CN101614154A - The carbonization of living beings and gasification and electricity generating device - Google Patents

The carbonization of living beings and gasification and electricity generating device Download PDF

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Publication number
CN101614154A
CN101614154A CN200910150227A CN200910150227A CN101614154A CN 101614154 A CN101614154 A CN 101614154A CN 200910150227 A CN200910150227 A CN 200910150227A CN 200910150227 A CN200910150227 A CN 200910150227A CN 101614154 A CN101614154 A CN 101614154A
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vaporizer
gas
temperature
gasification
heat
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CN101614154B (en
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市川和芳
犬丸淳
木户口和浩
原三郎
芦泽正美
金井正夫
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Central Research Institute of Electric Power Industry
Kanai Office Corp
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Central Research Institute of Electric Power Industry
Kanai Office Corp
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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
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/30—Use of alternative fuels, e.g. biofuels
    • 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
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/78—Recycling of wood or furniture waste

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Abstract

The invention provides the method that a kind of living beings that will comprise useless living beings gasify, this method may further comprise the steps: at first carbonization living beings, high-temperature gasification part and the gas converter part that will deliver to the two-stage vaporizer respectively from the carbon and the cracking gas of carbonizer then.Gasifying agent is delivered to the gasification part continuously, and delivers to gas converter off and on, to keep avoiding tar to form needed temperature in the gas converter section.A plurality of carbonizations chamber is that alternately is operated.When carbonization/gasification installation is used for when the power generation unit provides fuel, come the used heat of self-generating device to be sent back to carbonizer, and can be replenished by exchanging the heat that comes to be transported to the gas of power station since the vaporizer outlet.

Description

The carbonization of living beings and gasification and electricity generating device
The present invention for the applying date be that March 22, application number in 2005 are 200510056829.4, denomination of invention divides an application for the patent application of " carbonization of living beings and gasification and electricity generating device ".
Technical field
The carbonization and the gasification that the present invention relates to by living beings produce gas, and relate to and utilize living beings effectively to generate electricity as the energy.
Background technique
As refer to the material that comprises in a large number derived from the material of live organism in term as used herein " living beings (biomass) ".Living beings can comprise, for example, and the refuse that produces in agricultural wastes, forestry waste, municipal waste, structural material refuse, the food production, waste disposal mud or the like and this class mixtures of material.Living beings can comprise some inorganic matter, and can also comprise relevant with live organism more indirectly a large amount of organic materials, as waste plastics.
Japanese patent application has been described a kind of widely used technology that is used for carbonization and gasification for No. 35837/2004.In this technology, char-forming material (carbon) produces in the carbonization chamber, and is introduced into vaporizer, and it is converted to gas by using air and steam herein.This carburising step removes from thick fuel and anhydrates, and stays an amount of volatile matter simultaneously in char-forming material, thereby improves the efficient of gasification step.
Another kind of device has been proposed, living beings are directly delivered to vaporizer by for example feeding screw in this device, and do not have a precarburization, then air or oxygen and steam be introduced into be installed in the vaporizer downstream side converter to decompose the tar that in vaporizer, produces.This device is described in No. the 326241/2003rd, Japanese patent application.
In traditional carbonization/gasification technology, has low-down water content because be sent to the char-forming material of vaporizer, so can realize higher gasification efficiency.On the other hand, because big energy is used to carbonation process and the heat that obtains as the by product of carbonation process and flammable cracking gas are released and be not used, so the total efficiency of tradition gasification/carbonization technology is lower.
Do not have directly living beings being introduced vaporizer under the situation that precarburization gasifies since in living beings higher water content, in the vaporizer temperature inside is maintained at about 600 ℃ to 1000 ℃ scope.Therefore, often produce tar, and tar adheres to pipeline, cause invalid operation and need the counter measure as decomposing tar by steam.Especially under the situation that fuel is made of the mixture of various living beings, be difficult to utilize steam to decompose tar, it is usually in 400 ℃ to 450 ℃ temperature range.Therefore, must in the another one step, utilize suitable washing unit to remove the tar of adhesion.Remove tar and must remove carbon and the hydrogen that is included in wherein, so the gross calorific value of removing in the process gas that produces by vaporizer at tar can lose a part.Tar can also utilize oxygen to be decomposed, but this process causes the minimizing of the calorific value of the gas that produces equally.
Therefore, the objective of the invention is by reducing in carbonation process through the discharging energy that cracking gas lost and reduce owing to form the decline of the calorific value of the gas that produces that tar caused, thereby the more effective carbonization and the gasification of living beings are provided.
At present obtainable have the electricity generating device that is roughly 1 megawatts capacity and preferably have about 10% generating efficiency, and wherein wood-based living beings such as arbor, and refuse based biomass as municipal solid waste, rubbish, waste plastics or the like, are used as the fuel of boiler.Can improve the generating efficiency of biomass-based electricity generating device.As described in No. the 253274/2003rd, Japanese patent application, exploitation is as the rotary kiln of waste treatment equipment, and as the fluidized bed furnace described in No. the 160141/1998th, Japanese patent application, be suitable for biomass fermentation electric installation as described.The technology of the carbon that produces in the carbonization chamber of being used for gasifying for example also has been disclosed in No. the 275732/2003rd, the Japanese patent application.In this case, the drying of raw material and carbonization are to utilize the fuel (as kerosene, heavy oil or the like) that replenishes to carry out in the carbonization chamber.
Except that above-mentioned inefficient and will remove the problem of tar because burning be in to low temperature, carry out, so also may produce dioxin, it is a serious environmental problem.In addition, ash content is to discharge with powder type.Therefore, when handling the refuse ash content, it is normally transported and carries out landfill disposal, needs the counter measure with the heavy metal that prevents ash content and the wash-out of other harmful constituents, especially under the situation of ash content from the refuse based biomass, as rubbish and municipal solid waste.Under these circumstances, can in independent melting solid unit, melt the refuse ash content and change into slag.
The moving vaporizer of entrained flow of operating so that can not form tar under at least 1100 ℃ temperature can change into slag with ash content.The moving vaporizer of a kind of entrained flow is in the development phase that is used for coal gasification, and expection can be avoided the problem of tar adhesion.Yet under the situation of carrying the coal gasifier that flows secretly, coal must become subparticle, for example the particle of the about 100 μ m of granularity.In fact living beings such as wood-based living beings and refuse based biomass can not be processed, and are not easy to handle.Therefore, if living beings gasify in such device, then need to utilize independent device to handle, thereby need increase considerably plant layout.
The wood-based living beings can be used as fuel individually.Yet, being difficult to reliably and as one man guarantee such fuel, this is because the amount of obtainable wood-based living beings changes and be subject to the influence of climatic change seasonally.Therefore, the wood-based living beings have higher compiling costs and do not have cost benefit when individually as fuel.In addition, owing to be difficult to collect the wood-based living beings of aequum, thus be difficult to enlarge the scale of power generating equipment, and be difficult to use the wood-based living beings to realize the high efficiency generating.
Therefore, another object of the present invention provides a kind of biomass fermentation electric installation, it has the higher thermal efficiency and generating efficiency, and it can come stable electric generation by carbonization, burning and gasification, and raw material wherein to be processed not only comprises the wood-based living beings but also comprises refuse based biomass such as municipal solid waste.
Summary of the invention
Utilize the software for calculation of prediction gasification performance, we study two kinds of diverse ways: " a step charging process ", intermediate product wherein, promptly char-forming material and flammable cracking gas are added into vaporizer; And " two step charging process ", wherein intermediate product is delivered to high-temperature gasification part (burner) and gas converter (reductor) respectively, and it constitutes two stages of separating of two-stage vaporizer.
In two step charging process, promptly in the method for utilizing the two-stage vaporizer, gasifying agent (air or oxygen) only can be delivered to the high-temperature gasification part.Only utilize a spot of gasifying agent, just total oxygen ratio controllably can be remained on low-levelly, and the thermal efficiency that can be higher is realized gasification.
Yet, in two step charging process, changing in vaporizer outlet (that is, the outlet of gas converter) temperature experience, it depends on the amount of the flammable cracking gas that produces in the carbonization chamber.If the flow rate of flammable cracking gas increases, the outlet port temperature then descends, and the danger of tangible one-tenth tar.For fear of forming tar, need to keep the vaporizer outlet temperature being not less than the level of predetermined minimum temperature.
As the result of our research, we are definite, can avoid problem that tar forms in the two step charging process and the needed characteristics that can not damage two step charging process.
In preferred biomass carbonization-gasification installation according to the present invention and method, the heating biomass fuel is to produce char-forming material in the carbonization chamber.These apparatus and method are utilized the two-stage vaporizer, and it comprises the high-temperature gasification part that is used for the vaporized carbon formed material, and the gas converter that is used to transform flammable cracking gas, and wherein flammable cracking gas contains the tar that volatilizees when producing char-forming material.Feeder is provided, has been used for the char-forming material that produces in the carbonization chamber is transferred to the high-temperature gasification part of two-stage vaporizer.The cracking gas stream also is provided, and the flammable cracking gas that is used for producing in the carbonization chamber is sent to the gas converter of vaporizer.The gasifying agent feeder is introduced the high-temperature gasification part of vaporizer with gasifying agent, and controllably gas converter is delivered in oxygenousization agent, drops to below the predetermined temperature preferred 1100 ℃ so that can prevent in the temperature of vaporizer outlet.
Particularly under the ratio condition with higher of the cracking gas lower, that in carbonizer, produce with respect to amount of the fixed carbon content in living beings as by-product available from the char-forming material of carbonization, with respect to the flow rate of high-temperature gas from the high-temperature gasification part to converter, the flow rate of cracking gas becomes higher.Cracking gas and comes the gas temperature of autopneumatolysis part to be generally at least 1500 ℃ usually in 400 ℃ to 600 ℃ temperature range, thereby rapid decline that can occurrence temperature in gas converter.
If gasifying agent is sent to gas converter and high-temperature gasification part, when the flow rate of flammable cracking gas increases, then between gasifying agent and flammable cracking gas combustion reaction takes place.The burning of cracking gas, it can be called " reburning " or " back burning process ", can prevent that gas temperature from dropping to below the predetermined minimum value, and can prevent effectively that tar from forming and can not damage the low consumption of the needed characteristics, particularly its gasifying agent of two step charging process.
Preferably, the gasifying agent feeder is delivered to gas converter with oxygenousization agent off and on, and comprises pipeline, and this pipeline is configured to high-temperature gasification part and gas converter are delivered in oxygenousization agent.When this device of equipment like this, the charging that can optionally switch gasifying agent, it depends on the condition in vaporizer inside.Therefore, when normal running carbonization-gasification installation, gasifying agent can only be delivered to the high-temperature gasification part.Yet, if the temperature in the vaporizer outlet drops to predetermined temperature, or by observing or detecting the danger of this class incident of generation by automatic sensing equipment, gasifying agent then can be delivered to gas converter and high-temperature gasification part, thereby the condition of avoiding tar to form.
For biomass carbonization-gasification installation according to the present invention, the char-forming material (carbon) that produces in the carbonization chamber is used as the high-temperature gasification part that fuel adds vaporizer.Simultaneously, the air or oxygen as gasifying agent is added into the high-temperature gasification part.The moisture of char-forming material is removed in carbonization treatment, and therefore the high-temperature gasification atmosphere partly at vaporizer can remain on high temperature, and for example, 1500 ℃ or higher, it far surpasses 1100 ℃, the decomposition temperature of tar.On the other hand, flammable cracking gas in the carbonization chamber as by product generation and adding gas converter contains water, and with respect to the total amount of the living beings that add the carbonization chamber, the moisture of cracking gas can strengthen gasification efficiency, so that it is higher and do not have the gas of tar content effectively to produce calorific value.
In a word, the present invention can effectively prevent from not damage in the going out interruption-forming tar of vaporizer the advantage of two step charging process.In the gas that produces, do not have tar, therefore do not have because the calorific value of the gas that produces that tar content caused reduces.In addition, need not to utilize supplementary equipment to clean and adhere to the tar of pipeline, or utilize oxygen to decompose tar, it impels the calorific value of the gas that produces to reduce equally.Because utilized the flammable cracking gas that in the carbonization chamber, produces,, can obtain higher gasification efficiency so compare with traditional carbonization-gasification installation as by product.Gasifying agent is being delivered under the situation of high-temperature gasification part and gas converter by single gasifying agent feeder and through lateral, then can be implemented in the advantage of the equipment miniaturization and the aspect that reduces cost.
Except the performance of research carbonization-gasification installation, when when carrying out work derived from the wood-based living beings and derived from the gaseous fuel of refuse based biomass (as municipal solid waste or waste plastics), we also concentrate on attention and utilize gas engine, gas turbine and fuel cell effectively to produce electric power, and concentrate on the used heat that effective utilization is emitted when this kind equipment of operation.
With regard to biomass power generation, according to the inventive system comprises: generator set, it is operated by gaseous fuel, and discharges used heat in its operation; Carbonizer, it is used to accept living beings, and accepts the used heat by generator set release, and utilizes used heat to come pyrolysis and carbonization living beings and generation carbon and the cracking gas that contains the tar that volatilizees.This electricity generating device also comprises vaporizer, and it is preferably aforesaid two-stage vaporizer.This vaporizer is accepted carbon and the cracking gas from described carbonizer.In this vaporizer, the burning and the gasification of carbon take place, and transform the cracking gas that contains tar, so that vaporizer produces gaseous fuel thus, generator set is operated with this gaseous fuel.
This electricity generating device preferably includes heat exchanger, its part heat that is configured to the gaseous fuel that will be produced by vaporizer is delivered to the used heat that is discharged by generator set, so that the heat that is used for the carbonization living beings in carbonizer not only comprises from the used heat of generator set but also comprises coming the heat of the gaseous fuel that free vaporizer produces.
In this biomass fermentation electric installation, but carbonizer also preferably includes the carbonization chamber of a plurality of alternately operations.That is to say that a carbonization chamber operation very first time, carbon was sent to vaporizer from the second carbonization chamber simultaneously at interval to realize the conveying of carbonization and cracking gas.After this, second Room living beings of recharging, and the function of carbonization chamber can be exchanged.That is to say that carbonization and cracking gas produce and occur in the second carbonization chamber, send into carbon from first Room simultaneously.Alternately is operated three or more carbonizers in a similar manner.In addition, in this electricity generating device, from the preferably fusing and change into slag in vaporizer of the ash content of volatilization tar.
With biomass fermentation electric installation according to the present invention, by in conjunction with utilizing the carbonation process and the gasification of generator used heat, can realize efficient power generation and do not use auxiliary fuel.
Also preferably use aforesaid reinforced gasifying method of two steps according to electricity generating device of the present invention.
The used heat that is sent by generator set is preferably maintained in the range of from about in 600 ℃ to 700 ℃ the higher temperature scope, and is delivered to the carbonization chamber directly or indirectly.This heat is effective to the pyrolysis of living beings and carbonization and does not use postcombustion.Therefore, the overall thermal efficiency of device is higher, and this is because different with traditional device, do not need postcombustion, and this device is preferable aspect environmetal impact.
Not only install used heat and be utilized effectively, and biomass fuel is subjected to pyrolysis and stirring when by the carbonization chamber, thereby be converted to fine materials in the carbonization chamber.In addition, be maintained at about in 600 ℃ to 700 ℃ the temperature range if supply to the used heat of carbonization chamber, it sufficiently vaporizes the moisture of biomass fuel to produce carbonized fuel, and it contains small amount of moisture and calorific value is higher.In the temperature of carbonization chamber interior carbon is preferably maintained in the range of from about 500 ℃ to 600 ℃ scope, and produce the high-quality carbonized fuel.Yet,, but be difficult to realize the even efflorescence of biomass fuel even biomass fuel becomes aforesaid fine powder form.Therefore, though will present particle size distribution to a certain extent for the biomass fuel of fine powder form.Yet can realize the problem of enough efflorescence to avoid when gasifying, running into.Drying, fragmentation and carbonization are carried out in the carbonization chamber of device, therefore do not need independent disintegrator.
In vaporizer, available from the burning of the high quality carbon of carbonization chamber and gasification meeting temperature in the oven of vaporizer is brought up at least the same high temperature of decomposition temperature with tar, thereby avoid tar to adhere to the problem of pipeline, and then the tar that need not to clean or add is removed equipment.In addition, when temperature in the oven of vaporizer remains on like this when high-level, also avoid producing dioxin (dioxin ， bioxin).In addition, because need not to utilize steam activation and oxygen to decompose tar, thus avoided reducing as the gas heating value of generator set fuel, thereby can strengthen overall apparatus efficient.
Because the high temperature of vaporizer, thereby might melt ash content, convert it into the slag form, and the almost not danger of wash-out heavy metal before discharging.Thereby, the refuse based biomass can be used as fuel, and need not scorification ash content in independent device.Therefore, utilize the present invention, the wood-based living beings of mixing with the refuse based biomass can be used as fuel, and the collection of an amount of biomass fuel becomes and seldom is not subject to the influence of season and climatic change.Thereby can significantly reduce the needed expense of biomass collection fuel, time and effort.Compare with utilizing the wood-based living beings separately, it has higher compiling costs usually, certainly when utilizing the refuse based biomass, as municipal solid waste, waste plastics and analog, other advantages is economically arranged.Owing to use the refuse based biomass except that the wood-based living beings, so can stablize output power, except that the above-mentioned fact, the present invention is the scale of feasible easier expansion power station also, thereby realizes the more high efficiency of generating.In addition, significant ecological dominance when being fused into slag, ash content is arranged.
Utilization is according to biomass fermentation electric installation of the present invention, by non-existent equipment before utilizing, can realize the efficient improved and save the space, wherein before non-existent equipment be a kind of vaporizer, its simultaneously vaporized carbon, decompose tar and ash content be fused into slag.The present invention also has following advantage: handle wood-based living beings and refuse based biomass and no matter its reducibleness make to need not comminution of fuel in independent disintegrator.Therefore, can with the overall dimensions of electricity generating device with and overall cost remain on reduced levels.
Utilization no longer needs to worry the harmful constituent of wash-out ash content according to biomass fermentation electric installation of the present invention, and no longer needs to prevent the counter measure of wash-out danger.Contain at waste, for example, 5% or the situation of more ash contents under, ash content must be changed into the environmetal impact of slag to avoid being harmful to.In biomass fermentation electric installation according to the present invention, can easily ash content be changed into slag.In order to produce high temperature condition, do not need to use and contain, for example, the China fir sheet or the analog of about 1% ash content.Utilize the present invention, can discharge the ash content of relatively small amount and the gas of generation with the form of flying dust from the outlet of vaporizer, and ash content can be stopped in the gas purifier that is installed in vaporizer section downstream.Utilization is according to biomass fermentation electric installation of the present invention, can melt the operation of ash content therein and not melt between the operation of ash content to select, and it depends on the dust burdening of biomass fuel, even use identical oven in both cases.
Utilize the biomass fermentation electric installation, can also retrieve the heat of autopneumatolysis gas that device produces and, be used for the operation of carbonization chamber from the used heat of generator set.Therefore, the carbonization chamber can at high temperature be operated, and has high thermal efficiency.
By using a plurality of carbonizations chamber and alternately to operate on it, just can improve operation so that carbon and cracking gas are delivered to vaporizer continuously.
Description of drawings
Fig. 1 is the organigram according to biomass carbonization-gasification installation of the present invention;
Fig. 2 is a comparison calculated value and from the chart of oil emulsion gasification test result's test value (oxygen ratio is 0.40);
Fig. 3 is a plotted curve, and the prediction (input temp of gasifying agent: 50 ℃) that it shows the gasification performance of the moving vaporizer of oxygen blast type, single-stage, entrained flow shows the variation of carbon conversion efficiency and vaporizer outlet temperature when oxygen ratio changes;
Fig. 4 is a plotted curve, and the prediction (input temp of gasifying agent: 50 ℃) that it shows the gasification performance of oxygen blast type, single-stage, the moving vaporizer of entrained flow shows the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Fig. 5 is a plotted curve, and the prediction (air input temp: 250 ℃) that it shows the gasification performance of the moving vaporizer of air oxidation type, single-stage, entrained flow has shown the variation of carbon conversion efficiency and vaporizer outlet temperature when oxygen ratio changes;
Fig. 6 is a plotted curve, and the prediction of gasification performance that it shows oxygen blast, a step charging process has shown the variation of carbon conversion efficiency and vaporizer outlet temperature when oxygen ratio changes;
Fig. 7 is a plotted curve, and the prediction that it shows the gasification performance of one step of oxygen blast charging process has shown the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Fig. 8 is a plotted curve, and the prediction of gasification performance that it shows air oxidation, a step charging process has shown the variation of carbon conversion efficiency and vaporizer outlet temperature when oxygen ratio changes;
Fig. 9 is a plotted curve, and the prediction that it shows the gasification performance of air oxidation, a step charging process has shown the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Figure 10 is a plotted curve, and the prediction that it shows the gasification performance of air oxidation, two step charging process has shown the variation of carbon conversion efficiency, burner outlet temperature and vaporizer outlet temperature when oxygen ratio changes;
Figure 11 is a plotted curve, and the prediction that it shows the gasification performance of air oxidation, two step charging process has shown the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Figure 12 is a plotted curve, it shows prediction (the burner oxygen ratio: 0.64), shown the variation of carbon conversion efficiency, burner outlet temperature and vaporizer outlet temperature when oxygen ratio changes of gasification performance that air adds the method for gas converter;
Figure 13 is a plotted curve, and it shows burner oxygen ratio (total oxygen ratio: 0.20) to the influence of gasification performance, shown the variation of carbon conversion efficiency, burner outlet temperature and vaporizer outlet temperature when oxygen ratio changes;
Figure 14 is a plotted curve, and it shows burner oxygen ratio (total oxygen ratio: 0.20) to the influence of gasification performance, shown the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Figure 15 is a plotted curve, and the prediction that it shows the gasification performance of the two step charging process that are used for waste has shown the variation of carbon conversion efficiency, burner outlet temperature and vaporizer outlet temperature when oxygen ratio changes;
Figure 16 is a plotted curve, and the prediction that it shows the gasification performance of the two step charging process that are used for waste has shown the gas ratio of generation when oxygen ratio changes and the variation of cold air efficiency;
Figure 17 is a rough schematic view, and it shows the structure according to the biomass fermentation electric installation of the specific embodiment of the invention; And
Figure 18 is the stereogram according to electricity generating device of the present invention, the wherein a plurality of carbonization chambers that can sequentially operate be set at single vaporizer around.
Embodiment
Specific embodiments of the invention shown in Figure 1 are the biomass carbonization-gasification installations that are used for pyrolysis biomass fuel 1, and this biofuel is as wood-based living beings, the refuse based biomass that comprises municipal solid waste and the mixture of this biolobic material.This biomass carbonization-gasification installation comprises: carbonization chamber 2 is used for acceptance and heating biomass fuel 1 to produce char-forming material 4; Two-stage vaporizer 7, by the high-temperature gasification part 8 that is used for vaporized carbon formed material 4 and the gas converter 9 that is used to transform flammable cracking gas 3 form; Char-forming material feeder 13 is used for char-forming material 4 is delivered to the high-temperature gasification part 8 of vaporizer 7; Cracking gas stream 12 is used for flammable cracking gas 3 is sent to the gas converter 9 of vaporizer 7; And gasifying agent feeder 14, be used for gasifying agent 5 is delivered to the high-temperature gasification part 8 of vaporizer and gas converter 9 is delivered in oxygenousization agent 6.
Cracking gas 3 contains the tar that volatilizees in the process that produces char-forming material 4.The tar of this volatilization will form tar deposits on pipeline, unless remain on more than the predetermined temperature in the temperature of vaporizer outlet 10.In normal running, gasifying agent 5 is to deliver to high-temperature gasification part 8 continuously.Yet, have only when the temperature in the outlet 10 of vaporizer 7 drop to predetermined temperature, maybe when existing temperature will drop to predetermined temperature dangerous, gasifying agent 6 just is sent to gas converter 9.
Biomass fuel 1 has higher water content and relatively poor reducibleness, and it makes that coarse biometric matter fuel is not suitable for handling with the moving vaporizer of entrained flow.Therefore, in specific embodiment shown in Figure 1, adopt carbonization-gasifying method, wherein in carbonization chamber 2 and be added into before the vaporizer 7, biomass fuel 1 is divided into volatility, flammable cracking gas 3 and char-forming material 4.Gas 3 comprises moisture and the volatile matter in the biomass fuel 1, and char-forming material 4 is mainly by fixed carbon and ash composition.
Carbonization chamber 2 comprises the inside that is used for pyrolysis biomass fuel 1,2a is surrounded by chuck, gas 11 is introduced into wherein under 600 ℃ temperature preferably approximately, be used for indirect heating biomass fuel 1 and carry out carbonization by evaporating its moisture, and under anoxia condition the pyrolysis organic substance, the inclusion of chamber 2 and outside air are isolated.As described later on, the carbonization treatment of biomass fuel can be carried out from the used heat of combustion gas motor, gas turbine, fuel cell or other electricity generating devices by being used to, and wherein other electricity generating devices are to utilize the gas that is produced by vaporizer to act as a fuel.Therefore, gas 11 can come the waste gas of self-generating device.
The moisture of living beings and flammable cracking gas 3 are discharged from the top of carbonization chamber continuously, and char-forming material 4 is then discharged from its bottom.Moisture and flammable cracking gas 3 are sent to gas converter 9 through cracking gas stream 12.Char-forming material 4 is sent to the high-temperature gasification part 8 of vaporizer 7 through char-forming material feeder 13.Char-forming material feeder 13 can be any suitable feeder, for example, and feeding screw.
Vaporizer 7 makes the char-forming material of sending into from carbonization chamber 24 and contains moisture and the flammable cracking gas of volatile matter 3 carries out gasification reaction, thereby produces CO (carbon monoxide) and H 2(hydrogen).
Gasifying agent feeder 14 can be selectively only delivered between the state of high-temperature gasification part 8 and the state that gasifying agent is delivered to high-temperature gasification part 8 and gas converter 9 at gasifying agent and is switched.Air or oxygen is to be admitted to by gasifying agent feeder 14, thereby makes combustion reaction occur in high-temperature gasification part 8 or occur in high-temperature gasification part 8 and gas converter 9.Gasifying agent feeder 14 can be by being used to be blown into the device of air and suitable pipeline is formed.
In Fig. 1, two gasifying agent feeders 14 are shown as parts separately for convenience's sake, and the gasifying agent that is sent to high-temperature gasification part 8 is represented with drawing reference numeral 5 and the gasifying agent that is sent to gas converter 9 is represented with drawing reference numeral 6.Yet gasifying agent feeder 14 can comprise that single feeder so that gasifying agent (air or oxygen) with lateral and valve can be from wherein it only is sent to the state-transition of high-temperature gasification part 8 to wherein it is sent to the state of high-temperature gasification part 8 and gas converter 9.Under the situation that single feeder and branch's feed pipe use together, then can reduce the overall dimensions of device and reduce its cost.
The biomass fuel 1 that is sent to carbonization chamber 2 at first in carbonization chamber 2 approximately, for example, carry out the sufficiently long time of indirect thermal under 600 ℃ of temperature to be carbonized.When carbonization biomass fuel 1, its moisture and volatile matter are discharged from the top of carbonization chamber 2 and are transferred to gas converter 9 through cracking gas stream 12.1 needed time of the pyrolysis biomass fuel kind that depends on raw material with and water content.For example, if temperature is adjusted to about 600 ℃, then just can finish carbonization with about 30 minutes to 1 hour usually.After gratifying carbonization, contain char-forming material 42 discharges of fixed carbon, ash content and relatively small amount volatile matter from the carbonization chamber.Therefore, the char-forming material in the carbonization chamber 4 is sent to vaporizer 7 with escaping gas through different devices.
Gasifying agent 5 is sent to high-temperature gasification part 8, and it is the bottom of vaporizer 7, utilizes char-forming material 4 to act as a fuel then and burns and gasify in gasification part.Because come the moisture of authigenic material to be removed and not moisture relatively at the char-forming material 4 in this stage, so can produce high-temperature gas, its temperature does not have 1500 ℃ or higher.In addition, in gas converter 9, it is the top of vaporizer 7, utilizes high-temperature gas as thermal source and be included in the tar of conveying in the cracking gas 3 of carbonization chamber 2 by decomposition and carry out gas reforming.If the flow rate of flammable cracking gas 3 (it is usually in about 400 ℃ to 600 ℃ temperature range) then may stand the quick decline of temperature greater than the flow rate of char-forming material 4 in the device in gas converter 9 from the gas of high-temperature gasification part 8.Gas temperature in converter 9 does not allow to drop to and is lower than 1100 ℃ temperature, and this temperature is the decomposition temperature of tar.Therefore, if temperature drops to 1100 ℃ or the urgent danger of determining to exist this temperature to descend by sensor apparatus or observation, the gasifying agent 6 that then contains air or oxygen is sent to gas converter 9, and part is flammable, and cracking gas 3 burns, thereby the temperature of high-temperature gas is brought up at least 1100 ℃ temperature, so that the decomposition of tar can take place.
Reaction in the vaporizer 7 can be with following simple chemical formulation.Comprise reaction in the combustion reaction of high-temperature gasification part 8 by following expression:
(1) CO+1/2O 2→ CO 2And
(2)H 2+1/2O 2→H 2O
And gasification reaction comprises the reaction by following expression:
(3) C+CO 2→ 2CO and
(4)C+H 2O→CO+H 2
After aforesaid reaction, CO, CO 2, H 2, H 2O, N 2, fixed carbon and ash content move on to gas converter 9 from high-temperature gasification part 8.After this, transfer reaction by following expression takes place in gas converter 9:
Figure G2009101502273D00151
The ash content that is produced by combustion reaction of carrying out in high-temperature gasification part 8 and gasification reaction is converted into slag, and its bottom from vaporizer 7 is removed.
Can carry out various changes and modifications to aforesaid device.For example, as will occurring thereafter, a plurality of carbonizations chamber can be operated in chronological order, so that char-forming material and flammable cracking gas are delivered to vaporizer continuously.In addition, in vaporizer, high-temperature gasification part and gas converter can be equipped in the chamber, and betwixt not obviously not separately.For example, single chamber can be used, maybe the single chamber that between two parts, has restriction (restriction) can be used.
In order to check the process of gasification wood-based and refuse based biomass (it can be called as " waste "), the present inventor has set up the computing technique of easy prediction gasification performance based on fuel performance and gasification reaction speed, and inspected the gasify process of various fuel and the target zone of operational condition, purpose is to obtain efficient and stable operation.
Utilization by electrical equipment center research association fund (hereinafter only being called " fund ") exploitation with coal gasifier and extra heavy oil vaporizer highi degree of accuracy numerical analysis technology as target, plenty of time is used to prepare to calculate the detailed results of dot matrix with the various performances of acquisition vaporizer 7, distribute or the like, and need several hrs to calculate a state as particle characteristic, gas performance, gas temperature.Therefore, based on as the performance of the fuel type of target with and gasification reaction speed, fund has been set up the computing technique that can predict various gasification performances easily, as carbon conversion efficiency, cold air efficiency, gas temperature or the like, so that can easily check gasification, optimum operation condition or the like.With regard to this computing technique, there are not to consider radiation, the particle characteristic from the furnace wall of vaporizer 7, shape of vaporizer 7 or the like, yet, can understand the degree that the reaction that fuel took place that adds vaporizer 7 after a period of time has been carried out based on gasification reaction speed and gas-phase reaction speed.
Computing technique as being set up hereinafter will briefly be described.Suppose that the fixed carbon of finding from the performance evaluation value is the purpose of coke as gasification reaction about adding the fuel of vaporizer 7, and result from and add the later pyrolysis of vaporizer 7 that volatile matter is changed into gas immediately.In addition, suppose H 2The moisture of O form is added into vaporizer 7 to participate in water gas reaction and transfer reaction.
Suppose that C, H and O as volatile matter add with gas form, cause the transfer equilibrium state (CO+H based on equilibrium constants (shifting equilibrium constants Ks) basically 2O=CO 2+ H 2), wherein equilibrium constants is shown in the formula of the Ks of being used for given below.Yet, if the ratio of C, H and O attempts to determine CO, CO in the based on fuel 2, H 2, and H 2The ratio of O can find that then in most of the cases O is not enough.Therefore, in the time can not reaching the transfer equilibrium state, O combines with C to form CO, in addition, when O is not enough with respect to C, then utilizes the O in the gasifying agent.Suppose that hydrogen is H 2
The heat content of determining respectively based on fuel and gasifying agent (air, oxygen) of initial temperature and when changing into CO the calorific value or the like of volatile matter.Constant voltage (Cpi) down the avergae specific heat of all gases calculated by the six rank polynoimal approximations that utilization is used for gas temperature, as following given.
The formula that is used for Ks is:
(6)Ks＝([CO 2]×[H 2])÷([CO]×[H 2O])
＝0.0265×exp(3956)÷(T+273)
Wherein T is ℃.
The multinomial of approximate Cpi is:
(7)Cpi＝Ai+BiT+CiT 2+DiT 3+EiT 4+FiT 5+GiT 6
In vaporizer 7, consider four kinds of gas-phase reactions representing by following formula, but do not consider to relate to the reaction of methane, sulphur and other trace components.
(8)CO+1/2O 2→CO 2
(9)H 2+1/2O 2→H 2O
(10)CO+H 2O→CO 2+H 2
(11)CO 2+H 2→CO+H 2O
The constant of reaction rate that following table 1 expression utilizes the calculating of corresponding gas-phase reaction to obtain
(" c.f. " refers to above-mentioned numbered chemical formula).
Table 1
Formula ??A ??b ??E(J/kmol)
??8 ??2.2×10 12 ??0 ??1.67×10 8
??9 ??0.68×10 16 ??-1 ??1.68×10 8
??10 ??2.75×10 9 ??0 ??8.38×10 7
??11 ??2.65×10 -2 ??0 ??3.96×10 3
About the gasification reaction of coke, consider three kinds of reactions by Chemical formula 13 to 15 expressions given below.For the gasification reaction velocity constant, the numerical value that has adopted the thermobalance that utilizes fund and PDTF (superhigh temperature pressurized fuel reaction test equipment) to record.For the coke gasification Rate Models, adopted as n rank reaction rate laws by 12 expressions of arrhenius equation formula, wherein consider the influence of temperature and pressure.Table 2 shows the numerical value of China fir bark, as the example of gasification reaction velocity constant.According to the research of being undertaken by fund up to now, known gasification reaction becomes speed limit at high-temperature area.Therefore, about CO as representing by Chemical formula 14 2Gasification reaction, compared the corresponding gasification reaction speed at low temperature and high-temperature area as shown in table 2, thereby adopted littler numerical value.In addition, according to the research of being undertaken by fund up to now, known as H by Chemical formula 15 expressions 2The gasification reaction of O compares CO 2Gasification reaction faster, and in this case, suppose the former than the latter fast 0.5 times.
(12)dx/dt＝A 0P i nexp(-E Ai/RT)
(13)CO+1/2O 2→CO 2
(14)C+CO 2→2CO
(15)C+H 2O→CO+H 2
Table 2
Formula ??A 0 ??n ??E A[J/kmol]
??13 ??3.53×10 6 ??0.68 ??1.30×10 8
14 (low-temperature regions) ??3.64×10 10 ??0.49 ??2.77×10 8
14 (high-temperature areas) ??4.95×10 6 ??0.745 ??1.78×10 8
Suppose that vaporizer 7 usefulness refractory materials make, and utilize relation between the Outlet Gas Temperature of vaporizer 7 to find ratio, and when study the ratio of having found thermal loss shown in the expression and hot input quantity when oven carries out the gasification test of oil emulsion and residual oil at the novel species class I liquid I fuel gasification of fund by the caused thermal loss in furnace wall that is emitted to vaporizer 7.When temperature is lower than 1370 ℃, used first representation of the gasification test that derives from oil emulsion, temperature and second representation of then having used the gasification test that derives from residual oil when being higher than 1370 ℃.The ratio of thermal loss is to determine according to the outlet temperature of vaporizer 7 and those representations, in addition, proofreaies and correct by the long-pending ratio with hot input quantity of the wall surface of considering vaporizer 7.Thereby, can consider the influence that enlarges vaporizer 7 in proportion.
When temperature is lower than 1370 ℃:
The ratio of thermal loss (%)=3.7666 * 10 -34* vaporizer outlet temperature (℃) 10.836When temperature is not less than 1370 ℃:
The ratio of thermal loss (%)=-2.97 * 10 -5* vaporizer outlet temperature (℃) 2+ 9.545 * 10 -2* vaporizer outlet temperature (℃)-71.35
In order to check the accuracy of computing technique, its gasification test result with the oil emulsion that is undertaken by fund compares.It is the comparison of test value and the calculated value after about 5 seconds of the retention time in oven under 0.40 the situation that Fig. 2 shows at oxygen ratio (λ), and the gasification reaction in test this moment is determined almost to be finished.For constant of reaction rate, the numerical value that has adopted the PDTF with fund to record.
In Fig. 2, about the various gasification performances of generation gas: calorific value (HHV: more higher calorific value), carbon conversion efficiency (CCE) and cold air efficiency (CGE), discover that test value is consistent each other basically with calculated value.Between the respective performances of all gases, find to have small difference.Yet, because and H 2In conjunction with the concentration of CO, it is a combustible constituent, the concentration with test value is consistent basically, so two kinds of numerical value of cold air efficiency are consistent each other basically.The chances are for this because the most of C of supposition in the volatile matter of fuel is converted into CO immediately after adding vaporizer 7, so that CO concentration is calculated at higher a little numerical value.
Prove, as mentioned above, CO is calculated at higher a little concentration numerical value, and other components are calculated at lower a little numerical value, but from the angle of prediction gasification performance, the carbon conversion efficiency and the cold air efficiency of expression gasification efficiency are within gratifying numerical value.
The computing technique of utilizing as having set up has been investigated the process of high-efficiency gasification as the China fir sheet of living beings example.In the survey, pay special attention to following some.
Gas temperature (under the situation of two-stage type vaporizer) in high-temperature gasification part (burner) 8 outlets ... consider from the heat resistance (not being higher than 2000 ℃) of burner wall and the angle of the molten ash of discharge (being not less than 1600 ℃)
Gas temperature in vaporizer 7 outlets ... the angle that produces (being not less than 1100 ℃) from tar is considered
Carbon conversion efficiency ... do not have the angle of recycling equipment to consider (be not less than 99.5%: cold air efficiency is not less than 75) from efficiently utilizing fuel
Table 3 shows the characteristic of the China fir sheet that is used to investigate.Because the dust burdening of China fir sheet belongs to trace (0.09%), thus the supposition ash content be as flying dust discharge in the downstream rather than vaporizer 7 in by scorification with dissolve and discharge afterwards.For the gasification reaction velocity constant, utilized the numerical value of China fir bark as shown in table 2.
Table 3
??C ??H ??O ??N ??S ??Cl Fixed carbon Ash content Water
??30.45 ??3.71 ??25.68 ??0.06 ??0.01 ??＜0.01 ??6.07 ??0.09 ??40
(the supposition fusing point of * ash content: 1600 ℃)
One step was carried current method secretly
At first, carry current method secretly, under the situation of oxygen blast and air oxidation type, investigated optimum operation condition respectively about utilizing one of simple structure to go on foot.Explored a kind of condition, the temperature in the vaporizer outlet under this condition is not less than 1100 ℃ with prevention formation tar, and sees that from the angle of high gasification efficiency carbon conversion efficiency is not less than 99.5%.This investigation is to carry out under the following conditions.
Pressure in vaporizer is barometric pressure, and the vaporizer capacity is 100t/d.
Retention time in vaporizer is about 5 seconds when almost finishing when the gasification reaction of test is determined.
One step of oxygen blast type is carried current method secretly
Fig. 3 and Fig. 4 show the investigation result about the oxygen blast type.Because the general concentration of sending into from the oxygen generation device of oxygen is 95%, so the oxygen concentration of supposition in gasifying agent is 95%, and 5% remainder is a nitrogen.The input temp of gasifying agent is 50 ℃.According to the result of calculation prediction, be feasible at the efficient operation that is not less than 99.5% above carbon conversion efficiency in 0.58 the oxygen ratio scope.Generally speaking, the fuel O content of living beings is higher, and consequently compare its calorific value with fossil fuel lower.Therefore, although calculate show be the oxygen blast type under surpassing 0.58 high oxygen ratio, operate remain needs to be used in the sufficiently high temperature complete operation of maintenance in the vaporizer 7.In this case, be 58.9% as the cold air efficiency of another index of efficient operation, and the gas heating value that produces become low to about 1000kcal/m 3N.
One step of air oxidation type is carried current method secretly
Fig. 5 is illustrated under the situation of air oxidation type, the result of calculation of carbon conversion efficiency and vaporizer outlet port gas temperature.The air input temp is 250 ℃.Compare with the situation of oxygen blast type, carbon conversion efficiency and gas temperature all reduce when operating with identical oxygen ratio, and this is because the amount of nitrogen is increased to the about 70 times (percentages of nitrogen in gasifying agent: 5% → 79%) when operating with identical oxygen ratio.Therefore, discovery can not reach and surpass 99% carbon conversion efficiency, promptly uses 0.80 oxygen ratio.So, think that carrying current method secretly with a step is difficult to realize the air oxidation gasification.
Carbonization-gasification
A kind of process is investigated, wherein, before adding vaporizer 7, have the living beings of higher moisture in order to gasify, by the preprocessing process in carbonization chamber 2, fuel is broken down into mainly the volatile matter in char-forming material 4, the volatility cracking gas 3 that contains water and the fuel of being made up of fixed carbon.
Biomass fuel is sent to carbonization chamber 2, then 600 ℃ of sufficiently long times of carbonization.For carbonization, can be used to the high-temp waste gas of autopneumatolysis device 7 downstream processes.Discharge on moisture and the volatile matter top from carbonization chamber 2 between the carbon period, and after enough carbonizations, comprise char-forming material 42 discharges from the carbonization chamber of fixed carbon, ash content and a small amount of volatile matter.Thereby the char-forming material 4 in carbonization chamber 2 is sent to vaporizer 7 with cracking gas (escaping gas) 3 through different paths.Need to investigate and how to think the definite optimum operation condition of gasification to vaporizer 7 supply char-forming materials 4 and cracking gas 3.
When investigating optimum process, the boiling characteristics of having measured the China fir sheet is to determine what degree the volatile matter in the China fir sheet evaporate into.Thereby, determined at 600 ℃ following 92.6% volatile matter volatilized.Therefore, suppose that except that fixed carbon and ash content, char-forming material 4 contains 7.4% volatile matter.
One step charging process
At first, a step charging process is investigated, wherein separately char-forming material 4 and volatility cracking gas 3 only add high-temperature gasification part 8 in carbonization chamber 2.In this case, only the efficient of vaporizer is investigated, and got rid of carbonization chamber 2.As the situation of investigating the moving vaporizer of a step entrained flow, investigation is to carry out under the following conditions: the pressure in the vaporizer is barometric pressure, the vaporizer capacity is 100t/d, and the retention time in vaporizer was 5 seconds, and the oxygen concentration in the gasifying agent is 95%.Fig. 6 and Fig. 7 show result of calculation.
In this case, because biomass fuel 12 carries out pretreatment in the carbonization chamber, so input temp is brought up to 600 ℃, and the gas temperature in the vaporizer 7 is owing to lack latent heat (because moisture is sent into as steam) meeting raising, consequently compare on identical oxygen ratio basis and can improve gasification performance, as carbon conversion efficiency, cold air efficiency or the like with the moving vaporizer of one-level entrained flow.(with reference to Fig. 3 and Fig. 4).Find that according to calculating carbon conversion efficiency is not less than 99.5% in oxygen ratio surpasses 0.27 scope, and cold air efficiency is to surpass 85% high value at this moment.
Then, investigate with the air oxidation type.For the situation with the moving vaporizer of one-level entrained flow compares, the air input temp is 250 ℃.Fig. 8 and Fig. 9 show result of calculation.Picture is under the situation of oxygen blast type, compare with the moving vaporizer of one-level entrained flow, under identical oxygen ratio, the rising of gas temperature is attended by the raising of carbon conversion efficiency in the operation and cold air efficiency in vaporizer 7, thereby even also can make efficient operation become possibility with the air oxidation type.Result of calculation shows, is not less than at oxygen ratio under 0.43 the situation, and it is feasible that carbon conversion efficiency is not less than 99.5% efficient operation.Yet cold air efficiency is 67.8% in this case, and the gas heating value that produces becomes low about 840kcal/m of arriving 3N.
Two step charging process
Then, two step charging process are investigated, wherein, the char-forming material 4 that separates in carbonization chamber 2 is added into high-temperature gasification part 8, and volatility cracking gas 3 is added into gas converter (reductor) 7.Gasifying agent 5 only is added into high-temperature gasification part 8, so owing between char-forming material 4 and gasifying agent 5, react, form high temperature combustion zone in high-temperature gasification part 8, and the gas reforming reaction is carried out in gas converter 9 owing to add moisture and this transfer reaction of volatile matter of gas converter 9 mainly based on transfer reaction.Figure 10 and Figure 11 show result of calculation.Retention time in high-temperature gasification part 8 was adjusted to for 3 seconds, and the retention time in gas converter 9 was adjusted to for 1 second.In this case, because thinking, following reason is difficult to carry out the oxygen blast operation.At first, become high temperature combustion zone in the temperature high-temperature gasification part 8 that surpasses 3000 ℃.Secondly, with respect to 9 specific gas flow rate from high-temperature gasification part 8 to gas converter, the amount of the escaping gas of sending into from carbonization chamber 2 is bigger, thereby the quick decline of occurrence temperature in gas converter 9, thereby makes the level that the temperature of vaporizer outlet can not be remained at least 1100 ℃.Therefore, only the situation of air oxidation type is investigated.
Can expect that from Figure 10 and Figure 11 when operating with 0.14 ultralow oxygen ratio, it has been feasible that carbon conversion efficiency is not less than 99.5% efficient operation.At this moment, the oxygen ratio of high-temperature gasification part 8 is 0.56 separately.Yet the temperature of vaporizer outlet is about 900 ℃, will worry the formation of tar under this temperature.Simultaneously, be that the temperature of vaporizer outlet reaches 1100 ℃ under 0.20 the situation at oxygen ratio, and be 2200 ℃ in the temperature computation of high-temperature gasification part 8 outlets this moment, and therefore this is considered to inoperable oxygen ratio condition when considering the heat resistance of furnace wall.
Based on calculating, oxygen ratio is that the temperature expection in 8 outlets of high-temperature gasification part in 0.17 o'clock surpasses 2000 ℃, and at this moment, the temperature of vaporizer outlet is 1030 ℃, and it is lower than 1100 ℃, and this temperature is considered to the guide of stable operation.That be because, with respect to from high-temperature gasification part 8 about 2300m 3The specific gas flow rate of N/h, the flow rate of delivering to the escaping gas of gas converter 9 from carbonization chamber 2 is about 5400m 3N/h, it almost is equivalent to the former 2.5 times, so that is descended rapidly from the gas temperature (about 2000 ℃) of high-temperature gasification part 8.Therefore, when the temperature considered in the temperature of high-temperature gasification part 8 outlet and vaporizer 7 outlets, think to be difficult to realize in this way stable operation.
Air adds the method for gas converter (reductor)
Carry current method secretly with a step and compare, with two step charging process, under the situation of operating, can obtain higher carbon conversion efficiency, so that two step charging process are considered to effective method when requiring efficient operation with the low oxygen ratio with a step charging process.Therefore, a kind of method is investigated, wherein, air 6 is added into gas converter 9, and from the inflammable gas CO and the H of high-temperature gasification part 8 2Burn, thereby improve the gas temperature gas converter 9 in so that the temperature that improves the vaporizer outlet will remain in the temperature that high-temperature gasification part 8 exports simultaneously and not be higher than 2000 ℃ level to being not less than 1100 ℃.
Be higher than 2000 ℃ because must operate (the burner oxygen ratio is greater than 0.64) so that prevent that temperature in high-temperature gasification part 8 outlet from becoming with the oxygen ratio that is not more than 0.16, as shown in figure 10, so decision increases total oxygen ratio, the burner oxygen ratio is fixed on 0.64 simultaneously.Figure 12 shows the result of calculation of carbon conversion efficiency and gas temperature.
Result of calculation shows that the simultaneously total oxygen ratio of level that the temperature of vaporizer outlet can be brought up at least 1100 ℃ is not less than 0.20.When with as shown in Figure 6 and Figure 7 a step charging process relatively the time, obviously efficient operation is feasible under low oxygen ratio more.In this case, the cold air efficiency that can obtain 99.8% carbon conversion efficiency and surpass 85%.
The result is, a kind of method is suitable for the situation that the China fir sheet is used for carbonization-gasification, wherein, char-forming material 4 from carbonization chamber 2 is added into high-temperature gasification part 8, volatility cracking gas 3 is added into gas converter 9, the burner oxygen ratio is set lower so that make the thermal load of the furnace wall of high-temperature gasification part 8 lowly as far as possible, and in addition, air 6 is added into gas converter 9 so that vaporizer 7 outlet temperatures suitable temperature (being not less than 1100 ℃).
Then, in order to investigate the influence of burner oxygen ratio, be held constant under 0.20 the situation variation of having sought gasification performance at total oxygen ratio.Figure 13 and Figure 14 show the result of investigation.When not changing total oxygen ratio when reducing the burner oxygen ratio, observe: the vaporizer outlet temperature does not almost change, and burner outlet temperature and carbon conversion efficiency then have the tendency that becomes lower.When the thermal load considered the furnace wall, the burner oxygen ratio is preferably low as far as possible, and can expect according to Figure 13 and Figure 14, can obtain gasification performance with regard to carbon conversion efficiency, it is as the index of efficient operation and be not less than 99.5%, and the burner oxygen ratio is not less than 0.56 simultaneously.
Can expect from The above results, optimum operation condition when some conditions will be to use the China fir sheet, under these conditions, it is low as far as possible that gas temperature when the burner oxygen ratio is 0.56 in burner can become, promptly, oxygen ratio makes efficient operation become possibility, and total oxygen ratio is 0.20.
Investigation to the waste gasification method
The efficient waste gasification method of utilizing waste rather than China fir sheet to act as a fuel is investigated.Used waste is typical municipal solid waste, and its performance is shown in table 4.Because opposite, in waste, contain the ash content of a few percent, so in vaporizer 7, melt so that investigate under the situation of discharging as slag at the supposition ash content with the China fir sheet of investigating so far.Because can not get the survey data of ash content fusing point, so the supposition fusing point is 1600 ℃.
Table 4
Article content (%) ??C?????H????O?????N????S????Cl The ash content water content Fixed carbon
Wood chip 30.0 ??4.4???5.6??29.7??0.1??0.1??0.1 ??5.0???15.0 ??13.0
Waste paper 15.0 ??38.2??5.4??35.9??0.4??0.0??0.1 ??5.0???15.0 ??8.9
Useless fiber 15.0 ??40.2??5.8??30.7??3.1??0.1??0.1 ??5.0???15.0 ??21.2
Waste plastics 19.0 ??72.0??8.6??7.2???4.8??0.5??2.9 ??2.0???2.0 ??2.0
Useless PVC 1.0 ??30.7??3.8??0.0???0.0??0.0??45.5 ??12.0??8.0 ??9.9
Waste rubber 0.1 ??85.5??7.6??0.0???0.5??1.4??0.0 ??1.04??5.0 ??5.5
Rubbish 10.0 ??21.2??2.7??14.1??0.0??0.0??0.0 ??1.02??60.0 ??6.4
Mud 9.9 ??1.5???0.2??1.1???0.2??0.0??0.0 ??17.0??80.0 ??1.5
Amount to 100.0 ??41.4??5.3??21.8??1.5??0.1??1.1 ??5.4???23.4 ??9.8
* the supposition fusing point of ash content: 1600 ℃
As the result who utilizes the China fir sheet to investigate, determined to utilize carbonization-gasification that char-forming material 4 is added high-temperature gasification part 8 and volatility cracking gas 3 is added gas converter 9, efficient operation is feasible, therefore at first investigates the situation that air is only added high-temperature gasification part 8 as gasifying agent 5.Figure 15 and Figure 16 show result of calculation.Situation fuel throughput as the China fir sheet is adjusted to 100t/d.Yet, about the volatilization ratio in carbonization chamber 2, utilizing when at the measured value that Okadora Co., Ltd (MANUFACTURER of carbonizer) is actual to be obtained when carrying out carbonization, the part by weight of char-forming material 4 and cracking gas 3 is adjusted to 40: 60.
Compare with the situation of China fir sheet (with reference to Figure 10 and Figure 11), because the volatilization ratio descends in carbonization chamber 2, so the gas temperature of not observing in the gas converter 9 descends fast.In addition, increase because add the amount of the char-forming material 4 of high-temperature gasification part 8, so with respect to total oxygen ratio, the burner oxygen ratio becomes lower.Can determine according to aforementioned, do not form the ultra-high temperature zone in high-temperature gasification part 8, and there is a kind of oxygen ratio condition, the burner temperature is not higher than 2000 ℃ under this condition, and be not less than 1100 ℃ at the gas temperature of vaporizer outlet, be considered to be in the temperature in the stable operation scope.Based on calculating, estimate that carbon conversion efficiency is not less than 99.5%, simultaneously total oxygen ratio is not less than 0.32.In this case, obtaining cold air efficiency is to surpass 75% value, and this value is a desired value.
In addition, owing to be not less than at total oxygen ratio under 0.32 the situation, temperature in 8 outlets of high-temperature gasification part is not less than 1600 ℃, therefore can think, the ash content that contains in investigating used waste can be melted satisfactorily and discharge from the high-temperature gasification part 8 of vaporizer.
Conclusion
The gasification reaction speed of finding based on the PDTF of the performance of utilizing fuel, thermobalance and fund, set up the computing technique that is used for the gasification performance prediction, after investigating, obtain following result to the gasification that is applicable to the living beings that comprise China fir sheet (having 40% water content) and waste (typical municipal solid waste) and to efficient and steady operation conditions.
Under the situation of China fir sheet, carry current method secretly with air oxidation (air-blown) step and be difficult to carry out efficient operation, wherein fuel is directly to add vaporizer 7.Yet, along with employing carbonization-gasification, the cracking gas 3 that utilizes carbonization chamber 2 fuel to be broken down into char-forming material 4 and to contain water thus, and then add vaporizer 7 in two steps, thereby efficient and stable operation is feasible.
Utilize carbonization-gasification, under volatilization ratio condition with higher,,, air or oxygen 6 must be added gas converters 9 for the temperature with vaporizer 7 outlets remains on the temperature (1100 ℃) that is enough to stop tar formation as the China fir sheet.
Because waste contains many ash contents, therefore need to consider the fusing ash content to discharge as slag from point of view of environment protection.Because the low volatilization ratio in waste, by adopting the method that air is only added the high-temperature gasification part 8 of two-stage vaporizer, efficient and molten ash content discharging operation is feasible.
Figure 17 and Figure 18 show another aspect of the present invention, and its medium power produces authigenic material.The biomass fermentation electric installation comprises: carbonizer 15, and it not only can pyrolysis and carbonized wood based biomass and can pyrolysis and carbonization refuse based biomass, as municipal solid waste or the like; Vaporizer 16 is used for the carbon that burns and gasify and produce at carbonizer 15; And generator set 17, it can be used on the gas that produces in the vaporizer 16 and turns round as the energy, is used to produce electric power.Generator set is emitted used heat, and as will be seen, it is used for the operation of carbonizer.
Carbonizer 15 can be identical with the carbonizer 2 among Fig. 1, and it has the inner room that is used to accept living beings, and surrounded by being used to accept the chuck of hot gas as thermal source, with pyrolysis in inner room and carbonization living beings.The chuck of carbonizer 15 is connected in generator set 17 through waste gas feed path 18, be used for the waste gas that directly acceptance is emitted by generator set 17, so that device reaches the higher thermal efficiency by the heat that effectively utilizes waste gas.The chuck of carbonization chamber 15 is the shape of vertical annular barrel, and high temperature (for example 600 ℃) waste gas is introduced into chuck, to carry out carbonization by external heat.The cylindrical interior of carbonizer can be equipped with the rotor blade (not shown), and can push down the inwall of carbonization chamber by rotor blade fuel, thereby strengthens transmission of heat and improve carbonization efficient.Be applicable to that the carbonization chamber 15 of implementing this specific embodiment can be, for example, by the ultra high speed carbonizer of Okadora Co., Ltd manufacturing.Yet various forms of carbonizations chamber is fit to.For example, can use the tubular rotary kiln of external heat.
Utilization has the carbonization chamber 15 of said structure, can produce high quality carbon,, has seldom moisture but the higher carbonized fuel of calorific value that is.After release heat was given biomass fuel, waste gas was emitted by the cigarette fontanel.That is to say that the device used heat that carbonization chamber 15 process waste gas feed paths 18 are used to self power generation unit 17 is used for indirect pyrolysis biomass fuel as thermal source.Required time of pyrolysis is with changing as the kind of the living beings of raw material supplying and the water content in the living beings.Yet, in most of the cases, when using about 600 ℃ waste gas, can in about 30 minutes to 1 hour, finish carbonization.
Can be for carbonization provide a plurality of chambers, and alternately operation in chronological order, thereby continuously carbon and cracking gas are delivered to vaporizer 16.With regard to the amount of evaporation, must follow some variation at the carbonation process that carbonization is indoor.Yet,, can alleviate the influence of this variation if a plurality of unit alternately of carbonizer is operated.
Raw material storage tank 19 is connected in carbonizer, and the living beings that are used for acting as a fuel add carbonizer 15.The raw material of being made up of the wood-based living beings or can at first deliver to raw material storage tank 19 by the raw material that the mixture of wood-based living beings and refuse based biomass is formed sequentially supplies to the carbonization chamber of multicell carbonizer then.
Vaporizer 16 is a kind of oven, and this oven is used to burn and 15 carbon that produce in the carbonization chamber that gasify, and transforms the flammable cracking gas that contains tar that volatilizees between the carbon period, and the ash content in the fuel is changed into slag.This vaporizer can be used as single oven and is installed in the biomass fermentation electric installation.Yet under the situation of extensive biomass fermentation electric installation, for example, capacity surpasses for example factory of 50 megawatts, and a plurality of gasifier units can interconnect by gas turbine, and the number of unit and structure thereof depend on the pattern and the scale of device.
The amount that depends on calorific value and the amount and the input air of carbon in the temperature of vaporizer 16 outlets.For example, temperature in the oven bottom can reach the level up to 1500 ℃ in some cases, this is because be introduced into vaporizer with the calorific value of carbon with relative a large amount of air that amount adapts, because carbon and cracking gas are added into vaporizer 16 under at least about 600 ℃ temperature, because the moisture before entering vaporizer in the biomass fuel is transformed into steam under 600 ℃, and because high quality carbon (that is, calorific value higher and contain the seldom carbon of water) as fuel.Thereby, utilization is according to biomass fermentation electric installation of the present invention, wherein temperature reaches 1100 ℃ (they are the decomposition temperatures of tar) or is higher than this temperature in the oven of vaporizer 16, and the cracking gas that contains tar that has volatilized during carbonization in carbonization chamber 15 transforms on the top of vaporizer 16 (gas converter).Because the tar that is included in the cracking gas is to decompose under high temperature condition, wherein high temperature condition is to utilize the high hot of oven bottom (gasification/melt portions) to produce, so can avoid tar to adhere to pipeline or the like.Thereby, vaporizer 16 according to the present invention is realized high-temp combustion in the oven bottom, thereby the ash content in the fusing fuel, and utilize the heat that produces in its underpart to realize the conversion of cracking gas simultaneously on the top of oven, thus finish two kinds of functions with individual unit.Considering 1100 ℃ from the angle that stops tar to form reliably is preferred temperature, but even also can stop the formation of tar in the temperature that is lower than 1100 ℃.Yet, with utilization, for example, can not be at the fluidized bed furnace of this humidity province operation and fixedly the conventional apparatus of oven is opposite, biomass fermentation electric installation according to this specific embodiment has following characteristics: because the specified structure of vaporizer, temperature can reach 1100 ℃ or higher in the oven.
In addition, utilize vaporizer 16 because reach temperature in the higher oven, so not only can decompose the tar in the cracking gas, and even tar in ash content can at high temperature melt and change into slag.If the refuse based biomass mixes with the wood-based living beings to burn, this will cause ash content to contain heavy metal probably.Yet, if ash content can melt and change into slag, can discharge ash content under certain condition, wherein there are not the danger of wash-out heavy metal or so little danger consequently to need not to take the specific counter measure to stop the component of Xian's de-ash.
Tar-cracking gas feed path 20 and carbon feed path 21 are arranged between vaporizer 16 and the carbonization chamber 15.The former, that is, tar-cracking gas feed path 20 is streams that 15 tar that produce and cracking gas in the carbonization chamber are delivered to vaporizer 16, and the latter, that is, carbon feed path 21 is streams of the carbon of 15 generations in identical carbonization chamber being delivered to vaporizer 16.For example, with regard to this specific embodiment, utilize the carbon feed path 21 of screw conveyor for example to be connected in the bottom of carbonization chamber 15, thereby utilize carbon to act as a fuel to burn and gasify, so that especially the temperature in the oven bottom is elevated to higher temperature, so can produce and be not less than 1100 ℃ high-temperature gas or be not less than 1500 ℃ in some cases by air being delivered to the oven bottom.Simultaneously, carry out gas reforming on oven top, and utilize high-temperature gas as thermal source, the tar of part pyrolysis is decomposed on oven top in carbonizer 15.The gas that produces in vaporizer 16 is transported to generator set 17 as thermal source at the feed path 22 of the subsequent phase process gas that produces.
In this case, though the gas that produces can be delivered directly to generator set 17 through the feed path 22 of the gas that produces, preferably carry out heat exchange at the gas that produces with between from the waste gas of generator set 17.This can cause the waste gas from the heat transfer arrival self power generation unit 17 of generation gas, and the waste gas as thermal source of consequently delivering to carbonizer 15 can have higher temperature, thereby can obtain the higher thermal efficiency.For example, in being shown in the specific embodiment of Figure 17, the heat exchanger 23 of the gas that produces is installed by this way so that the feed path 22 that causes the gas that produces intersects near about mid point and waste gas feed path 18 or its.The gas that produces in vaporizer 16 loses its heat in heat exchanger 23, thereby be cooled, and after the dust in being included in gas, sulphur and other pollutants remove with gas purifier 24, be transported to generator set 17, wherein gas purifier is installed between heat exchanger 23 and the generator set 17.
Generator set 17 is to be used in the gas that produces in the vaporizer 16 to operate, and is used to produce electric power.It also is sent to carbonizer through waste gas feed path 18 with used heat.In this case, waste gas feed path 18 can be directly connected in carbonization chamber 15.Yet in illustrated specific embodiment, the heat exchanger 23 of the gas that produces is installed in along the mid point of waste gas feed path 18 so that the gas that can produce in vaporizer 16 and from carrying out heat exchange between the waste gas of generator set 17.Therefore, can retrieve self power generation unit 17 waste gas heat and from the heat of vaporizer 16 gas that produces and be used for carbonizer, thereby make whole device can reach the higher thermal efficiency.Can adopt other patterns, as exchanging the back utilizes used heat by steam medium pattern with waste gas heat.
In specific embodiment shown in Figure 180, a plurality of carbonizations chamber 25 is arranged on around the single vaporizer 26, it has high-temperature gasification part 27 and gas converter 28.These carbonization chamber alternately operations are to supply with vaporizer 26 continuously with carbon and cracking gas.That is to say that carbonization occurs in first carbonization chamber 25, and cracking gas delivered to from the first carbonization chamber gas converter 28 simultaneously carbon delivered to the high-temperature gasification part 27 of vaporizer from the second carbonization chamber.Thereafter, the second carbonization chamber living beings of recharging, and the function of exchanging the carbonization chamber, so that supply with carbon from first Room and carbonization occurs in second Room, and cracking gas is delivered to gas converter from second Room.Certainly, plural carbonization chamber can link with single vaporizer, and operates by the reasonable time order.
As indicated above, combine by carbonation process and gasification utilized device used heat, the biomass fermentation electric installation can be realized efficient power generation and not use postcombustion.We estimate, with biomass fermentation electric installation according to the present invention, can obtain 34% the thermal efficiency, it surpasses 30%, and 30% be the desired value (under the situation of 100t/d scale) of the thermal efficiency of " living beings Nippon (Japan) composite strategies ", as described below.More specifically, utilization is according to the biomass fermentation electric installation of the specific embodiment of Figure 17, by systematize carbonization chamber 15 and generator set 17, can effectively utilize the used heat of the waste gas of following generating, so can be than under traditional situation, obtaining the higher thermal efficiency and not only pyrolysis and carbonized wood based biomass but also pyrolysis and carbonization refuse based biomass, as municipal solid waste or the like, and do not use postcombustion.In other words, because the water content of wood-based living beings is higher than the refuse based biomass, so two kinds of living beings that are difficult to be in admixture change into the fuel with stability.Yet, under situation according to the biomass fermentation electric installation of this specific embodiment, utilization can effectively utilize used heat and be equipped in the carbonization chamber 15 of the leading portion of device, can be in carbonation process dryly be in two kinds of living beings (being heterogeneous body fuel in some sense) of admixture and change into fuel thereafter with stability, it contains given water content (for example, about 1%) also if necessary can efflorescence.In addition, opposite with the electricity generating device of present obtainable 1 mw scale, its based on, for example, the burning in its boiler, wherein generating efficiency approximately only is 10% at the most, utilization is according to biomass fermentation electric installation of the present invention, can obtain 30% or better generating efficiency.
" living beings Nippon composite strategies " is the strategy that promotes to utilize living beings, it is by Japanese agriculture, forestry and fishery portion, economy, trade and the Department of Industry, soil, basic facilities and Department of Transportation, Department of Environment, and the ministry of education arranges jointly, and determines in the cabinet council in December, 2002.On the date is in " the living beings Nippon composite strategies " on December 12nd, 2002, for example, at the 12nd page, a kind of description is arranged, to the effect that, relevant with the technology in the gentle chemical plant of direct burning or the like, be used for the living beings that water content is lower and change into energy, remain to be developed a kind of technology, can realize about 20% (at concerned power) in factory's (supposition is based on several urban districts scale) thus, or the energy conversion efficiency of about 80% (aspect heat), wherein the living beings throughput is approximately 20t/d, or can realize the energy conversion efficiency of about 30% (at concerned power) in factory's (supposition in the urban district), wherein the living beings throughput is approximately 100t/d, as long as set up the environment (energy conversion efficiency refers to that the chemical energy (calorific value) of biomass fuel changes into the ratio of electric power) that is suitable for biomass collection in extensive region here.Biomass fermentation electric installation according to this specific embodiment just in time utilizes the living beings unanimity with promoting, it is the purpose of " composite strategies ".
Biomass fermentation electric installation according to the present invention has several advantages than conventional electric generators group.First, because not only wood-based living beings but also refuse based biomass such as municipal solid waste, waste plastics or the like, can be used, so the wood-based biomass fuel that availability is influenced by seasonal variations can be replenished by the refuse based biomass, therefore can obtain stable output power.The second, comprise that the refuse based biomass of waste is handled with relative higher cost usually.Yet,, can improve the economic effect of wood-based biomass collection if such waste is collected as the part of the fuel that is used to generate electricity.The 3rd, by the feasible scale that can increase power generating equipment of increase that obtains fuel quantity provided by the invention, make efficient power generation become possibility.The 4th, because do not produce dioxin and become harmless,, and help environmental protection so electricity generating device can be used as the processing equipment of general refuse and industrial waste by changing into the slag ash content.The 5th, by the combination of carbonation process and gasification, the volume of coarse biometric matter is reduced to the about 1/5 to 1/7 of its initial volume, so that can use the compact type vaporizer.At last, this device can be operated by the workman who does not have technical skill.
The above is the preferred embodiments of the present invention only, is not limited to the present invention, and for a person skilled in the art, the present invention can have various changes and variation.Within the spirit and principles in the present invention all, any modification of being done, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.For example, with regard to above-mentioned specific embodiment, municipal solid waste, waste plastics or the like are the particular instances that is enumerated as the refuse based biomass.Yet, those materials are only enumerated by way of example, and under the situation of biomass fermentation electric installation according to the present invention, can use other biological matter, the living beings that comprise higher moisture, as the waste of agricultural resource, the forest resources, pastoral farming resource and aquatic resources, these resources, structural material refuse, food waste, mud or the like, and no matter it is wood-based living beings or refuse based biomass.

Claims (13)

1. biomass fermentation electric installation comprises:
Generator set, described generator set is operated by means of gaseous fuel, and discharges used heat in its operation;
Carbonizer is used to accept living beings, accepts the used heat that is discharged by described generator set and is used for described used heat and the described living beings of carbonization and the generation carbon of pyrolysis and contain the cracking gas of the tar that volatilizees; And
Vaporizer, described vaporizer are configured to accept described carbon and the described cracking gas that contains the tar that volatilizees from described carbonizer, are used to burn and the described carbon and transform the described cracking gas that contains tar of gasifying, thereby produce gaseous fuel;
Wherein, described generator set is to use the described gaseous fuel that forms by described vaporizer to operate.
2. biomass fermentation electric installation according to claim 1, wherein, under at least 1100 ℃ temperature, described vaporizer can decompose the described tar in described cracking gas, thereby transforms described cracking gas.
3. biomass fermentation electric installation according to claim 1, further comprise heat exchanger, the part heat that described heat exchanger is configured to the described gaseous fuel that will be produced by described vaporizer is delivered to the used heat that is discharged by described generator set, thereby the heat that is used for the described living beings of carbonization in described carbonizer not only comprises from the described used heat of described generator set but also comprises coming the heat of the gaseous fuel that free described vaporizer produces.
4. biomass fermentation electric installation according to claim 2, further comprise heat exchanger, the part heat that described heat exchanger is configured to the described gaseous fuel that will be produced by described vaporizer is delivered to the used heat that is discharged by described generator set, thereby the heat that is used for the described living beings of carbonization in described carbonizer not only comprises from the described used heat of described generator set but also comprises coming the heat of the gaseous fuel that free described vaporizer produces.
5. biomass fermentation electric installation according to claim 1, wherein, described carbonizer comprises a plurality of carbonizations chamber, it can the alternately blocked operation.
6. biomass fermentation electric installation according to claim 2, wherein, described carbonizer comprises a plurality of carbonizations chamber, it can the alternately blocked operation.
7. biomass fermentation electric installation according to claim 3, wherein, described carbonizer comprises a plurality of carbonizations chamber, it can the alternately blocked operation.
8. biomass fermentation electric installation according to claim 4, wherein, described carbonizer comprises a plurality of carbonizations chamber, it can the alternately blocked operation.
9. biomass fermentation electric installation according to claim 1, wherein:
Described vaporizer is the two-stage vaporizer, the high-temperature gasification part that comprises the described char-forming material that is used to gasify, and the gas converter that is used to transform flammable cracking gas, wherein said flammable cracking gas contains the tar that volatilizees when producing described char-forming material, and described gas converter has outlet;
And wherein said electricity generating device comprises:
Be used for to deliver to the device of the described high-temperature gasification part of described two-stage vaporizer at the char-forming material that described carbonizer produces;
The cracking gas stream, the described flammable cracking gas that is used for producing at described carbonizer is sent to the described gas converter of described vaporizer; And
The gasifying agent feeder is used for gasifying agent is delivered to the described high-temperature gasification part of described vaporizer, and controllably described gas converter is delivered in oxygenousization agent, thereby can prevent to drop to below the predetermined temperature in the outlet temperature of described vaporizer.
10. electricity-generating method may further comprise the steps:
The operate generator group also discharges used heat in the operation of described generator set;
Be used to described used heat from described generator set with pyrolysis in carbonizer and carbonization living beings, thereby produce carbon and contain the cracking gas of the tar that volatilizees;
In vaporizer, burn and the described carbon that gasifies, and transform described cracking gas, thereby produce gaseous fuel; And
Utilize the fuel of described gaseous fuel as the described generator set of operation.
11. electricity-generating method according to claim 10, wherein, in described vaporizer and at the described tar that volatilized that transforms under at least 1100 ℃ the temperature in described cracking gas.
12. electricity-generating method according to claim 10 wherein, is melted and changes into slag from the ash content of the described tar that volatilized in described vaporizer.
13. electricity-generating method according to claim 10, wherein, described carbonizer comprises a plurality of carbonizations chamber, and wherein said carbonization chamber is that alternately is operated.
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Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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