CN115340304A - Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln - Google Patents
Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln Download PDFInfo
- Publication number
- CN115340304A CN115340304A CN202210866736.1A CN202210866736A CN115340304A CN 115340304 A CN115340304 A CN 115340304A CN 202210866736 A CN202210866736 A CN 202210866736A CN 115340304 A CN115340304 A CN 115340304A
- Authority
- CN
- China
- Prior art keywords
- kiln
- cyclone
- furnace
- raw material
- rotary kiln
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
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
- C04B2/00—Lime, magnesia or dolomite
- C04B2/10—Preheating, burning calcining or cooling
- C04B2/102—Preheating, burning calcining or cooling of magnesia, e.g. dead burning
-
- 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
- Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Furnace Details (AREA)
- Muffle Furnaces And Rotary Kilns (AREA)
Abstract
The invention relates to the technical field of magnesite calcination, in particular to a device and a method for producing light-burned magnesia by decomposing a five-stage suspension preheating kiln, wherein the device for producing the light-burned magnesia comprises a raw material treatment mechanism, a five-stage suspension preheating decomposing furnace mechanism, a rotary kiln mechanism, a grate cooler and a clinker grinding mechanism which are sequentially connected, wherein the five-stage suspension preheating decomposing furnace mechanism comprises a multi-stage suspension preheater and an outside-kiln pre-decomposing furnace, the outside-kiln pre-decomposing furnace is arranged between the last two stages of suspension preheaters, and tail gas generated by the outside-kiln pre-decomposing furnace can be used by the raw material treatment mechanism after being subjected to solid-gas separation by each stage of suspension preheater. The invention overcomes the limitation of the existing equipment for producing light-burned magnesia by suspension calcination of magnesite on high gas flow rate, can carry out suspension calcination under higher gas flow rate, and has the advantages of negative pressure operation of the whole device, controllable gas material stroke, uniform material sintering, adjustable and controllable product activity, stable quality, small heat loss of the device, high efficiency and low tail gas discharge.
Description
Technical Field
The invention relates to the technical field of magnesite calcination, in particular to a device and a method for producing light-burned magnesium oxide by decomposing a five-stage suspension preheating kiln.
Background
The magnesite is mainly used in the field of production of magnesium materials, the produced magnesium materials such as light burned magnesia powder, heavy burned magnesia, medium-grade magnesia, high-purity magnesia, large-crystal fused magnesia and the like and the derived finished products thereof are materials which are necessary to be used by industrial kilns in the industries of metallurgy, chemical engineering, building materials and the like, and the light burned magnesia produced by low-grade magnesite is also applied to the aspects of building materials, flue gas desulfurization, metal smelting slagging, soil improvement and the like. Therefore, magnesite has become a necessary basic and strategic substance in the high-temperature industrial field.
At present, the production of light-burned magnesia in China continues to use the traditional reflection kiln for production, and the reflection kiln has the advantages of small kiln body, low yield, high energy consumption, low utilization rate of magnesite, serious environmental pollution, high labor intensity and low automation degree. Therefore, the light-burned magnesia produced by the kiln can not meet the requirements of green low-carbon development at present. In addition, the production mode takes the blocky magnesite as a raw material, so that the specific surface area is small, the conditions of over-burning on the surface and under-burning inside are easy to occur, the product quality is unstable, and the activity is low.
In recent years, the light-burned magnesia produced by calcining magnesite in a suspension furnace enters the visual field of people, and the magnesite powder is used as a raw material, so that the light-burned magnesia has the characteristics of uniform calcination, stable product quality, high activity, continuous production and the like, but the single set of the device has low yield and high energy consumption.
Chinese patent publication No. CN208218696U discloses a light-burned MgO suspension calcination production apparatus, which includes a raw material bin, a cyclone preheating cylinder, a suspension calciner, three sets of combustion systems, a suspension cooling cylinder, a fluidized bed, a sleeve type water-cooled screw conveyor, a finished product bin, etc., and can realize accurate partition calcination of different active magnesium oxides, and the product quality is stable. Although the device has carried out certain utilization to the flue gas waste heat, there is great problem to the waste heat utilization of product, does not utilize the heat of product in the suspension cooling section of thick bamboo, and waste heat recovery is not significant.
Chinese patent publication No. CN106007415A discloses a complete set of apparatus for preparing high-activity light-burned magnesium oxide by suspension flash, which comprises a feeding device, a material preheating device, a suspension calciner, a product cooling device, and a waste gas treatment device. The complete equipment uses magnesite powder as a raw material, the materials are sequentially preheated, suspended calcined and cooled, the raw material is preheated through smoke, and the product preheats combustion air to realize preliminary waste heat recovery, so that the burning heat consumption of light-burned magnesia is reduced, the operating environment is improved, and the production efficiency is high. However, the device adopts direct mixing with cold air in the aspect of flue gas waste heat utilization, and carries out heat exchange in the cyclone separator, and the operation makes combustion-supporting air carry a large amount of products to re-enter the calcining furnace, so that the partial products are over-burnt, and the overall quality of the products is finally influenced.
In view of the above, the invention provides a novel device and a novel method for producing light-burned magnesia based on five-stage suspension preheating, out-of-kiln predecomposition and a rotary kiln, so as to solve the series problems of backward production process, low capacity, high energy consumption, low comprehensive utilization rate of magnesite, unstable and uneven product quality and the like of the existing domestic light-burned magnesia production enterprises.
Disclosure of Invention
The invention aims to provide a device for producing light-burned magnesia by decomposing a five-stage suspension preheating kiln, which solves the problems of poor waste heat recovery and utilization rate and uneven product quality of the existing light-burned magnesia calcining equipment;
the second purpose of the invention is to provide a method for producing light-burned magnesia by decomposing the outside of a five-stage suspension preheating kiln, which can obviously reduce the energy consumption of magnesite calcination in a rotary kiln.
The invention provides a novel device for producing light-burned magnesium oxide by decomposing outside a five-stage suspension preheating kiln, which comprises a raw material treatment mechanism, a five-stage suspension preheating decomposition furnace mechanism, a rotary kiln mechanism, a grate cooler and a clinker grinding mechanism which are sequentially connected, wherein the five-stage suspension preheating decomposition furnace mechanism comprises a multi-stage suspension preheater and an outside-kiln preheating decomposition furnace, the outside-kiln preheating decomposition furnace is arranged between the last two stages of suspension preheaters, and tail gas generated by the outside-kiln preheating decomposition furnace can be used by the raw material treatment mechanism after being subjected to solid-gas separation by the suspension preheaters of all stages; oxygen-enriched hot air generated by cooling finished products by the grate cooler can be used by the rotary kiln mechanism and the out-of-kiln predecomposition furnace.
The invention provides a novel device for producing light-burned magnesia by decomposing a five-stage suspension preheating kiln outside, which comprises a raw material treatment mechanism, a five-stage suspension preheating decomposing furnace mechanism, a rotary kiln mechanism, a grate cooler and a clinker grinding mechanism which are connected in sequence. Dust generated in the whole production process is recycled, clean production is realized, and the high pollution phenomenon caused by material discharge is avoided; in the production process, the heat energy generated by fuel calcination in the production process is effectively utilized to dry the raw materials; oxygen-enriched hot air generated in the cooling process of the finished product discharged from the kiln is supplied to the kiln and the kiln tail decomposing furnace for production and utilization.
Preferably, in the technical scheme, the five-stage suspension pre-pyrolysis furnace mechanism comprises a C1 cyclone, a C2 cyclone, a C3 cyclone, a C4 cyclone, an out-of-kiln pre-pyrolysis furnace and a C5 cyclone which are sequentially connected, wherein the C5 cyclone, the C4 cyclone, the C3 cyclone, the C2 cyclone and the C1 cyclone are sequentially and reversely communicated;
the outlet pipeline of the C1 cyclone is connected with the raw material processing mechanism, the kiln tail waste gas discharge dust collector and the kiln tail exhaust fan through a high-temperature fan, and the C5 cyclone is connected with the rotary kiln mechanism.
The five-stage suspension pre-pyrolysis furnace mechanism specifically comprises a C1 cyclone, a C2 cyclone, a C3 cyclone, a C4 cyclone, an external kiln pre-pyrolysis furnace and a C5 cyclone which are sequentially connected, wherein each stage of cyclone mainly plays a role in gas-material separation, materials mainly exchange heat in a connecting pipeline between each stage of cyclone, and materials collected by the cyclones are driven by airflow to enter the next stage of cyclone through a rising flue at the outlet of the next stage of cyclone to fully exchange heat in the driving process. The material collected by the four-stage cyclone enters a predecomposition furnace outside the kiln, is heated by high temperature generated by fuel combustion in the predecomposition furnace outside the kiln and is carried into a C5 cyclone, the material is subjected to gas-solid separation by the C5 cyclone, and the material enters a rotary kiln mechanism to be calcined into a finished product.
An external predecomposition furnace is additionally arranged between the four-stage cyclone cylinder and the C5 cyclone cylinder, and the magnesite powder is further decomposed and collected by the C5 cyclone cylinder and then enters a rotary kiln mechanism, so that the decomposition rate of the magnesite powder can reach 80-90%;
and tail gas generated by the predecomposition furnace outside the kiln is subjected to solid-gas separation in sequence through the C5 cyclone, the C4 cyclone, the C3 cyclone, the C2 cyclone and the C1 cyclone, and then is supplied to a raw material treatment mechanism through a high-temperature fan, or enters a kiln tail waste gas discharge dust collector or a kiln tail exhaust fan.
Preferably, in the technical scheme, the rotary kiln mechanism comprises a rotary kiln, a kiln head cover and a kiln tail smoke chamber, the kiln head cover and the kiln tail smoke chamber are respectively arranged at two ends of the rotary kiln, a discharge hole of the C5 cyclone is communicated with the kiln tail smoke chamber, and a discharge hole of the kiln head cover is communicated with the grate cooler; and a smoke outlet of the kiln tail smoke chamber is communicated with the precalciner outside the kiln.
The rotary kiln mechanism specifically comprises a rotary kiln and a kiln tail smoke chamber arranged at the rear end of the rotary kiln, the magnesite five-stage suspension preheating decomposing furnace mechanism is heated and mostly decomposed and then is sent into the rotary kiln for calcination, the materials slowly move from the feeding end to the discharging end in the rotary kiln along with the rotation of the rotary cylinder body, and finally decomposition reaction is completed in the rotary kiln to prepare the magnesia powder. The decomposition rate and activity of the magnesium oxide can be adjusted by the calcination temperature and the material residence time, so that the function of producing magnesium oxide with different active products can be achieved.
The smoke outlet of the kiln tail smoke chamber is communicated with the kiln outside predecomposition furnace, namely, the ground raw materials (magnesite with the particle size less than 200 meshes) enter the kiln outside predecomposition furnace and then can exchange heat with kiln tail waste gas in the kiln tail smoke chamber, and further the heat of the rotary kiln is effectively recovered.
The kiln head burner of the rotary kiln is arranged at the discharge end of the rotary kiln, and the kiln tail burner is arranged in the predecomposition furnace outside the kiln. The kiln head burner enters the rotary kiln through the kiln head cover. High-temperature airflow generated by fuel combustion is guided to flow from the discharge end of the rotary kiln to the feed end under the suction action of a high-temperature fan at the tail of the rotary kiln, magnesite is calcined into magnesium oxide, and a product is discharged from the discharge end of the rotary kiln; the method comprises the steps that air flow after magnesium oxide sintering is completed carries waste heat to enter the tail part of the feeding end of a rotary kiln, then the air flow enters a predecomposition furnace outside the kiln through a kiln tail smoke chamber, after magnesite in the predecomposition furnace outside the kiln is preheated, waste gas passes through different levels of cyclone cylinders and is subjected to the action of a high-temperature fan, the waste gas is connected through pipelines and respectively goes to a raw material processing mechanism to be preliminarily purified through a cyclone dust collector, and then the waste gas is sent to a waste gas processing procedure through the fan. Or directly sent to the waste gas treatment process without the raw material treatment mechanism.
Preferably, the kiln head cover is communicated with the kiln outside precalciner by the tertiary air pipe, and the gas system is used for providing heat sources required by calcination for the rotary kiln and the kiln tail precalciner respectively.
Preferably, in the technical scheme, the clinker grinding mechanism comprises a coarse powder bin, raymond mill equipment, a lifter, a fine powder bin, metering and conveying equipment, finished product conveying equipment and a finished product warehouse which are connected in sequence; the grate cooler is communicated with the coarse powder bin through a grate cooler lifter.
Discharging light calcined magnesia obtained by calcining in a rotary kiln into a fourth generation grate cooler through a discharge end of a kiln head of the rotary kiln, rapidly performing heat exchange between high-temperature materials and cold air entering the grate cooler, discharging the cooled light calcined magnesia from the grate cooler, enabling the cooled light calcined magnesia to enter a powder concentrator through a lifter, classifying magnesia powder with different granularities and grades, and enabling the material with qualified granularity to enter a finished product bin through a zipper machine for storage; the larger magnesium oxide particle size material is further milled by a Raymond mill to meet the use requirement, and the qualified material is sent into a steel plate bin for storage by a spiral metering scale and finished product conveying equipment to obtain the final magnesium oxide product.
The calcined material can bring a large amount of heat when entering the grate cooler after leaving the rotary kiln, and the grate cooler cools the material by blowing a large amount of cold air, thereby generating a large amount of hot air. In order to fully utilize the heat, part of hot air enters the rotary kiln through the kiln head to be used as secondary combustion-supporting air, and the heat recovery rate reaches 17.3 percent; a part of hot air enters the predecomposition furnace outside the kiln through the tertiary air pipe to be used as combustion-supporting air, the materials are heated and decomposed, and the heat recovery rate reaches 46.9%; a low-temperature waste heat boiler can be considered to be arranged for the redundant hot air, the waste heat of the flue gas system after desulfurization, denitrification and purification is utilized, according to heat balance calculation, the waste heat boiler can generate hot water with the pressure of 0.75MPa and the temperature of 155 ℃ for 53.5t/h, the hot water is pumped to be supplied to a low-temperature steam turbine generator for power generation, and the heat recovery rate reaches 29%. Therefore, the recovery rate of the heat after cooling of the grate cooler reaches 93.3 percent, and the grate cooler has extremely high heat recovery utilization rate.
Preferably, the raw material treatment mechanism comprises a raw material bin, a raw material vertical mill and a raw material warehouse which are sequentially connected, wherein the raw material warehouse is communicated with the C1 cyclone, and tail gas generated by the kiln external predecomposition furnace can be used by the raw material vertical mill after solid-gas separation.
The raw material treatment mechanism comprises a raw material bin, a raw material vertical mill and a raw material bin, wherein raw materials in the raw material bin are vertically ground into 200-mesh powdery magnesite powder through raw materials, the raw materials are small in particle size and large in specific surface area, and are fully calcined in a multistage suspension preheater, a predecomposition furnace outside a kiln and a rotary kiln, so that the production period can be shortened, and the uniformity and stability of product quality are ensured.
The invention also discloses a method for producing light-burned magnesium oxide by using the device, which also belongs to the protection scope of the invention, and the method specifically comprises the following steps:
s1, vertically grinding and crushing magnesite ore or flotation concentrate, and sequentially dehydrating, crushing and drying to obtain dried magnesite powder;
s2, preheating the dried magnesite powder step by step, and placing the preheated material in a predecomposition furnace outside a kiln for predecomposition to obtain a predecomposed material;
s3, carrying out solid-gas separation on the pre-decomposed material, and then calcining the material by using a rotary kiln to obtain a calcined material;
s4, sequentially cooling and grading the calcined materials to obtain a light-burned magnesium oxide product
Preferably, in the technical scheme, during the predecomposition, the temperature of a combustion chamber of the predecomposition furnace outside the kiln is controlled to be 800-950 ℃, and the decomposition rate of the magnesite powder and magnesium carbonate is 85-90%; during calcination, the temperature of flue gas in the rotary kiln is controlled to be 1100-1300 ℃, and the decomposition rate of magnesite powder and magnesium carbonate is 96-98%.
Preferably, in the step S1, the magnesite powder is dried by using waste heat of tail gas generated by the kiln external predecomposition furnace during the vertical grinding; in the step S2, the tail gas generated by the kiln external predecomposition furnace and the tail gas generated by the C5 cyclone are used by the C4 cyclone.
Preferably, in step S2, the out-of-kiln pre-decomposition furnace adopts an ammonia-free denitration technology.
The kiln outer predecomposition furnace adopts a heightening design, on one hand, in order to ensure that the smoke entering from the bottom of the rotary kiln has enough residence time in the kiln, a reducing atmosphere zone can be formed above a fuel injection point, so that nitrogen oxides in the rotary kiln are reduced by utilizing an ammonia-free denitration process in the dry-method cement rotary kiln production technology, and meanwhile, a kiln outer predecomposition furnace combustion decomposition zone is formed above a tertiary air inlet, so that the injected fuel is ensured to be fully combusted, and the purpose of decomposing most of materials is achieved.
And the kiln tail adopts an ammonia-free denitration technology, the technology is formed by sublimation of the existing staged combustion technology, and the main purpose of the technology is to reduce thermal NOx. The classified combustion is mainly characterized in that a denitrogenation pipe is added in a predecomposition furnace outside a kiln, so that air used for combustion is sprayed into the predecomposition furnace outside the kiln twice, and the air quantity of a fuel combustion area is reduced. The scheme of the denitriding pipe is adopted, and the air distribution is not easy to control in the actual operation process, so that the tertiary air pipe is moved upwards in the invention, so that a reduction zone is formed below the tertiary air inlet, and a combustion decomposition zone is formed above the tertiary air pipe. According to the thermodynamic NOx formation mechanism, higher temperatures generate more NOx; the calcining temperature in the rotary kiln is high, fuel is combusted to form a large amount of NOx, the NOx and high-temperature waste gas enter the predecomposition furnace outside the kiln through the smoke chamber, the oxygen content of the waste gas is about 2 percent, and if a large amount of reducing substances can be formed at the bottom of the predecomposition furnace outside the kiln, thermal NOx formed by high-temperature calcining of the rotary kiln can be efficiently reduced.
Namely, the ammonia-free denitration technology of the invention is that the cone part of the predecomposition furnace outside the kiln is contracted from a smoke chamber to tertiary airA reduction combustion zone is established between the tubes. Therefore, the kiln outside predecomposition furnace adopts lengthening treatment to ensure that the whole gas has enough residence time in the kiln outside predecomposition furnace, and fuel for the kiln outside predecomposition furnace is injected above the throat of the smoke chamber to ensure that the smoke chamber is subjected to anoxic combustion so as to generate CO and CH 4 、H 2 Reducing agents such as HCN and fixed carbon, and the reducing agents react with NOx in the kiln tail flue gas to reduce the NOx into N 2 And the like, and inert gas without pollution. In addition, the injected fuel is combusted under the anoxic condition, the generation of self-fuel type NOx is also inhibited, and the NOx emission reduction in the production process is realized.
In addition, the invention also adopts an energy-saving strong cyclone inflow furnace combustion device without external wind, so that the fuel enters a strong reduction zone at a certain speed in a cyclone manner, and the dispersion effect of the fuel is ensured. By adjusting and controlling the air quantity, the proper air-fuel ratio of the nozzle of the burner is maintained, the mixing effect of the fuel and the waste gas is improved, and the decomposition rate of the fuel is improved, so that the maximum reducing atmosphere is generated.
The novel device for producing light-burned magnesium oxide by decomposing the outside of the five-stage suspension preheating kiln at least has the following technical effects:
1. the raw material treatment mechanism of the invention endows the material to be processed with larger specific surface area, and adopts the powder with small particle size and larger specific surface area for calcination, thus shortening the production period, ensuring the uniformity of calcination and the stability of product quality, and adjusting the decomposition rate and activity of magnesium oxide to adapt to the technical requirements of different types of magnesium oxide (refractory light-burned powder, building material light-burned powder, desulfurization powder and the like);
2. the five-stage suspension pre-pyrolysis furnace mechanism can perform out-of-kiln pre-decomposition on materials, so that magnesite powder entering a kiln can achieve the effect of about 85% of pre-decomposition, the tail gas discharge pressure of a rotary kiln is greatly reduced, and the rotating speed and the yield of the rotary kiln are improved;
3. the kiln inlet air used by the rotary kiln mechanism of the invention is secondary hot air provided by the grate cooler, plays an important role in recovering waste heat and has an important role in reducing the energy consumption of products;
4. the out-of-kiln predecomposition furnace adopts an ammonia-free denitration technology, can effectively reduce NOx emission, and can reach NOx removal rate of more than 70%; the operation cost is avoided, and the normal production of the product is not adversely affected; the method has the advantages that secondary pollution is avoided, the ammonia-free denitration technology is a clean technology, and no solid or liquid pollutant or by-product is generated;
5. the novel device for producing light-burned magnesium oxide by decomposing outside the five-stage suspension preheating kiln overcomes the limitation of the existing device for producing light-burned magnesium oxide by suspending and calcining magnesite on high gas flow velocity, can perform suspension calcination at high gas flow velocity, is wholly operated by negative pressure, has controllable gas material stroke, uniform material sintering and adjustable and controllable product activity (the activity of the light-burned magnesium oxide prepared by a citric acid method is 50-300 seconds, the activity can be produced according to orders, other kilns cannot be realized), has stable quality, small heat loss of the device, high efficiency and low tail gas emission.
6. The daily output of the light-burned magnesia powder of the novel five-stage suspension preheating device for producing light-burned magnesia by decomposing outside the kiln is at least over 500 tons, which is ten times of the output of a reflection kiln of the traditional light-burned magnesia device and 2-3 times of that of the novel suspension kiln;
in conclusion, the novel device for producing light-burned magnesia by decomposing the light-burned magnesia outside the five-stage suspension preheating kiln solves the problems of poor waste heat recovery and utilization rate and uneven product quality of the existing light-burned magnesia calcining equipment, and can obviously reduce the energy consumption of calcining magnesite in a rotary kiln.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the prior art descriptions 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 can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic diagram of a device for producing light-burned magnesia by decomposing outside a novel five-stage suspension preheating kiln of the invention;
FIG. 2 is a schematic diagram of a five-stage suspension preheating decomposing furnace mechanism in the novel device for producing light-burned magnesium oxide by decomposing outside the five-stage suspension preheating kiln of the invention;
fig. 3 is a schematic diagram of a clinker grinding mechanism in the novel device for producing light-burned magnesium oxide by decomposing outside the five-stage suspension preheating kiln.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments, and it should be understood that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", and the like are used in the orientations and positional relationships indicated in the drawings, which are merely for convenience of description and simplicity of description, and do not indicate or imply that the devices or elements referred to must have a particular orientation, be constructed in a particular orientation, and be operated, and thus, are not to be construed as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, features defined as "first" and "second" may explicitly or implicitly include one or more of the described features. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise. Furthermore, the terms "mounted," "connected," and "coupled" are to be construed broadly and may include, for example, fixed connections, removable connections, or integral connections; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in fig. 1-3, the present invention provides a novel device for producing light-burned magnesia by using a five-stage suspension preheating kiln through decomposition, which comprises a raw material treatment mechanism, a five-stage suspension preheating decomposition furnace mechanism, a rotary kiln mechanism, a grate cooler and a clinker grinding mechanism which are connected in sequence, wherein the five-stage suspension preheating decomposition furnace mechanism comprises a multistage suspension preheater and an off-kiln predecomposition furnace, the off-kiln predecomposition furnace is arranged between the last two stages of suspension preheaters, and tail gas generated by the off-kiln predecomposition furnace can be used by the raw material treatment mechanism after solid-gas separation of each stage of suspension preheater; oxygen-enriched hot air generated by cooling finished products by the grate cooler can be used by the rotary kiln mechanism and the out-of-kiln predecomposition furnace.
The invention provides a novel device for producing light-burned magnesium oxide by decomposing outside a five-stage suspension preheating kiln, which comprises a raw material treatment mechanism, a five-stage suspension preheating decomposing furnace mechanism, a rotary kiln mechanism and a clinker grinding mechanism which are connected in sequence. Dust generated in the whole production process is recycled, clean production is realized, and the high pollution phenomenon caused by material discharge is avoided; in the production process, the heat energy generated by fuel calcination in the production process is effectively utilized to dry the raw materials; oxygen-enriched hot air generated in the cooling process of the finished product discharged from the kiln is supplied to the production of a decomposing furnace in the kiln and at the tail of the kiln for utilization.
In a specific embodiment of the invention, the five-stage suspension pre-pyrolysis furnace mechanism comprises a C1 cyclone, a C2 cyclone, a C3 cyclone, a C4 cyclone, an extrakiln pre-pyrolysis furnace and a C5 cyclone which are connected in sequence, wherein the raw material treatment mechanism is connected with the C1 cyclone, and the C5 cyclone is connected with the rotary kiln mechanism. The cyclone cylinders at all levels mainly play a role in gas-material separation, materials mainly exchange heat in connecting pipelines among the cyclone cylinders at all levels, and the materials collected by the cyclone cylinders enter the next-level cyclone cylinder along with the driving of airflow through a rising flue at the outlet of the next-level cyclone cylinder to fully exchange heat in the driving process. The material collected by the four-stage cyclone enters a predecomposition furnace outside the kiln, is heated by high temperature generated by fuel combustion in the predecomposition furnace outside the kiln and is carried into a C5 cyclone, the material is subjected to gas-solid separation by the C5 cyclone, and the material enters a rotary kiln mechanism to be calcined into a finished product. An external predecomposition furnace is additionally arranged between the four-stage cyclone cylinder and the C5 cyclone cylinder, and the magnesite powder is further decomposed and collected by the C5 cyclone cylinder and then enters a rotary kiln mechanism, so that the decomposition rate of the magnesite powder can reach 80-90%.
On the basis of the technical scheme, the rotary kiln mechanism further comprises a rotary kiln and a kiln tail smoke chamber arranged at the rear end of the rotary kiln, a discharge port of the C5 cyclone is communicated with the kiln tail smoke chamber, and a discharge port of the rotary kiln is communicated with the clinker grinding mechanism; and a smoke outlet of the kiln tail smoke chamber is communicated with the kiln external predecomposition furnace.
The rotary kiln mechanism specifically comprises a rotary kiln and a kiln tail smoke chamber arranged at the rear end of the rotary kiln, the magnesite five-stage suspension preheating decomposing furnace mechanism is heated and mostly decomposed and then is sent into the rotary kiln for calcination, the materials slowly move from the feeding end to the discharging end in the rotary kiln along with the rotation of the rotary cylinder body, and finally decomposition reaction is completed in the rotary kiln to prepare the magnesia powder. The smoke outlet of the kiln tail smoke chamber is communicated with the predecomposition furnace outside the kiln, namely, the ground raw materials (magnesite with the particle size less than 200 meshes) enter the predecomposition furnace outside the kiln and then can exchange heat with kiln tail waste gas in the kiln tail smoke chamber, and further the heat of the rotary kiln is effectively recovered.
In another embodiment of the invention, the burner of the rotary kiln is located at the discharge end of the rotary kiln and enters the rotary kiln through a kiln hood. High-temperature airflow generated by fuel combustion flows from the discharge end of the rotary kiln to the feed end under the suction action of a high-temperature fan, magnesite is calcined into magnesium oxide, and a product is discharged from the discharge end of the rotary kiln; the method comprises the steps that air flow after magnesium oxide sintering is completed carries waste heat to enter the tail part of the feeding end of a rotary kiln, then the air flow enters a predecomposition furnace outside the kiln through a kiln tail smoke chamber, after magnesite in the predecomposition furnace outside the kiln is preheated, waste gas passes through different levels of cyclone cylinders and is subjected to the action of a high-temperature fan, the waste gas is connected through pipelines and respectively goes to a raw material processing mechanism to be preliminarily purified through a cyclone dust collector, and then the waste gas is sent to a waste gas processing procedure through the fan. Or directly sent to the waste gas treatment process without the raw material treatment mechanism.
On the basis of the technical scheme, the heat source of the kiln outside pre-decomposition furnace also comprises a tertiary air pipe and a gas system, wherein the tertiary air pipe is used for communicating the kiln head cover with the kiln outside pre-decomposition furnace, and the gas system is used for providing heat sources required by calcination for the rotary kiln and the kiln tail pre-decomposition furnace respectively.
In a specific embodiment of the present invention, the specific access position scheme of the tertiary air duct is as follows: the strong reduction area of the ammonia-free denitration technology is formed at the bottom of the predecomposition furnace outside the kiln, and the area range of the strong reduction area is between the tertiary air pipe and the throat of the kiln tail smoke chamber. Therefore, the position of the tertiary air pipe needs to form the upper part of a strong reduction zone in the pre-decomposition furnace outside the kiln, and the tertiary air pipe is laterally screwed into the pre-decomposition furnace outside the kiln, so that the dispersion of raw materials of a feeding pipe of the multistage suspension preheater is facilitated.
On the basis of the technical scheme, the clinker grinding mechanism comprises a coarse powder bin, raymond mill equipment, a lifter, a fine powder bin, metering conveying equipment, finished product conveying equipment and a finished product warehouse which are sequentially connected; the grate cooler is communicated with the coarse powder bin through a grate cooler lifter.
The raw material treatment mechanism comprises a raw material bin, a raw material vertical mill and a raw material bin, wherein raw materials in the raw material bin are vertically ground into 200-mesh powdery magnesite powder through raw materials, the raw materials are small in particle size and large in specific surface area, and are fully calcined in a multistage suspension preheater, a predecomposition furnace outside a kiln and a rotary kiln, so that the production period can be shortened, and the uniformity and stability of the product quality are ensured. Tail gas generated by the five-stage suspension preheating mechanism is introduced during raw material vertical grinding, the moisture in the magnesite is dried by using the waste heat in the tail gas, particularly, the concentrate subjected to flotation and filter pressing contains about 10% of moisture during calcination and flotation of the concentrate, and the concentrate is dried by using the waste heat of the tail gas during vertical grinding, so that the magnesite powder subjected to vertical grinding can be quantitatively distributed to the five-stage suspension preheating mechanism without resistance through a raw material bin; and the tail gas after vertical grinding, crushing and drying is discharged through a cloth bag dust collector.
The materials in the specific embodiment of the invention are as follows:
magnesite powder enters a five-stage suspension preheating decomposing furnace mechanism from a raw material warehouse bin through a hoist, and exchanges heat with recovered high-temperature flue gas, so that the material temperature and the decomposition rate of magnesium carbonate are increased step by step. The method specifically comprises the following steps: powder from a raw material warehouse enters a five-stage suspension preheating decomposing furnace mechanism from an air outlet of a C2 cyclone cylinder through a kiln elevator, solid-gas separation is completed in a C1 cyclone cylinder firstly, the material enters a C2 cyclone cylinder, a C3 cyclone cylinder and a C4 cyclone cylinder sequentially to complete solid-gas separation step by step, the preheating temperature of magnesite powder is about 600-750 ℃, and the decomposition rate of magnesium carbonate can reach 85-90%; the material enters the kiln external predecomposition furnace from the discharge port of the C4 cyclone cylinder and is fully predecomposed with tertiary air, kiln tail flue gas of the rotary kiln and fuel supplemented into the kiln external predecomposition furnace; the material and the flue gas discharged from the decomposing furnace enter a C5 cyclone for solid-gas separation, the material enters a rotary kiln for calcination through a discharge port of the C5 cyclone, the temperature of the material entering the kiln reaches over 800 ℃, the decomposition rate of magnesium carbonate reaches 85-90%, only 5-10% of the undecomposed magnesium carbonate is left, the pressure of the rotary kiln for calcining the light calcined powder is greatly reduced, and sufficient conditions are created for improving the yield of the rotary kiln; the materials calcined by the rotary kiln enter a grate cooler at the discharge end of the kiln head of the rotary kiln, a large amount of cold air enters the grate cooler to be cooled in the grate cooler, the cooled materials enter a powder concentrator, the materials with the particle size larger than 200 meshes directly enter a finished product warehouse, and the materials with the particle size smaller than 200 meshes are ground to 200 meshes through a Raymond mill and then enter the finished product warehouse.
The gas runs as follows:
natural gas and secondary air are sprayed into a rotary kiln calcining zone through a natural gas nozzle, generated high-temperature flue gas enters the kiln external predecomposition furnace through a kiln tail smoke chamber of the rotary kiln under the action of a high-temperature draught fan, meanwhile, tertiary air and supplementary fuel are added into the gas entering the kiln external predecomposition furnace, the gas participates in the predecomposition process of materials entering from a C4 cyclone cylinder, tail gas generated by the kiln external predecomposition furnace enters a multistage suspension preheater, the tail gas generated after solid-gas separation of C5, C4, C3, C2 and C1 five-stage cyclone cylinders enters a system dust collector, and the generated tail gas is used for a vertical mill.
The waste heat utilization mode is as follows:
1. the light calcined powder obtained by the rotary kiln can bring a large amount of heat when entering the grate cooler, and the grate cooler cools materials by blowing a large amount of cold air, so that a large amount of hot air is generated. In order to fully utilize the heat, a part of hot air enters the rotary kiln through the kiln head to be used as secondary combustion air; a part of hot air enters the predecomposition furnace outside the kiln through the tertiary air pipe and is also used as combustion-supporting air to heat and decompose the materials; the redundant hot air is used by a low-temperature waste heat boiler;
2. high-temperature flue gas at the tail of the rotary kiln and tertiary air generated by the grate cooler enter a predecomposition furnace outside the kiln for predecomposition;
3. high-temperature tail gas generated by the kiln external predecomposition furnace is used by a kiln external multistage suspension preheater; the tail gas from the multistage suspension preheater is used for a vertical mill which is the main equipment of a raw material treatment mechanism and is used for drying raw materials entering the kiln.
Therefore, the key point of the device for energy conservation and emission reduction is the use of the high-efficiency product heat recovery and the flue gas heat recovery.
At the same time, the present invention also provides an embodiment of producing light-burned magnesium oxide using the most preferred apparatus described above.
Examples
The magnesite physicochemical indexes adopted in the embodiment are as follows: mgO (45.5-47%), siO 2 (0.15-2％)、CaO(0.2-0.7％)、Fe 2 O 3 (0.2-0.7％)、Al 2 O 3 (0.1-0.4%) and the granularity is 0-30mm.
S1, magnesite entering a factory is coarsely crushed and then vertically crushed, tail gas generated by a five-stage suspension preheating decomposing furnace mechanism is introduced into a vertical mill, waste heat in the tail gas is used for drying moisture in the magnesite, particularly, concentrate subjected to flotation and filter pressing during calcination of the flotation concentrate contains about 10% of moisture, the concentrate is dried through the waste heat of the tail gas in the vertical mill, and the magnesite powder subjected to the vertical mill can be quantitatively distributed to the five-stage suspension preheating decomposing furnace mechanism without resistance; the tail gas after vertical grinding, breaking and drying is discharged through a cloth bag dust collector;
s2, quantitatively feeding crushed and dried magnesite powder into a five-stage suspension pre-thermal decomposition furnace mechanism from a raw material warehouse through a hoister, preheating each stage of suspension pre-heater step by step, increasing the temperature of the material step by step, increasing the decomposition of magnesium carbonate step by step, feeding the preheated material into a kiln external pre-decomposition furnace at a discharge port of a C4 cyclone, enabling the decomposition rate of the magnesium carbonate at the position to reach 85-90% under the combined action of the material in the kiln external pre-decomposition furnace, tertiary air, tail gas discharged from the kiln tail of the rotary kiln and supplementary fuel, feeding the decomposed material into a C5 cyclone for solid-gas separation, and feeding the pre-decomposed material into the rotary kiln for calcining light burning powder through a discharge port of the C5 cyclone; tail gas generated by the precalciner outside the kiln and tail gas discharged by the C5 cyclone are used by the C4 cyclone; tail gas discharged by each stage of suspension preheater is used for finely breaking and drying materials by a vertical mill;
the temperature and the pressure of the flue gas in the kiln outer pre-decomposition furnace are adjusted by adjusting the supply amount of natural gas and the supply amount of tertiary air, so that the temperature of the flue gas in the decomposition furnace is controlled to be 800-900 ℃, the decomposition rate of magnesite powder magnesium carbonate passing through the pre-decomposition furnace reaches 85-90%, and the temperature of the flue gas discharged out of the kiln outer pre-decomposition furnace reaches 700-800 ℃;
s4, after magnesite powder with the pre-decomposition rate of 85-90% enters the rotary kiln from a kiln tail smoke chamber of the rotary kiln, a large amount of natural gas, high-temperature smoke generated by combustion-supporting secondary air and a high-temperature furnace lining are sprayed through a natural gas spray gun at the kiln head of the rotary kiln, and under the combined action of a kiln tail high-temperature induced draft fan and the rotary kiln with high rotating speed, the decomposition rate of magnesite powder and magnesium carbonate entering the rotary kiln quickly reaches 96-98%, or even is higher; the high-temperature flue gas discharged from the kiln tail of the rotary kiln can be directly supplied to a predecomposition furnace outside the kiln through a kiln tail smoke chamber;
the rotation speed of the rotary kiln and the calcining temperature of the calcining zone are adjusted by regulating and controlling the natural gas supply quantity, the secondary air supply quantity, the raw material blanking quantity and the high-temperature fan rotation speed, and the temperature of the calcining zone of the rotary kiln is controlled between 1050 and 1150 ℃, so that the decomposition rate of the light calcined magnesia reaches 96 to 98 percent, and the temperature of the flue gas discharged from the tail of the kiln reaches 700 to 900 ℃.
The magnesite of the embodiment is ground, broken and dried immediately, and the particle size of raw materials entering a kiln is less than or equal to 75 mu m; the temperature of the discharged kiln after the rotary kiln calcination is 1000 ℃, the temperature of the light-burned magnesia powder before entering the grate cooler is 400-750 ℃, and the temperature of the powder concentrator after cooling is 100 ℃; the exhaust temperature of the tail gas of the kiln is less than 100 ℃.
The chemical indexes of the finally obtained light-burned magnesia powder are as follows: mgO (85.5-97%), siO 2 (0.3-4％)CaO(0.4-1.7％)、Fe 2 O 3 (0.3-0.8％)、Al 2 O 3 (0.1-0.7%) with 200 mesh size; the product meets the index requirements of 80, 90 and 95 light-burned magnesia in YB/T5206-2004 ' light-burned magnesia, a standard of ferrous metallurgy industry of the people's republic of China '.
Table 1 waste heat recovery situation of each waste heat utilization link in the present invention
| Waste heat recovery project | Amount of heat exchange (KJ/KG) 3 ) | Percentage of relative fuel calorific value% |
| Secondary air heat recovery | 202.994 | 4.95 |
| Tertiary air heat recovery | 549.37 | 13.4 |
| Waste heat power generation heat recovery | 339.881 | 8.29 |
| Vertical mill for recovering heat | 31.492 | 0.77 |
TABLE 2 kiln System Heat balance calculation-Heat input (based on 1kg magnesium oxide, 0 ℃ C.)
TABLE 3 kiln System Heat balance calculation-output Heat (based on 1kg magnesium oxide, 0 ℃ C.)
TABLE 4 kiln System Heat balance calculation-Heat recovery (based on 1kg magnesium oxide, 0 ℃ C.)
In summary, the table 1-4 shows that the device for producing light-burned magnesia overcomes the limitation of the existing device for producing light-burned magnesia by suspending and calcining magnesite on high gas flow rate, can perform suspending and calcining at higher gas flow rate, adopts negative pressure operation on the whole device, and has the advantages of controllable gas material stroke, uniform material sintering, adjustable and controllable product activity, stable quality, small heat loss of the device, high efficiency and low tail gas emission.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A device for producing light-burned magnesia by decomposing outside a five-stage suspension preheating kiln is characterized by comprising a raw material treatment mechanism, a five-stage suspension preheating decomposing furnace mechanism, a rotary kiln mechanism, a grate cooler and a clinker grinding mechanism which are connected in sequence,
the five-stage suspension pre-pyrolysis furnace mechanism comprises a multi-stage suspension preheater and an extrakiln pre-pyrolysis furnace, the extrakiln pre-pyrolysis furnace is arranged between the last two stages of suspension preheaters, and tail gas generated by the extrakiln pre-pyrolysis furnace can be used by the raw material treatment mechanism after being subjected to solid-gas separation by the suspension preheaters of all stages;
oxygen-enriched hot air generated by cooling finished products by the grate cooler can be used by the rotary kiln mechanism and the out-of-kiln predecomposition furnace.
2. The device according to claim 1, wherein the five-stage suspension pre-pyrolysis furnace mechanism comprises a C1 cyclone, a C2 cyclone, a C3 cyclone, a C4 cyclone, an extrakiln pre-pyrolysis furnace and a C5 cyclone which are connected in sequence, and the C5 cyclone, the C4 cyclone, the C3 cyclone, the C2 cyclone and the C1 cyclone are communicated in sequence and in reverse direction;
the outlet pipeline of the C1 cyclone is connected with the raw material processing mechanism, the kiln tail waste gas discharge dust collector and the kiln tail exhaust fan through a high-temperature fan, and the C5 cyclone is connected with the rotary kiln mechanism.
3. The device as claimed in claim 2, wherein the rotary kiln mechanism comprises a rotary kiln, a kiln head cover and a kiln tail smoke chamber, the kiln head cover and the kiln tail smoke chamber are respectively arranged at two ends of the rotary kiln, a discharge port of the C5 cyclone is communicated with the kiln tail smoke chamber, and a discharge port of the kiln head cover is communicated with the grate cooler;
and a smoke outlet of the kiln tail smoke chamber is communicated with the kiln external predecomposition furnace.
4. The device as claimed in claim 3, further comprising a tertiary air duct and a gas system, wherein the tertiary air duct communicates the kiln head cover with the kiln external pre-decomposition furnace, and the gas system provides heat sources for the rotary kiln and the kiln tail pre-decomposition furnace respectively.
5. The device of claim 4, wherein the clinker grinding mechanism comprises a coarse powder bin, a Raymond mill, a hoister, a fine powder bin, a metering conveying device, a finished product conveying device and a finished product warehouse which are connected in sequence;
the grate cooler is communicated with the coarse powder bin through a grate cooler lifter.
6. The apparatus of claim 5, wherein the raw material processing mechanism comprises a raw material bin, a raw material vertical mill and a raw material warehouse which are connected in sequence,
the raw material warehouse is communicated with the C1 cyclone, and tail gas generated by the kiln external predecomposition furnace can be used for the raw material vertical mill after solid-gas separation.
7. A method for producing light-burned magnesium oxide using the apparatus of any one of claims 1 to 6, comprising the steps of:
s1, immediately grinding and crushing magnesite ore or flotation concentrate, and sequentially dehydrating, crushing and drying to obtain dried magnesite powder;
s2, preheating the dried magnesite powder step by step, and placing the preheated material in a predecomposition furnace outside a kiln for predecomposition to obtain a predecomposed material;
s3, carrying out solid-gas separation on the pre-decomposed material, and then calcining the material by using a rotary kiln to obtain a calcined material;
and S4, sequentially cooling and grading the calcined material to obtain a light-burned magnesium oxide product.
8. The method as claimed in claim 7, characterized in that during the predecomposition, the temperature of the combustion chamber of the predecomposition furnace outside the kiln is controlled to be 800-950 ℃, and the decomposition rate of the magnesite powder magnesium carbonate is 85-90%; during calcination, the temperature of flue gas in the rotary kiln is controlled to be 1100-1300 ℃, and the decomposition rate of magnesite powder and magnesium carbonate is 96-98%.
9. The method according to claim 7, wherein in step S1, the magnesite powder is dried by waste heat of tail gas generated by the kiln-outside predecomposition furnace during the vertical grinding; in the step S2, the tail gas generated by the kiln external predecomposition furnace and the tail gas generated by the C5 cyclone are used by the C4 cyclone.
10. The method of claim 7, wherein in step S2, the out-of-kiln predecomposition furnace employs an ammonia-free denitration technique.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210866736.1A CN115340304A (en) | 2022-07-22 | 2022-07-22 | Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210866736.1A CN115340304A (en) | 2022-07-22 | 2022-07-22 | Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115340304A true CN115340304A (en) | 2022-11-15 |
Family
ID=83950094
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210866736.1A Pending CN115340304A (en) | 2022-07-22 | 2022-07-22 | Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115340304A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116854383A (en) * | 2023-06-29 | 2023-10-10 | 唐金泉 | Novel low-energy-consumption process system for producing light-burned MgO powder |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4627948A (en) * | 1982-03-18 | 1986-12-09 | Dolomitwerke Gmbh | Method of manufacturing a sintered dolomite in a shaft kiln |
| CN201268663Y (en) * | 2008-09-19 | 2009-07-08 | 仝仲盛 | Apparatus for producing concrete from magnesium smelting waste slag |
| CN103304168A (en) * | 2013-06-27 | 2013-09-18 | 宁夏平罗恒达水泥有限责任公司 | Method for producing cement clinker by using dry-process predecomposition kiln |
| CN108558239A (en) * | 2018-06-26 | 2018-09-21 | 武汉三源特种建材有限责任公司 | A kind of accurate preparation facilities of magnesia and method |
| CN110960967A (en) * | 2019-11-05 | 2020-04-07 | 辽宁天宝华瑞建材有限公司 | Pre-combustion denitration system and method for kiln |
| CN115073024A (en) * | 2022-06-15 | 2022-09-20 | 合肥水泥研究设计院有限公司 | Device and process for preparing active magnesium oxide dry-process light-burning section |
-
2022
- 2022-07-22 CN CN202210866736.1A patent/CN115340304A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4627948A (en) * | 1982-03-18 | 1986-12-09 | Dolomitwerke Gmbh | Method of manufacturing a sintered dolomite in a shaft kiln |
| CN201268663Y (en) * | 2008-09-19 | 2009-07-08 | 仝仲盛 | Apparatus for producing concrete from magnesium smelting waste slag |
| CN103304168A (en) * | 2013-06-27 | 2013-09-18 | 宁夏平罗恒达水泥有限责任公司 | Method for producing cement clinker by using dry-process predecomposition kiln |
| CN108558239A (en) * | 2018-06-26 | 2018-09-21 | 武汉三源特种建材有限责任公司 | A kind of accurate preparation facilities of magnesia and method |
| CN110960967A (en) * | 2019-11-05 | 2020-04-07 | 辽宁天宝华瑞建材有限公司 | Pre-combustion denitration system and method for kiln |
| CN115073024A (en) * | 2022-06-15 | 2022-09-20 | 合肥水泥研究设计院有限公司 | Device and process for preparing active magnesium oxide dry-process light-burning section |
Non-Patent Citations (2)
| Title |
|---|
| 杨泽波;李福洲;张威;: "带预分解系统水泥回转窑煅烧MgO膨胀剂技术研究", no. 10 * |
| 罗先进等: "《新能源利用技术》", 合肥工业大学出版社, pages: 298 - 299 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116854383A (en) * | 2023-06-29 | 2023-10-10 | 唐金泉 | Novel low-energy-consumption process system for producing light-burned MgO powder |
| CN116854383B (en) * | 2023-06-29 | 2024-04-19 | 唐滨江 | Novel low-energy-consumption process system for producing light-burned MgO powder |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US11905181B2 (en) | Method for preparing calcium oxide using a multistage suspension preheater kiln | |
| CN103755171B (en) | A kind of nsp kiln works in coordination with activating coal gangue technique | |
| CN111977995A (en) | Powder lime calcining and reforming system based on novel dry-process cement clinker calcining system | |
| CN107226627A (en) | A kind of two grades of suspension calcining devices of active powder lime | |
| CN212669567U (en) | Powder lime calcining and reforming system based on novel dry-process cement clinker calcining system | |
| CN112142350A (en) | Phosphogypsum desulfurization and calcination treatment system and treatment method | |
| CN213865977U (en) | Ardealite desulfurization calcination processing system | |
| CN103193400A (en) | Temperature-controlled suspension roaster | |
| CN102001837A (en) | Method and device for calcining materials by using low calorific value fuel | |
| CN102180604A (en) | Spinning bed equipment and process for producing high-activity lime with spinning bed | |
| CN207002588U (en) | A kind of active powder lime two level suspension calcining device | |
| CN217127294U (en) | Carbide slag suspension calcining system | |
| CN114134316A (en) | System for extracting vanadium by coarse and fine grading oxidation roasting of stone coal vanadium ore and oxidation roasting method | |
| CN102992661A (en) | Beam type heat storage lime kiln | |
| CN107673637A (en) | The suspension roasting device and its production technology of a kind of powdery active lime | |
| CN115340304A (en) | Device and method for producing light-burned magnesium oxide through decomposition outside five-stage suspension preheating kiln | |
| CN203212470U (en) | Temperature-controllable suspension roaster | |
| CN108585555B (en) | Industrial powder clinker homogeneous calcination preparation equipment and preparation method | |
| CN212504610U (en) | Device for preparing light-burned magnesia and enriching carbon dioxide by self-circulation pyrolysis of flue gas | |
| CN111777340B (en) | Device for preparing light burned magnesia and enriching carbon dioxide by smoke self-circulation pyrolysis | |
| CN108910836A (en) | A kind of technique and device of gypsum Sulphuric acid coproduction lime | |
| CN105152141A (en) | Thermal technology for making acid from gypsum as well as device | |
| CN116083673B (en) | Synchronous desulfurization and denitrification system for cascade utilization of flue gas of blast furnace hot blast stove | |
| CN115259102B (en) | Process and equipment for preparing sulfur dioxide concentrated flue gas and silicate clinker by flue gas diversion | |
| CN214009940U (en) | Energy-saving suspension roasting coal gangue treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |