CN116535117A - Metakaolin preparation system and method capable of realizing decoupling function - Google Patents
Metakaolin preparation system and method capable of realizing decoupling function Download PDFInfo
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- CN116535117A CN116535117A CN202310508826.8A CN202310508826A CN116535117A CN 116535117 A CN116535117 A CN 116535117A CN 202310508826 A CN202310508826 A CN 202310508826A CN 116535117 A CN116535117 A CN 116535117A
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- decomposing furnace
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- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 title claims abstract description 107
- 238000002360 preparation method Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims description 21
- 238000001816 cooling Methods 0.000 claims abstract description 159
- 239000000463 material Substances 0.000 claims abstract description 89
- 239000000725 suspension Substances 0.000 claims abstract description 70
- 239000002994 raw material Substances 0.000 claims abstract description 35
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 22
- 239000001301 oxygen Substances 0.000 claims abstract description 19
- 239000007789 gas Substances 0.000 claims abstract description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 17
- 230000000694 effects Effects 0.000 claims abstract description 15
- 239000000446 fuel Substances 0.000 claims abstract description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 142
- 239000003546 flue gas Substances 0.000 claims description 142
- 239000005995 Aluminium silicate Substances 0.000 claims description 44
- 235000012211 aluminium silicate Nutrition 0.000 claims description 44
- 239000002826 coolant Substances 0.000 claims description 31
- 238000002485 combustion reaction Methods 0.000 claims description 19
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 239000000428 dust Substances 0.000 claims description 10
- 239000002918 waste heat Substances 0.000 claims description 10
- 238000010791 quenching Methods 0.000 claims description 9
- 230000000171 quenching effect Effects 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 8
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 239000002893 slag Substances 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000000779 smoke Substances 0.000 abstract description 18
- 238000005265 energy consumption Methods 0.000 abstract description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 27
- 238000000354 decomposition reaction Methods 0.000 description 19
- 239000004568 cement Substances 0.000 description 17
- 239000007787 solid Substances 0.000 description 17
- 238000000926 separation method Methods 0.000 description 11
- 239000000843 powder Substances 0.000 description 10
- 238000001354 calcination Methods 0.000 description 9
- 235000012054 meals Nutrition 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 238000009826 distribution Methods 0.000 description 7
- 230000002829 reductive effect Effects 0.000 description 7
- 239000004567 concrete Substances 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 239000002131 composite material Substances 0.000 description 3
- 230000002779 inactivation Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 229910052595 hematite Inorganic materials 0.000 description 2
- 239000011019 hematite Substances 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- CSDREXVUYHZDNP-UHFFFAOYSA-N alumanylidynesilicon Chemical compound [Al].[Si] CSDREXVUYHZDNP-UHFFFAOYSA-N 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005284 excitation Effects 0.000 description 1
- 238000001879 gelation Methods 0.000 description 1
- 229910052598 goethite Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- AEIXRCIKZIZYPM-UHFFFAOYSA-M hydroxy(oxo)iron Chemical compound [O][Fe]O AEIXRCIKZIZYPM-UHFFFAOYSA-M 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000003908 quality control method Methods 0.000 description 1
- 229910021646 siderite Inorganic materials 0.000 description 1
- 239000003469 silicate cement Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/38—Preparing or treating the raw materials individually or as batches, e.g. mixing with fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/36—Silicates having base-exchange properties but not having molecular sieve properties
- C01B33/38—Layered base-exchange silicates, e.g. clays, micas or alkali metal silicates of kenyaite or magadiite type
- C01B33/40—Clays
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/44—Burning; Melting
-
- 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
- F27B19/00—Combinations of furnaces of kinds not covered by a single preceding main group
- F27B19/04—Combinations of furnaces of kinds not covered by a single preceding main group arranged for associated working
-
- 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
- F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges
-
- 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
-
- 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
- F27D9/00—Cooling of furnaces or of charges therein
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Ceramic Engineering (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Inorganic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
The invention discloses a metakaolin preparation system capable of realizing a decoupling function and a preparation method thereof, comprising a suspension preheating system, a decomposing furnace system, a first cooling system, a second cooling system and a hot blast furnace system, wherein the decomposing furnace outlet is connected with the inlet of a final cyclone preheater, the material outlet of the final cyclone preheater is connected with the material inlet of the first cooling system, the discharge outlet of the penultimate cyclone preheater is connected with a decomposing furnace raw material feeding port, and a fuel feeding port is not arranged on the decomposing furnace; the oxygen content in the exhaust smoke of the suspension preheating system is 1-3%, the smoke outlet of the suspension preheating system is connected with the smoke inlet of the first cooling system, the smoke outlet of the first cooling system is connected with the smoke inlet of the decomposing furnace, the gas outlet of the second cooling system is connected with the combustion-supporting air inlet of the hot blast stove, and the smoke outlet of the hot blast stove is connected with the smoke outlet pipeline of the first cooling system. The invention can produce metakaolin meeting the requirements of color and activity index, and has low system energy consumption.
Description
Technical Field
The invention relates to the technical field of metakaolin preparation, in particular to a metakaolin preparation system and a metakaolin preparation method capable of achieving a decoupling function.
Background
Kaolin (Al) 2 O 3 ·2SiO 2 ·2H 2 O，AS 2 H 2 ) Is a common mineral in natural kaolin or kaolin tailings, and can generate a plurality of structural changes when heated in air, and the layered structure of the kaolin is destroyed by the removal of hydroxyl groups when heated to about 600 ℃ to form amorphous transition phase-metakaolin (Al) 2 O 3 ·2SiO 2 ，AS 2 ). Metakaolin has irregular molecular arrangement, presents thermodynamic prepositive state, has gelation property under alkali excitation, and can be matched with calcium hydroxide (Ca (OH) 2 ) The water reacts with the pozzolan to produce a highly active hydration product similar to cement.
By utilizing the characteristics, the mixed material is prepared by calcining the kaolin containing the kaolin and the aluminum-silicon minerals with similar structures, and then the mixed material is compounded with gypsum, silicate cement clinker or limestone to prepare the calcined kaolin-based composite cement, so that the calcined kaolin-based composite cement becomes a research hot spot in the international cement and concrete industry in recent years. The clinker consumption of the cement can be reduced from 70-75% to 45-50% by adopting the calcined kaolin with higher activity instead of clinker, the compressive strength of the cement for 28 days is kept not to be reduced, the flexural strength can be improved by more than 20%, and the technical aims of low clinker coefficient, low carbon emission and high strength in the cement preparation process are fulfilled.
Because the preparation cost of the calcined kaolin is lower than that of the clinker, CO in the preparation process of the calcined kaolin 2 The emission is lower than CO in the clinker preparation process 2 The emission and the raw materials of kaolin are very widely available, and the use of calcined kaolin in the concrete and cement industries to replace clinker in large amounts has a significant competitive advantage in reducing the clinker dosage in the cement in the context of the positive advancement of carbon emission reduction in the building concrete and cement industries.
The existing preparation methods of the calcined kaolin mainly comprise a fixed bed type, a semi-fixed bed type, a fluidized bed type, a suspension calcination type and the like. The method for preparing the calcined kaolin by adopting rotary kiln calcination and suspension calcination is a commonly adopted method, but when adopting rotary kiln calcination, the problems of high system heat consumption, easy overburning and inactivation of products, difficult quality control and the like often exist. Although the suspension calcination can effectively reduce the heat consumption of the system, the conventional suspension calcination often couples the combustion of fuel and the decomposition process of kaolin into a decomposing furnace, and the decomposition temperature of the kaolin is relatively narrow due to the relatively narrow decomposition temperature interval of the kaolin, so that the decomposition of the kaolin is incomplete (namely, so-called 'underburn') when the temperature in the decomposing furnace is relatively low; when the temperature in the decomposing furnace is higher, the kaolin is recrystallized and deactivated (namely, the so-called 'overburning'), so that the design and development difficulty of the suspension calcination decomposing furnace is obviously increased. On the other hand, kaolin materials typically contain some amount of iron, mainly in the form of goethite, hematite, siderite, and the like. The iron phase undergoes decomposition reaction during the kaolin calcination to finally form red hematite (iron phase forms Fe 3+ ) In a form such that the calcined kaolin appears visibly red. The direct use of red calcined kaolin to prepare cement affects the color of the finished cement product, and is easily mistaken as inferior cement by the market to affect sales. Thus, calcined kaolin with high activity and consistent color with cement clinker is produced with lower energy consumption and higher efficiency by reasonable process technologyIs key for mass production and wide application of calcined kaolin and calcined kaolin-limestone composite cement.
Therefore, based on market demands and the key technical problems faced by the market demands, the preparation system and the preparation method of the metakaolin which can realize the decoupling function fully consider the requirements of the cement concrete industry on the color control and the activity index control of the calcined kaolin, and solve the problems of high energy consumption, small processing capacity, difficult control of product quality and the like of the calcined kaolin preparation system at the same time have important practical significance.
Disclosure of Invention
The invention provides a metakaolin preparation system and a preparation method capable of realizing a decoupling function, which can fully consider the control requirements of the cement concrete industry on the color and activity index of a metakaolin finished product, produce metakaolin meeting the control requirements of the color and activity index, and solve the problems of high energy consumption, small processing capacity, difficult control of the product quality and the like of the metakaolin preparation system.
The invention is realized in such a way, a metakaolin preparation system capable of realizing a decoupling function comprises a suspension preheating system, a decomposing furnace system, a first cooling system, a second cooling system and a hot blast furnace system, wherein the decomposing furnace system comprises a decomposing furnace, the bottom of the decomposing furnace is a flue gas inlet, the top outlet of the decomposing furnace is connected with the inlet of a final cyclone preheater of the suspension preheating system, the material outlet at the bottom of the final cyclone preheater of the suspension preheating system is connected with the material inlet of the first cooling system, the discharge port of a penultimate cyclone preheater of the suspension preheating system is connected with a raw material feeding port of the decomposing furnace, the decomposing furnace is not provided with a fuel feeding port, and the temperature in the decomposing furnace is controlled to be 650-850 ℃;
the top flue gas outlet of the suspension preheating system is connected with the flue gas inlet of the indirect heat exchanger, the flue gas outlet of the indirect heat exchanger is connected with the flue gas inlet of the first cooling system, the first cooling system is used for quenching materials to a temperature range of 300-350 ℃ and below, and the flue gas outlet of the first cooling system is connected with the decomposing furnaceThe flue gas inlet of the suspension preheating system is connected, and the oxygen content in the flue gas discharged from the top of the suspension preheating system is 1-3%; the material outlet of the first cooling system is connected with the material inlet of the second cooling system, the gas outlet of the second cooling system is connected with the combustion air inlet of the hot blast stove system, and the flue gas outlet of the hot blast stove system is connected with the flue gas outlet pipeline of the first cooling system; o in flue gas at outlet of hot blast stove system 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm.
Preferably, the high-temperature flue gas temperature of the outlet of the hot blast stove system is controlled at 800-1000 ℃, the hot blast stove system comprises a hot blast stove, a fuel feeding port is arranged at the top of the hot blast stove, a combustion air inlet of the hot blast stove system is positioned at one side of the fuel feeding port, a slag discharging port is arranged at the bottom of the hot blast stove, and a flue gas outlet of the hot blast stove system is positioned at one side of the lower part of the hot blast stove. Preferably, the decomposing furnace is provided with a plurality of raw material feeding ports in the height direction, and the temperature distribution in the decomposing furnace can be controlled in a reasonable range by adjusting the raw material amount fed into the decomposing furnace, the smoke amount entering the decomposing furnace and the smoke temperature.
Preferably, the indirect heat exchanger is used for indirectly cooling the flue gas discharged by the suspension preheating system to 80-120 ℃, the bottom of the indirect heat exchanger is provided with a cooling medium inlet and a flue gas outlet, the top of the indirect heat exchanger is provided with a flue gas inlet and a cooling medium outlet, so that the flue gas and the cooling medium exchange heat in a countercurrent way, and the cooling medium channel of the indirect heat exchanger is internally communicated with the cooling medium.
Further preferably, the cooling medium of the indirect heat exchanger is cooling water, cooling oil or other suitable cooling medium.
Preferably, a flue gas circulating fan is respectively arranged between the indirect heat exchanger and the first-stage cyclone preheater of the suspension preheating system and between the indirect heat exchanger and the first cooling system.
Preferably, the gas outlet of the second cooling system is connected with the combustion air inlet of the hot blast stove system through the dust collector and the combustion air circulating fan in sequence.
Preferably, the second cooling system comprises at least one stage of cyclone cooler for cooling the material to below 100 ℃.
Preferably, the flue gas outlet of the suspension preheating system and the gas outlet of the second cooling system are also connected with a drying crusher or other waste heat utilization equipment.
The method for preparing metakaolin by adopting the system comprises the steps that raw materials enter a decomposing furnace after being preheated by a suspension preheating system, decomposed materials and generated hot flue gas leave the decomposing furnace and enter a final cyclone preheater of the suspension preheating system, and materials separated by the final cyclone preheater of the suspension preheating system enter a first cooling system; the flue gas discharged from the top of the suspension preheating system is cooled by an indirect heat exchanger and then enters a first cooling system to exchange heat with materials entering the first cooling system, the flue gas discharged from the first cooling system enters a decomposing furnace system, the gas discharged from the second cooling system enters a hot blast furnace system to support combustion, the high-temperature flue gas discharged from the hot blast furnace system is mixed with the flue gas discharged from the outlet of the first cooling system and then enters the decomposing furnace, the raw material quantity fed into the decomposing furnace, the flue gas quantity entering the decomposing furnace and the flue gas temperature are regulated, and the temperature in the decomposing furnace is controlled to be between 650 and 850 ℃, so that the kaolin is fully decomposed and not burned, and the activity index of the finished metakaolin meets the requirement of subsequent production; the first cooling system quenches the material to a temperature range of 300-350 ℃ and below, then the material enters the second cooling system, and the material is cooled by the second cooling system to obtain the metakaolin with controllable finished product color.
Preferably, the residence time of the flue gas in the decomposing furnace is 2-10 seconds.
Preferably, the high-temperature flue gas temperature of the hot blast stove outlet system is controlled to be 800-1000 ℃, and O in the flue gas 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm.
Preferably, the cooling medium of the first cooling system is flue gas with the temperature of 80-120 ℃ after being cooled by an indirect heat exchanger, the oxygen content in the flue gas is 1-3%, and the temperature of the flue gas at the outlet of the first cooling system is 500-600 ℃.
Preferably, the cooling medium of the second cooling system is normal-temperature air, and the temperature of the material cooled by the second cooling system is lower than 100 ℃.
The specific principle of the invention is as follows:
the key of the activity control of the metakaolin finished product is that the temperature field in the decomposing furnace system is uniformly controlled, the fuel combustion and material decomposition processes are completely decoupled, the first cooling system and the hot blast furnace system are reasonably designed, the enthalpy carried by the flue gas entering the decomposing furnace is ensured to promote the complete decomposition of the kaolin materials in the decomposing furnace system, meanwhile, the temperature of the flue gas can avoid the high-temperature inactivation of the kaolin materials, and the activity index of the metakaolin finished product is ensured to meet the subsequent production requirements.
The key of the color control of the finished metakaolin is decomposition control and cooling control, wherein the decomposition control needs to strictly control the decomposition atmosphere and the decomposition temperature; the cooling control requires a comprehensive control of the cooling atmosphere and the cooling temperature. In order to control the color of the finished metakaolin, the invention controls the excessive air coefficient of the outlet of the hot blast stove system in the process of decomposing and forming metakaolin by using the metakaolin, thereby realizing that the oxygen content in the kiln tail gas of the outlet of the hot blast stove system and the suspension preheating system is in the preferable oxygen content range, and simultaneously, considering that the content of the reducing gas CO of the outlet of the hot blast stove is controlled in a reasonable range of 1000-2000ppm, the Fe in the kaolin material in the decomposing furnace system is easy to be decomposed 3+ Reduction to Fe 2+ . In the cooling process of high-temperature metakaolin, the cooling atmosphere and the cooling temperature control need to be comprehensively considered. As proved by detailed experimental study, if the cooling medium of metakaolin is inert gas (such as N 2 Etc.) or low-oxygen flue gas (the oxygen concentration in the flue gas is preferably controlled to be 1-3 percent), and Fe in the metakaolin prepared by reductive decomposition 2+ Will not be oxidized into Fe again in the cooling link 3+ The method comprises the steps of carrying out a first treatment on the surface of the Also has experimental study to verify that Fe in the metakaolin prepared by reduction decomposition 2+ Is stable at 300-350deg.C and below, and will not be oxidized to Fe again even in contact with conventional air 3+ . Based on the theoretical research work, the oxygen concentration in the flue gas at the outlet of the suspension preheating system can be controlled to be 1-3%, so that the suspension preheating system is an ideal cooling medium, and meanwhile, the flue gas contains a certain amount of reducing gas COProtection of Fe in the primary quenching process of hot materials 2+ Will not be oxidized into Fe again 3+ Therefore, the invention can be used for realizing the first-stage quenching of the hot material, so the invention firstly fully cools the flue gas at the outlet of the suspension preheating system, then cools the hot material entering the first cooling system, and can realize the quenching of the hot material to a temperature range of 300-350 ℃ and below through detailed theoretical calculation. The material after the first-stage quenching enters a second cooling system and is cooled to about 100 ℃ by normal-temperature air.
In the process, according to the material flow direction, the kaolin raw material is subjected to a raw material pretreatment procedure to obtain raw material powder meeting the production requirement. The raw meal powder is fed into a suspension preheating system after being subjected to gas-solid separation by a feeding device or a cyclone separator through a raw meal lifting machine. The suspension preheating system comprises a multi-stage cyclone preheater, a high-efficiency material scattering device, a connecting pipeline and the like. The raw meal powder is preheated and gas-solid separated in the cyclone preheater, and the raw meal powder subjected to multiple heat exchange and gas-solid separation enters the decomposing furnace system from the discharging pipe of the second last cyclone preheater of the suspension preheating system. The decomposing furnace system comprises a decomposing furnace, a high-efficiency material scattering device, a flue gas inlet pipeline, a flue gas outlet pipeline and the like. The temperature distribution in the decomposing furnace can be controlled within a reasonable range by adjusting the material quantity fed into the decomposing furnace, the smoke quantity entering the decomposing furnace and the smoke temperature, the reasonable temperature distribution in the decomposing furnace can ensure the full decomposition of the kaolin, meanwhile, the kaolin is ensured not to be over-burned, and the activity index of the finished metakaolin meets the subsequent production requirement. The decomposed hot materials and the generated hot flue gas leave the decomposing furnace, and the hot materials and the hot flue gas enter a first cooling system after gas-solid separation in a final cyclone preheater of a suspension preheating system. The first cooling system comprises one-stage or multi-stage cyclone coolers, a high-efficiency material scattering device, a connecting pipeline and the like. The hot material is cooled and gas-solid separated in a cyclone cooler of the first cooling system, and the material cooled by the first cooling system enters the second cooling system after gas-solid separation. The second cooling system comprises one-stage or multi-stage cyclone coolers, a high-efficiency material scattering device, a connecting pipeline and the like. The material is further realized in a cyclone cooler of a second cooling systemAnd cooling and gas-solid separation, wherein most of the materials finally leave from a blanking pipe of the cyclone cooler at the lowest stage of the second cooling system and fall into a finished product zipper machine, and a small part of the materials fall into the finished product zipper machine after being collected by a dust collector, so that a finished product meeting the requirements is finally obtained. According to the air flow direction, normal-temperature air enters a second cooling system, then materials entering the second cooling system are cooled, heat exchange-completed air leaves from an air outlet of the upmost cyclone cooler of the second cooling system, then metakaolin finished products contained in the air are separated into a finished product zipper machine by a dust collector, and air at an outlet of the dust collector is divided into the following two paths: the first path enters the hot blast furnace system to support combustion, and the second path enters the drying crusher to dry raw materials or to perform other forms of waste heat utilization. The temperature of the flue gas at the outlet of the hot blast stove is controlled in a reasonable range of 800-1000 ℃ by reasonably controlling the amount of fuel entering the hot blast stove, and meanwhile, O in the flue gas 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm; the high-temperature flue gas from the hot blast stove is mixed with the flue gas from the outlet of the first cooling system and then enters the decomposing furnace, the water vapor generated by fully decomposing the material in the decomposing furnace through heat absorption is mixed with the flue gas and then leaves the decomposing furnace system, then the raw material powder fed into the suspension preheating system is preheated for multiple times and subjected to gas-solid separation, finally leaves from the air outlet of the cyclone preheater at the uppermost stage of the suspension preheating system, and then is divided into the following two paths: one path of the flue gas enters an indirect heat exchanger through a flue gas circulating fan, the indirect heat exchanger sufficiently cools the flue gas by adopting cooling water, cooling oil or other applicable cooling mediums, the sufficiently cooled flue gas enters a first cooling system, then high-temperature materials entering the first cooling system are cooled, the cooled circulating flue gas leaves from an air outlet of an uppermost stage cyclone cooler of the first cooling system, and then the cooled circulating flue gas is mixed with high-temperature flue gas at an outlet of a hot blast furnace and enters a decomposing furnace; and the second path is fed into a drying crusher to dry the raw materials or perform other forms of waste heat utilization, and the raw materials are discharged into the atmosphere after being treated by smoke.
Compared with the prior art, the invention has the advantages and positive effects that:
1. in order to prepare the metakaolin finished product with the activity index meeting the subsequent requirements, the fuel combustion and material decomposition processes are completely decoupled, and the first cooling system and the hot blast stove system are reasonably designed to ensure that the enthalpy carried by the flue gas entering the decomposing furnace can promote the complete decomposition of the kaolin material in the decomposing furnace system, and meanwhile, the temperature of the flue gas can avoid the high-temperature inactivation of the kaolin material, so that the activity index of the metakaolin finished product meets the subsequent production requirements.
2. The invention realizes that the oxygen content in the flue gas at the outlet of the hot blast furnace system and the suspension preheating system is within the preferable oxygen content range by reasonably designing the hot blast furnace system, and the flue gas contains a certain amount of reducing gas CO, and the circulating flue gas is cooled to a proper temperature range by adopting an indirect heat exchanger and is then used for carrying out primary quenching on high-temperature metakaolin (the oxygen concentration in the flue gas is lower, and a certain amount of reducing gas CO is added), so that Fe in the metakaolin can be effectively avoided 2+ Is re-oxidized to Fe by contact with an oxygen-containing cooling medium 3+ Further losing control over the color of the finished metakaolin product; meanwhile, the circulating flue gas after heat exchange is mixed with the flue gas at the outlet of the hot blast stove, so that the temperature in the decomposing furnace is distributed at 650-850 ℃, the content of reducing gas CO at the outlet of the hot blast stove is controlled in a reasonable range, and Fe in kaolin materials in a decomposing furnace system can be easily decomposed 3+ Reduction to Fe 2+ . The invention is mainly designed in the decomposition and cooling links, thereby realizing the control of the color of the finished metakaolin product.
3. The invention sequentially sets the first cooling system and the second cooling system, and the two cooling systems have definite function positioning. Wherein, the first cooling system fully utilizes the low-oxygen flue gas at the outlet of the suspension preheating system to carry out primary cooling on the metakaolin, so as to avoid Fe in the metakaolin 2+ Is oxidized to Fe in contact with an oxygen-containing cooling medium (such as air at normal temperature) during cooling 3+ . Meanwhile, the low oxygen smoke quantity which is reasonably designed can cool the metakaolin to a safe temperature range of 300-350 ℃ and below. The second cooling system fully utilizes normal-temperature air to cool the metakaolin to about 100 ℃;
4. the suspension preheating system outlet flue gas and the second cooling system outlet air both consider full waste heat recycling, so that the system heat consumption can be effectively reduced, and the production cost is reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the description of the embodiments will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a system flow diagram of a metakaolin preparation system that may implement decoupling functionality provided by an embodiment of the present invention.
Wherein: 1. a suspension preheating system; 1-1, a cyclone preheater; 2. a decomposing furnace system; 2-1, a decomposing furnace; 3. a first cooling system; 3-1, a first cyclone cooler; 4. a second cooling system; 4-1, a second cyclone cooler; 4-2, a third cyclone cooler; 6. an indirect heat exchanger; 7. a dust collector; 8. a hot blast stove system; 8-1, hot blast stove.
Detailed Description
The following description of the embodiments of the present invention will be made apparent and fully in view of the accompanying drawings, in which some, but not all embodiments of the invention are shown. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
In the description of the present invention, it should be noted that the positional or positional relationship indicated by the terms such as "upper", "lower", "top", "bottom", "inner", "outer", etc. are based on the positional or positional relationship shown in the drawings, are merely for convenience of describing the present invention and simplifying the description, and do not indicate or imply that the apparatus or element in question must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
Examples
Referring to fig. 1, an embodiment of the present invention provides a metakaolin preparation system capable of implementing a decoupling function, which includes a suspension preheating system 1, a decomposing furnace system 2, a first cooling system 3, a second cooling system 4 and a hot blast stove system 8.
The suspension preheating system 1 comprises a multi-stage cyclone preheater 1-1, a high-efficiency material scattering device, a connecting pipeline and the like, wherein the cyclone preheater 1-1 of the suspension preheating system 1 has three-seven preferred stages for preheating raw materials; in this embodiment, the cyclone preheater 1-1 of the suspension preheating system 1 is preferably five stages, namely, the first, second, third, fourth and fifth cyclone preheaters. The decomposing furnace system 2 comprises a decomposing furnace 2-1, a high-efficiency material scattering device, a flue gas inlet pipeline, a flue gas outlet pipeline and the like. The preferred number of the cyclone cooler of the first cooling system 3 is one-four, in this embodiment, a first cyclone cooler is selected, and the first cooling system 3 includes a first cyclone cooler 3-1, a high-efficiency material scattering device, a connecting pipeline, and the like. The preferred number of the cyclone coolers of the second cooling system 4 is one-four, in this embodiment, two-stage cyclone coolers are selected, and the second cooling system 4 comprises a second cyclone cooler 4-1, a third cyclone cooler 4-2, a high-efficiency material scattering device, a connecting pipeline and the like. The hot blast stove system 8 comprises a hot blast stove 8-1, a combustion air inlet pipeline, a burner, a flue gas outlet pipeline, a slag discharge pipeline and the like.
The bottom of the decomposing furnace 2-1 is a flue gas inlet, the top outlet of the decomposing furnace 2-1 is connected with the inlet of a fifth cyclone preheater of the suspension preheating system 1, the material outlet at the bottom of the fifth cyclone preheater of the suspension preheating system 1 is connected with the material inlet of a first cyclone cooler 3-1 of a first cooling system 3, the discharge outlet of a fourth cyclone preheater of the suspension preheating system 1 is connected with a raw material feeding port of the decomposing furnace 2-1, and a fuel feeding port is not arranged on the decomposing furnace 2-1. Specifically, the decomposing furnace 2-1 is provided with a plurality of raw material feeding ports in the height direction, and the temperature distribution in the decomposing furnace 2-1 can be controlled in a reasonable range by adjusting the raw material amount fed into the decomposing furnace 2-1, the smoke amount entering the decomposing furnace and the smoke temperature.
The top of the hot blast stove 8-1 is provided with a fuel feeding port, a combustion air inlet of the hot blast stove is positioned at one side of the fuel feeding port, the bottom of the hot blast stove is provided with a slag discharging port, a flue gas outlet of the hot blast stove is positioned at one side of the lower part of the hot blast stove 8-1, and a flue gas outlet of the hot blast stove 8-1 is connected with a flue gas outlet pipeline of the first cooling system 3.
The top flue gas outlet of the suspension preheating system 1 is connected with the flue gas inlet of the indirect heat exchanger 6, the indirect heat exchanger 6 is used for indirectly cooling the flue gas discharged by the suspension preheating system 1 to 80-120 ℃, the bottom of the indirect heat exchanger 6 is provided with a cooling medium inlet and a flue gas outlet, the top of the indirect heat exchanger 6 is provided with a flue gas inlet and a cooling medium outlet, so that the flue gas and the cooling medium exchange heat in a countercurrent way, and the cooling medium channel of the indirect heat exchanger 6 is internally filled with the cooling medium. The cooling medium of the indirect heat exchanger 6 is cooling water, cooling oil or other suitable cooling medium.
Considering that the oxygen content in the flue gas at the outlet of the suspension preheating system 1 can be controlled to be 1-3%, the suspension preheating system can be used for realizing the primary quenching of hot materials in the first cooling system 3, the flue gas outlet of the indirect heat exchanger 6 is connected with the flue gas inlet of the first cooling system 3, the first cooling system 3 is used for quenching the materials to a temperature range of 300-350 ℃ and below, the flue gas outlet of the first cooling system 3 is connected with the flue gas inlet of the decomposing furnace 2-1, and the flue gas after heat exchange is mixed with high-temperature flue gas from the hot blast furnace system and then sent to the decomposing furnace 2-1.
The material outlet of the first cooling system 3 is connected with the material inlet of the second cooling system 4, the cooling medium of the second cooling system 4 is normal-temperature air, the second cooling system 4 is used for cooling the material to below 100 ℃, and the gas outlet of the second cooling system 4 is connected with the combustion-supporting air inlet of the hot blast stove 8-1 through the dust collector 7 and the combustion-supporting air circulating fan in sequence and is used for supporting combustion of the hot blast stove 8-1.
The flue gas outlet of the suspension preheating system 1 and the gas outlet of the second cooling system 4 are also connected with a drying crusher for drying raw materials or connecting other waste heat utilization equipment for carrying out other forms of waste heat utilization, so that the waste heat recycling is fully considered, the heat consumption of the system can be effectively reduced, and the production cost is reduced.
The specific method for preparing metakaolin by adopting the system comprises the following steps:
raw materials enter a decomposing furnace 2-1 after being preheated by a suspension preheating system 1, decomposed materials and generated hot flue gas leave the decomposing furnace 2-1 and enter a final cyclone preheater 1-1 of the suspension preheating system 1, and materials separated by the final cyclone preheater 1-1 of the suspension preheating system 1 enter a first cooling system 3; the flue gas with the oxygen content of 1-3% discharged from the top of the suspension preheating system 1 is cooled to 80-120 ℃ by an indirect heat exchanger 6 and then enters a first cooling system 3 to exchange heat with materials entering the first cooling system 3, the flue gas discharged from the first cooling system 3 enters a decomposing furnace 2-1, and the gas discharged from a second cooling system 4 enters a hot blast stove 8-1 to support combustion; the temperature of high-temperature flue gas from the hot blast stove 8-1 is controlled at 800-1000 ℃, and O in the flue gas 2 The concentration is controlled to be 1-3%, the CO content is controlled to be 1000-2000ppm, the high temperature flue gas from the hot blast stove 8-1 is mixed with the flue gas with the outlet temperature of 500-600 ℃ in the first cooling system 3 and then fed into the decomposing furnace 2-1, the raw material amount fed into the decomposing furnace 2-1, the flue gas amount fed into the decomposing furnace and the flue gas temperature are regulated, the temperature distribution in the decomposing furnace 2-1 is controlled to be 650-850 ℃, the residence time of the flue gas in the decomposing furnace is 2-10 seconds, and Fe in the raw material is added 3+ Reduction to Fe 2+ The kaolin is fully decomposed, the kaolin is not over-burned, and the activity index of the finished metakaolin meets the subsequent production requirement; the first cooling system 3 rapidly cools the decomposed hot material (metakaolin) to a temperature of 300-350 ℃ and below to enable Fe in the metakaolin 2+ Here, theThe cooling link is not oxidized into Fe again 3+ The hot materials are cooled and gas-solid separated in a first cyclone cooler 3-1 of a first cooling system 3; the materials cooled by the first cooling system 3 enter the second cooling system 4, the cooling medium of the second cooling system 4 is normal-temperature air, the materials are cooled to below 100 ℃ by the second cooling system 4, cooling and gas-solid separation are further realized in the third cyclone cooler 4-2 of the second cooling system 4, and finally the materials leave from the blanking pipe of the second cyclone cooler 4-1 and fall into a finished product zipper machine, so that the finished product meeting the requirements is obtained.
According to the material flow direction, the kaolin raw material is subjected to a raw material pretreatment procedure to obtain raw material powder meeting the production requirement. The raw meal powder is fed into a suspension preheating system 1 after being subjected to gas-solid separation by a feeding device or a cyclone separator through a raw meal lifting machine. The raw meal powder is preheated and gas-solid separated in the cyclone preheater 1-1, and the raw meal powder subjected to multiple heat exchange and gas-solid separation enters the decomposing furnace system 2 from the discharging pipe of the fourth cyclone preheater 1-1 of the suspension preheating system 1. The decomposing furnace system 2 comprises a decomposing furnace 2-1, a high-efficiency material scattering device, a flue gas inlet pipeline, a flue gas outlet pipeline and the like. The decomposing furnace is provided with a plurality of raw material feeding ports in the height direction, the temperature distribution in the decomposing furnace can be controlled at 650-850 ℃ by adjusting the amount of materials fed into the decomposing furnace 2-1, the amount of smoke entering the decomposing furnace and the temperature of the smoke, the reasonable temperature distribution in the decomposing furnace 2-1 can ensure the full decomposition of the kaolin, the kaolin is not over-burned, and the activity index of the finished metakaolin meets the subsequent production requirement. The decomposed hot materials leave the decomposing furnace in the decomposing furnace system 2, and then enter the first cooling system 3 after being separated from hot flue gas in the fifth cyclone preheater 1-1 of the suspension preheating system 1. The hot materials are cooled and gas-solid separated in the cyclone cooler of the first cooling system 3, and the materials cooled by the first cooling system 3 enter the second cooling system 4 through the blanking pipe of the first cyclone cooler 3-1 after gas-solid separation. The material is further cooled and gas-solid separated in the third cyclone cooler 4-2 of the second cooling system 4, and finally most of the material leaves from the blanking pipe of the second cyclone cooler 4-1 of the second cooling system 4 and falls into a finished product zipper machine, and a small part of the material falls into the finished product zipper machine after being collected by the dust collector 7, so that a finished product meeting the requirement is finally obtained.
According to the air flow direction, normal-temperature air enters the second cooling system 4, then the materials entering the second cooling system 4 are cooled, the air subjected to heat exchange leaves from the air outlet of the third cyclone cooler 4-2 of the second cooling system 4, then the meta-kaolin finished product contained in the air is separated into a finished product zipper machine by entering the dust collector 7, and the air at the outlet of the dust collector 7 is divided into the following two paths: the first path enters the hot blast furnace system 8 to support combustion, and the second path enters the drying crusher to dry raw materials or to perform other forms of waste heat utilization. The temperature of the flue gas at the outlet of the hot blast stove is controlled in a reasonable range of 800-1000 ℃ by reasonably controlling the amount of fuel entering the hot blast stove 8-1, and meanwhile, O in the flue gas 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm; mixing the high-temperature flue gas from the hot blast stove 8-1 with the flue gas from the outlet of the first cooling system 3, and then feeding the mixture into a decomposing furnace, so that the temperature in the decomposing furnace is distributed at 650-850 ℃, and Fe in the kaolin raw material is added 3+ Fully reduce to Fe 2+ The water vapor generated by the heat absorption and full decomposition of the materials in the decomposing furnace is mixed with the flue gas and then leaves the decomposing furnace system 8; then, the raw material powder fed into the suspension preheating system 1 is preheated for a plurality of times and subjected to gas-solid separation, and finally leaves from the air outlet of the first cyclone preheater 1-1 of the suspension preheating system 1, and then is divided into the following two paths: one path of the circulating flue gas enters an indirect heat exchanger 6 through a circulating fan, the circulating flue gas is fully cooled through cooling water, cooling oil or other applicable cooling mediums, the fully cooled flue gas enters a first cooling system 3, then high-temperature materials entering the first cooling system 3 are cooled, the cooled circulating flue gas leaves from an air outlet of a first cyclone cooler 3-1 of the first cooling system 3, and then the cooled circulating flue gas is mixed with high-temperature flue gas at an outlet of a hot blast furnace and enters a decomposing furnace; and the second path is fed into a drying crusher to dry the raw materials or perform other forms of waste heat utilization, and the raw materials are discharged into the atmosphere after being treated by smoke.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (13)
1. A metakaolin preparation system capable of realizing decoupling function is characterized in that: the device comprises a suspension preheating system, a decomposing furnace system, a first cooling system, a second cooling system and a hot blast furnace system, wherein the decomposing furnace system comprises a decomposing furnace, the bottom of the decomposing furnace is provided with a flue gas inlet, the outlet at the top of the decomposing furnace is connected with the inlet of a final cyclone preheater of the suspension preheating system, the outlet of the bottom of the final cyclone preheater of the suspension preheating system is connected with the inlet of the first cooling system, the outlet of a penultimate cyclone preheater of the suspension preheating system is connected with a raw material feeding port of the decomposing furnace, the decomposing furnace is not provided with a fuel feeding port, and the temperature in the decomposing furnace is controlled at 650-850 ℃;
the top flue gas outlet of the suspension preheating system is connected with the flue gas inlet of the indirect heat exchanger, the flue gas outlet of the indirect heat exchanger is connected with the flue gas inlet of the first cooling system, the first cooling system is used for quenching materials to a temperature range of 300-350 ℃ and below, the flue gas outlet of the first cooling system is connected with the flue gas inlet of the decomposing furnace, and the oxygen content in the flue gas discharged from the top of the suspension preheating system is 1-3%; the material outlet of the first cooling system is connected with the material inlet of the second cooling system, the gas outlet of the second cooling system is connected with the combustion air inlet of the hot blast stove system, and the flue gas outlet of the hot blast stove system is connected with the flue gas outlet pipeline of the first cooling system; o in flue gas at outlet of hot blast stove system 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm.
2. The metakaolin preparation system capable of realizing the decoupling function according to claim 1, wherein the high-temperature flue gas temperature of the outlet of the hot blast stove system is controlled to be 800-1000 ℃, the hot blast stove system comprises a hot blast stove, a fuel feeding port is arranged at the top of the hot blast stove, a combustion air inlet of the hot blast stove system is positioned at one side of the fuel feeding port, a slag discharging port is arranged at the bottom of the hot blast stove, and a flue gas outlet of the hot blast stove system is positioned at one side of the lower part of the hot blast stove.
3. The system for preparing metakaolin capable of realizing decoupling function according to claim 1, wherein the decomposing furnace is provided with a plurality of raw material feeding ports in a height direction.
4. The metakaolin preparation system capable of realizing the decoupling function according to claim 1, wherein the indirect heat exchanger is used for indirectly cooling the flue gas discharged from the suspension preheating system to 80-120 ℃, a cooling medium inlet and a flue gas outlet are arranged at the bottom of the indirect heat exchanger, a flue gas inlet and a cooling medium outlet are arranged at the top of the indirect heat exchanger, so that the flue gas and the cooling medium exchange heat in a countercurrent manner, and the cooling medium is introduced into a cooling medium channel of the indirect heat exchanger.
5. The decoupling zero metakaolin production system of claim 4, wherein the cooling medium of the indirect heat exchanger is cooling water, cooling oil, or other suitable cooling medium.
6. The metakaolin preparation system capable of realizing the decoupling function according to claim 1, wherein flue gas circulating fans are respectively arranged between the indirect heat exchanger and the first stage cyclone preheater of the suspension preheating system and between the indirect heat exchanger and the first cooling system.
7. The metakaolin preparation system capable of realizing the decoupling function according to claim 1, wherein the gas outlet of the second cooling system is connected with the combustion air inlet of the hot blast stove system sequentially through a dust collector and a combustion air circulating fan.
8. The decoupling zero metakaolin production system of claim 1, wherein the second cooling system comprises at least one stage cyclone cooler for cooling the material to below 100 ℃.
9. The metakaolin preparation system capable of realizing the decoupling function according to claim 1, wherein a flue gas outlet of the suspension preheating system and a gas outlet of the second cooling system are also connected with a drying crusher or other waste heat utilization equipment.
10. A method for preparing metakaolin capable of realizing decoupling function by adopting the system as claimed in any one of claims 1-9, which is characterized in that raw materials enter a decomposing furnace after being preheated by a suspension preheating system, decomposed materials and generated hot flue gas leave the decomposing furnace to enter a final cyclone preheater of the suspension preheating system, and materials separated by the final cyclone preheater of the suspension preheating system enter a first cooling system; the flue gas discharged from the top of the suspension preheating system is cooled by an indirect heat exchanger and then enters a first cooling system to exchange heat with materials entering the first cooling system, the flue gas discharged from the first cooling system enters a decomposing furnace system, the gas discharged from the second cooling system enters a hot blast furnace system to support combustion, the high-temperature flue gas discharged from the hot blast furnace system is mixed with the flue gas discharged from the outlet of the first cooling system and then enters the decomposing furnace, the raw material quantity fed into the decomposing furnace, the flue gas quantity entering the decomposing furnace and the flue gas temperature are regulated, and the temperature in the decomposing furnace is controlled to be between 650 and 850 ℃, so that the kaolin is fully decomposed and not burned, and the activity index of the finished metakaolin meets the requirement of subsequent production; the first cooling system quenches the material to a temperature range of 300-350 ℃ and below, then the material enters the second cooling system, and the material is cooled by the second cooling system to obtain the metakaolin with controllable finished product color.
11. The method for preparing metakaolin capable of realizing decoupling function according to claim 10, wherein the residence time of the flue gas in the decomposing furnace is 2-10 seconds.
12. The method for preparing metakaolin capable of realizing decoupling function according to claim 10, wherein the high-temperature flue gas temperature of the hot blast stove system is controlled to be 800-1000 ℃, and O in flue gas is as follows 2 The concentration is controlled to be 1-3%, and the CO content is controlled to be 1000-2000 ppm.
13. The method for preparing metakaolin capable of realizing decoupling function according to claim 10, wherein the cooling medium of the first cooling system is flue gas with the temperature of 80-120 ℃ after being cooled by an indirect heat exchanger, the oxygen content in the flue gas is 1-3%, and the temperature of the flue gas at the outlet of the first cooling system is 500-600 ℃; the cooling medium of the second cooling system is normal-temperature air, and the temperature of the material cooled by the second cooling system is lower than 100 ℃.
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