CN116143425B - Central burner type lime kiln - Google Patents
Central burner type lime kiln Download PDFInfo
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- CN116143425B CN116143425B CN202310089589.6A CN202310089589A CN116143425B CN 116143425 B CN116143425 B CN 116143425B CN 202310089589 A CN202310089589 A CN 202310089589A CN 116143425 B CN116143425 B CN 116143425B
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- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 74
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 74
- 239000004571 lime Substances 0.000 title claims abstract description 74
- 238000002485 combustion reaction Methods 0.000 claims abstract description 135
- 239000000446 fuel Substances 0.000 claims abstract description 75
- 230000002093 peripheral effect Effects 0.000 claims abstract description 72
- 238000001035 drying Methods 0.000 claims abstract description 35
- 239000002918 waste heat Substances 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims abstract description 32
- 238000005338 heat storage Methods 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims description 36
- 239000004575 stone Substances 0.000 claims description 27
- 238000001816 cooling Methods 0.000 claims description 23
- 238000000034 method Methods 0.000 claims description 16
- 238000010438 heat treatment Methods 0.000 claims description 12
- 238000007664 blowing Methods 0.000 claims description 10
- 238000007789 sealing Methods 0.000 claims description 8
- 239000002737 fuel gas Substances 0.000 claims description 7
- 238000005303 weighing Methods 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 2
- 208000028659 discharge Diseases 0.000 claims 17
- 239000002028 Biomass Substances 0.000 abstract description 89
- 239000000843 powder Substances 0.000 abstract description 59
- 238000004519 manufacturing process Methods 0.000 abstract description 27
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 16
- 238000000197 pyrolysis Methods 0.000 abstract description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 8
- 239000001569 carbon dioxide Substances 0.000 abstract description 8
- 230000000694 effects Effects 0.000 abstract description 5
- 238000002156 mixing Methods 0.000 abstract description 5
- 230000002269 spontaneous effect Effects 0.000 abstract description 5
- 239000006229 carbon black Substances 0.000 abstract description 3
- 238000005336 cracking Methods 0.000 abstract description 3
- 238000005507 spraying Methods 0.000 abstract description 2
- 230000001360 synchronised effect Effects 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 description 43
- 238000001354 calcination Methods 0.000 description 18
- 229910052799 carbon Inorganic materials 0.000 description 13
- 239000012071 phase Substances 0.000 description 12
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 11
- 230000008569 process Effects 0.000 description 11
- 230000008901 benefit Effects 0.000 description 10
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 10
- 239000000292 calcium oxide Substances 0.000 description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 9
- 235000019738 Limestone Nutrition 0.000 description 8
- 239000006028 limestone Substances 0.000 description 8
- 230000009467 reduction Effects 0.000 description 8
- 238000000354 decomposition reaction Methods 0.000 description 7
- 239000003546 flue gas Substances 0.000 description 7
- 230000006870 function Effects 0.000 description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000003245 coal Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000009841 combustion method Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 150000001720 carbohydrates Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 210000001503 joint Anatomy 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010742 number 1 fuel oil Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 230000029553 photosynthesis Effects 0.000 description 1
- 238000010672 photosynthesis Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002699 waste material Substances 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
- C04B2/00—Lime, magnesia or dolomite
- C04B2/10—Preheating, burning calcining or cooling
- C04B2/12—Preheating, burning calcining or cooling in shaft or vertical furnaces
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- 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
- F27D99/00—Subject matter not provided for in other groups of this subclass
- F27D99/0001—Heating elements or systems
- F27D99/0033—Heating elements or systems using burners
-
- 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
Abstract
The invention discloses a central burner type lime kiln, which solves the key technical problems of mixing and synchronous conveying and burning of combustion air and biomass powder dilute phase and spontaneous combustion ignition of biomass powder through the combined application of key devices such as a novel central burner in a furnace, a peripheral combustion chamber outside the furnace, a honeycomb type waste heat fuel drying device, a high-temperature heat storage device and the like. High-temperature cracking of biomass powder into the biomass powder rich in H in a furnace 2 +CO+CH 4 The combustible pyrolysis gas and the pyrolysis carbon black of the components are directly combusted to produce lime, so that the purpose of producing high-activity lime by independently and directly spraying biomass powder in a shaft kiln is achieved, and the purpose of producing lime by double combustion of gas and powder is also achieved. Has important significance in improving the production process level of the whole lime, deeply utilizing the cleanness of the biomass fuel, reducing the emission of carbon dioxide, improving the ecological environment, guaranteeing the national energy safety and the like.
Description
Technical Field
The invention relates to the technical field of lime production, in particular to a central burner type lime kiln.
Background
Along with the ecological environment protection entering a new stage of pollution reduction and carbon reduction cooperative treatment, lime kilns adopting solid traditional fossil energy fuels such as coal are phased out or forbidden to be constructed, and lime production links are also listed as important fields needing ultra-low emission reconstruction. The lime industry develops alternative novel energy sources to reduce the consumption of primary fossil fuel while improving the production technology, and is a necessary way for realizing the low-carbon development of the lime industry.
Among various alternative renewable energy sources, the nuclear energy and the large hydropower have potential ecological environment risks, regional resources such as wind energy, geothermal energy and the like are restricted and questioned greatly, and biomass energy is approved by the characteristics of ubiquitous property, richness, renewable property and the like. Biomass is unique in that it can store not only solar energy, but also a renewable carbon source, which can be converted into conventional solid, liquid and gaseous fuels, and coal, petroleum, natural gas, and other energy sources are also substantially converted from biomass energy. Moreover, biomass energy, which is a clean renewable energy source, has the characteristics of wide sources, environmental friendliness, neutrality of carbon and the like, is listed as a fourth most energy source. It is predicted that by the middle of the 21 st century, various biomass alternative fuels produced using new technology will account for over 40% of total global energy consumption.
The natural biomass energy has high volatile content and is easy to burn, the physicochemical property of the pyrolyzed biochar is close to that of pulverized coal, and the biomass energy is used as fuel for lime production, so that the energy saving and emission reduction effects of the biomass energy can be effectively exerted. And according to the calculation of the output of a stone ash shaft kiln capable of producing 10 ten thousand tons per year, if biomass fuel is adopted to replace coal, the carbon emission can be reduced by 1 ten thousand tons per year, and the carbon emission can be reduced by 3.6 ten thousand tons, so that the energy-saving and emission-reducing potential is huge.
Biomass energy modem utilization can be divided into four basic types: direct combustion, pyrolysis, gasification and liquefaction.
Direct combustion is the simplest way of biomass application and is also the earliest traditional way of biomass use, but partial biomass is used as a low-grade fuel, the combustion efficiency is extremely low, the temperature reached by combustion is low, and the industrial application of biomass energy is greatly influenced.
Pyrolysis is a basic thermochemical process that converts biomass into useful fuels. Biomass is combusted in the presence of anoxic heating or partial oxygen, which can produce a hydrocarbon rich gas mixture, an oily liquid, and a carbon rich solid residue. The pyrolysis has the advantages of simple equipment and capability of producing carbon and various chemical products; the method has the defects of low utilization rate and low applicability.
Gasification is also a pyrolysis technology, and mainly is a technology for converting substances into combustible gas, and can be low-heating-value gas or medium-heating-value gas according to different technical routes. The biomass fuel has the main advantages that after being converted into combustible gas, the biomass fuel has higher utilization efficiency and wide application, and can be used as domestic gas, boiler gas or direct power generation; the main disadvantages are the complex system and the necessity of special users or supporting utilization facilities due to the inconvenient storage and transportation of the generated fuel gas.
The liquefaction is to decompose the macromolecules of the raw materials into small molecular compounds under the action of a proper catalyst, and then polymerize the small molecular compounds into oil compounds with proper molecular weight. The main advantage of liquefaction is that biomass can be made into oil products for combustion, and the biomass can be used as a substitute of petroleum, so that the application range and the added value are greatly improved; the main disadvantage is the complex technology and the current costs are still high.
Through practice and research, the biomass gasification and liquefaction technology has the advantages of complex process investment, low yield and unreasonable economy, and difficult industrialization and further popularization in the recent years, although clean and efficient secondary fuel can be obtained. Direct combustion is the simplest and earliest biomass energy utilization mode, but in the traditional combustion mode, the biomass combustion efficiency is extremely low, and the waste of energy and resources is great. Therefore, if a convenient and efficient biomass direct combustion technology can be researched and developed, the method has good economic and social benefits.
At present, the lime production mode mainly adopts a shaft kiln process, and a single-hearth shaft kiln and a double-hearth shaft kiln are produced by adopting a single fuel structure mode: firstly, a mixing type production process of mixing and burning massive coal fuel and stone is adopted, and secondly, fluid fuels such as fuel gas, fuel oil and the like are adopted for production. Although the industry has also attempted to adopt a production method in which solid fuels such as biomass particles and briquettes are directly mixed with stone for combustion, the biomass fuels cannot be used in conventional shaft kilns because the biomass fuels have the disadvantages of low heat value, high volatile matter, high ash content, short combustion time and the like. Especially, the calorific value of biomass is only about 4000 kilocalories, the decomposition temperature of lime production can not be reached by direct combustion, and the volatile component is more than 70 percent, so that the calcination zone which can not reach the lime shaft kiln in the shaft kiln production can not be discharged out of the kiln along with flue gas after participating in combustion, the heat loss is larger, and the decomposition temperature of lime production can not be reached.
Disclosure of Invention
Therefore, the invention provides a central burner type lime kiln, which solves the key technical problems of mixing and synchronous conveying and burning of combustion air and biomass powder dilute phase and spontaneous combustion ignition of biomass powder through the combined application of key devices such as a novel central burner in the kiln, a peripheral combustion chamber outside the kiln, a honeycomb type waste heat fuel drying device, a high-temperature heat storage device and the like, thereby solving the corresponding technical problems mentioned in the background art.
The invention breaks through the traditional biomass utilization mode, proposes to make biomass into powder for utilization, obtains enough energy, and has important significance for sustainable utilization of energy and environmental protection.
The invention discloses a method for directly burning and calcining lime by cracking biomass powder into pyrolysis gas and pyrolyzed carbon black in a lime shaft kiln and the key points of production process control and the like from the in-depth research of a production mode, technological parameters, physical mechanism, chemical dynamics and the like in the production of active lime by biomass fuel, solves the common problem of the shaft kiln for calcining active lime by adopting biomass solid powder fuel from a brand-new production process and concept, particularly realizes the purpose of directly blowing solid biomass powder fuel into a furnace by arranging a central burner, and simultaneously realizes the production of lime by a gas-powder double combustion method and an oxyhydrogen combustion method. The typical characteristics of direct combustion and thermal cracking coupling combustion of biomass are realized, and the active lime production process and device with short calcination time, low energy consumption, high activity of produced lime and low C, S element content are provided.
The invention can promote the transformation and generation of fuel selection for producing lime, and has key significance for realizing green and carbon reduction upgrading of lime industry and solving industry common bottlenecks.
The invention not only achieves the aim of producing high-activity lime by independently and directly spraying biomass powder, but also has the function of synchronously mixing and conveying combustion-supporting air and the dilute phase of the biomass powder, and solves the key technical problem of spontaneous ignition of the biomass powder through the combined use of the opposite double-screw quantitative feeding device, the fuel dilute phase porous air distributor, the central burner nozzle sprayer in the furnace, the peripheral combustion chamber of the furnace, the honeycomb type waste heat fuel drying device, the high-temperature heat storage device and the like.
The invention also has the function of independently using low-heat-value gas fuel such as blast furnace gas, producer gas and the like for production, can be automatically allocated and switched according to production working conditions, adopts full-automatic DCS control for free allocation, and can meet the ideal technological characteristic requirements of ignition temperature, ignition concentration limit, flame propagation speed, combustion reaction speed and the like. The technology has the advantages of simple, practical and compact structure, high production efficiency, high yield and good economy. The method has the advantages of deep utilization of biomass fuel, reduction of serious pollution to the environment caused by the use of fossil fuel, and great significance in improving the overall lime production process level, reducing the production cost, improving the product quality, reducing pollution and carbon reduction, improving the ecological environment, guaranteeing the energy safety and the like.
Adopts one or more of the following key technological measures:
(1) And the waste heat exchange function of the central burner in the furnace and the high-strength heat storage device in the preheating zone in the furnace is utilized to fully heat the combustion air, so that the combustion air achieves the function of spontaneous combustion ignition and combustion of biomass powder.
(2) And high-temperature cracking the biomass powder into pyrolysis gas and pyrolysis carbon black by blowing the biomass powder into the lime shaft furnace. Pyrolysis gas mainly being H 2 CO reacts with oxygen in a calcining zone of the lime shaft furnace to generate carbon monoxide and participate in combustion, the unit calorific value and the combustion temperature of the biomass powder can be effectively improved by controlling the blowing amount of the biomass powder, and when the blowing amount of the biomass powder is higher, the carbon monoxide can be generated by reacting with carbon dioxide.
(3) The technology of coupling combustion of biomass powder and hydrogen-rich gas is adopted, by utilizing the moisture characteristic of the biomass powder with the moisture content of 10-30 percent, when the water vapor is in the environment of more than 1200 ℃ in the combustion process, the water vapor is decomposed into hydrogen and oxygen to participate in combustion, so that the hydrogen is fully combusted to release more heat, the aim of generating heat by using part of water as fuel for combustion is realized, the aims of supporting combustion and improving the combustion temperature are also achieved,
(4) Pyrolysis gas H generated when biomass powder is combusted in high temperature zone in furnace 2 The content of CO can reach more than 14 percent, the content of CH can reach more than 20 percent 4 The content can reach more than 5%, and the combustible gases are converted into heat energy in the combustion process, so that the combustion temperature is increased, and the decomposition temperature of the limestone is reached.
One or more of the following key equipment and measures are adopted:
(1) The pressure and pneumatic dilute phase material conveying required by the conveying of biomass fuel powder are realized through the combined application of the solid biomass powder fuel opposite double-screw quantitative feeding device, the combustion-supporting fan (high-pressure fan), the porous air distributor and the conveying pipeline, so that the aim of synchronously conveying and burning the combustion-supporting air and the biomass fuel is fulfilled.
(2) And arranging a honeycomb type waste heat fuel drying device, preheating and drying biomass powder by using waste heat of furnace top flue gas, and partially dehydrating the biomass powder by using a vapor phase pressure swing flash evaporation process principle to prepare biomass hydrogen-rich micro powder with high heat value and high oxygen content, and simultaneously, achieving ideal conveying performance and ideal ignition point.
(3) The biomass powder after preheating and drying is conveyed in dilute phase, and independent branch pipelines are arranged at the outlet of the porous air distributor and are independently butted with the peripheral burner of the furnace arranged in the roasting system of the lime shaft furnace body, so that each independent burner is provided with an independent fuel conveying pipeline.
(4) And a furnace center burner is arranged in the lime shaft furnace body, biomass powder fuel is injected into the furnace center, and when flames of the furnace peripheral burner cannot reach the furnace center, the furnace center burner can effectively supplement heat energy (the biomass powder burns to provide heat energy).
(5) The combustion air preheating function is arranged in the central burner in the furnace to preheat the combustion air of the central burner in the furnace and the peripheral burner outside the furnace, so that the purposes of saving energy and improving combustion efficiency are achieved.
(6) And the biomass powder fuel is injected into the furnace by using a central burner in the furnace, so that the aim of directly burning the biomass powder is fulfilled.
(7) And a plurality of high-temperature heat storage devices are arranged in the furnace body preheating zone, the primary preheated combustion air from the central burner in the furnace is subjected to secondary high-temperature heat storage by utilizing the high-temperature exhaust gas temperature of the furnace body preheating zone, so that the temperature of the combustion air is raised to be more than 350 ℃, the ignition point of biomass powder is reached, and the spontaneous combustion ignition combustion is realized.
(8) The multifunctional lifting rotary distributor is arranged in the lime shaft furnace body distribution system, and stone materials with different particle sizes in the stone materials are distributed in a grading way through the lifting, tilting, rotating and other functions of the device, so that stone materials with large particle sizes are uniformly distributed on the periphery of the kiln wall, and the combustion penetration resistance of flames of a burner on the periphery of the furnace is reduced.
(9) The ash discharging system is provided with a multipoint rotary metering ash discharging device (a movable material flow control device, a liftable material flow control device, a unidirectional rotary ash discharging device and a two-stage sealing discharger), and the furnace condition can be controlled and adjusted in a manner of precisely controlling the ash discharging amount.
(10) The high-pressure combustion-supporting cooling type multifunctional blast cap is arranged in the air supply system of the lime shaft furnace body, so that the purposes of supporting air and cooling the combustion device in the central furnace are achieved.
In order to achieve the above object, the present invention provides the following technical solutions:
the utility model provides a center burner formula lime kiln, includes shaft furnace body, in-furnace center burner, opposite direction double helix dosing device, porous air distributor and honeycomb formula waste heat fuel drying device, the burning area of shaft furnace body is equipped with the peripheral combustion chamber of stove, in-furnace center burner sets up on the axis in the shaft furnace body and be located in the below of peripheral combustion chamber of stove, opposite direction double helix dosing device is connected with porous air distributor process, porous air distributor with honeycomb formula waste heat fuel drying device's material inlet connection, honeycomb formula waste heat fuel drying device's flue gas inlet pass through the pipeline with the top of shaft furnace body is connected, honeycomb formula waste heat fuel drying device's material export with peripheral combustion chamber of stove and in-furnace center burner are connected.
Further, the honeycomb type waste heat fuel drying device is a honeycomb type multi-section drying device and comprises an inner furnace feeding section and an outer furnace feeding section, wherein multi-pipe type channels are arranged in the inner furnace feeding section and the outer furnace feeding section, the multi-pipe type air distributor is connected with the inner furnace feeding section and the outer furnace feeding section through two pipelines, the inner furnace feeding section is connected with the multi-layer blowing chamber of the inner furnace center burner in a one-to-one correspondence manner through a plurality of independent pipelines, and the outer furnace feeding section is connected with the outer furnace peripheral combustion chamber in a one-to-one correspondence manner through a plurality of independent pipelines.
Further, the honeycomb type waste heat fuel drying device further comprises a plurality of sections of combustion-supporting gas heating sections, and the plurality of sections of combustion-supporting gas heating sections are connected in series; the lime kiln further comprises a first combustion-supporting fan, the first combustion-supporting fan is connected with the porous air distributor through a pipeline, the first combustion-supporting fan is connected with an air inlet at the head part of the combustion-supporting gas heating section which is connected in series through another pipeline, and a combustion-supporting gas outlet at the tail part of the combustion-supporting gas heating section which is connected in series is connected with the peripheral combustion chamber outside the furnace through a pipeline.
Further, the furnace outer peripheral combustion chamber comprises at least one furnace outer peripheral short flame combustion chamber and at least one furnace outer peripheral flat long flame combustion chamber, and the furnace outer peripheral short flame combustion chamber is positioned above the furnace outer peripheral flat long flame combustion chamber.
Further, the furnace outer periphery combustion chamber further comprises a furnace outer periphery inclined long flame combustion chamber, the furnace outer periphery inclined long flame combustion chamber is positioned below the furnace outer periphery flat long flame combustion chamber, the furnace outer periphery inclined long flame combustion chamber is positioned above the furnace inner center burner, and the furnace outer periphery inclined long flame combustion chamber can spray fuel gas obliquely downwards towards the furnace inner center burner.
Further, the lime kiln further comprises a second combustion-supporting fan, a high-temperature heat storage device and a furnace outer hot-air peripheral pipe, a cooling channel is arranged in the furnace inner central burner, the second combustion-supporting fan is connected with the cooling channel in the furnace inner central burner through a pipeline, the high-temperature heat storage device is arranged at the top of the shaft furnace body, an outlet of the cooling channel in the furnace inner central burner is connected with the high-temperature heat storage device through a pipeline, the high-temperature heat storage device is connected with the furnace outer hot-air peripheral pipe through a descending pipeline, and a material outlet of a furnace outer feeding section of the honeycomb type waste heat fuel drying device is connected with the furnace outer peripheral combustion chamber through a corresponding pipeline and the furnace outer hot-air peripheral pipe.
Further, the lime kiln further comprises a combustion-supporting air cap, wherein the combustion-supporting air cap is arranged at the center of the bottom of the shaft furnace body, and the shaft furnace body is positioned below the burner of the center burner in the furnace.
Further, the lime kiln further comprises a stone weighing device, a feeding trolley and a lifting type rotary distributor which are connected in sequence, wherein the stone weighing device and the feeding trolley are arranged outside the shaft furnace body, and the lifting type rotary distributor is arranged at the top of the shaft furnace body.
Further, the lime kiln further comprises a peripheral discharging bin, a peripheral discharging tube, a movable material flow control device, a central discharging bin, a liftable material flow control device, a unidirectional rotation ash discharging device, a metering device, a discharging controller, an ash discharging bin and a two-stage sealing discharger, wherein the peripheral discharging bin and the central discharging bin are arranged at the bottom of the shaft furnace body, the peripheral discharging bin is uniformly distributed at the peripheral side of the central discharging bin, the unidirectional rotation ash discharging device is arranged below the central discharging bin, the peripheral discharging bin is connected with the unidirectional rotation ash discharging device through the peripheral discharging tube, the movable material flow control device is arranged in the peripheral discharging tube, the bottom of the central discharging bin is provided with the liftable material flow control device, the unidirectional rotation ash discharging device is connected with the metering device, the metering device is provided with the discharging controller, and the ash discharging bin is connected with the two-stage sealing discharger.
The invention has one or more of the following advantages:
(1) The wood, the wood dust and the straw are used for replacing fuels such as coal, coal gas, natural gas and the like to calcine lime, so that the fuel cost is reduced, and the environment is protected.
(2) The biomass powder is conveyed to the double-screw quantitative feeding device only by one device, and the feeding and switching of the fuel can be completed under the condition of almost no increase of cost.
(3) The problem of uneven heat supply of biomass powder caused by physical characteristics can be reduced to the greatest extent, and corresponding fuel quantity can be obtained for each burner and each combustion chamber.
(4) The ideal combustion effect is realized by controlling the key process nodes such as the particle size of the biomass powder, the powder flow, the primary air inlet quantity, the secondary air inlet quantity and the optimal concentration of the powder in the air.
(5) The fuel gas can be independently produced by using the fuel gas; or produced by using biomass powder fuel singly and completely; or can realize the mixed combustion production of fuel gas and biomass powder fuel.
(6) Because the central burner in the furnace is arranged, the central heat energy supply in the furnace is more balanced, the problems of low yield and high lime burning rate caused by the fact that the heat energy of the traditional peripheral burner type gas shaft kiln cannot reach the center of the furnace are solved, the yield of the traditional single-hearth shaft furnace is increased by times, and the yield and the production utilization coefficient are higher than those of the existing double-hearth lime kiln.
(7) The system has simple and compact structure and is convenient to operate.
(8) The main technological structural characteristics of the traditional coal-fired lime shaft furnace and the gas-fired lime shaft furnace are not changed, so that most of the lime shaft furnace can be applied to the technical scheme of the invention, and industrial popularization is facilitated.
(9) Realize carbon dioxide emission reduction: the main component of biomass fuel is carbohydrate, carbon dioxide emitted in the combustion process corresponds to carbon dioxide absorbed in photosynthesis, and a natural carbon balance is formed, and the carbon balance is scientifically called zero emission.
(10) Sulfur dioxide low emissions: the sulfur content of the biomass fuel is low, the sulfur dioxide emission is less than 1mg/m < 3 >, the carbon dioxide emission is far lower than the carbon dioxide emission of burning coal and fuel oil, and the sulfur dioxide emission reduction can be realized without installing a desulfurization device.
(11) The biomass fuel has rich resources, can be regenerated and circularly grown, and is inexhaustible.
(12) The investment is low, and the characteristics of high return on investment and high cost performance of the traditional lime shaft furnace are continued; compared with the investment of the traditional single-hearth mixed type coal-fired lime shaft furnace, the investment of the whole production system is not increased except for the increased investment of the combustion system device; compared with the investment of the double-hearth lime kiln, the investment of the double-hearth lime kiln with the same yield is about one third of that of the double-hearth lime 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 description of the embodiments or the prior art will be briefly described below. It will be apparent to those skilled in the art from this disclosure that the drawings described below are merely exemplary and that other embodiments may be derived from the drawings provided without undue effort.
The structures, proportions, sizes, etc. shown in the present specification are shown only for the purposes of illustration and description, and are not intended to limit the scope of the invention, which is defined by the claims, so that any structural modifications, changes in proportions, or adjustments of sizes, which do not affect the efficacy or the achievement of the present invention, should fall within the scope of the invention.
Fig. 1 is a schematic structural diagram of a central burner lime kiln according to an embodiment of the present invention.
In the figure: 1: a counter-rotating double screw dosing device; 2: a porous air distributor; 3: honeycomb type waste heat fuel drying device; 3-1: a furnace feeding section; 3-2: an external furnace feeding section; 4: a feed branch conduit; 5: a first combustion fan; 6: a furnace outer hot air surrounding pipe; 7: a central burner in the furnace; 8: a shaft furnace body; 9: a stone weighing device; 10: feeding trolley; 11: lifting type rotary distributing device; 12: a furnace outer peripheral short flame combustion chamber; 13-1: a furnace outer periphery is provided with a long flame combustion chamber in a flat direction; 13-2: a furnace outer periphery inclined long flame combustion chamber; 14: a combustion-supporting air cap; 15: peripheral discharging bins; 16: peripheral blanking pipes; 17: a movable material flow control device; 18: a central discharging bin; 19: a liftable material flow control device; 20: a unidirectional rotation ash discharging device; 21: a metering device; 22: a discharge controller; 23: an ash discharge bin; 24: a two-stage sealing discharger; 25: a second combustion fan; 26: a high temperature heat storage device; 27: furnace bottom hot air surrounding pipe; 28: a first combustion air duct; 29: and a second combustion-supporting air pipeline.
Detailed Description
Other advantages and advantages of the present invention will become apparent to those skilled in the art from the following detailed description, which, by way of illustration, is to be read in connection with certain specific embodiments, but not all embodiments. 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.
The terms such as "upper", "lower", "left", "right", "middle" and the like are also used in the present specification for convenience of description, but are not intended to limit the scope of the present invention, and the changes or modifications of the relative relationship thereof are considered to be within the scope of the present invention without substantial modification of the technical content.
As shown in fig. 1, the embodiment provides a central burner lime kiln, which is used for accurately feeding biomass powder to a double-screw quantitative feeding device 1 and realizing dilute phase conveying of biomass powder fuel by combining with a porous air distributor 2. In the conveying process, the honeycomb type waste heat fuel drying device 3 exchanges heat with high-temperature flue gas with the temperature higher than 500 ℃ from the furnace top, the biomass powder is partially dehydrated and dried by a gas phase pressure-variable flash evaporation process principle, so that the biomass hydrogen-rich micro powder with high heat value and rich oxygen is formed, and meanwhile, the moisture in the conveyed fuel reaches the proportion suitable for combustion.
The honeycomb type waste heat fuel drying device 3 is internally designed into a tubular honeycomb structure, is in butt joint (single pipe is opposite to single pipe) with the same number of pipelines of the porous air distributor 2, and is respectively supplied with biomass powder to a furnace peripheral burner (a furnace peripheral short flame combustion chamber 12, a furnace peripheral flat long flame combustion chamber 13-1 and a furnace peripheral inclined long flame combustion chamber 13-2) arranged outside the furnace body and a furnace inner central burner 7 inside the furnace body through a plurality of independent conveying branch pipelines arranged on the porous air distributor 2, and meanwhile, the furnace peripheral burner and the furnace inner central burner 7 are communicated with combustion-supporting fans (a first combustion-supporting fan 5 and a second combustion-supporting fan 25) through pipelines, and high-pressure oxygen-enriched combustion of biomass powder in a calcination zone area inside the lime shaft furnace is realized through controlling a flow control device, a pressure control device, a valve and the like arranged on the corresponding pipelines.
The stones sequentially pass through the stone weighing device 9, the feeding trolley 10 and the lifting rotary distributor 11 at the furnace top and are uniformly arranged in the preheating zone in the furnace. When the stone in the preheating zone slowly descends to the upper part of the calcining zone in the furnace, the stone firstly exchanges heat with the flame sprayed by the short flame combustion chamber 12 at the periphery of the furnace, so that the stone reaches the initial decomposition temperature above 890 ℃. When the initially decomposed stone slowly descends to the middle part of the calcining zone in the furnace, heat exchange is carried out again with flames ejected from the long flame combustion chamber 13-1 at the outer periphery of the furnace, so that the stone reaches a temperature above 1100 ℃ at which the stone can be completely decomposed, carbon dioxide in the limestone in the region can be fully decomposed and released, and more than 70% of the limestone is decomposed into calcium oxide (lime). Because of the short combustion characteristics of the biomass pulverized fuel flame and the stone resistance in the furnace, the flame of the combustion chamber at the outer periphery of the furnace cannot penetrate into the central area in the furnace body, and about 30% of limestone at the central part in the furnace cannot be completely decomposed at the moment, and other decomposed calcium oxide slowly descends to the lower part of the calcining zone in the furnace, and the lime is combusted again with the fuel sprayed by the burner 7 of the central burner in the furnace to perform heat exchange, so that the limestone in the furnace can be completely decomposed. The calcium oxide produced after complete decomposition slowly descends to the cooling zone inside the furnace body.
The central burner 7 has a heat exchange function, and can exchange waste heat between cooling air and high-temperature calcium oxide while cooling the central burner, so that the temperature of combustion air is raised once, and the raised combustion air and high-temperature flue gas with the temperature of 450-550 ℃ in a preheating zone at the top of the furnace are subjected to secondary high-temperature heat accumulation and temperature rise, and the temperature reaches the ideal ignition temperature of biomass powder through the high-temperature heat accumulation device 26. The high-temperature combustion-supporting air is communicated with the peripheral combustion chamber of the furnace through a pipeline and a peripheral hot air pipe 6 outside the furnace, and is mixed with biomass powder dried by the honeycomb type waste heat fuel drying device 3 for combustion. Because the ignition point of the biomass powder is only 300-350 ℃, the biomass powder is self-ignited and burnt after encountering high-temperature combustion air of 350-450 ℃ to form a stable combustion flame.
In the whole calcining process, the secondary combustion air (cold air) blown out by the combustion-supporting air cap 14 of the cooling belt in the furnace and the high-temperature hot calcium oxide with the temperature of 750-950 ℃ reduced by the cooling belt are subjected to heat exchange in countercurrent, and the exchanged high-temperature air with the same temperature continuously goes up to the calcining belt in the furnace to participate in the calcining, so that the temperature of the calcining belt is stabilized at the optimal limestone decomposition temperature of 1250 ℃.
When the calcium oxide which is completely decomposed and cooled slowly drops to the lower area of the furnace auxiliary combustion fan cap 14 device, the temperature of the calcium oxide is reduced to about 200 ℃, and the purposes of cooling and heat exchange of the calcium oxide are achieved. The cooled calcium oxide enters a plurality of peripheral discharging bins 15 which are arranged at the bottom of the furnace and are equally divided according to the periphery of the kiln wall, and a central discharging bin 18 which is positioned at the center of the furnace, and descends to the upper side of a unidirectional rotation ash discharging device 20 through a peripheral discharging pipe 16 and a central discharging pipe 17 under the control of a movable material flow control device 17 and a liftable material flow control device 19, and the calcium oxide is discharged into a plurality of metering devices 21 through rotation, and the metered calcium oxide is discharged into an ash discharging bin 23 at the bottom of the furnace through a discharging controller 22, and the materials are discharged out of the furnace through a two-stage sealing discharger 24.
The main process flow is as follows:
the counter-double screw dosing device 1 delivers powder into a porous air distributor 2, which porous air distributor 2 is connected to a feed branch pipe 4. The first combustion fan 5 feeds combustion air into the porous air distributor 2 through a first combustion air duct 28. The porous air distributor 2 distributes the combustion air uniformly and uniformly, so that the combustion air is combined with the powder supplied to the double-screw quantitative feeding device 1 to form dilute phase conveying. Dilute phase materials enter the honeycomb type waste heat fuel drying device 3 to be preheated and dried with flue gas from the furnace top. The honeycomb type waste heat fuel drying device 3 is arranged in a multi-section mode, wherein an inlet of a feeding section 3-1 in the furnace is a multi-pipe type channel, dilute phase materials from a feeding branch pipeline 4 are split in a multi-channel mode, and the materials in each pipeline are equal in quantity. The outlet of the feeding section 3-1 in the furnace of the honeycomb type waste heat fuel drying device 3 is equal to the inlet pipeline in number, the outlet of each pipeline is connected with an independent pipeline to form an independent conveying channel, and the independent conveying channels are respectively communicated with a plurality of channels in the independent furnace bottom hot air surrounding pipe 27 of the lime shaft furnace body. The number of burners connected with the furnace bottom bustle pipe 27 is equal to the number of outlet pipelines of the feeding section 3-1 in the furnace. The outlet of each pipeline is connected with an independent pipeline to form an independent conveying channel which is respectively communicated with a plurality of layers of nozzles of a central burner 7 in the shaft furnace body 8. The inside of the central burner 7 is provided with a plurality of layers of blowing chambers, and each blowing chamber is respectively connected with a plurality of independent conveying pipelines from the outlet of the feeding section 3-1 in the furnace to form independent conveying and blowing units.
The inlet of the feeding section 3-2 outside the furnace of the honeycomb type waste heat fuel drying device 3 is also a multi-pipe type channel, and dilute phase materials from the feeding branch pipeline 4 are split in a multi-channel way, so that the materials in each pipeline are equal in quantity. The outlet of the external furnace feeding section 3-2 of the honeycomb type waste heat fuel drying device 3 is equal to the number of the inlet pipelines, the outlet of each pipeline is connected with an independent pipeline to form an independent conveying channel, and the independent conveying channel is communicated with the external furnace periphery short flame combustion chamber 12, the external furnace periphery flat long flame combustion chamber 13-1 and the external furnace periphery inclined long flame combustion chamber 13-2 of the shaft furnace body 8, and each independent external furnace periphery combustion chamber is respectively connected with the outlet of the external furnace feeding section 3-2 through an independent conveying pipeline to form an independent conveying and blowing unit.
The tail end of the feeding branch pipe 4 is divided into at least two parts which are respectively connected with the inlets of the in-furnace feeding section 3-1 and the out-furnace feeding section 3-2, and the feeding branch pipe 4 can be divided into two parts with different diameters which are connected with the outlets of the porous air distributor 2, so that the quantity of powder entering the in-furnace feeding section 3-1 and the in-furnace feeding section 3-1 is controlled. Because the honeycomb type waste heat fuel drying device 3 is of a multi-stage type, the in-furnace feeding section 3-1 and the out-furnace feeding section 3-2 are only one section of the honeycomb type waste heat fuel drying device 3, and the rest sections are used for heating combustion air.
The whole production system of the shaft furnace is completed by a shaft furnace body 8, stones enter a feeding trolley 10 through a weighing device 9 and are lifted into a furnace top lifting type rotary distributor 11, when the stones enter the furnace body 8, the stones are preheated with smoke gas at about 450-550 ℃ in a preheating zone in the furnace, when the preheated stones reach more than 600 ℃, the stones slowly descend to a calcining zone, the furnace body 8 is provided with three or more layers of combustion chambers in the middle of the furnace body, wherein a furnace outer periphery short flame combustion chamber 12 of the uppermost layer and a furnace outer periphery flat long flame combustion chamber 13-1 of the middle layer jointly emit incandescent flames, and the area forms a stable calcining zone high-temperature area and carries out heat exchange with the stones. When the limestone is decomposed to about 70%, the limestone slowly descends to the upper part of the central burner 7 in the furnace, the powder dilute phase fuel sprayed by the multi-layer nozzles of the central burner 7 in the furnace and the obliquely downward flame sprayed by the obliquely long flame combustion chamber 13-2 at the periphery of the lowest layer of the calcining zone form a cross flame combustion area, a combustion layer with an integral section is formed in the furnace, and the decomposition of the stone materials with the residual content of about 30% is completed. The secondary combustion air of the whole calcining zone comes from the combustion air cap 14 and the second combustion air fan 25 arranged at the bottom of the furnace.
The central burner 7 is internally provided with a cooling channel, the cooling air is from a second combustion-supporting fan 25 in an air cooling mode, the temperature of the cooling air reaches about 100 ℃ after passing through the inside of the central burner 7, the cooling air rises to a high-temperature heat storage device 26 (a heat exchange tube of the cooling air is positioned in the furnace) arranged on the furnace top through a pipeline, and the cooling air carries out high-temperature heat storage (exchange) with flue gas in the range of 450-550 ℃ at the top of a preheating zone in the furnace to enable the temperature to rise to about 400 ℃, and the cooling air descends to a furnace outer hot air surrounding tube 6 outside a furnace body calcining zone through a plurality of descending tubes in different directions, and a plurality of branch pipes are arranged on the furnace outer hot air surrounding tube to convey high-temperature combustion-supporting air to the furnace outer periphery short flame combustion chamber 12 and the furnace outer periphery long flame combustion chamber 13 for ignition and combustion supporting. Since the ignition point of the biomass powder is only 300-350 ℃, when encountering high-temperature air, the biomass powder is directly ignited to form a combustion area.
The outlet of the first combustion-supporting fan 5 is divided into two pipelines, the first combustion-supporting air pipeline 28 is connected with the porous air distributor 2, the other second combustion-supporting air pipeline 29 is connected with the air inlet of the honeycomb type waste heat fuel drying device 3, the supplied combustion-supporting air is preheated outside the furnace in the honeycomb type waste heat fuel drying device 3, after five-stage preheating, the combustion-supporting air reaches about 400 ℃, the high-temperature combustion-supporting air is connected with the furnace peripheral hot air peripheral pipe 6 through the pipeline, and the high-temperature combustion-supporting air is conveyed into the furnace peripheral short flame combustion chamber 12 and the furnace peripheral long flame combustion chamber 13 for ignition and combustion supporting.
After the lime heat exchange of the cooling belt is finished, the temperature of the lime is reduced to 70-150 ℃, about 70% of the lime enters a rotary ash discharging device 20 through a peripheral discharging bin 15, a peripheral discharging pipe 16 and a movable material flow control device 17, the rest about 30% of the lime also synchronously enters a unidirectional rotary ash discharging device 20 through a central discharging bin 18 and a liftable material flow control device 19, the unidirectional rotary ash discharging device 20 distributes the lime into a plurality of metering devices 21 through unidirectional rotary and distributing devices, the metered lime enters a discharging bin 23 through a discharging controller 22, and the whole lime discharging process is completed through a two-stage sealing discharger 24.
While the invention has been described in detail in the foregoing general description and specific examples, it will be apparent to those skilled in the art that modifications and improvements can be made thereto. Accordingly, such modifications or improvements may be made without departing from the spirit of the invention and are intended to be within the scope of the invention as claimed.
Claims (7)
1. The central burner lime kiln is characterized by comprising a shaft furnace body, a central burner in the shaft furnace, a counter double-spiral quantitative feeding device, a porous air distributor and a honeycomb type waste heat fuel drying device, wherein a combustion zone of the shaft furnace body is provided with a peripheral combustion chamber outside the shaft furnace, the central burner in the shaft furnace is arranged on an axis in the shaft furnace and below the peripheral combustion chamber outside the shaft furnace, the counter double-spiral quantitative feeding device is connected with a porous air distributor in a working procedure, the porous air distributor is connected with a material inlet of the honeycomb type waste heat fuel drying device, a smoke inlet of the honeycomb type waste heat fuel drying device is connected with the top of the shaft furnace body through a pipeline, and a material outlet of the honeycomb type waste heat fuel drying device is connected with the peripheral combustion chamber outside the shaft furnace and the central burner in the shaft furnace;
the honeycomb type waste heat fuel drying device is a multi-section type drying device and comprises an in-furnace feeding section and an out-furnace feeding section, wherein multi-pipe type channels are arranged in the in-furnace feeding section and the out-furnace feeding section, a multi-hole air distributor is connected with material inlets of the in-furnace feeding section and the out-furnace feeding section through two pipelines, material outlets of the in-furnace feeding section are connected with multi-layer blowing chambers of a burner of an in-furnace center in a one-to-one correspondence manner through a plurality of independent pipelines, and material outlets of the out-furnace feeding section are connected with combustion chambers of the periphery of the outside of the furnace in a one-to-one correspondence manner through a plurality of independent pipelines;
the lime kiln further comprises a stone weighing device, a feeding trolley and a lifting type rotary distributor which are connected in sequence, wherein the stone weighing device and the feeding trolley are arranged outside the shaft furnace body, and the lifting type rotary distributor is arranged at the top of the shaft furnace body.
2. The lime kiln of claim 1, wherein the honeycomb type waste heat fuel drying device further comprises a plurality of sections of combustion-supporting gas heating sections, and the plurality of sections of combustion-supporting gas heating sections are connected in series; the lime kiln further comprises a first combustion-supporting fan, the first combustion-supporting fan is connected with the porous air distributor through a pipeline, the first combustion-supporting fan is connected with an air inlet at the head part of the combustion-supporting gas heating section which is connected in series through another pipeline, and a combustion-supporting gas outlet at the tail part of the combustion-supporting gas heating section which is connected in series is connected with the peripheral combustion chamber outside the furnace through a pipeline.
3. Lime kiln according to claim 2, characterized in that the furnace peripheral combustion chamber comprises at least one furnace peripheral short flame combustion chamber and at least one furnace peripheral flat-to-long flame combustion chamber, the furnace peripheral short flame combustion chamber being located above the furnace peripheral flat-to-long flame combustion chamber.
4. A lime kiln according to claim 3, wherein the furnace outer peripheral combustion chamber further comprises a furnace outer peripheral inclined long flame combustion chamber located below the furnace outer peripheral flat long flame combustion chamber and above the furnace inner central burner, the furnace outer peripheral inclined long flame combustion chamber being operable to eject a fuel gas obliquely downwards towards the furnace inner central burner.
5. The lime kiln according to claim 4, further comprising a second combustion-supporting fan, a high-temperature heat storage device and a furnace outer hot-air peripheral pipe, wherein a cooling channel is arranged in the furnace inner central burner, the second combustion-supporting fan is connected with the cooling channel in the furnace inner central burner through a pipeline, the high-temperature heat storage device is arranged at the top of the shaft furnace body, an outlet of the cooling channel in the furnace inner central burner is connected with the high-temperature heat storage device through a pipeline, the high-temperature heat storage device is connected with the furnace outer hot-air peripheral pipe through a descending pipeline, and a material outlet of an outer feeding section of the honeycomb type waste heat fuel drying device is connected with the furnace outer peripheral combustion chamber through a corresponding pipeline and the furnace outer hot-air peripheral pipe.
6. The lime kiln of claim 1, further comprising a combustion cap disposed at a bottom center of the shaft furnace body, and the shaft furnace body is located below the center burner in the furnace.
7. The lime kiln of claim 1, further comprising a peripheral discharge bin, a peripheral discharge tube, a movable material flow control device, a central discharge bin, a liftable material flow control device, a unidirectional rotation ash discharge device, a metering device, a discharge controller, an ash discharge bin and a two-stage sealing discharger, wherein the peripheral discharge bin and the central discharge bin are arranged at the bottom of the shaft furnace body, the peripheral discharge bin is uniformly distributed at the peripheral side of the central discharge bin, the unidirectional rotation ash discharge device is arranged below the central discharge bin, the peripheral discharge bin is connected with the unidirectional rotation ash discharge device through the peripheral discharge tube, the movable material flow control device is arranged in the peripheral discharge tube, the bottom of the central discharge bin is provided with the liftable material flow control device, the unidirectional rotation ash discharge device is connected with the metering device, the metering device is provided with the ash discharge bin, and the metering device is provided with the discharge controller, and the ash discharge bin is connected with the two-stage sealing discharger.
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| CN116589206B (en) * | 2023-05-30 | 2023-12-05 | 浙江钙科科技股份有限公司 | Calcium oxide suspension calcination production line suitable for biomass fuel based on Internet |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109574523A (en) * | 2018-12-25 | 2019-04-05 | 石家庄新华能源环保科技股份有限公司 | A kind of limekiln that the hot sending of gasification furnace coal gas of high temperature is directly burnt |
| CN113154868A (en) * | 2021-04-07 | 2021-07-23 | 中冶焦耐(大连)工程技术有限公司 | Double-chamber lime shaft kiln heat supply system taking straw powder and sawdust powder as fuel |
| CN114656170A (en) * | 2022-03-29 | 2022-06-24 | 唐山市丰南区金泉冶金能源新技术开发有限公司 | Process and device for co-producing active lime by natural gas and biomass fuel |
| CN218879751U (en) * | 2023-02-09 | 2023-04-18 | 唐山金泉冶化科技产业有限公司 | Central burner type lime kiln |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109574523A (en) * | 2018-12-25 | 2019-04-05 | 石家庄新华能源环保科技股份有限公司 | A kind of limekiln that the hot sending of gasification furnace coal gas of high temperature is directly burnt |
| CN113154868A (en) * | 2021-04-07 | 2021-07-23 | 中冶焦耐(大连)工程技术有限公司 | Double-chamber lime shaft kiln heat supply system taking straw powder and sawdust powder as fuel |
| CN114656170A (en) * | 2022-03-29 | 2022-06-24 | 唐山市丰南区金泉冶金能源新技术开发有限公司 | Process and device for co-producing active lime by natural gas and biomass fuel |
| CN218879751U (en) * | 2023-02-09 | 2023-04-18 | 唐山金泉冶化科技产业有限公司 | Central burner type lime kiln |
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