WO2009139404A1 - バイオマス混焼微粉炭焚きボイラ及び同ボイラの運転方法 - Google Patents
バイオマス混焼微粉炭焚きボイラ及び同ボイラの運転方法 Download PDFInfo
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- WO2009139404A1 WO2009139404A1 PCT/JP2009/058887 JP2009058887W WO2009139404A1 WO 2009139404 A1 WO2009139404 A1 WO 2009139404A1 JP 2009058887 W JP2009058887 W JP 2009058887W WO 2009139404 A1 WO2009139404 A1 WO 2009139404A1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J1/00—Removing ash, clinker, or slag from combustion chambers
- F23J1/06—Mechanically-operated devices, e.g. clinker pushers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B21/00—Water-tube boilers of vertical or steeply-inclined type, i.e. the water-tube sets being arranged vertically or substantially vertically
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C1/00—Combustion apparatus specially adapted for combustion of two or more kinds of fuel simultaneously or alternately, at least one kind of fuel being either a fluid fuel or a solid fuel suspended in a carrier gas or air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C5/00—Disposition of burners with respect to the combustion chamber or to one another; Mounting of burners in combustion apparatus
- F23C5/08—Disposition of burners
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J1/00—Removing ash, clinker, or slag from combustion chambers
- F23J1/02—Apparatus for removing ash, clinker, or slag from ash-pits, e.g. by employing trucks or conveyors, by employing suction devices
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
- F23C2900/01001—Co-combustion of biomass with coal
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/30—Solid combustion residues, e.g. bottom or flyash
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2700/00—Ash removal, handling and treatment means; Ash and slag handling in pulverulent fuel furnaces; Ash removal means for incinerators
- F23J2700/001—Ash removal, handling and treatment means
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2700/00—Ash removal, handling and treatment means; Ash and slag handling in pulverulent fuel furnaces; Ash removal means for incinerators
- F23J2700/002—Ash and slag handling in pulverulent fuel furnaces
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K2201/00—Pretreatment of solid fuel
- F23K2201/10—Pulverizing
- F23K2201/1003—Processes to make pulverulent fuels
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- 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
- F27D15/00—Handling or treating discharged material; Supports or receiving chambers therefor
- F27D15/02—Cooling
- F27D15/0206—Cooling with means to convey the charge
- F27D15/0266—Cooling with means to convey the charge on an endless belt
Definitions
- This invention relates to a boiler (biomass mixed fired pulverized coal fired boiler) that co-fires biomass fuel (mainly wood fuel) and pulverized coal.
- the pulverized particle size of biomass fuel in this specification refers to the size of a mesh for selecting the pulverized powder particles with a sieve.
- “pulverized particle size of 5 mm” is a powder particle in which 90% by weight of the entire powder particle passes through a 5 mm mesh
- “pulverized particle size of 5 mm or more” is a particle material in which the particle particle passing through a 5 mm mesh is 90% or less Yes
- “pulverized particle size of 5 mm or less” means that 90% or more of the powder particles passing through a 5 mm mesh.
- the 5 mm particle size adopted here means “the limit biomass particle size for floating combustion”, which differs depending on the type, shape, moisture content, etc. of the biomass, but for woody biomass it is about 3-5 mm. It is being watched.
- Coal fossil fuels such as coal and biomass fuels are required to reduce the consumption of fossil fuels.
- biomass fuels for example, woody biomass fuels
- a method of co-firing biomass fuel with a pulverized coal-fired boiler a method is adopted in which a small amount of biomass is put into a coal bunker, pulverized with coal and pulverized, and this is air conveyed to a burner and burned in a furnace. Yes.
- biomass fuel is pulverized by a dedicated mill and supplied to a furnace with a burner different from coal fine powder to co-firing.
- the biomass fuel co-firing rate can be increased without reducing the coal pulverization ability.
- the combustion efficiency will deteriorate.
- the particle size must be less than the limit particle size (about 3 to 5 mm for woody biomass) for floating combustion.
- the graph shown in FIG. 8 shows three particle size distributions shifted to ⁇ 5 mm and pulverized particle size 5 mm based on data ( ⁇ 3 mm) obtained by pulverizing woody biomass with a dedicated pulverizer. If the average pulverized particle size d50 (50% by weight particle size) obtained from this figure is entered in a graph showing the relationship between the average pulverized particle size d50 and the power consumption unit described in a known research report (NEDO), as shown in FIG. Thus, it can be seen that the power unit is reduced by about one digit at a pulverized particle size of 5 mm as compared with a pulverized particle size ⁇ 3 mm.
- pulverization of biomass fuel by a dedicated mill may have a pulverization particle size of 5 mm or more, the pulverization power will be greatly reduced.
- Patent Document 1 Japanese Patent Application Laid-Open No. 2005-291431
- first prior art Japanese Patent Application Laid-Open No. 2005-291431
- the pulverized coal burner 4 and the biomass burner 5 are provided in multiple stages at the same level.
- Coal supplied from the coal bunker 11 is pulverized by the coal mill 6 and supplied to the furnace 1 by the pulverized coal burner 4.
- the biomass fuel 16 is charged into the biomass bunker 12, pulverized by the biomass mill 13, and supplied to the furnace 1 by the biomass burner 5.
- the pulverized coal and the biomass fuel are burned with the combustion air from the wind box 3 and blown upward, and further, the combustion air is further added from the air outlet 2 and burned.
- the biomass fuel with small particle size burns while floating and flows out of the furnace together with the exhaust gas, but some large particle size biomass fuel falls to the furnace bottom against the combustion gas while burning .
- pulverization power (necessary for pulverization) Power) tends to increase exponentially.
- the pulverization particle size of the biomass fuel by the dedicated mill is larger than 5 mm (the maximum particle size is 5 mm or more and less than 5 mm is 90% or less), the pulverization power is significantly reduced.
- the first prior art is based on the above knowledge and uses a biomass fuel having a pulverized particle size of 5 mm.
- the biomass fuel can be pulverized to a particle size of 5 mm and mixed and fired without reducing the coal pulverization efficiency by the coal mill.
- the wet separation apparatus 14 is provided in the wet clinker processing apparatus, the carbide bunker 15 is provided, and the carbide conveyance apparatus 18 is provided between the wet separation apparatus 14 and the carbide bunker 15.
- the unburned biomass (carbide) which fell to the clinker processing apparatus 17 is processed with a wet process, and after that, the wet separation apparatus 14 isolate
- the first conventional technique is based on cooling the carbonized unburned bimass fuel with the wet clinker processing apparatus and recovering the unburned matter (carbide) with the wet separation apparatus 14, but the dry clinker processing apparatus. It is also described that can be used.
- the biomass fuel (carbide etc.) cooled and recovered by the wet clinker processing apparatus is the medium grain b in FIG.
- the resistance is small and it is relatively easy to grind.
- the size of the biomass fuel particles co-fired by the first prior art is limited to those within the range where they are completely carbonized and fall to the furnace bottom.
- a dry clinker processing apparatus is known as a clinker processing apparatus, and an example thereof is described in Japanese Patent Publication No. 7-56375 (Patent Document 4).
- An outline of this known dry clinker processing apparatus is as shown in FIG. 7, which is provided with a metal conveyor belt 23 having high heat resistance, and is provided by a transition hopper 20 provided between the furnace 1 and the furnace. The bottom ash of the furnace 1 is guided to the conveyor belt 23. The conveyor belt 23 is driven by drive wheels 24.
- the casing 22 of the dry clinker processing apparatus has a sealed structure, and a plurality of cooling air suction holes 31 are provided on the side of the conveyor belt 23, and clinker cooling air is supplied thereby.
- the bottom ash dropped on the bottom (furnace bottom) of the furnace 1 is received by the conveyor belt 23 and slowly transferred (about 5 mm per second), and gradually cooled by air for about 1 hour (conveyor belt 23 transport time). It is discharged and collected by the clinker collecting means 41.
- cooling air is supplied into the main body of the clinker processing apparatus 21, and the bottom ash dropped on the conveyor belt 23 is slowly cooled by the air while moving inside the main body and discharged outside.
- the cooling air supplied to the main body is heated by the burned bottom ash and becomes high temperature, sucked into the furnace 1 and merged with the combustion gas in the furnace.
- the amount of cooling air supplied to the dry clinker treatment apparatus is limited and is about 2% of the amount of combustion air supplied to the furnace.
- the bottom ash is cooled to approximately 100 ° C. while moving in the main body of the processing apparatus (FIG. 7) to the discharge position (about 1 hour).
- the biomass burner 5 of the first prior art is disposed above the pulverized coal burner 4, and the biomass fuel is combusted in the upper combustion region, and the combustion in the furnace 1 is performed.
- Time is slightly longer. Therefore, the pulverization particle size of the biomass fuel can be somewhat increased.
- the ratio of coarse particles B of 5 mm or more increases, so that even if the biomass burner 5 is disposed above the pulverized coal burner 4 and the combustion time in the furnace is slightly increased, The problem that the core remains cannot be solved.
- the first conventional technology (patent document 1) related to a mixed-fired boiler requires a wet separation device, a transport line, a storage bunker, a cutting device, etc. in order to collect the biomass fuel carbide and put it into a coal bunker. For this reason, there is a problem that additional equipment for co-firing biomass fuel with an existing coal boiler is large, and this equipment cost is very high.
- the present invention has been made in consideration of the above-mentioned problems of the prior art, and does not require a significant addition of equipment to the configuration of the conventional biomass fuel mixed fired pulverized coal fired boiler, and relatively large grains. It is an object to make it possible to use a biomass fuel having a diameter (particularly, a biomass fuel having a pulverized particle size of 5 mm or more) and to increase the co-firing rate of the biomass fuel.
- a biomass fuel co-fired pulverized coal fired boiler includes a furnace for co-firing pulverized coal and biomass fuel, a pulverized coal burner for supplying the pulverized coal to the furnace, A biomass burner for supplying the biomass fuel to the furnace, a biomass mill for pulverizing the biomass fuel supplied to the biomass burner, and a bottom ash provided below the furnace and discharged from the furnace
- a dry clinker processing apparatus having a clinker conveyor for transporting the ash, and supplying combustion air toward the bottom ash on the clinker conveyor, thereby removing unburned biomass fuel contained in the bottom ash Combustion air supply means for burning on the clinker conveyor And features.
- the biomass mill is configured to pulverize the biomass fuel into particles having a pulverization particle size of 5 mm or more.
- the combustion air supply means supplies the combustion air toward the bottom ash so that unburned biomass fuel is completely burned on the clinker conveyor.
- the boiler has a flow rate of combustion air supplied toward the inside of the furnace and a flow rate of the combustion air supplied from the combustion air supply means toward the bottom ash on the clinker conveyor.
- a combustion air control device is further included for controlling and optimizing the combustion efficiency of the entire boiler.
- the biomass burner is disposed at a position above the pulverized coal burner.
- the boiler further includes a cooling air supply means for supplying cooling air to the dry clinker processing apparatus.
- the boiler further includes a coal mill for pulverizing coal to produce the pulverized coal supplied to the pulverized coal burner.
- the present invention is a method for operating a biomass-mixed pulverized coal-fired boiler, the step of pulverizing biomass fuel by a biomass mill, and supplying the pulverized biomass fuel to a furnace by a biomass burner
- the combustion efficiency of the entire boiler is optimized by controlling the flow rate of the combustion air supplied toward the inside of the furnace and the flow rate of the combustion air supplied toward the bottom ash on the clinker conveyor. Turn into.
- the boiler operation method further includes a step of supplying cooling air to the dry clinker processing apparatus.
- the biomass mill is used as a dedicated mill for pulverizing the biomass fuel
- the coal mill is used as a dedicated mill for pulverizing the coal.
- the present invention includes a coal-dedicated mill and a biomass-dedicated mill, and a biomass fuel co-fired pulverized coal fired boiler that co-fires biomass fuel pulverized by a dedicated pulverizer with coal fine powder without adding special equipment. It is an object of the present invention to devise a method for co-firing biomass fuel so that coarse-grained biomass fuel can be completely burned into ash and the co-firing rate can be increased.
- the means for solving the above problems is based on the premise of a biomass-mixed pulverized coal fired boiler that is equipped with a coal-dedicated mill and a biomass-dedicated mill, supplying biomass fuel crushed by the biomass-dedicated mill and co-firing with pulverized coal. This is due to the following (a) to (d).
- the biomass fuel to be co-fired is a granular material having a pulverized particle size of 5 mm or more
- a dry clinker treatment device is provided below the transition hopper of the boiler
- the dry clinker treatment device includes combustion air supply means, and the unburned biomass fuel that has fallen into the dry clinker treatment device is completely burned on a conveyor belt to become ash
- D) The amount of combustion air supplied is controlled so that the pulverized coal and biomass fuel are combusted by the amount of air supplied to the dry clinker treatment device and the amount of combustion air supplied to the furnace by the combustion air supply means, etc. is being done.
- the biomass fuel is pulverized into a pulverized particle size of 5 mm or more by a dedicated mill and mixed with pulverized coal.
- the biomass fuel is blown up by the combustion gas from the pulverized coal burner and floats and burns, and the coarse particles descend in the furnace and finally fall to the dry clinker processing apparatus disposed below the transition hopper.
- the fine particles of 3 mm or less are completely burned out in the furnace to become ash, and the medium particles of about 5 mm are almost carbonized and fall into the dry clinker processing apparatus, and coarse particles B significantly larger than 5 mm. Falls onto the conveyor belt with the wooden core remaining.
- the moving speed of the conveyor belt of the dry clinker processing apparatus is extremely slow (about 5 mm / second), and the time required for discharging to the clinker collecting means is about 1 hour.
- the combustion gas of unburned biomass that has fallen into the dry clinker treatment apparatus is sucked into the furnace through the transition hopper from the lower end of the furnace, and merges with the combustion gas of pulverized coal and biomass fuel.
- the present invention drops a large amount of unburned biomass with a wooden core remaining on a conveyor belt of a dry clinker processing apparatus, and provides a combustion air supply means in the dry clinker processing apparatus, and a large amount of combustion air is provided by the combustion air supply means. And the unburned biomass that has fallen is actively burned on the conveyor belt.
- biomass fuel is dropped in a large amount while being cored, and the conveyor belt is used as a combustion dish directly below the transition hopper to be actively burned thereon, and the combustion heat is taken into the furnace.
- the temperature, oxygen, and time required for burning the wood are necessary, but the temperature is sufficient because the bottom ash that has fallen from the furnace is 1000 ° C or higher.
- the moving speed of the conveyor is very low, a sufficient combustion time is ensured. Therefore, if air is sufficiently supplied to the biomass fuel on the high-temperature conveyor belt, the biomass is sufficiently combusted.
- the surplus oxygen when the sufficient amount of air is supplied to the biomass fuel on the conveyor belt is completely sucked into the furnace and used for combustion in the furnace.
- a device that efficiently blows the biomass fuel on the conveyor belt is desired. When the air is efficiently supplied, the excess amount of combustion air can be reduced. .
- the additional equipment for carrying out the co-firing method of the present invention is extremely small, and a small-sized biomass fuel pulverizer can be adopted, so that the equipment cost and operation cost are greatly improved.
- the biomass pulverizer is downsized and its driving power is reduced, so that the effect of reducing the equipment cost and the operating cost is remarkable.
- biomass fuel depends on the economic and social demands of co-firing biomass fuel with a pulverized coal fired boiler. Economic efficiency depends on the price of biomass fuel to be used, the price of processing, the price of coal fuel, and societal demands include fossil fuel consumption control, promotion of CO 2 emission reduction, and effective use of local biomass. Promotion etc.
- the level of the pulverized particle size of the biomass fuel and the level of the co-firing rate of the biomass fuel are appropriately selected in consideration of the above.
- Embodiment 1 is that the biomass burner is arranged at a position above the pulverized coal burner.
- the arrangement of this biomass burner is a conventionally known arrangement (FIG. 6).
- the floating combustion time of the biomass fuel in the furnace becomes longer. Therefore, the unburned portion (carbonized portion and woody portion) falling by that amount is reduced, and accordingly, the amount of combustion air supplied to the dry clinker processing device is reduced by that amount. Therefore, it is possible to suppress a decrease in the thermal efficiency of the biomass-mixed pulverized coal-fired boiler and improve the biomass fuel mixed-burning rate.
- the second embodiment is that the combustion air supply means is an air supply means that is separate from the cooling air supply means, and is disposed in the vicinity of the transition hopper.
- the unburned biomass that has fallen on the conveyor belt is supplied with fresh air by the combustion air supply means, and the biomass fuel is continuously burned on the conveyor belt, and the combustion is promoted. Therefore, the unburned portion burns out in a very short time with a small amount of air supply, and the unburned portion is not stacked on the conveyor belt and the combustion is not delayed. The clinker will not remain unburned.
- the unburned biomass fuel on the clinker conveyor is provided by means (process) for actively burning unburned biomass fuel contained in the bottom ash on the clinker conveyor on the clinker conveyor. Even if it falls, it can be made to burn on a conveyor and the combustion heat can be utilized with a boiler. For this reason, a biomass fuel having a relatively large particle size, for example, a biomass fuel having a pulverized particle size of 5 mm or more, is used without the need to add significant facilities to the configuration of the conventional biomass fuel co-fired pulverized coal fired boiler. Thus, the pulverization power of the biomass fuel can be reduced, and the co-firing rate of the biomass fuel can be increased.
- the coal pulverization efficiency of the coal mill is not reduced due to biomass fuel pulverization, and the pulverization particle size of the biomass fuel is 5 mm or more. This significantly reduces the pulverization power of the biomass fuel.
- a woody (miscellaneous) biomass fuel dried to a moisture content of 20% is mixed and fired at 2.6 tons per hour.
- a pulverized coal burner 4 is provided at the lower part of the furnace 1
- a biomass burner 5 is provided at a position higher than the burner 4, and a transition is provided below the furnace 1.
- a dry clinker processing device 21 is provided via a hopper 20.
- the structure of the dry clinker processing apparatus 21 is substantially the same as that of the conventionally known dry clinker processing apparatus shown in FIG. 7, and a conveyor belt 23 having high heat resistance is provided in the casing 22 to receive the dropped bottom ash. In FIG. 3, the movement is from the left side to the right side at a speed of about 5 mm per second.
- the conveyor belt 23 is driven by drive wheels 24. Further, a large number of cooling air suction holes 31 are provided on the side wall of the casing 22 of the dry clinker processing apparatus 21 as shown in FIG.
- the cooling air suction hole 31 is an air supply hole opened to the outside air and is opened and closed by a flap plate.
- the flap is opened and outside air is sucked from the cooling air suction hole 31.
- the pressure is positive, the flap is closed by the flap and the injection of combustion gas in the furnace is prevented.
- a combustion air supply means 32 composed of an air source, piping and the like is provided in the vicinity of the transition hopper 20.
- the flow rate of the combustion air supplied from the combustion air supply means 32 is controlled by the combustion air control device 60.
- the coal supplied from the coal bunker 11 is pulverized by the coal mill 6, supplied to the furnace 1 by the pulverized coal burner 4, and burned in the lower region F1.
- the biomass fuel is charged into the biomass bunker 12 and pulverized to a pulverization particle size of 5 mm by the biomass mill 13, and the granular material of this biomass fuel is supplied from the upper biomass burner 5 to the furnace 1 and burned in the upper region F 2. It blows up and floats with the combustion gas in the lower region F 1, and its middle and coarse particles descend on the inner wall side of the furnace 1 and fall on the conveyor belt 23 of the dry clinker processing apparatus 21 through the transition hopper 20.
- Granules of less than 5 mm of biomass fuel are completely burned out in the furnace 1 until they fall on the conveyor belt, and become ash, and a part of them becomes unburned carbide.
- most of the medium grains b slightly exceeding 5 mm and coarse grains B significantly exceeding 5 mm fall on the conveyor belt 23 in the state of unburned carbide or carbide with a woody core remaining.
- the amount of biomass that may fall to the dry clinker processing apparatus 21 is 0.26 tons per hour of 5 mm or more, and the breakdown of the unburned portion is about 70% of wood (volatile component) and 30% of carbide (Remaining charcoal component). Most of the medium grains close to 5 mm out of 0.26 t are burned during the fall, and about 0.13 t per hour, which is about half as a whole, is expected to fall on the conveyor belt 23.
- the cooling air suction hole 31 supplies 2,000 Nm 3 of air per hour to the lower side of the conveyor belt.
- the amount of air supplied for combustion in the boiler furnace of this embodiment is 100,000 Nm 3 per hour.
- the total of the combustion air amount of 1,000 Nm 3 per hour supplied by the combustion air supply means 32 to the dry clinker processing apparatus and the cooling air amount of 2,000 Nm 3 per hour by the cooling air suction holes 31 is 3,000 Nm 3 per hour. Is sucked into the furnace 1 through the transition hopper 20, the amount of combustion air supplied from the windbox 3 to the furnace 1 is 97,000 Nm 3 per hour, and this air is the combustion air supply device 50 (FIG. 1). Supplied by
- the wire rod of the mesh belt 23a is squeezed between the crosspieces 23d and the steel plate 23b and fixed with bolts and nuts 8 and 10, and a large number of the steel plates 23b are combined in a state where a part of them is overlapped.
- the belt 23a is covered.
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Abstract
Description
(ロ)上記ボイラのトランジションホッパの下方に乾式クリンカ処理装置が設けられており、
(ハ)上記乾式クリンカ処理装置が燃焼空気供給手段を備えていて当該乾式クリンカ処理装置に落下したバイオマス燃料の未燃分をコンベアベルト上で完全燃焼させて灰にするようになっており、
(ニ)燃焼空気供給手段等によって上記乾式クリンカ処理装置に供給される空気量と火炉に供給される燃焼空気量で微粉炭及びバイオマス燃料が燃焼されるように、供給される燃焼空気量が制御されていること。
専用ミルでバイオマス燃料を粉砕粒度5mm以上に粉砕してこれを微粉炭と混焼させる。このときバイオマス燃料は微粉炭バーナによる燃焼ガスで吹き上げられて浮遊燃焼し、粗大粒子は火炉内を降下し、最終的にトランジションホッパの下方に配置された乾式クリンカ処理装置に落下する。このとき、3mm以下の微粒分は火炉内で完全に燃え尽きて灰になり、5mm程度の中粒分はほぼ炭化状態で乾式クリンカ処理装置に落下し、また、5mmよりも大幅に大きい粗粒Bは木質の芯が残ったままでコンベアベルトに落下する。
実施態様1は、微粉炭バーナよりも上方位置にバイオマスバーナを配置したことである。
実施態様2は、燃焼空気供給手段を冷却空気供給手段とは別個の空気供給手段とし、これをトランジションホッパの近傍に配置したことである。
本発明によれば、クリンカコンベア上のボトムアッシュ中に含まれるバイオマス燃料の未燃分をクリンカコンベア上で積極的に燃焼させる手段(工程)を備えることにより、クリンカコンベア上に未燃焼のバイオマス燃料が落下してもコンベア上で燃焼させてその燃焼熱をボイラで利用することができる。このため、従来のバイオマス燃料混焼微粉炭焚きボイラの構成に対して大幅な設備の追加を必要とせずに、比較的大きな粒径のバイオマス燃料、例えば「粉砕粒度5mm以上」のバイオマス燃料を使用することによりバイオマス燃料の粉砕動力を低減することができ、また、バイオマス燃料の混焼率を高めることができる。
Claims (16)
- 微粉炭とバイオマス燃料とを混焼させるための火炉と、
前記火炉に前記微粉炭を供給するための微粉炭バーナと、
前記火炉に前記バイオマス燃料を供給するためのバイオマスバーナと、
前記バイオマスバーナに供給される前記バイオマス燃料を粉砕するためのバイオマスミルと、
前記火炉の下方に設けられ、前記火炉から排出されたボトムアッシュを搬送するためのクリンカコンベアを有する乾式クリンカ処理装置と、
前記クリンカコンベア上の前記ボトムアッシュに向けて燃焼空気を供給することにより、前記ボトムアッシュの中に含まれる前記バイオマス燃料の未燃分を前記クリンカコンベア上で燃焼させるための燃焼空気供給手段と、を備えたことを特徴とするバイオマス混焼微粉炭焚きボイラ。 - 前記バイオマスミルは、前記バイオマス燃料を粉砕粒度5mm以上の粉粒体に粉砕するように構成されていることを特徴とする請求項1記載のバイオマス混焼微粉炭焚きボイラ。
- 前記燃焼空気供給手段は、前記バイオマス燃料の未燃分が前記クリンカコンベア上で完全燃焼するように前記ボトムアッシュに向けて前記燃焼空気を供給することを特徴とする請求項1又は2に記載のバイオマス混焼微粉炭焚きボイラ。
- 前記火炉の内部に向けて供給される燃焼空気の流量と、前記燃焼空気供給手段から前記クリンカコンベア上の前記ボトムアッシュに向けて供給される前記燃焼空気の流量とを制御して、ボイラ全体の燃焼効率を最適化するための燃焼空気制御装置をさらに有する請求項1乃至3のいずれか一項に記載のバイオマス混焼微粉炭焚きボイラ。
- 前記微粉炭バーナよりも上方位置に前記バイオマスバーナを配置したことを特徴とする請求項1乃至4のいずれか一項に記載のバイオマス混焼微粉炭焚きボイラ。
- 前記乾式クリンカ処理装置に冷却空気を供給するための冷却空気供給手段をさらに備えたことを特徴とする請求項1乃至5のいずれか一項に記載のバイオマス混焼微粉炭焚きボイラ。
- 前記微粉炭バーナに供給される前記微粉炭を生成するために石炭を粉砕する石炭ミルをさらに有することを特徴とする請求項1乃至6のいずれか一項に記載のバイオマス混焼微粉炭焚きボイラ。
- 前記バイオマスミルは、前記バイオマス燃料の粉砕のための専用ミルであり、前記石炭ミルは、前記石炭の粉砕のための専用ミルであることを特徴とする請求項7に記載のバイオマス混焼微粉炭焚きボイラ。
- バイオマス混焼微粉炭焚きボイラの運転方法であって、
バイオマスミルによってバイオマス燃料を粉砕する工程と、
粉砕された前記バイオマス燃料をバイオマスバーナによって火炉に供給する工程と、
微粉炭バーナによって微粉炭を前記火炉に供給する工程と、
前記火炉の下方に設けられた乾式クリンカ処理装置のコンベアベルト上に排出されたボトムアッシュに向けて燃焼空気を供給することにより、前記ボトムアッシュの中に含まれる前記バイオマス燃料の未燃分を前記クリンカコンベア上で燃焼させる工程と、を備えたことを特徴とするボイラ運転方法。 - 前記バイオマスミルによって前記バイオマス燃料を粉砕粒度5mm以上の粉粒体に粉砕することを特徴とする請求項9に記載のボイラ運転方法。
- 前記バイオマス燃料の未燃分が前記クリンカコンベア上で完全燃焼するように前記ボトムアッシュに向けて前記燃焼空気を供給することを特徴とする請求項9又は10に記載のボイラ運転方法。
- 前記火炉の内部に向けて供給される燃焼空気の流量と、前記クリンカコンベア上のボトムアッシュに向けて供給される前記燃焼空気の流量とを制御して、ボイラ全体の燃焼効率を最適化することを特徴とする請求項9乃至11のいずれか一項に記載のボイラ運転方法。
- 前記微粉炭バーナよりも上方位置にある前記バイオマスバーナから前記バイオマス燃料を前記火炉に供給することを特徴とする請求項9乃至12のいずれか一項に記載のボイラ運転方法。
- 前記乾式クリンカ処理装置に冷却空気を供給する工程をさらに有することを特徴とする請求項9乃至13のいずれか一項に記載のボイラ運転方法。
- 前記微粉炭バーナに供給される前記微粉炭を生成するために石炭ミルによって石炭を粉砕する工程をさらに有することを特徴とする請求項9乃至14のいずれか一項に記載のボイラ運転方法。
- 前記バイオマスミルを前記バイオマス燃料の粉砕のための専用ミルとして使用し、前記石炭ミルを前記石炭の粉砕のための専用ミルとして使用することを特徴とする請求項15に記載のボイラ運転方法。
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MX2010012333A MX2010012333A (es) | 2008-05-16 | 2009-05-13 | Caldera alimentada por mezcla de biomasa y carbon pulverizado y metodo de operación de la caldera. |
KR1020107025134A KR101280199B1 (ko) | 2008-05-16 | 2009-05-13 | 바이오매스혼소미분탄연소보일러 및 동 보일러의 운전방법 |
BRPI0911995A BRPI0911995A2 (pt) | 2008-05-16 | 2009-05-13 | caldeira a carvão pulverizado e à queima nisturada com biomassa, e, método para operar a mesma |
DK09746610.6T DK2287529T3 (en) | 2008-05-16 | 2009-05-13 | Biomass blend fired boiler fueled by pulverized coal, and the method of operating the boiler |
EP09746610.6A EP2287529B1 (en) | 2008-05-16 | 2009-05-13 | Biomass-mixed-firing pulverized coal fired boiler and operation method of the boiler |
US12/988,804 US9068746B2 (en) | 2008-05-16 | 2009-05-13 | Biomass-mixed-firing pulverized coal fired boiler and operation method of the boiler |
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CN110986065B (zh) * | 2019-11-18 | 2021-08-17 | 国网河北省电力有限公司电力科学研究院 | 利用干渣机的冷却空气加热烟气的系统及消除烟羽的方法 |
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CN112032745B (zh) * | 2020-08-31 | 2022-12-06 | 井冈山大学 | 一种污水治理用金鱼藻焚烧装置 |
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EP2287529A1 (en) | 2011-02-23 |
MX2010012333A (es) | 2011-04-04 |
US9068746B2 (en) | 2015-06-30 |
EP2287529A4 (en) | 2014-07-30 |
JP5051721B2 (ja) | 2012-10-17 |
KR20110031153A (ko) | 2011-03-24 |
BRPI0911995A2 (pt) | 2015-10-27 |
US20110107948A1 (en) | 2011-05-12 |
DK2287529T3 (en) | 2015-12-07 |
EA201001798A1 (ru) | 2011-06-30 |
KR101280199B1 (ko) | 2013-06-28 |
ZA201008158B (en) | 2011-09-28 |
EP2287529B1 (en) | 2015-08-26 |
JP2009276027A (ja) | 2009-11-26 |
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