail section 3 is lower.
When the device is used for the pyrolysis process, gaseous suction device is add to feeding storehouse 4, collects after taking out the combustible gas of sneaking into in feeding storehouse 4.
The conical inlet 11 of the particle internal circulation device 10 can be arranged at a certain position from the middle part to the tail end of the middle section 2 of the kiln according to different materials and reaction processes thereof.
The invention has the beneficial effects that:
(1) By the self-circulation of the particles in the reactor, various media can be provided for different reactions, and the reaction time is greatly reduced.
(2) Through the forced self-circulation mixing of particles in the device, the addition of other auxiliary equipment can be reduced, and further the total equipment investment and the occupied area are reduced.
(3) The equipment can be used together with other equipment, such as a fluidized bed for treating partial dangerous wastes, and has good use effect.
Drawings
FIG. 1 is a schematic view of the whole set of the apparatus of the present invention.
FIG. 2 is a three-dimensional layout of the in-kiln-middle-section particle circulating device of the invention.
In the figure: 1, a kiln head section; 2, middle section of the kiln; 3, a kiln tail section; 4, feeding a bin; 5, sealing the feeding valve; 6, a buffer bin; 7 a feeding device; 8, a preheating device; 9 air outlet; 10 an intra-granular circulation device; 11 a conical inlet; 12 a circulation line; 13 a circulating material outlet; 14, filtering a screen; 15 a casting material layer; 16 outer insulation layer; 17, a baffle plate; 18 a solid phase product outlet; 19 air inlet.
Detailed Description
The following further describes the specific embodiments of the present invention with reference to the drawings and technical solutions.
Examples
Biological drying and composting processes: raw materials to be processed are sent into a buffer bin 6 through a feeding bin 4 and a two-stage sealing feeding valve 5, are pushed to the head end of a kiln middle section 2 by a feeding device 7, along with the circumferential movement of a rotary kiln reactor, partial solid products at the tail end of the kiln middle section 2 enter a circulating pipeline 12 through a tapered inlet 11 of a particle internal circulating device 10 and return to the head end of the kiln middle section 2 through a circulating material outlet 13 in a counter-current mode, so that the raw materials and the solid products are fully and uniformly mixed, the water content and the number of florae of initial reactants are adjusted, the reaction starting time can be effectively shortened, and the temperature rise of the materials is promoted; meanwhile, high-temperature air is fed into the rotary kiln reactor through the air inlet 19, so that oxygen and a high-temperature background environment are provided for the fermentation process, and the total reaction time is further shortened; waste gas generated in the drying process is sent into a preheating device 8, the waste gas is heated as an initial reactant in an indirect heat exchange mode and then is discharged from a gas outlet 9, after the fermentation process is finished, part of solid particles return to the head end of the middle section 2 of the kiln to regulate the amount of water and flora in the fermentation process of the raw material again, and the rest solid product is discharged from a solid product outlet 18;
and (3) pyrolysis process: the sealed feed valve 5 at the top of the device is opened, the sealed feed valve 5 at the bottom is closed, raw materials to be processed are sent into the feed bin 4, the sealed feed valve 5 at the top is closed after the raw materials reach a certain quantity, the sealed feed valve 5 at the bottom is opened, the raw materials are sent into the buffer bin 6 and pushed to the head end of the kiln middle section 2 by the feed device 7, along with the circumferential movement of the rotary kiln reactor, partial solid products at the tail end of the kiln middle section 2 enter the circulating pipeline 12 through the conical inlet 11 of the particle internal circulating device 10 and return to the head end of the kiln middle section 2 through the circulating material outlet 13 in a countercurrent mode, so that the raw materials and the solid products are fully and uniformly mixed, and the high-temperature solid products provide energy for the quick drying and pyrolysis of the raw materials; meanwhile, high-temperature inert gas is sent into the rotary kiln reactor from the gas inlet 19 to further provide energy and a high-temperature background environment for the pyrolysis process; pyrolysis volatile products generated in the pyrolysis process are sent into a preheating device 8, initial reactants are heated in an indirect heat exchange mode and then discharged from a gas outlet 9 to be condensed and collected, after the pyrolysis process is finished, partial solid particles return to the head end of the middle section 2 of the kiln to provide energy for quick drying and pyrolysis of the raw materials again, and residual solid products are discharged from a solid product outlet 18;
and (3) cement calcination process: raw materials are fed into a buffer bin 6 through a feeding bin 4 and a two-stage sealing feeding valve 5 and pushed to the head end of the middle section 2 of the kiln by a feeding device 7, along with the circumferential movement of the rotary kiln reactor, partial clinker at the tail end of the middle section 2 of the kiln enters a circulating pipeline 12 through a conical inlet 11 of an in-particle circulating device 10 and returns to the head end of the middle section 2 of the kiln through a circulating material outlet 13 in a counter-current mode, so that the raw materials and the clinker are fully and uniformly mixed, and the high-temperature clinker provides energy for quick drying and preheating decomposition of the raw materials; meanwhile, high-temperature flue gas is sent into the rotary kiln reactor through the gas inlet 19, so that energy and a high-temperature background environment are further provided for the subsequent sintering process; high-temperature waste gas generated in the calcining process is sent into a preheating device 8, secondary waste heat recovery is carried out after raw materials are heated and discharged from a gas outlet 9 in an indirect heat exchange mode, after the calcining process is finished, partial clinker is returned to the head end of the middle section 2 of the kiln to provide energy for quick drying and preheating decomposition of the raw materials again, and the residual clinker is discharged from a solid-phase product outlet 18.
The present invention includes but is not limited to the embodiment, and it should be noted that, for those skilled in the art, other substitutions can be made without departing from the technical principle of the present invention, and these substitutions should also be regarded as the protection scope of the present invention.
Claims (5)
1. The rotary kiln internal circulation particle bed reactor is characterized by comprising a kiln head section (1), a kiln middle section (2) and a kiln tail section (3) which are sequentially connected;
the kiln head section (1) is provided with a feeding bin (4), a sealed feeding valve (5), a buffer bin (6), a feeding device (7) and a preheating device (8); the feeding bin (4) is arranged between the two stages of sealed feeding valves (5), the outlet of the sealed feeding valve (5) at the bottom is connected with the buffer bin (6), the feeding device (7) is distributed at the bottom of the buffer bin (6), the preheating device (8) is distributed outside the buffer bin (6), the preheating device (8) is provided with an air outlet (9), and the air inlet of the preheating device (8) and the feeding device (7) are communicated with the reaction bin of the middle kiln section (2);
more than one group of particle internal circulation devices (10) are arranged in the reaction bin of the kiln middle section (2), the particle internal circulation devices (10) are provided with a conical inlet (11), a circulation pipeline (12) and a circulation material outlet (13) which are sequentially arranged from the tail end to the head end of the kiln middle section (2), and a filter screen (14) can be additionally arranged at the front end of the conical inlet (11) according to different treatment raw materials; according to the difference of the friction performance and the application temperature among the particles, a casting material layer (15) and an outer heat-insulating layer (16) are respectively arranged inside and outside the middle section (2) of the kiln, in order to control the residence time of reactants, baffles (17) are locally arranged at the lower parts of the head end and the tail end of the middle section (2) of the kiln, and the baffles (17) do not rotate along with the middle section (2) of the kiln;
the kiln tail section (3) is provided with a solid-phase product outlet (18) and an air inlet (19).
2. The method for using a circulating granular bed reactor in a rotary kiln as recited in claim 1, wherein the reactor is used in three ways:
the biological drying and composting process comprises the following steps: raw materials to be processed are sent into a buffer bin (6) through a feeding bin (4) and a two-stage sealing feeding valve (5), are pushed to the head end of a kiln middle section (2) by a feeding device (7), along with the circumferential movement of a rotary kiln reactor, partial solid products at the tail end of the kiln middle section (2) enter a circulating pipeline (12) through a conical inlet (11) of a particle internal circulating device (10), and return to the head end of the kiln middle section (2) through a circulating material outlet (13) in a counter-current mode, so that the raw materials and the solid products are fully and uniformly mixed, the water content and the bacterial population quantity of initial reactants are adjusted, the reaction starting time is shortened, and the temperature rise of the materials is promoted; meanwhile, high-temperature air is sent into the rotary kiln reactor from the air inlet (19) to provide oxygen and a high-temperature background environment for the fermentation process, so that the total reaction time is further shortened; waste gas generated in the drying process is sent into a preheating device (8), is heated as an initial reactant in an indirect heat exchange mode and then is discharged from a gas outlet (9), after the fermentation process is finished, part of solid particles return to the head end of the middle section (2) of the kiln to be used as the raw material again in the fermentation process, so that the moisture and the number of floras are adjusted, and the rest solid product is discharged from a solid-phase product outlet (18);
(II) pyrolysis process: the sealed feed valve (5) at the top of the device is opened, the sealed feed valve (5) at the bottom is closed, raw materials to be treated are sent into the feed bin (4), the sealed feed valve (5) at the top is closed after the raw materials reach a certain number, the sealed feed valve (5) at the bottom is opened, the raw materials are sent into the buffer bin (6) and pushed to the head end of the kiln middle section (2) by the feed device (7), and along with the circumferential movement of the rotary kiln reactor, partial solid products at the tail end of the kiln middle section (2) enter the circulating pipeline (12) from the conical inlet (11) of the particle internal circulating device (10) and return to the head end of the kiln middle section (2) from the circulating material outlet (13) in a countercurrent mode, so that the raw materials and the solid products are fully and uniformly mixed, and the high-temperature solid products provide energy for the rapid drying and pyrolysis of the raw materials; meanwhile, high-temperature inert gas is sent into the rotary kiln reactor from the gas inlet (19) to further provide energy and a high-temperature background environment for the pyrolysis process; pyrolysis volatile products generated in the pyrolysis process are sent into a preheating device (8), the initial reactants are heated in an indirect heat exchange mode and then discharged from a gas outlet (9) to be condensed and collected, after the pyrolysis process is finished, partial solid particles return to the head end of the middle section (2) of the kiln to provide energy for quick drying and pyrolysis of the raw materials again, and residual solid products are discharged from a solid product outlet (18);
(III) cement calcination process: raw materials are fed into a buffer bin (6) through a feeding bin (4) and a two-stage sealing feeding valve (5), the raw materials are pushed to the head end of a middle kiln section (2) through a feeding device (7), along with the circumferential movement of a rotary kiln reactor, partial clinker at the tail end of the middle kiln section (2) enters a circulating pipeline (12) through a conical inlet (11) of a particle internal circulating device (10) and returns to the head end of the middle kiln section (2) through a circulating material outlet (13) in a countercurrent mode, so that the raw materials and the clinker are fully and uniformly mixed, and the high-temperature clinker provides energy for quick drying and preheating decomposition of the raw materials; meanwhile, high-temperature flue gas is sent into the interior of the rotary kiln reactor through a gas inlet (19) to further provide energy and a high-temperature background environment for the subsequent firing process; high-temperature waste gas generated in the calcining process is sent into a preheating device (8) and is discharged from a gas outlet (9) after being heated for the material in an indirect heat exchange mode, secondary waste heat recovery is carried out, after the calcining process is finished, partial clinker is returned to the head end of the middle section (2) of the kiln to provide energy for quick drying and preheating decomposition of the raw material again, and the residual clinker is discharged from a solid-phase product outlet (18).
3. The rotary kiln internal circulating particle bed reactor as claimed in claim 1, wherein the inclination angle of the rotary kiln internal circulating particle bed reactor to the horizontal plane is 3-15 degrees, and the rotary kiln internal circulating particle bed reactor is arranged in a manner that a kiln head section (1) is higher than a kiln tail section (3) and is lower than the kiln head section.
4. The method for using a circulating granular bed reactor in a rotary kiln according to claim 2, characterized in that when the circulating granular bed reactor in a rotary kiln is used in a pyrolysis process, a gas suction device is additionally arranged in the feeding bin (4) to suck out and collect combustible gas mixed in the feeding bin (4).
5. A rotary kiln internal circulating granular bed reactor as claimed in claim 1 or 3, characterized in that the conical inlet (11) of the granular internal circulating means (10) is arranged at a position from the middle to the end of the kiln intermediate section (2) according to different materials and their reaction processes.
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| CN202211109661.9A CN115477558A (en) | 2022-09-13 | 2022-09-13 | Rotary kiln internal circulation granular bed reactor and using method thereof |
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| CN202211109661.9A CN115477558A (en) | 2022-09-13 | 2022-09-13 | Rotary kiln internal circulation granular bed reactor and using method thereof |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130136674A1 (en) * | 2010-08-18 | 2013-05-30 | Jun Wei | Powder Lime Calcining Process and System |
| CN103215444A (en) * | 2013-04-27 | 2013-07-24 | 包头华美稀土高科有限公司 | Process for preventing rotary kiln from forming ring |
| CN105441132A (en) * | 2015-12-09 | 2016-03-30 | 张建臣 | Homogeneous progressive gasification furnace |
| CN113847809A (en) * | 2021-10-18 | 2021-12-28 | 亚德（上海）环保系统有限公司 | Material conveying structure for rotary kiln |
| CN114479890A (en) * | 2022-01-04 | 2022-05-13 | 江苏鹏飞集团股份有限公司 | Waste rubber thermal cracking rotary kiln system |
| CN216837823U (en) * | 2022-03-16 | 2022-06-28 | 四川君和环保股份有限公司 | Rotary furnace |
-
2022
- 2022-09-13 CN CN202211109661.9A patent/CN115477558A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130136674A1 (en) * | 2010-08-18 | 2013-05-30 | Jun Wei | Powder Lime Calcining Process and System |
| CN103215444A (en) * | 2013-04-27 | 2013-07-24 | 包头华美稀土高科有限公司 | Process for preventing rotary kiln from forming ring |
| CN105441132A (en) * | 2015-12-09 | 2016-03-30 | 张建臣 | Homogeneous progressive gasification furnace |
| CN113847809A (en) * | 2021-10-18 | 2021-12-28 | 亚德（上海）环保系统有限公司 | Material conveying structure for rotary kiln |
| CN114479890A (en) * | 2022-01-04 | 2022-05-13 | 江苏鹏飞集团股份有限公司 | Waste rubber thermal cracking rotary kiln system |
| CN216837823U (en) * | 2022-03-16 | 2022-06-28 | 四川君和环保股份有限公司 | Rotary furnace |
Non-Patent Citations (1)
| Title |
|---|
| 赵由才: "《生活垃圾处理与资源化技术手册》", 31 May 2007, 冶金工业出版社, pages: 670 - 671 * |
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