WO2015128910A1 - 流動仮焼炉 - Google Patents
流動仮焼炉 Download PDFInfo
- Publication number
- WO2015128910A1 WO2015128910A1 PCT/JP2014/004795 JP2014004795W WO2015128910A1 WO 2015128910 A1 WO2015128910 A1 WO 2015128910A1 JP 2014004795 W JP2014004795 W JP 2014004795W WO 2015128910 A1 WO2015128910 A1 WO 2015128910A1
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- WO
- WIPO (PCT)
- Prior art keywords
- pulverized coal
- furnace body
- raw material
- calciner
- air
- Prior art date
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
- F27B7/2016—Arrangements of preheating devices for the charge
- F27B7/2025—Arrangements of preheating devices for the charge consisting of a single string of cyclones
- F27B7/2033—Arrangements of preheating devices for the charge consisting of a single string of cyclones with means for precalcining the raw material
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/44—Burning; Melting
- C04B7/45—Burning; Melting in fluidised beds, e.g. spouted beds
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
- F27B7/38—Arrangements of cooling devices
-
- 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
- F27D7/00—Forming, maintaining, or circulating atmospheres in heating chambers
- F27D7/04—Circulating atmospheres by mechanical means
Definitions
- the present invention relates to a fluid calciner that can reduce the unburned rate of fuel at the calciner outlet by optimizing the supply position of pulverized coal.
- the raw material heated by the heat exchange with the high-temperature gas in the suspension preheater 7 is transferred from the lower cyclone 8 of the suspension preheater 7.
- a part of the exhaust gas is discharged into the rotary kiln exhaust gas conduit 9 and the remainder is supplied to the raw material supply chute 12 of the fluid calciner 11.
- the calcined raw material enters the separation cyclone 21 with the entire amount accompanying the calcining furnace exhaust gas.
- a part of the raw material dispersedly charged into the rotary kiln exhaust gas conduit 9 is also calcined by the high-temperature rotary kiln exhaust gas and enters the separation cyclone 21 together with the rotary kiln exhaust gas.
- the calcined raw material collected by the separation cyclone 21 is introduced into the rotary kiln 20 through the raw material chute 22.
- the high-temperature air generated in the clinker cooler 18 is sucked into the rotary kiln 20 and the flow calciner 11 by the suction force of the attracting fan 23, respectively.
- the suction amount to the rotary kiln 20 having a small ventilation resistance becomes excessive, the sectional area is reduced in a part of the rotary kiln exhaust gas conduit 9 and the suction amount to the fluid calciner 11 is adjusted by the damper 24. is doing.
- a solid fuel such as coal
- bituminous coal with good combustibility is pulverized into fine powder.
- fuels such as poorly combustible coal and oil coke.
- the pulverized coal is conventionally supplied from the pulverized coal supply pipe 16 connected to one side of the furnace body with respect to the thick fluidized bed formed of the cement raw material at the bottom. Since the pulverized coal is not sufficiently dispersed, the pulverized coal concentration tends to flow from the free board 17 to the outlet side.
- Patent Document 1 a cylindrical furnace body whose vertical direction is the cylinder axis direction, an air distribution plate provided substantially horizontally at the bottom of the furnace body, and an air under the air distribution plate A chamber, a raw material supply chute for supplying a raw material on the upper side of the air dispersion plate, a fuel supply nozzle for supplying solid fuel to a fluidized bed on the upper side of the air dispersion plate, and secondary air
- a fluidized calcining furnace of cement raw material having a secondary air duct for supplying (bleed air) the fuel supply nozzle is deflected to a tangential side from the centripetal direction with a downward slope of 20 ° or more with respect to the horizontal plane.
- a fluid calcining furnace of cement raw material connected to the furnace body has been proposed.
- the conventional fluidized calciner of cement raw material is for calcining the raw material by burning fuel, but the connection position of the fuel supply nozzle is based on experience values, and in the fluidized calciner Since the presence or absence of the raw material concentration and gas concentration (especially O 2 ) distribution is not considered, sufficient calcination cannot be performed when pulverized coal such as coal or coke is used as fuel. Furthermore, there is a problem that the operation is hindered due to the blockage of the conduit.
- the present invention has been made in view of such circumstances. Even when pulverized coal such as coal or coke is used as fuel, the preburner reduces the unburned rate at the outlet of the fluid calciner. It is an object of the present invention to provide a fluid calcining furnace capable of performing sufficient calcining while preventing clogging.
- a fluid calciner according to the present invention is a cylindrical furnace in which the axial center direction is arranged in the vertical direction and the upper end is closed by a top plate.
- First to fourth bleed conduits are connected, and a fluidized air blow-in port for blowing fluidized air into the furnace body is disposed at the bottom of the furnace body, and the first and / or second bleed conduits are provided.
- An exhaust duct for discharging combustion gas containing cement raw material in the furnace body is connected to the upper side wall of the furnace body located above the top plate with a space between the top plate and the pulverized coal injection
- the inlet of the line is disposed below the suction port of the bleed conduit and above the fluidized air inlet, and the inlet of one of the pulverized coal injection lines is the third or fourth bleed conduit. It is arrange
- the invention described in claim 2 is characterized in that, in the invention described in claim 1, the blowing ports of the pulverized coal blowing line are arranged in two places.
- the invention according to claim 3 is the invention according to claim 1 or 2, wherein the raw material chute is disposed adjacent to the first bleed conduit and the inlet of the pulverized coal injection line. Is arranged below the third extraction conduit that is radially opposed to the first extraction conduit.
- the upper end portion of the cylindrical furnace body is closed by the top plate, and the top side wall of the furnace body is spaced apart from the top plate. Since an exhaust duct through which air in the body flows out is connected, a mixing chamber for a mixed fluid of cement raw material, pulverized coal and furnace gas flowing into the exhaust duct is formed in the upper part of the furnace body.
- mixing with a furnace gas and pulverized coal can be promoted, and combustibility can be improved.
- heat exchange of the cement raw material, pulverized coal, and the gas in the furnace is also promoted by mixing, the decarboxylation rate of the cement raw material can be improved.
- the concentration of pulverized coal in the furnace is increased on the side wall side where the exhaust duct is connected by the suction force from the exhaust duct, It becomes relatively low at a distant position. For this reason, when pulverized coal is blown from one place, the dispersibility of the pulverized coal may be further deteriorated due to the synergistic effect of both.
- the inlets of the plurality of pulverized coal injection lines are respectively disposed below the suction port of the extraction conduit and above the fluidizing air injection port, and one of them is provided. Since the inlet is arranged at a position away from the position where the exhaust duct is connected, the pulverized coal can be effectively dispersed in the furnace to improve the combustion.
- the second aspect of the present invention as seen in the computational fluid dynamics calculation described later, by disposing at least one pulverized coal inlet at a position away from the position where the exhaust duct is connected.
- the pulverized coal injection ports By arranging the pulverized coal injection ports in two places in total, it is possible to obtain substantially the same effect as in the case where they are arranged under all of the first to fourth extraction conduits (four places in total). For this reason, while being able to hold down equipment cost, management becomes easy and it is economical.
- the pulverized coal injection port has a diameter with respect to the first extraction conduit.
- FIG. 1 is a longitudinal sectional view showing an embodiment of a fluid calciner according to the present invention.
- FIG. 2 is a perspective view showing main trajectories of pulverized coal particles in the fluid calciner of FIG.
- FIG. 3 is a layout view of the pulverized coal injection port in the embodiment of the present invention.
- FIG. 4 is a layout diagram of pulverized coal injection ports in a comparative example.
- FIG. 5 is a pulverized coal concentration distribution diagram in the furnace of Comparative Example 5 of FIG. 4 by the above-described numerical fluid dynamics calculation.
- FIG. 6 is a distribution diagram of the oxygen concentration in the furnace of the comparative example 5 of FIG.
- FIG. 7 is a schematic configuration diagram showing a cement manufacturing facility equipped with a conventional fluid calciner.
- the fluid calciner 1 of the present embodiment includes a plurality of pulverized coal injection lines 3 for injecting fuel into the furnace body 2, a raw material chute 4 for introducing cement raw material, and bleed air in the furnace body 2.
- a fluidized air blowing port 2a for blowing fluidized air into the furnace body 2 is generally configured.
- the furnace body 2 is formed in a cylindrical shape having an inner diameter of 5.0 to 6.5 m.
- the furnace body 2 is arranged with the axial direction facing the vertical direction and the upper end portion is closed by the top plate 2b.
- the first to fourth four bleed conduits 5a to 5d are connected to the lower side of the furnace body 2 by being piped in a downward slope whose angle between the center line and the horizontal plane is 55 to 65 °. Has been.
- first to fourth extraction conduits 5a to 5d are arranged in the circumferential direction sequentially in plan view from the viewpoint that the centers of the respective suction ports are arranged on the same circumference and supply air evenly to the furnace bottom. They are arranged at substantially equal intervals in the clockwise direction.
- the center of the suction port of the extraction conduits 5a to 5d is arranged at a height of 1500 to 2500 mm (H in FIG. 1) upward from the fluidizing air blowing port 2a, and inside the extraction conduits 5a to 5d.
- the gas flow rate is generally set to 15 to 18 m / s.
- the fluidized air inlet 2a is configured so that, for example, in the cement manufacturing facility including the conventional fluid calciner 11 shown in FIG. It will be blown into.
- the air dispersion plate 14 is disposed in the horizontal direction.
- the fluidizing air blowing speed from the fluidizing air blowing port 2a is determined by the raw material density and particle size distribution, and is set to 1.0 to 2.0 m / s for ordinary cement raw materials. ing.
- the exhaust duct 6 is connected to the upper side wall of the furnace body 2 located above the first and second extraction conduits 5a and 5b.
- the exhaust duct 6 is piped so as to rise upward as it is separated from the furnace body 2, and is connected so that the upper side wall 6a is located at a distance from the top plate 2b.
- the mixing chamber C is formed between the connection part of the exhaust gas duct 6 and the top plate 2b.
- the material chute 4 is disposed adjacent to the first extraction conduit 5a or the second extraction conduit 5b (in the present embodiment, adjacent to the first extraction conduit 5a), and at an angle to the horizontal plane. Is connected to the side wall of the furnace body 2 by a descending slope that generally ranges from 50 ° to 70 °.
- the height of the raw material chute 4 is generally in the range of 1500 to 3000 mm (h in FIG. 1) upward from the fluidized air inlet 2a. Has been placed.
- a raw material dispersion base 4a formed of a refractory is disposed at the lower portion of the inlet of the raw material chute 4.
- a plurality of pulverized coal injection lines 3 for injecting pulverized coal as fuel, for example, coal or coke into the furnace body 2 are arranged 4).
- These air inlets 3a are respectively disposed below the suction ports of the bleed conduits 5a to 5d and above the fluidized air air inlet 2a, and at least one of the air inlets 3a is a first air outlet 3a. It is arranged below the third or fourth extraction conduits 5c and 5d.
- pulverized coal blowing lines 3 are connected so as to blow pulverized coal perpendicular to the axis of the furnace body 2 and toward the center of the furnace body 2, and the center of the blowing port 3a is, for example,
- the bleed ducts 5a to 5d are arranged so as to be collinear with the center of the bleed conduits 5a to 5d.
- the pulverized coal conveying air speed in the pulverized coal blowing line 3 is an adjustment item in operation, but the range is usually set to a range of 10 to 20 m / s.
- the flow of the pulverized coal injected from the pulverized coal injection line 3 is input from the raw material chute 4 by the computational fluid dynamics calculation CFD (Computational Fluid Dynamics) performed by the present inventors. Is affected by the flow of the raw material to be discharged, the flow of gas from the extraction pipes 5a to 5d, and the flow of exhaust of the combustion gas containing cement raw material and pulverized coal in the furnace body 2 based on the connection position of the exhaust gas duct 6 It is obtained by locating.
- CFD computational Fluid Dynamics
- the actual flow calciner shape and operating conditions are digitized, and the gas flow, particle movement, chemical reaction, and heat transfer are numerically calculated by a computer with an analysis program installed. Is used to grasp the state of combustion / calcination in a fluid calciner, which is difficult by actual measurement. Note that the influence of the extracted air on the flow of pulverized coal is the same even if the extracted air is blown into or sucked into the extraction conduit 5.
- the computational fluid dynamics calculation method and model are as follows.
- Computational fluid dynamics calculation software Rflow (2) Turbulence model: k- ⁇ Model (3) Fluid: Incompressible ideal gas (4) Pressure-speed coupling: SIMPLE (5) Discretization scheme: Finite Volume Method (6) Momentum: Second Order Upwind (7) Turbulent kinetic energy: First Order Upwind (8) Turbulent dissipation rate: First Order Upwind (9) Energy: Second Order Upwind (10) Particle analysis: Discrete Element Method (11) Particulate fluid training: Two Way Coupling (12) Pulverized coal combustion: H 2 + O 2 -H 2 O, CH 4 + O 2 -H 2 O + CO 2 , CO + O 2 -CO 2 , C + O 2 -CO 2 (13) Raw material decarboxylation model: CaCO 3 -CaO + CO 2 , unreacted nuclear model Note that (2) to (11) are numerical fluid analysis of gas flow, etc., (12) is combustion analysis (13) is a general-purpose model widely used by those skilled in the
- composition of coal used in this computational fluid dynamics calculation is as follows. Name Calorific value Volatile content Fixed carbon Water Ash (Kcal / Kg) (%) (%) (%) (%) (%) (%) (%) (%) (%) (%) Bituminous coal 6700 34.3 49.4 6.8 9.5
- the amount of pulverized coal feed was also adjusted so that the total calorific value of pulverized coal thrown into a calcining furnace might become constant.
- Example A In Example A, the inlets 3a of the plurality of pulverized coal injection lines 3 as shown in FIGS. 3 (a) to 3 (f) are respectively below the suction ports of the extraction pipes 5a to 5d and flowed.
- Example 1 (FIG. 3 (a)) is the example which has arrange
- Example 2 (FIG. 3B) is an example in which the inlets 3a of the two pulverized coal injection lines 3 are arranged below the second and third extraction conduits 5b and 5c, respectively.
- 3 (FIG. 3C) is an example in which the inlets 3a of the two pulverized coal injection lines 3 are respectively disposed below the third and fourth extraction conduits 5c and 5d.
- Example 4 is the example which has arrange
- Example 5 is an example in which the inlets 3a of the two pulverized coal injection lines 3 are respectively arranged below the first and fourth extraction conduits 5a and 5d.
- 6 is an example in which the injection ports 3a of the four pulverized coal injection lines 3 are respectively arranged below the first to fourth extraction conduits 5a to 5d.
- a comparative example a comparative example in which the blowing port 3a of the pulverized coal blowing line 3 is disposed below the suction ports of the extraction conduits 5a to 5d and at the positions shown in FIGS. 4 (a) to (e). Similarly, for 1 to 5, the char reaction rate (%), the decarboxylation rate of the cement raw material particles (%), and the oxygen concentration (% ), Particle temperature (° C.) and gas temperature (° C.) of the cement raw material were calculated.
- Comparative Example 1 is an example in which the inlet 3a of one pulverized coal injection line 3 is disposed below the second extraction conduit 5b.
- FIG. 4B is an example in which the inlet 3a of one pulverized coal injection line 3 is disposed below the third extraction conduit 5c
- Comparative Example 3 is This is an example in which the inlet 3a of one pulverized coal blowing line 3 is disposed below the fourth extraction conduit 5d.
- the comparative example 4 (FIG.4 (d)) is the example which has arrange
- (E)) is an example in which the inlets 3a of the two pulverized coal blowing lines 3 are arranged below the first and second extraction conduits 5a and 5b, respectively.
- the decarbonation rate (%) of the cement raw material is a weighted average of the decarboxylation rate of each raw material particle at the calciner outlet according to the mass before calcining
- the char reaction rate (%) Is a weighted average of the char reaction rate for each pulverized coal particle at the calciner outlet according to the mass of the char before reacting.
- the performance is high when the average char reaction rate (%) is 60% or more and the decarboxylation rate (%) of the cement raw material is 45% or more.
- Table 1 is a chart showing the results of the computational fluid dynamics calculation in the arrangement of FIG. 3, and shows the average value at the outlet of the exhaust gas duct 6 of Examples 1 to 6.
- Table 2 is a chart showing the results of the numerical fluid dynamic calculation in the comparative example of FIG. 4, and shows the average value at the outlet of the exhaust gas duct 6 of the comparative examples 1 to 5.
- Comparative Example 5 Although pulverized coal is blown into the furnace body 2 from two pulverized coal injection ports 3 a, the first and second injection ports 3 a are located below the exhaust duct 6. , The distribution of the pulverized coal introduced from the inlet 3a is biased, and the concentration of pulverized coal on the side wall connected to the exhaust duct, as shown in FIG. As a result, the pulverized coal dispersion effect is not improved even when compared with Comparative Examples 1 to 4 in which pulverized coal is blown from one place.
- the pulverized coal injection line 3a has a plurality of injection ports 3a (two in Examples 1 to 5, In the sixth embodiment, and one of the inlets 3a is disposed below the extraction conduits 5c and / or 5d spaced from the position where the exhaust duct 6 is connected. Combustion can be improved by effectively dispersing pulverized coal inside.
- the dispersibility of the pulverized coal in the furnace body 2 is improved, the oxygen consumption is uniform, the combustion is promoted, the gas temperature is increased, and the decarboxylation rate of the cement raw material is increased. It can be seen that the above average char reaction rate (%) is obtained, and the decarboxylation rate (%) of the cement raw material is 45% or more.
- At least one air inlet 3a is disposed below the extraction conduit 5c and / or 5d spaced from the connection position of the exhaust duct 6, so that the air inlet If 3a is arranged in two places, an effect almost the same as the case where it is arranged in four places can be obtained. Therefore, considering the equipment cost and the ease of management, a sufficient effect can be obtained with two places. understood.
- the pulverized coal inlet 3a is The char reaction rate and the decarboxylation rate of the cement raw material are further improved by disposing them below the first extraction conduit 5a and below the third extraction conduit 5c facing the radial direction of the furnace body 2. It becomes possible.
- the raw chute 4 is disposed adjacent to the second extraction conduit 5b, and the pulverized coal injection port 3a is disposed below the second extraction conduit 5b and in the radial direction of the furnace body 2. The same effect can be obtained when it is arranged below the 4 extraction conduits 5d.
- FIG. 2 shows the main trajectory of the pulverized coal particles in the fluidized calciner having the configuration of Example 3 by numerical fluid dynamics calculation based on the shape and operating conditions of an actual furnace similar to Example A. is there.
- the upper end portion of the cylindrical furnace body 2 is closed by the top plate 2b, and the upper side wall of the furnace body 2 is spaced from the top plate 2b.
- a mixing chamber C for a mixed fluid of cement raw material, pulverized coal and furnace gas flowing to the exhaust duct is formed in the upper part of the furnace body 2.
- FIG. 5 and FIG. 6 show the case where the pulverized coal injection ports 3a are arranged as shown in Comparative Example 5 by numerical fluid dynamics calculation based on the same shape and operating conditions of the actual furnace as in Example A. The result of having analyzed the particle distribution and oxygen concentration distribution of the pulverized coal in the furnace body 2 is shown.
- the present invention can provide a fluidized calciner capable of performing sufficient calcining while reducing the unburned rate at the outlet of the fluidized calciner and preventing clogging with a preheater.
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Abstract
Description
これらの図において、本実施形態の流動仮焼炉1は、炉体2内に燃料を吹き込む複数の微粉炭吹込ライン3と、セメント原料を投入する原料シュート4と、炉体2内に抽気空気を導入するための第1~第4の抽気導管5a~5dと、炉体2内のセメント原料を含む燃焼ガスを流出させる排気ダクト6が炉体2に接続されるとともに、炉体2の底部に当該炉体2内に流動化空気を吹き込む流動化空気吹込口2aが形成されることによって概略構成されたものである。
また、第1~第4の4本の抽気導管5a~5dは、その中心線と水平面とのなす角度が55~65°の範囲の下り勾配に配管されて炉体2の下部側部に接続されている。
(1) 数値流体力学計算ソフト:Rflow (株式会社アールフロー)
(2) 乱流モデル:k -ε Model
(3) 流体:非圧縮性理想気体
(4) 圧力-速度カップリング:SIMPLE
(5) 離散化スキーム:Finite Volume Method
(6) 運動量:Second Order Upwind
(7) 乱流運動エネルギー:First Order Upwind
(8) 乱流散逸率:First Order Upwind
(9) エネルギー:Second Order Upwind
(10)粒子解析:Discrete Element Method
(11)粒子流体練成:Two Way Coupling
(12)微粉炭燃焼:H2+O2-H2O、CH4+O2-H2O+CO2、CO+O2-CO2、C+O2-CO2
(13)原料脱炭酸モデル:CaCO3-CaO+CO2、未反応核モデル
なお、(2)~(11)はガスの流れ等についての数値流体解析を行う際に、(12)は燃焼解析を行う際に、(13)は石灰石の脱炭酸反応を解析する際に、いずれも当業者において広く用いられている汎用のモデルである。
名称 発熱量 揮発分 固定炭素 水分 灰分
(Kcal/Kg) (%) (%) (%) (%)
瀝青炭 6700 34.3 49.4 6.8 9.5
なお、微粉炭の種類が変わった場合は、上記の工業分析値の変更に加え、仮焼炉へ投入する微粉炭の総発熱量が一定となるように微粉炭フィード量も調整した。
・炉体2
炉内径=5.1m
炉長=14m
・微粉炭吹込ライン3
微粉炭のフィード量=9.1t/h
搬送空気流速=11m/s
温度=50℃
・原料シュート4
セメント原料:272t/h
温度=740℃
搬送空気流速=0.5m/s
・抽気導管5(円周方向に4箇所配置)
抽気空気
温度=880℃
流速=16.5m/s
・流動化空気吹込口2a
流動化空気
温度=800℃
流速=1.64m/s
実施例Aにおいては、図3(a)~(f)に示すような複数本の微粉炭吹込ライン3の吹込口3aを、各々抽気導管5a~5dの吸引口の下方であって、かつ流動化空気吹込口2aの上方に配設するとともに、そのうちの少なくとも1つの吹込口3aを、第3または第4の抽気導管5c、5dの下方に配置した実施例1~6について、上述した実炉の形状および運転条件に基づいて、数値流体力学計算によって、チャー反応率(%)、セメント原料粒子の脱炭酸率(%)、酸素濃度(%)、セメント原料の粒子温度(℃)およびガス温度(℃)を算出した。
図2は、実施例Aと同様の実炉の形状および運転条件に基づいて、数値流体力学計算によって、実施例3の構成の流動仮焼炉における微粉炭粒子の主な軌跡を示したものである。
上述したように、本発明に係る流動仮焼炉1においては、円筒状の炉体2の上端部を天板2bによって塞ぎ、炉体2の上部側壁に天板2bとの間に間隔をおいて排気ダクト6を接続することにより、炉体2の上部に、排気ダクトへと流れるセメント原料、微粉炭および炉内ガスの混合流体のミキシングチャンバーCが形成されている。
他方、図5および図6は、実施例Aと同様の実炉の形状および運転条件に基づいて、数値流体力学計算によって、微粉炭の吹込口3aを比較例5に示した配置とした場合の炉体2内における微粉炭の粒子分布および酸素濃度分布を解析した結果を示すものである。
2 炉体
2a 流動化空気吹込口
2b 天板
3 微粉炭吹込ライン
3a 吹込口
4 原料シュート
5a~5d 第1~第4の抽気導管
6 排ガスダクト
Claims (3)
- 軸心方向を上下方向に向けて配置されるとともに上端部が天板によって塞がれた筒状の炉体の下部側壁に、当該炉体内に燃料を吹き込む複数の微粉炭吹込ラインおよびセメント原料を投入する原料シュートならびに周方向に順次間隔をおいて配置されて当該炉体内に抽気空気を導入するための第1~第4の抽気導管が接続され、上記炉体の底部に当該炉体内に流動化空気を吹き込む流動化空気吹込口が配設されるとともに、上記第1および/または第2の抽気導管の上方に位置する上記炉体の上部側壁に、上記天板との間に間隔をおいて上記炉体内のセメント原料を含む燃焼ガスを流出させる排気ダクトが接続されてなり、
かつ上記微粉炭吹込ラインの吹込口は、各々上記抽気導管の吸引口の下方であり、かつ上記流動化空気吹込口の上方に配設されるとともに、そのうちの1つの上記吹込口は、上記第3または第4の抽気導管の下方に配置されていることを特徴とする流動仮焼炉。 - 上記微粉炭吹込ラインの上記吹込口は、2箇所に配設されていることを特徴とする請求項1に記載の流動仮焼炉。
- 上記原料シュートは、上記第1の抽気導管に隣接して配置されるとともに、上記吹込口は、上記第1の抽気導管に対して径方向に対向する第3の抽気導管の下方に配置されていることを特徴とする請求項1または2に記載の流動仮焼炉。
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US15/119,429 US10209006B2 (en) | 2014-02-28 | 2014-09-18 | Fluidized calciner |
KR1020167023116A KR20160129845A (ko) | 2014-02-28 | 2014-09-18 | 유동 하소로 |
CN201480076430.XA CN106029600B (zh) | 2014-02-28 | 2014-09-18 | 流动煅烧炉 |
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US (1) | US10209006B2 (ja) |
JP (1) | JP6187315B2 (ja) |
KR (1) | KR20160129845A (ja) |
CN (1) | CN106029600B (ja) |
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JP2018118861A (ja) * | 2017-01-23 | 2018-08-02 | 三菱マテリアル株式会社 | セメントの製造方法 |
JP7102965B2 (ja) * | 2018-06-15 | 2022-07-20 | 住友金属鉱山株式会社 | 流動焙焼炉 |
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TW201541045A (zh) | 2015-11-01 |
JP2015161479A (ja) | 2015-09-07 |
KR20160129845A (ko) | 2016-11-09 |
CN106029600B (zh) | 2018-09-18 |
JP6187315B2 (ja) | 2017-08-30 |
US10209006B2 (en) | 2019-02-19 |
CN106029600A (zh) | 2016-10-12 |
TWI614474B (zh) | 2018-02-11 |
US20170219287A1 (en) | 2017-08-03 |
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