WO2010047042A1 - 微粉炭燃焼ボイラを用いたバイオマスの利用装置およびそれを用いたバイオマスの利用方法 - Google Patents
微粉炭燃焼ボイラを用いたバイオマスの利用装置およびそれを用いたバイオマスの利用方法 Download PDFInfo
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- WO2010047042A1 WO2010047042A1 PCT/JP2009/004928 JP2009004928W WO2010047042A1 WO 2010047042 A1 WO2010047042 A1 WO 2010047042A1 JP 2009004928 W JP2009004928 W JP 2009004928W WO 2010047042 A1 WO2010047042 A1 WO 2010047042A1
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- pyrolysis
- biomass
- pulverized coal
- tar
- carbide
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2201/00—Pretreatment
- F23G2201/30—Pyrolysing
- F23G2201/303—Burning pyrogases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2201/00—Pretreatment
- F23G2201/30—Pyrolysing
- F23G2201/304—Burning pyrosolids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
- F23G2206/203—Waste heat recuperation using the heat in association with another installation with a power/heat generating installation
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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
- F23G2209/26—Biowaste
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Definitions
- the present invention relates to a biomass utilization method and apparatus for efficiently pyrolyzing biomass and using gas, tar and carbide in a pulverized coal combustion boiler.
- a typical example of biomass and waste treatment is a waste incineration power generation system that collects electric power by combining steam power generation with incineration facilities.
- a waste incineration power generation system that collects electric power by combining steam power generation with incineration facilities.
- a lot of water and a low calorific value for example, biomass, general garbage
- a high calorific value but a high-efficiency operation for example, a waste plastic containing chlorine
- III For the reason that the amount that can be collected economically is limited, the power transmission efficiency by waste power generation is generally only 10-15%.
- the transmission end efficiency by pulverized coal combustion power generation using fossil fuel is generally 41 to 42%.
- High-efficiency incinerator technology that generates electricity with power transmission efficiency of 20% to 30% by improving boiler materials, adjusting raw materials (using RDF), and improving efficiency by using external fuel (super garbage power generation).
- these high-efficiency equipments require additional elements such as pretreatment of raw materials, improvement of boiler materials, introduction of external fuel (fossil fuel), etc., and chlorine in waste (mainly from waste plastic)
- the increase in operating energy such as increased use of electric power, increased water treatment energy, and increased energy related to equipment manufacturing and construction, including the carbon dioxide generated in these processes, the reduction of carbon dioxide due to the use of waste is considered. Even so, there are many cases in which carbon dioxide reduction is not necessarily achieved and energy is often increased, and as a result, it is easy to become a facility that only “treats” waste.
- the steam is converted into electric power by a steam turbine or used as heat as it is.
- a steam turbine When using biomass, if it is put directly into a coal crusher for the purpose of crushing to the same particle size as coal for airflow conveyance, productivity may be reduced due to deterioration of crushability (eg wood), drying, granulation, Pre-treatment such as carbonization is necessary (for example, sewage sludge), or the boiler efficiency is reduced by burning low-reactivity, low-calorific raw materials in the boiler (for example, wood, sewage sludge). ), Etc., and the disadvantage is that the mixing rate of biomass cannot be increased.
- Patent Document 1 discloses that a pulverized coal combustion boiler has a dedicated pulverization and drying device for supplying wood to the pulverized coal combustion boiler. Disclosed are facilities and methods that make it possible to keep energy low. Patent Document 2 discloses that wood that is poorly combustible (biomass) that has been directly put into the boiler is recovered and dropped into the lower part of the boiler and is put into a coal-side mill (wood is dried). ⁇ It is heated and improves crushability), and discloses a facility and a method capable of suppressing the total crushing power.
- Both (A) and (B) are converted into another form (gas or carbide) once, and the effect of improving the overall efficiency rather than simply burning is expected. ) It has the effect of being able to enjoy the merits of increasing the degree of freedom such as removal and handling (because it can be basically handled by piping because it is gas).
- the present invention mainly has the former effect and belongs to the type (A).
- Patent Literature 3 and Patent Literature 4 have the latter effect.
- Patent document 3 belongs to the type (A), and focuses on carbonization, and discloses a system in which carbide is burned together with coal in a business boiler (gas is burned and used as a thermal decomposition heat source by indirect heating).
- Patent Document 4 belongs to the type (B), and discloses a system in which chlorine in partially burned gas is removed and burned in a boiler (the char in the gas is mixed with coal and used in the boiler). Yes. In the system disclosed in Patent Document 4, most of the inorganic chlorine that occupies about half of the total chlorine remains in the char, but it can be processed twice or more by removing chlorine in the gas.
- Japanese Unexamined Patent Publication No. 2005-291526 Japanese Unexamined Patent Publication No. 2005-291531 Japanese Unexamined Patent Publication No. 2000-283431 Japanese Unexamined Patent Publication No. 2000-283434
- Patent Document 1 the use of sensible heat of combustion exhaust gas suppresses a decrease in energy used in crushing / drying wood pretreatment.
- only drying can prevent a decrease in boiler efficiency due to moisture, but cannot prevent a decrease in boiler efficiency due to low reactivity and low calorific value of wood (compared to coal).
- Patent Document 2 can reduce the overall crushing power, there is energy that is lost when recovering wood that is not sufficiently reacted (sensible heat loss, power for transportation), which is very advantageous. It's not a method.
- Patent Document 3 and Patent Document 4 are technologies mainly aimed at suppressing the disadvantages caused by chlorine (hydrochloric acid corrosion), and are not focused on improving efficiency.
- a gasification furnace (partial combustion type using air in a fluidized bed in the embodiment) is an air ratio (that is, a ratio between an actual air amount and a theoretical air amount, and the theoretical air amount is Operates at 1.0 to 1.3 (the amount of air supplying the amount of oxygen necessary for complete combustion of the fuel being supplied) to produce combustible gases and carbides including carbon monoxide
- the air ratio is 1 or more and carbides are also generated, the main components of the gas are carbon dioxide, water vapor, and nitrogen (derived from combustion air).
- the present invention solves these problems of the prior art, utilizes the features of the shaft-type pyrolysis furnace, pyrolyzes waste with high efficiency, and burns and uses gas, tar, and carbide in a boiler.
- An object of the present invention is to provide an efficient biomass utilization method and apparatus in a pulverized coal combustion boiler.
- the present invention employs the following means in order to solve the above problems.
- the biomass utilization apparatus of the present invention pyrolyzes or partially oxidizes biomass to produce pyrolysis gas, pyrolysis tar, and carbide, and the pyrolysis gas and pyrolysis tar from the top of the furnace.
- a shaft-type pyrolysis furnace that discharges and discharges the carbide from the furnace bottom; a pulverized coal combustion boiler that burns pulverized coal to generate steam; and the shaft-type pyrolysis furnace that removes the pyrolysis gas and the pyrolysis tar And a pipe for feeding to the pulverized coal combustion boiler.
- the pulverized coal combustion boiler includes a coal pulverizer that finely carbonizes coal as fuel; the coal pulverizer is the shaft-type pyrolysis furnace. You may have the 1st conveying apparatus which conveys the produced
- the pulverized coal combustion boiler conveys the carbide generated in the shaft-type pyrolysis furnace to the pulverized coal combustion boiler. You may have a 2nd conveying apparatus.
- the piping separates the pyrolysis gas and the pyrolysis tar generated in the shaft-type pyrolysis furnace. And a tar separation device that collects the pyrolysis tar; and a pyrolysis gas pipe that sends the pyrolysis gas separated by the tar separation device to the pulverized coal combustion boiler.
- the biomass utilization method using the biomass utilization apparatus according to (1), (2), (3), or (4) thermally decomposes the biomass from a lower portion of the shaft-type pyrolysis furnace.
- a pyrolysis gas having sensible heat for thermal decomposition of the biomass in the shaft-type pyrolysis furnace or by introducing an oxygen-containing gas from the lower part of the shaft-type pyrolysis furnace
- the biomass in the shaft-type pyrolysis furnace is partially oxidized to produce the pyrolysis gas, the pyrolysis tar, and the carbide; the pyrolysis tar from the top of the shaft-type pyrolysis furnace
- the pyrolysis gas and the pyrolysis tar are discharged at a temperature at which the temperature does not condense; the carbide is discharged from the bottom of the furnace; the pyrolysis gas, or both the pyrolysis gas and the pyrolysis tar, Pulverized coal To introduce into the baked boiler.
- (6) The method for using biomass according to (5) described
- FIG. 1 shows a typical flow diagram of a biomass utilization apparatus using a shaft-type pyrolysis furnace and a pulverized coal combustion boiler 9 according to the first embodiment and the second embodiment of the present invention.
- the difference between the first embodiment and the second embodiment is that the pyrolysis tar 4 is not separated from the mixture of the pyrolysis gas 3 and the pyrolysis tar 4 generated together in the shaft-type pyrolysis furnace 2 (first Embodiment) and the case of separation (second embodiment), FIG. 1 clearly shows the flow of the second embodiment when tar is separated by the tar separation device 8 (the first embodiment is , Case excluding tar separation device 8).
- the biomass in the present embodiment refers to agricultural biomass (straw, sugarcane, rice straw, vegetation, etc.), forestry biomass (paper waste, sawn timber, thinned wood, wood charcoal, etc.), livestock biomass (livestock waste) Product), fishery biomass (fishery processing residue), waste biomass (raw garbage, RDF: solid waste fuel; Refused Fuel, garden trees, construction waste wood, sewage sludge), and the like.
- Biomass 1 is input from the upper part of the shaft type pyrolysis furnace 2 and descends in the furnace (moving bed).
- the size of the biomass 1 may be a size that enters the shaft-type pyrolysis furnace 2.
- biomass such as thinned thinned wood, construction waste, and garden trees is input in a size of about 300 mm square or less, and if necessary, roughly crushed and input.
- other waste biomass, forestry biomass, livestock biomass, and fishery biomass are input as they are.
- the biomass 1 While the biomass 1 is gradually lowered, the biomass 1 is dried and heated by the pyrolysis gas 6 rising inside the shaft-type pyrolysis furnace 2, and pyrolyzed to produce pyrolysis gas 3 and pyrolysis tar 4 to form a carbide 5. It becomes.
- the carbide 5 is discharged from the bottom of the shaft type pyrolysis furnace 2.
- the pyrolysis gas 6 as a pyrolysis heat source is largely supplied in two ways.
- One method is a method of introducing an oxygen-containing gas, which will be described later in an example.
- a part of the carbide 5 in the shaft-type pyrolysis furnace 2 is burned to form a heat source.
- the oxygen-containing gas may be air or oxygen-enriched air, and may be selected in consideration of both the oxygen production equipment cost and the gas processing equipment cost.
- oxygen-containing gas is introduced, for example, when pyrolyzing wood at a pace of 100 tons / day, the air ratio (that is, the ratio of the actual amount of air to be introduced and the theoretical amount of air, the theoretical air
- the amount is the amount of air that supplies the amount of oxygen necessary for complete combustion of the supplied fuel) and may be about 0.2.
- the temperature of the shaft-type pyrolysis furnace 2 may be managed by controlling the temperatures of the pyrolysis gas 3 and pyrolysis tar 4 discharged from the top of the furnace. This temperature should just be more than the temperature which the pyrolysis tar 4 does not condense, and it is preferable to manage to the temperature which does not condense even in the middle of conveyance to the pulverized coal combustion boiler 9 or the tar separation apparatus 8 of the latter stage. Although it depends on the type of biomass to be treated, it can be managed at a temperature of 300 to 600 ° C., for example.
- oxygen-enriched air that is, oxygen + air
- the concept of the air ratio is the same, and the supplied fuel is completely
- the amount of oxygen-enriched air supplying the amount of oxygen necessary for combustion is defined as the theoretical oxygen-enriched air amount, and the ratio with the supplied oxygen-enriched air is taken.
- the notation here is the air ratio.
- fuel is burned outside the shaft-type pyrolysis furnace 2 to produce a high-temperature gas of 1000 ° C. to 1200 ° C. and supplied as the pyrolysis gas 6.
- the pyrolysis gas 3 discharged from the top of the shaft-type pyrolysis furnace 2 (gas purification is performed if necessary) or the bottom of the shaft-type pyrolysis furnace 2 is discharged.
- Carbide 5 is assumed. When the pyrolysis gas 3 or the carbide 5 is used as a fuel, a cooling (separation) and supply process (equipment) is required.
- an external fuel such as fossil fuel may be used separately (the product gas or carbide increases correspondingly).
- the product gas or carbide increases correspondingly.
- the lower limit is 1000 ° C., and when it exceeds 1200 ° C., the clinker (melt agglomerates, The upper limit is set to 1200 ° C.
- the pyrolysis gas 3 and pyrolysis tar 4 are discharged from the upper outlet (top of the furnace) of the shaft type pyrolysis furnace 2 at 300 ° C. to 600 ° C. and proceed to the subsequent process via the pyrolysis gas delivery pipe 7.
- the pyrolysis gas 3 and pyrolysis tar 4 are directly blown into the pulverized coal combustion boiler 9.
- the pyrolysis gas 3 and pyrolysis tar 4 are blown into the pulverized coal combustion boiler 9 after the pyrolysis tar 4 is separated and recovered by the tar separator 8.
- biomass-derived pyrolysis gas 3 and pyrolysis tar 4 existing mixed combustion types (mixed combustion of pulverized coal and iron-producing gas, mixed pulverized coal and heavy oil, or mixed combustion of pulverized coal, iron-producing gas and heavy oil) Etc.), the pyrolysis gas 3 can be used without problems because it has many common components with the coke oven gas and has similar properties. Even when pyrolysis tar 4 is included, it can be supplied without any problem as a gas if condensation due to temperature drop is prevented (pipe temperature is not lowered to 300 ° C. or lower).
- the pyrolysis gas 3 and the pyrolysis tar 4 are likely to occur many times when the temperature falls to 300 ° C. or less.
- tar becomes a binder, and dust may adhere to and grow on the flue (delivery piping 7 such as pyrolysis gas).
- delivery piping 7 such as pyrolysis gas
- the temperature at the upper outlet of the shaft-type pyrolysis furnace 2 is less than 300 ° C., part of the pyrolysis tar 4 is likely to condense (particularly tar derived from wood), which is unsuitable because there is concern about clogging problems due to adhesion. .
- the temperature at the upper outlet of the shaft-type pyrolysis furnace 2 exceeds 600 ° C., the heat necessary for the shaft-type pyrolysis furnace 2 increases (it burns away from the carbide), which is inappropriate.
- an appropriate temperature is 300 ° C. to 600 ° C.
- tar separation device 8 There are two types of tar separation device 8: a separation method with a high temperature, and a separation method in which the gas temperature is once lowered to the tar condensation temperature.
- a separation method with a high temperature for example, a high-temperature filter (ceramic or metal) is used, and the dust is separated by condensing tar with the dust.
- the advantages are that there is no heat loss due to the temperature drop and that there is no need for a water treatment system, and the disadvantages are that the separation efficiency is as low as about 80% at most.
- direct quenching water circulation
- water spray or the like is used.
- the advantage is that the pyrolysis tar 4 can be separated efficiently (only about 100 mg / Nm 3 remains when lowered to 40 ° C. or lower). Disadvantages include heat loss due to temperature drop and the need for a water treatment system. In any system, since the separated tar has a large amount of heat, it is returned to the shaft-type pyrolysis furnace 2 as fuel for the pyrolysis gas 6 or as a pyrolysis raw material, or introduced into the pulverized coal combustion boiler 9 to generate heat. It is desirable to recover.
- the pyrolysis gas 3 and pyrolysis tar 4 or the sole pyrolysis gas 3 is fed into the pulverized coal combustion boiler 9 and combusted. After the heat is recovered by the heat recovery section 10 (steam 11 generation), the gas After detoxification in the processing unit 12, it is diffused into the atmosphere as a diffused gas 13.
- the pulverized coal combustion boiler 9 is separately charged with pulverized coal from the coal pulverization facility 14 and combusted. A part of the generated steam 11 is used in the system, but most of the steam is supplied to a steam turbine (not shown) and used for power generation.
- FIG. 1 The flow of the biomass utilization apparatus using the shaft-type pyrolysis furnace 2 and the pulverized coal combustion boiler 9 including the carbide utilization process according to the third embodiment and the fourth embodiment of the present invention is shown in FIG.
- the difference between the third embodiment and the fourth embodiment is that the generated carbide 5 is introduced into the coal crushing facility 14 (third embodiment: A), or the generated carbide 5 is directly pulverized coal combustion boiler 9. (Fourth embodiment: B).
- the carbide 5 generated in the shaft-type pyrolysis furnace 2 is processed by the carbide processing device 15 and finally charged into the pulverized coal combustion boiler 9.
- the carbide treatment device 15 includes a coarse crushing device and an inappropriate material separation device, but the coarse crushing device may be omitted depending on the state of the carbide 5.
- the unsuitable material separation device has a function of separating unsuitable materials 16 such as debris, stones and metals, which have no heat, and are not suitable for combustion in the pulverized coal combustion boiler 9, and screens, vibrating sieves, and magnetic separators. Have a machine.
- the coarse crushing device is installed for the purpose of improving the efficiency of sieving of the unsuitable material separating device (by making simple crushing, for example, so that nails digging into the carbide can be screened only by vibration). Crush to a size of about several tens of mm square.
- the crushed carbide is separated into the combustion inadequate material 16 and then introduced into the coal pulverization facility 14 through the route A by the carbide conveying device 17 and finely pulverized coal. Is burned in the pulverized coal combustion boiler 9.
- the crushed carbide is separated into the combustion inappropriate material 16 and then directly blown into the pulverized coal combustion boiler 9 through the B route.
- the carbide treatment device 15 includes a coarse crushing device, an inappropriate material separating device, and a fine crushing device.
- the rough crushing apparatus may be omitted for the reason described above.
- the carbide 5 is crushed to about several tens of ⁇ m, which is the same size as pulverized coal, and blown into the pulverized coal combustion boiler 9.
- route B since efficient combustion by direct blowing is required, an air current conveying system such as nitrogen is usually adopted as the carbide conveying device 17 after the carbide processing device 15 to the pulverized coal combustion boiler 9. Insufflation may be performed.
- the coal 5 may be fed into the coal crushing facility 14 by the carbide conveying device 17 including a bucket conveyor and the like.
- Example 1 which concerns on the 1st Embodiment of this invention which does not isolate
- Wood construction waste wood 100 tons / day (4167 kg / hr) is used as biomass, and the air ratio (supply is oxygen-enriched air of 10% by volume of oxygen, and 1 when complete combustion) is 0.18
- the shaft type pyrolysis furnace 2 the biomass 1 was partially burned with oxygen in oxygen-enriched air, and the shaft type pyrolysis furnace 2 was operated at a pyrolysis gas temperature of 400 ° C at the furnace outlet.
- pyrolysis gas 7986 Nm 3 / h, pyrolysis tar 389 kg / h, and carbide 395 kg / h (including dust) were generated.
- external fuel was almost unnecessary, but when starting up with insufficient heat, some LPG (+ oxygen-enriched air) was used.
- the pyrolysis gas 3 is composed of 14.7% by volume of CO, 14.5% by volume of H 2 , 3.9% by volume of CH 4 as a main combustible component, and 24.7% by volume of CO as other gas components. 2 and 33.4% by volume of H 2 O (water vapor), a trace amount of hydrocarbons having C 2 (carbon number of 2) or more, and the remainder was N 2 .
- the pyrolysis gas 3 and pyrolysis tar 4 were directly supplied to the pulverized coal combustion boiler 9. Different from the pulverized coal nozzle (burner), a dedicated blowing nozzle was installed, and the pyrolysis gas 3 and pyrolysis tar 4 were mixed with air immediately before the pulverized coal combustion boiler 9 and injected from four locations. 66% of the calorific value of the construction waste wood used as raw material was supplied to the pulverized coal combustion boiler 9 in the form of gas and tar. The remaining amount of heat is 10% carbide (taken outside and processed), about 9 to 11% is consumed by combustion in the shaft-type pyrolysis furnace 2, and the rest is composed of carbon adhering to unsuitable materials and heat dissipated. It was done. At this time, the amount of coal treated in the pulverized coal combustion boiler 9 was about 800 tons / day.
- Example 2 according to the third embodiment in which the carbide 5 is charged into the coal crushing facility 14 (A route) is shown below.
- Wood construction waste wood
- the air ratio supply is oxygen-enriched air with 10% by volume of oxygen, and 1 when complete combustion
- the biomass 1 was partially burned with oxygen in oxygen-enriched air in the shaft-type pyrolysis furnace 2, and the pyrolysis furnace was operated at a pyrolysis gas temperature of 400 ° C at the furnace outlet.
- the separated carbide contained almost no metal (1% by weight or less), and the carbon in the unsuitable material was 5% by mass or less, so that the separability was good. 61% by mass (about 240 kg / h) of carbide 395 kg / h is charged as product carbide into the coal crushing facility 14 of the pulverized coal combustion boiler 9 via the carbide conveying device 17 constituted by a bucket conveyor, together with other coal It was pulverized and blown into the pulverized coal combustion boiler 9 by airflow conveyance.
- the pyrolysis gas 3 is composed of 14.7% by volume of CO, 14.5% by volume of H 2 , 3.9% by volume of CH 4 as a main combustible component, and 24.7% by volume of CO as other gas components. 2 and 33.4% by volume of H 2 O (water vapor), a trace amount of hydrocarbons having C 2 (carbon number of 2) or more, and the remainder was N 2 .
- the pyrolysis gas 3 and pyrolysis tar 4 were directly supplied to the pulverized coal combustion boiler 9. Also in the case of this embodiment, a dedicated blowing nozzle is installed separately from the pulverized coal nozzle (burner), and the pyrolysis gas 3 and pyrolysis tar 4 are mixed with air immediately before the pulverized coal combustion boiler 9.
- Example 3 will be described below.
- Wood construction waste wood
- the air ratio supply is oxygen-enriched air with 10% by volume of oxygen, and 1 when complete combustion
- the biomass 1 was partially burned with oxygen in oxygen-enriched air in the shaft-type pyrolysis furnace 2, and the pyrolysis furnace was operated at a pyrolysis gas temperature of 400 ° C at the furnace outlet.
- the separated carbide contained almost no metal (1% by weight or less), and the carbon in the unsuitable material was 5% by mass or less, so that the separability was good.
- About 59% by mass (about 235 kg / h, loss of 5 kg / h in hammer type mill) of 395 kg / h of carbide is a pulverized coal combustion boiler via a carbide conveying device 17 composed of an air current conveying facility using nitrogen as product carbide. 9 was blown directly.
- the pyrolysis gas 3 is composed of 14.7% by volume of CO, 14.5% by volume of H 2 , 3.9% by volume of CH 4 as a main combustible component, and 24.7% by volume of CO as other gas components. 2 and 33.4% by volume of H 2 O (water vapor), a trace amount of hydrocarbons having C 2 (carbon number of 2) or more, and the remainder was N 2 .
- the pyrolysis gas 3 and pyrolysis tar 4 were directly supplied to the pulverized coal combustion boiler 9. Also in the case of this embodiment, a dedicated blowing nozzle is installed separately from the pulverized coal nozzle (burner), and the pyrolysis gas 3 and pyrolysis tar 4 are mixed with air immediately before the pulverized coal combustion boiler 9.
- separates a tar among the flows shown by FIG. 1 is shown below.
- the carbide was processed in the apparatus according to the third embodiment of the present invention that is fed into the coal crushing apparatus 14.
- Wood construction waste wood
- the air ratio supply is oxygen-enriched air with 10% by volume of oxygen, and 1 when complete combustion
- the biomass 1 was partially burned with oxygen in oxygen-enriched air in the shaft-type pyrolysis furnace 2, and the pyrolysis furnace was operated at a pyrolysis gas temperature of 400 ° C at the furnace outlet.
- the separated carbide contained almost no metal (1% by weight or less), and the carbon in the unsuitable material was 5% by mass or less, so that the separability was good. 61% by mass (about 240 kg / h) of carbide 395 kg / h is charged as product carbide into the coal crushing facility 14 of the pulverized coal combustion boiler 9 via the carbide conveying device 17 constituted by a bucket conveyor, together with other coal It was pulverized and blown into the pulverized coal combustion boiler 9 by airflow conveyance.
- the pyrolysis gas 3 is composed of 14.7% by volume of CO, 14.5% by volume of H 2 , 3.9% by volume of CH 4 as a main combustible component, and 24.7% by volume of CO as other gas components. 2 and 33.4% by volume of H 2 O (water vapor), a trace amount of hydrocarbons having C 2 (carbon number of 2) or more, and the remainder was N 2 .
- the pyrolysis tar 4 is separated by a tar separation device 8 composed of a high-temperature metal filter (20 pieces) (82% by mass of tar is collected together with dust), and the remaining light tar (a light light that avoids physical condensation). Min) was supplied to the pulverized coal combustion boiler 9 along with the pyrolysis gas 3.
- the separated tar-mixed dust was again charged into the shaft-type pyrolysis furnace 2 from an inlet different from the raw material.
- a dedicated blowing nozzle is installed separately from the pulverized coal nozzle (burner), and the pyrolysis gas 3 and light tar are mixed with air immediately before the pulverized coal combustion boiler 9 4. Blowed from the place.
- the biomass can be pyrolyzed with high efficiency and can be burned and used in a boiler without leaving any gas, tar, and carbide, so the industrial applicability is great.
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Abstract
Description
本願は、2008年10月22日に、日本に出願された特願2008-272155号に基づき優先権を主張し、その内容をここに援用する。
(A)(B)とも、一度別の形(ガスや炭化物)に転換することで、単に燃焼するより総合効率の向上が見込まれるという効果や、ガスという形にすることで不適物(塩酸等)除去やハンドリング等自由度増加(ガスなので基本的に配管で取り回せる)によるメリットを享受できるという効果を有する。
本発明は主に前者の効果が大きく、且つ、(A)のタイプに属する。特許文献3、特許文献4は後者の効果が大きい。特許文献3は(A)のタイプに属し、炭化に主眼を置き、炭化物を石炭とともに事業用ボイラで燃焼するシステム(ガスは燃焼して間接加熱により熱分解熱源とする)を開示する。この特許文献3が開示するシステムにおいては、熱分解して発生する塩素分をボイラに入れないようにすることで(加熱により炭化物には塩素はほとんど残らず、またガスはボイラに入らず燃焼熱利用されるとしている)、処理廃棄物利用時のボイラトラブル(腐食等)を回避している。さらに特許文献4は(B)のタイプに属し、部分燃焼したガス中の塩素を除去し、ボイラで燃焼するシステム(ガス中のチャーは、石炭と混合してボイラで利用する)を開示している。この特許文献4が開示するシステムにおいては、塩素分に関しては、全塩素の半分ほどを占める無機系塩素の大部分がチャーに残留するが、ガス中塩素を除去することで二倍以上処理できる。
本発明は、これら従来技術の課題点を解決し、シャフト型熱分解炉の特長を活かして廃棄物を高効率で熱分解し、ガス、タール、炭化物を余すところなくボイラで燃焼使用することで、効率的な、微粉炭燃焼ボイラでのバイオマス利用方法および装置を提供することを目的とする。
(1)本発明のバイオマスの利用装置は、バイオマスを熱分解又は部分酸化して、熱分解ガス、熱分解タール、及び炭化物を生成すると共に、前記熱分解ガス及び前記熱分解タールを炉頂から排出し、前記炭化物を炉底から排出するシャフト型熱分解炉と;微粉炭を燃焼して蒸気を生成する微粉炭燃焼ボイラと;前記熱分解ガス及び前記熱分解タールを前記シャフト型熱分解炉から前記微粉炭燃焼ボイラへと送る配管と;を含む。
(2)前記(1)に記載のバイオマスの利用装置では、前記微粉炭燃焼ボイラが、燃料となる石炭を微粉炭化する石炭粉砕装置を備え;前記石炭粉砕装置は、前記シャフト型熱分解炉で生成された前記炭化物を、前記石炭粉砕装置へと搬送する第1の搬送装置を有しても良い。
(3)前記(1)、(2)に記載のバイオマスの利用装置では、前記微粉炭燃焼ボイラが、前記シャフト型熱分解炉で生成された前記炭化物を、前記微粉炭燃焼ボイラへと搬送する第2の搬送装置を有しても良い。
(4)前記(1)、(2)、(3)に記載のバイオマスの利用装置では、前記配管が、前記シャフト型熱分解炉で生成された前記熱分解ガスと前記熱分解タールとを分離して前記熱分解タールを回収するタール分離装置と;前記タール分離装置で分離された前記熱分解ガスを、前記微粉炭燃焼ボイラへと送る熱分解ガス配管と;を有しても良い。
(6)前記(5)に記載のバイオマスの利用方法は、前記炉底から排出された前記炭化物から燃焼不適物を除去し;前記燃焼不適物が除去された前記炭化物を、前記微粉炭燃焼ボイラに投入しても良い。
この要因として、シャフト型熱分解炉2の熱交換方式が非常に高効率であること(即ち、対向流直接熱交換方式)、熱分解に必要な最小限の熱のみ与える方式であること(熱分解ガス3の一部は炭化水素のまま後段工程へ進むこと)とが挙げられる。
尚、本実施形態では、熱分解用ガス6として空気の代わりに酸素富化空気(即ち、酸素+空気)を使用しているが、空気比の考え方は同じで、供給している燃料が完全燃焼するのに必要な酸素量を供給している酸素富化空気量を理論酸素富化空気量とし、供給した酸素富化空気との比をとる。ここでの表記は空気比とする。
熱分解ガス3または炭化物5を燃料として利用する際には、冷却、分離、供給のプロセス(設備)が必要になるので、設備コスト等で比較して適宜選択する。また、二酸化炭素削減の手段としては好ましくないが、別途化石燃料等の外部燃料を使用してもよい(その分、製品ガスまたは炭化物が増加することになる)。
前述した高温ガスの温度範囲に関しては、1000℃未満では未反応炭化物が多くなることから1000℃を下限値とし、1200℃を超える場合には、クリンカ(溶融した灰の凝集物であり、物流を阻害する)が発生しやすくなることから1200℃を上限値とした。
シャフト型熱分解炉2の上部出口温度が300℃未満の場合、熱分解タール4の一部が凝縮しやすくなり(特に木材由来のタール)、付着による閉塞トラブルが懸念されるため不適当である。一方、シャフト型熱分解炉2の上部出口温度が600℃を超えると、シャフト型熱分解炉2で必要な熱が多くなり(炭化物をよけいに燃焼する)経済性が下がるため不適当であり、また、微粉炭燃焼ボイラ9に吹き込む際の配管内壁を耐火物で構成する必要があるため、流量調整の精度維持の観点からも、やはり不適当である。従って、300℃~600℃が適切な温度である。
シャフト型熱分解炉2で生成された炭化物5は、炭化物処理装置15で処理され、最終的に微粉炭燃焼ボイラ9に投入される。炭化物処理装置15は粗破砕装置と不適物分離装置とを有するが、粗破砕装置は炭化物5の状態によっては省略しても良い。不適物分離装置は、がれき、石や金属のような、熱量を持たず、微粉炭燃焼ボイラ9で燃焼するのに適さない燃焼不適物16を分離する機能を持ち、スクリーンや振動篩、磁力選別機等を有する。粗破砕装置は、不適物分離装置の篩分けを効率化する(簡単な破砕をすることで、たとえば炭化物に食い込んだ釘等が振動のみで篩い分けられるようにする)目的で設置され、炭化物を数10mm角程度のサイズへ破砕する。
炭化物のもう一つの投入方法である本発明の第4の実施形態においては、破砕された炭化物は、燃焼不適物16を分離後、Bルートを通り直接微粉炭燃焼ボイラ9に吹き込まれる。このとき炭化物処理装置15は粗破砕装置と不適物分離装置と微破砕装置とを有する。ただし、粗破砕装置は前述の理由で省略しても良い。微破砕装置では、微粉炭と同等のサイズである数10μm程度まで炭化物5が破砕されて、微粉炭燃焼ボイラ9に吹き込まれる。Bルートの場合、直接吹き込みによる効率的な燃焼が必要になることから、炭化物搬送装置17として、通常は炭化物処理装置15後から窒素等の気流搬送方式を採用し、微粉炭燃焼ボイラ9への吹き込みを行なっても良い。Aルートの場合、Bルートと同じ方式に加え、バケットコンベア等を含む炭化物搬送装置17により石炭粉砕設備14に石炭5を投入しても良い。
バイオマスとして木材(建設廃木材)100トン/日(4167kg/hr)を使用し、空気比(供給は酸素10体積%の酸素富化空気で、完全燃焼時を1とする)0.18とし、シャフト型熱分解炉2内でバイオマス1を酸素富化空気中の酸素で部分燃焼させて、炉出口の熱分解ガス温度400℃でシャフト型熱分解炉2を操業した。
その結果、熱分解ガス7986Nm3/h、熱分解タール389kg/h、炭化物395kg/h(ダスト含む)が生成した。このとき外部燃料はほぼ不要であったが、熱が不十分な立ち上げ時には、若干のLPG(+酸素富化空気)を使用した。
熱分解ガス3は、14.7体積%のCO、14.5体積%のH2、3.9体積%のCH4を主可燃成分とし、その他のガス成分として、24.7体積%のCO2、33.4体積%のH2O(水蒸気)、微量のC2(炭素数が2)以上の炭化水素類等を含み、残りはN2であった。熱分解ガス3および熱分解タール4は、直接微粉炭燃焼ボイラ9に供給された。なお微粉炭用ノズル(バーナ)とは区別して、専用の吹き込み用ノズルを設置し、微粉炭燃焼ボイラ9直前で熱分解ガス3および熱分解タール4を空気と混合して4カ所から吹き込んだ。
原料の建設廃木材の発熱量の66%が、ガス、タールの形で微粉炭燃焼ボイラ9に投入された。残りの熱量は、炭化物10%(外部搬出して処理)と、9~11%程度はシャフト型熱分解炉2内の燃焼で消費され、残りは不適物に付着した炭素と放散熱等で構成された。このとき、微粉炭燃焼ボイラ9での石炭処理量は、約800トン/日であった。
バイオマスとして木材(建設廃木材)を100トン/日(4167kg/hr)で使用し、空気比(供給は酸素10体積%の酸素富化空気で、完全燃焼時を1とする)0.18とし、シャフト型熱分解炉2内でバイオマス1を酸素富化空気中の酸素で部分燃焼させて、炉出口の熱分解ガス温度400℃で熱分解炉を操業した。
その結果、熱分解ガス7986Nm3/h、熱分解タール389kg/h、炭化物395kg/h(ダスト含む)が生成した。このとき外部燃料はほぼ不要であったが、熱が不十分な立ち上げ時には、若干のLPG(+酸素富化空気)を使用した。炭化物処理装置15に関しては、建設廃木材は釘等の金属を含むことから、50mmサイズの幅の刃を備えた二軸破砕機(粗破砕機)と、比重選別と振動を組み合わせた風力選別装置(不適物分離装置)と、を設置し、処理を行った。分離した炭化物中には金属はほとんど含まれず(1重量%以下)、また不適物中の炭素は5質量%以下と分離性も良好であった。炭化物395kg/hの61質量%(約240kg/h)が製品炭化物としてバケットコンベアで構成される炭化物搬送装置17を経由して微粉炭燃焼ボイラ9の石炭粉砕設備14に投入され、他の石炭とともに粉砕され、気流搬送により微粉炭燃焼ボイラ9に吹き込まれた。
原料の建設廃木材の発熱量の76%が、ガス、タール、炭化物の形で微粉炭燃焼ボイラ9に投入された。残りの熱量は、9~11%程度はシャフト型熱分解炉2内の燃焼で消費され、残りは不適物に付着した炭素と放散熱等で構成される。このとき、微粉炭燃焼ボイラ9での石炭処理量は、約800トン/日であった。破砕時のミルの電流値は、石炭単独の時と本発明の炭化物を混合したときでの差は検知できず(1%未満)、生産性や動力に対する影響は軽微と考えられる。
バイオマスとして木材(建設廃木材)を100トン/日(4167kg/hr)で使用し、空気比(供給は酸素10体積%の酸素富化空気で、完全燃焼時を1とする)0.18とし、シャフト型熱分解炉2内でバイオマス1を酸素富化空気中の酸素で部分燃焼させて、炉出口の熱分解ガス温度400℃で熱分解炉を操業した。
その結果、熱分解ガス7986Nm3/h、熱分解タール389kg/h、炭化物395kg/h(ダスト含む)が生成した。このとき外部燃料はほぼ不要であったが、熱の不十分な立ち上げ時には、若干のLPG(+酸素富化空気)を使用した。炭化物処理装置15に関しては、建設廃木材は釘等の金属を含むことから、実施例2と同様の50mmサイズの幅の刃を備えた二軸破砕機(粗破砕機)と、比重選別と振動を組み合わせた風力選別装置(不適物分離装置)と、に加え、10mm角のスクリーンを持つハンマー型ミルを設置し、処理を行った。分離した炭化物中には金属はほとんど含まれず(1重量%以下)、また不適物中の炭素は5質量%以下と分離性も良好であった。炭化物395kg/hの約59質量%(約235kg/h、ハンマー型ミルでのロス5kg/h)が製品炭化物として窒素による気流搬送設備で構成される炭化物搬送装置17を経由して微粉炭燃焼ボイラ9に直接吹き込まれた。
原料の建設廃木材の発熱量の74%が、ガス、タール、炭化物の形で微粉炭燃焼ボイラ9に投入された。残りの熱量は、9~11%程度はシャフト型熱分解炉2内の燃焼で消費され、残りは不適物に付着した炭素、微粉砕時ロスと放散熱等で構成される。このとき、微粉炭燃焼ボイラ9での石炭処理量は、約800トン/日であった。
バイオマスとして木材(建設廃木材)を100トン/日(4167kg/hr)で使用し、空気比(供給は酸素10体積%の酸素富化空気で、完全燃焼時を1とする)0.18とし、シャフト型熱分解炉2内でバイオマス1を酸素富化空気中の酸素で部分燃焼させて、炉出口の熱分解ガス温度400℃で熱分解炉を操業した。
その結果、熱分解ガス7986Nm3/h、熱分解タール389kg/h、炭化物395kg/h(ダスト含む)が生成した。このとき外部燃料はほぼ不要であったが、熱が不十分な立ち上げ時には、若干のLPG(+酸素富化空気)を使用した。炭化物処理装置15に関しては、建設廃木材は釘等の金属を含むことから、50mmサイズの幅の刃を備えた二軸破砕機(粗破砕機)と、比重選別と振動を組み合わせた風力選別装置(不適物分離装置)と、を設置した。分離した炭化物中には金属はほとんど含まれず(1重量%以下)、また不適物中の炭素は5質量%以下と分離性も良好であった。炭化物395kg/hの61質量%(約240kg/h)が製品炭化物としてバケットコンベアで構成される炭化物搬送装置17を経由して微粉炭燃焼ボイラ9の石炭粉砕設備14に投入され、他の石炭とともに粉砕され、気流搬送にて微粉炭燃焼ボイラ9に吹き込まれた。
また、特許文献4においては、流動床を用いた実施例において、空気比1.0~1.3でガス化操業を実施している。具体的な各種数値の提示はないが、このとき、本実施例と同じ建設廃木材(バイオマス)を同じ量使用したと仮定すると、約20%の熱量を持つ炭化物が発生するが、ガスとタールは空気比が1以上であることからほぼ燃焼に使用され、ガス発熱量の回収は期待できない。仮に酸素が使われないで残る計算で5%分の発熱量分のCO、H2の形で残存したとすれば、合計25%の熱量が微粉炭ボイラに投入されることになる。同等のボイラ熱回収及び蒸気タービンによる効率(38%)を想定すると、発電効率9.5%の発電端効率、8.6%の送電端効率が推定できる。
本発明の効果が高い理由は、主に、熱分解部(特許文献4では流動床ガス化)の熱効率の違いと、低空気比/高空気比の操業前提の差によるものと考えられる。
2 シャフト型熱分解炉
3 熱分解ガス
4 熱分解タール
5 炭化物
6 熱分解用ガス
7 熱分解ガス等配送配管
8 タール分離装置
9 微粉炭燃焼ボイラ
10 熱回収部
11 蒸気
12 ガス処理部
13 放散ガス
14 石炭粉砕設備
15 炭化物処理装置
16 燃焼不適物
17 炭化物搬送装置
Claims (6)
- バイオマスを熱分解又は部分酸化して、熱分解ガス、熱分解タール、及び炭化物を生成すると共に、前記熱分解ガス及び前記熱分解タールを炉頂から排出し、前記炭化物を炉底から排出するシャフト型熱分解炉と;
微粉炭を燃焼して蒸気を生成する微粉炭燃焼ボイラと;
前記熱分解ガス及び前記熱分解タールを前記シャフト型熱分解炉から前記微粉炭燃焼ボイラへと送る配管と;
を備えることを特徴とする、バイオマスの利用装置。 - 前記微粉炭燃焼ボイラは、燃料となる石炭を微粉炭化する石炭粉砕装置を備え;
前記石炭粉砕装置は、前記シャフト型熱分解炉で生成された前記炭化物を、前記石炭粉砕装置へと搬送する第1の搬送装置を有する;
ことを特徴とする請求項1に記載のバイオマスの利用装置。 - 前記微粉炭燃焼ボイラは、前記シャフト型熱分解炉で生成された前記炭化物を、前記微粉炭燃焼ボイラへと搬送する第2の搬送装置を備えることを特徴とする請求項1に記載のバイオマスの利用装置。
- 前記配管は:
前記シャフト型熱分解炉で生成された前記熱分解ガスと前記熱分解タールとを分離して前記熱分解タールを回収するタール分離装置と;
前記タール分離装置で分離された前記熱分解ガスを、前記微粉炭燃焼ボイラへと送る熱分解ガス配管と;
を備えることを特徴とする請求項1~3のいずれか1項に記載のバイオマスの利用装置。 - 請求項1に記載のバイオマスの利用装置を用いたバイオマスの利用方法であって、
前記シャフト型熱分解炉の下部から前記バイオマスを熱分解するための顕熱を有する熱分解用ガスを投入して、前記シャフト型熱分解炉内の前記バイオマスを熱分解することで、又は、前記シャフト型熱分解炉の下部から酸素含有ガスを投入して、前記シャフト型熱分解炉内の前記バイオマスを部分酸化することで、前記熱分解ガス、前記熱分解タール、及び前記炭化物を生成し;
前記シャフト型熱分解炉の前記炉頂から前記熱分解タールが凝縮しない温度以上で前記熱分解ガス及び前記熱分解タールを排出し;
前記炭化物を前記炉底から排出し;
前記熱分解ガス又は、前記熱分解ガスと前記熱分解タールとの両方を、前記微粉炭燃焼ボイラへと投入する;
工程を有することを特徴とするバイオマスの利用方法。 - 前記炉底から排出された前記炭化物から燃焼不適物を除去し;
前記燃焼不適物が除去された前記炭化物を、前記微粉炭燃焼ボイラに投入する;
ことを特徴とする請求項5に記載のバイオマスの利用方法。
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CN103534340A (zh) * | 2011-05-04 | 2014-01-22 | 奥图泰有限公司 | 用于燃料气体的生产和进一步处理的方法和设备 |
KR101598575B1 (ko) * | 2014-10-30 | 2016-03-02 | 한국생산기술연구원 | 혼소형 연소장치를 포함하는 혼소형 연소 시스템 및 이의 제어 방법 |
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