CN105542858A - Low tar biomass gasification power generation system - Google Patents
Low tar biomass gasification power generation system Download PDFInfo
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- CN105542858A CN105542858A CN201510959730.9A CN201510959730A CN105542858A CN 105542858 A CN105542858 A CN 105542858A CN 201510959730 A CN201510959730 A CN 201510959730A CN 105542858 A CN105542858 A CN 105542858A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01D—NON-POSITIVE DISPLACEMENT MACHINES OR ENGINES, e.g. STEAM TURBINES
- F01D15/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
- F01D15/10—Adaptations for driving, or combinations with, electric generators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
- F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
- F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B43/00—Engines characterised by operating on gaseous fuels; Plants including such engines
- F02B43/10—Engines or plants characterised by use of other specific gases, e.g. acetylene, oxyhydrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B63/00—Adaptations of engines for driving pumps, hand-held tools or electric generators; Portable combinations of engines with engine-driven devices
- F02B63/04—Adaptations of engines for driving pumps, hand-held tools or electric generators; Portable combinations of engines with engine-driven devices for electric generators
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1606—Combustion processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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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
- 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
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/12—Improving ICE efficiencies
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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
- 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
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- Engine Equipment That Uses Special Cycles (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The present invention relates to a low tar biomass gasification power generation system, the system is additionally provided with a combustion section, and brings greater convenience to a gasification system furnace-starting process, a furnace of the gasification system is warmed directly by combustion heat of a small size fluidized bed system, the fuel oil consumption of the furnace-starting can be greatly saved, heat produced by fluidized bed combustion can be recovered by a steam water system, a small steam turbine is sued for power generation to achieve the conversion recovery of chemical energy in carbon residue, high-temperature gasification gas discharged out of the gasification furnace and high-temperature exhaust gas after power generation of an internal combustion engine both can be recovered by a heat exchanger, an organic Rankine cycle system is used for realization of recovery of flue gas and process waste heat, and the energy conversion efficiency of the gasification system is significantly improved.
Description
Technical field
The present invention relates to a kind of power generation system, particularly a kind of low-tar biomass gasifying power generation system.
Background technology
Gasification is a kind of common biomass energy conversion regime, has the features such as the strong and flexible operation of clean, efficient, fuel tolerance, has broad application prospects.In various biomass gasification technology, in down-draft type gasifying furnace aerogenesis, there is minimum tar content, be about 0.5g/Nm
3; And updraft type is maximum, 50g/Nm can be reached
3; Fluidized-bed gasification furnace is then moderate, probably at 8g/Nm
3.In three kinds of gasification technologies, fluidized-bed gasification is applicable to large-scale application, updraft type gasification has most high energy gamma source transformation efficiency, and although there is in existing downdraft gasification technology aerogenesis minimum tar content, but still there is the less stable of aerogenesis quality, the problems such as gasification scale is less than normal, energy utilization rate is on the low side.
Although tradition low-suction type organism-gasifying furnace tar content is low, but the transformation efficiency of coke is not high, and system scale is also difficult to amplify, integrated gasification efficiency only 15%, far below general with energy equipment or energy conversion devices, as coal-fired power plant's whole efficiency can reach 40%, the cogeneration (CHP) of Sweet natural gas even can reach more than 80%, and visible gasification transformation technology also has greater room for improvement on transformation efficiency.According to detection, inhale the carbon content accounting of coke in vapourizing furnace under two-part about 50%, this part Energy resources can not obtain Appropriate application, on the impact of gasification system efficiency significantly.
On the other hand, in down-draft type gasifying furnace, the reactive behavior of coke to tar is the key factor determining the coal-tar middle oil content of down-draft type gasifying furnace aerogenesis, although coke is remarkable to tar removal effect, but because layer of charcoal in a large number " coking deactivation " process occurs removing in tar process, want further and stable reduction gasification gas tar content, improve gasification efficiency, need to adopt other effective means more.
Summary of the invention
The present invention be directed to and adopt now low-suction type organism-gasifying furnace to carry out gasifying electricity generation Problems existing, propose a kind of low-tar biomass gasifying power generation system, make full use of the vital role that down-draft type gasifying furnace layer of charcoal plays in tar removes, vapourizing furnace is improved to tar removal efficiency by effectively improving coke gasification reaction activity in layer of charcoal, utilize chemical chain reaction principle and in conjunction with low-grade heat source application technology as the second resource, develop a kind of novel low-tar biomass gasifying power generation system.
Technical scheme of the present invention is: a kind of low-tar biomass gasifying power generation system, comprises twin-stage downdraft low tar vapourizing furnace, hopper, return grey auger, feeding packing auger, pyrolysis cylinder, aditus laryngis air jet, returns ash and is in charge of, circulation ash tube, heap dust stratification layer of charcoal, continuous dust dislodging rotary grate, ash discharge auger, circulating fluidized bed main body, fluidized bed air distribution plate, ash discharging hole, cyclonic separator;
Twin-stage downdraft low tar vapourizing furnace is by hopper charging, feeding funnel bottom part is connected with feeding packing auger is vertical, twin-stage gate valve in fill process in hopper is isolated charging and atmospheric environment, charging is pushed ahead through feeding packing auger conveying again, at pyrolysis cylinder entrance, the high temperature circulation flying dust that fresh bio material is carried with time grey auger directly contacts, form the direct heating to fresh bio material, pyrolytic process progressively completes along with moving ahead of feeding packing auger, the pyrolytic tar that pyrolysis produces and pyrolysis gas flow out via feeding packing auger upper opening place, enter vapourizing furnace burner hearth upper end, pyrolysis Jiao that pyrolysis produces then enters circulation ash tube under the further propelling movement of feeding packing auger, circulation ash tube adopt twin-stage gate valve with the use of, pyrolysis Jiao is sent into ash discharge auger together with flying dust, circulating fluidized bed main body is advanced to carry out circulating combustion pyrolysis Jiao and flying dust by ash discharge auger, air intake is entered by the air distribution plate of circulating fluidized bed bottom part body, chemical energy in coke discharges and forms new high catalytic activity biomass char simultaneously, part lime-ash is by ash discharging hole discharge on circulating fluidized bed bottom part body limit, the cyclonic separator that activated coke connects through circulating fluidized bed body top again reclaims, a part of being in charge of through time ash enters vapourizing furnace formation heap dust stratification layer of charcoal, by continuous dust dislodging rotary grate, the grey layer of charcoal dropped is sent into ash discharge auger, the pyrolysis being mixed into the outlet of circulation ash tube in the middle part of ash discharge auger is again burnt, finally send into circulating fluidized bed opening for feed by ash discharge auger, another part then sends pyrolysis cylinder back to by returning grey auger, form the circulation of ash content,
After pyrolysis gas generates in pyrolysis cylinder, overflow through pyrolysis cylinder upper end outlet, enter the upper end of vapourizing furnace, pass downwardly through gasification stove aditus further, the oxygenant sprayed with aditus laryngis air jet carries out partial oxidation reaction, forms localized high temperature regions, the cracking accelerating pyrolytic tar transforms, enter high catalytic activity heap dust stratification layer of charcoal again, polymerization tar product, after transforming through the selective catalysis of heap dust stratification layer of charcoal, finally forms low tar/to gasify gas product without tar.
Described system also comprises vapourizing furnace cyclonic separator, air preheater, fan, the first waste-heat recoverer, sack cleaner, tar and dust filter unit, gas-holder, oil engine, the second waste-heat recoverer;
Gasification gas goes out from vapourizing furnace, then by after cyclonic separator, air preheater and waste-heat recoverer, enters sack cleaner, again through filter, gas-holder, enter oil engine and generate electricity, in oil engine, high-temperature tail gas is again after waste-heat recoverer, discharge enters air, completes the circulation of gasification gas;
The preheated air of aditus laryngis sucks ambient air via fan, then enters air preheater, and after preheating, air sprays into vapourizing furnace body via aditus laryngis air jet again.
Described aditus laryngis air jet is a circle ring structure, enters air scoop and is two and is arranged symmetrically with, and internal structure contains inverted trapezoidal loop buffer air chamber composition.
Described system also comprises steam turbine decompressor, service pump, condenser, the amount of heat that circulating fluidized bed main body discharges is converted into steam through water wall, export promotion turbo-expander from circulating fluidized bed main body to do work, and providing circulation power by service pump, condenser provides low-temperature receiver, forms independent loops.
Described system also comprises organic rankine cycle system, organic working medium recycle pump provides circulation power for organic rankine cycle system, adopt the using and the reserved, organic working medium condenser cools for finishing the exhaust steam of merit organic working medium, container for storing liquid is entered to form phlegma, normal temperature organic working medium sends into two waste-heat recoverers serving as vaporizer respectively from container for storing liquid via organic working medium recycle pump, finally converge and enter ORC decompressor and do work, exhaust steam is liquid working substance by organic working medium condenser condenses, then is back to container for storing liquid formation circulation.
Beneficial effect of the present invention is: low-tar biomass gasifying power generation system of the present invention, system adds combustion parts, also comparatively convenience is brought in gasification system furnace lifting process, directly can carry out radiator by the small-sized fluidized bed system combustion heat to gasification system, the consumption of fuel oil during furnace lifting can be saved in a large number; The heat that small-sized fluidized bed burning produces is reclaimed by boiler circuit, and generated electricity by small steam turbine, realize chemical transformation of energy in carbon residue to reclaim, on the other hand, reclaim by all caning be passed through interchanger to the high-temperature exhaust air after going out the high-temperature gasification gas of vapourizing furnace and oil engine generating, adopt organic Rankine bottoming cycle (ORC) system to realize the recovery of flue gas and process waste, realize significantly improving of gasification system energy conversion rate.
Accompanying drawing explanation
Fig. 1 is low-tar biomass gasifying power generation system structure schematic diagram of the present invention.
Embodiment
Patent of the present invention introduces circulating fluidized bed, by by gasification bed in after tar catalyzed reaction the coke of institute's coking deactivation carry out combustive activation, the ash content of original inactivation can be activated, original coke fault offset is reclaimed simultaneously, and the ash content with katalysis effect is recycled, use the heat storage function of ash content, pyrolysis is carried out in biomass charging, this adopts isolated pyrolysis cylinder heat transfer pyrolysis than general, its heat transfer efficiency can improve 1 ~ 2 order of magnitude, and added by the carbon residue in a large number with catalytic activity, biomass material is made namely to achieve the catalytic modification to elementary pyrolytic tar at pyrolytic process, this is conducive to coal-tar middle oil the removing further of subsequent process.
Low-tar biomass gasifying power generation system structure schematic diagram as shown in Figure 1, primarily of twin-stage downdraft low tar vapourizing furnace 1, hopper 11, return grey auger 12, feeding packing auger 13, pyrolysis cylinder 131, aditus laryngis air jet 14, return ash and be in charge of 15, circulation ash tube 16, heap dust stratification layer of charcoal 17, ash disposal fire grate 18, ash discharge auger 19, circulating fluidized bed main body 2, fluidized bed air distribution plate 21, ash discharging hole 22, cyclonic separator 23, steam turbine decompressor 3, service pump 4, condenser 5, vapourizing furnace cyclonic separator 6, air preheater 7, gas blower 8, waste-heat recoverer 9, sack cleaner 10, tar and dust filter unit 110, container for storing liquid 120, organic working medium recycle pump 130, gas-holder 140, oil engine 150, organic working medium condenser 160, waste-heat recoverer 170, the structures such as ORC decompressor 180 and unit are formed.
Twin-stage downdraft low tar vapourizing furnace 1 is by hopper 11 charging, be connected with feeding packing auger 13 is vertical bottom hopper 11, twin-stage gate valve in fill process in hopper 11 is effectively isolated charging and atmospheric environment, push ahead through feeding packing auger 13 conveying again, at pyrolysis cylinder 131 entrance, the high temperature circulation flying dust that fresh bio material is carried with time grey auger 12 directly contacts, form the direct heating to fresh bio material, pyrolytic process progressively completes along with moving ahead of feeding packing auger 13, the pyrolytic tar that pyrolysis produces and pyrolysis gas flow out via feeding packing auger 13 upper opening place, enter vapourizing furnace 1 burner hearth upper end, pyrolysis Jiao that pyrolysis produces then enters circulation ash tube 16 under the further propelling movement of feeding packing auger 13, circulation ash tube 16 adopt twin-stage gate valve with the use of, pyrolysis Jiao is sent into ash discharge auger 19 together with flying dust, circulating fluidized bed main body 2 is advanced to carry out circulating combustion pyrolysis Jiao and flying dust by ash discharge auger 19, air intake is entered by the air distribution plate 21 bottom circulating fluidized bed main body 2, chemical energy in coke discharges, form new high catalytic activity biomass char simultaneously, part lime-ash is discharged by ash discharging hole 22 in circulating fluidized bed main body 2 bottom sides, the cyclonic separator 23 that activated coke connects through circulating fluidized bed main body 2 top again reclaims, a part is in charge of 15 through time ash and is entered vapourizing furnace 1 formation heap dust stratification layer of charcoal 17, another part then passes through back grey auger 12 and sends pyrolysis cylinder 131 back to, form the circulation of ash content.Continuous dust dislodging rotary grate 18 can realize continuous rotation ash disposal, ensure the relative constancy of grey layer height simultaneously, ash layer of charcoal 17 enters the opening for feed of ash discharge auger 19 by dropping after fire grate 18, and discharge ash content continuously by ash discharge auger 19, be mixed into pyrolysis Jiao that circulation ash tube 16 exports at middle part again, finally send into circulating fluidized bed 2 opening for feed by ash discharge auger 19.
For gas, after pyrolysis gas generates in pyrolysis cylinder 131, overflow through pyrolysis cylinder 131 upper end outlet, enter the upper end of vapourizing furnace 1, pass downwardly through gasification stove aditus further, the oxygenant (air/oxygen/water vapour etc.) sprayed with aditus laryngis air jet 14 carries out partial oxidation reaction, form localized high temperature regions, the cracking accelerating pyrolytic tar transforms, enter high catalytic activity heap dust stratification layer of charcoal 17 again, polymerization tar product is after transforming through the selective catalysis of heap dust stratification layer of charcoal 17, final formation low tar/without tar gasification gas product, gasification gas goes out from vapourizing furnace 1, again by cyclonic separator 6, after air preheater 7 and waste-heat recoverer 9, enter sack cleaner 10, again through filter 110, gas-holder 140, enter oil engine 150 to generate electricity, in oil engine 150, high-temperature tail gas is again after waste-heat recoverer 170, discharge enters air, complete the circulation of gasification gas.
In addition, the preheated air of aditus laryngis sucks ambient air via fan 8, enter air preheater 7 again, after preheating, air sprays into vapourizing furnace body 1 via aditus laryngis air jet 14 again, aditus laryngis air jet 14, spout 14 is a circle ring structure, enters air scoop and is two and is arranged symmetrically with, and internal structure contains inverted trapezoidal loop buffer air chamber composition.
In order to improve system energy utilization ratio, introduce circulating fluidized bed main body 2, the amount of heat that circulating fluidized bed main body 2 discharges is converted into steam through water wall, export promotion turbo-expander 3 from circulating fluidized bed main body 2 to do work, and provide circulation power by service pump 4, condenser 5 provides low-temperature receiver, forms independent loops.
Container for storing liquid 120, be made up of a stainless steel storage tank, organic working medium recycle pump 130 provides circulation power for organic rankine cycle system, usual employing the using and the reserved, organic working medium condenser 160 cools for finishing the exhaust steam of merit organic working medium, enter container for storing liquid 120, ORC decompressor 180 and select to form phlegma the screw expander that transformation efficiency is high, load adaptability is good.
Organic working medium circulation primary process is that normal temperature organic working medium sends into the waste-heat recoverer 9,170 serving as vaporizer respectively from container for storing liquid 120 via organic working medium recycle pump 130, finally converge and enter ORC decompressor 180 and do work, exhaust steam is liquid working substance by organic working medium condenser condenses, then is back to container for storing liquid 120 formation circulation.
In order to make full use of system smoke discharging residual heat, arrange air preheater 7 and waste-heat recoverer 9, waste-heat recoverer 170, and utilize organic working medium to realize Rankine cycle (ORC), can at least improve system energy transformation efficiency 10%, energy-saving effect is remarkable.
In addition, if gasification gas to be applied in the fields such as chemical industry synthesis (as F-T synthesis), then oil engine 150 can be replaced the modular constructions such as synthetic tower.
By the auger type feed pyrolysis cylinder 131 taking back grey waste heat pyrolysis, and pyrolysis cylinder is containing pyrolysis gas outlet upwards, realize pyrolysis Jiao to be separated with the effective of pyrolysis gas, and the aditus laryngis spout 14 of band buffer air chamber, heap dust stratification layer of charcoal 17 is in charge of 15 introducings via returning ash, there is high tar catalytic activity, greatly can improve the selectively removing efficiency to polymerization tar ingredients, final realization removing completely tar.
The chemical looping of biomass gasification tar removes circulation, heap dust stratification layer of charcoal 17 is formed by high reactivity charcoal Jiao being introduced, progressively inactivation will to be polymerized after tar product catalyzed conversion, circulating fluidized bed 2 is entered by ash disposal fire grate 18 and ash discharge auger 19, in circulating fluidized bed 2, carry out burning reactivate, namely realize removing tar by chemical chain reaction principle.
Pyrolysis cylinder 131 separates out mouth containing the pyrolysis gas of upward opening, and pyrolysis Jiao outlet of auger conveying, realizes effective separation of pyrolysis gas solid product.
Aditus laryngis air jet 14 uses the structure being with buffer air chamber to elegance, to guarantee the homogeneity of jet amount between different spout.
This low-tar biomass gasifying power generation system is the organic rankine cycle system (ORC) comprising flue gas heat recovery, can realize improving about 10% to system energy utilization ratio entirety.
The pyrolytic process of twin-stage downdraft low tar vapourizing furnace 1 is the process adopting the circulation charcoal of high reactivity, high heat capacity ash to realize biomass pyrolytic, has that heat transfer capacity is large, heat-transfer effect good, pyrolysis is abundant and tar eduction rate high.
Pyrolysis cyclical ash quantity regulates by regulating circulating fluidized bed circulation ratio, and pyrolysis ash is in charge of 15 to regulate by returning ash with the grey ratio of gasification.
Another of patent of the present invention and traditional gasification technology significantly distinguish and is biomass pyrolytic Jiao and can't help gasification stove aditus place to fall, and namely partial oxidation district is homogeneous reaction district completely, and this mainly considers some reason following:
1, aditus laryngis place temperature is higher, when cold and hot solution burnt (500 DEG C) is directly by aditus laryngis (1000 DEG C), causes aditus laryngis temperature to decline, is unfavorable for that tar transforms further;
2, the dropping process of a large amount of pyrolysis Jiao, has interference to the stationary flame that aditus laryngis is formed, and affects particularly evident when burning insufficient;
3, excessive temperature (>700 DEG C) can cause the burnt reactive behavior of pyrolysis to decline, and is also unfavorable for removing of tar;
4, directly adopt residual Jiao after combustive activation to carry out catalyzed conversion tar, greatly can improve the removal efficiency to tar;
5, homogeneous partial oxidation process can be formed higher temperature region, reaction is faster, tar conversion is more abundant;
6, pyrolysis is burnt has realized the two material balance with pyrolysis gas in pyrolysis cylinder, greatly weakens, need to carry out effective activation to the effect that removes of tar;
In addition, because system adds combustion parts, also bring comparatively convenience in gasification system furnace lifting process, directly can carry out radiator by the small-sized fluidized bed system combustion heat to gasification system, the consumption of fuel oil during furnace lifting can be saved in a large number.
The heat that small-sized fluidized bed burning produces is reclaimed by boiler circuit, and generated electricity by small steam turbine, realize chemical transformation of energy in carbon residue to reclaim, on the other hand, reclaim by all caning be passed through interchanger to the high-temperature exhaust air after going out the high-temperature gasification gas of vapourizing furnace and oil engine generating, adopt organic Rankine bottoming cycle (ORC) system to realize the recovery of flue gas and process waste, realize significantly improving of gasification system energy conversion rate.
Claims (5)
1. a low-tar biomass gasifying power generation system, it is characterized in that, comprise twin-stage downdraft low tar vapourizing furnace (1), hopper (11), return grey auger (12), feeding packing auger (13), pyrolysis cylinder (131), aditus laryngis air jet (14), return ash to be in charge of (15), circulation ash tube (16), heap dust stratification layer of charcoal (17), continuous dust dislodging rotary grate (18), ash discharge auger (19), circulating fluidized bed main body (2), fluidized bed air distribution plate (21), ash discharging hole (22), cyclonic separator (23);
Twin-stage downdraft low tar vapourizing furnace (1) is by hopper (11) charging, hopper (11) bottom is connected with feeding packing auger (13) is vertical, twin-stage gate valve in fill process in hopper (11) is isolated charging and atmospheric environment, charging is pushed ahead through feeding packing auger (13) conveying again, at pyrolysis cylinder (131) entrance, the high temperature circulation flying dust that fresh bio material is carried with time grey auger (12) directly contacts, form the direct heating to fresh bio material, pyrolytic process progressively completes along with moving ahead of feeding packing auger (13), the pyrolytic tar that pyrolysis produces and pyrolysis gas flow out via feeding packing auger (13) upper opening place, enter vapourizing furnace (1) burner hearth upper end, pyrolysis Jiao that pyrolysis produces then enters circulation ash tube (16) under the further propelling movement of feeding packing auger (13), circulation ash tube (16) adopt twin-stage gate valve with the use of, pyrolysis Jiao is sent into ash discharge auger (19) together with flying dust, circulating fluidized bed main body (2) is advanced to carry out circulating combustion pyrolysis Jiao and flying dust by ash discharge auger (19), air intake is entered by the air distribution plate (21) of circulating fluidized bed main body (2) bottom, chemical energy in coke discharges and forms new high catalytic activity biomass char simultaneously, part lime-ash is by ash discharging hole (22) discharge in circulating fluidized bed main body (2) bottom sides, the cyclonic separator (23) that activated coke connects through circulating fluidized bed main body (2) top again reclaims, a part is in charge of (15) through time ash and is entered vapourizing furnace (1) formation heap dust stratification layer of charcoal (17), by continuous dust dislodging rotary grate (18), the grey layer of charcoal dropped is sent into ash discharge auger (19), pyrolysis Jiao that circulation ash tube (16) exports is mixed into again at ash discharge auger (19) middle part, finally send into circulating fluidized bed (2) opening for feed by ash discharge auger (19), another part then passes through back grey auger (12) and sends pyrolysis cylinder (131) back to, form the circulation of ash content,
After pyrolysis gas generates in pyrolysis cylinder (131), overflow through pyrolysis cylinder (131) upper end outlet, enter the upper end of vapourizing furnace (1), pass downwardly through vapourizing furnace (1) aditus laryngis further, the oxygenant sprayed with aditus laryngis air jet (14) carries out partial oxidation reaction, form localized high temperature regions, the cracking accelerating pyrolytic tar transforms, enter high catalytic activity heap dust stratification layer of charcoal (17) again, polymerization tar product, after transforming through the selective catalysis of heap dust stratification layer of charcoal (17), finally forms low tar/to gasify gas product without tar.
2. low-tar biomass gasifying power generation system according to claim 1, it is characterized in that, described system also comprises vapourizing furnace cyclonic separator (6), air preheater (7), fan (8), first waste-heat recoverer (9), sack cleaner (10), tar and dust filter unit (110), gas-holder (140), oil engine (150), the second waste-heat recoverer (170);
Gasification gas goes out from vapourizing furnace (1), again by after cyclonic separator (6), air preheater (7) and waste-heat recoverer (9), enter sack cleaner (10), again through filter (110), gas-holder (140), enter oil engine (150) to generate electricity, in oil engine (150), high-temperature tail gas is again after waste-heat recoverer (170), and discharge enters air, completes the circulation of gasification gas;
The preheated air of aditus laryngis sucks ambient air via fan (8), then enters air preheater (7), and after preheating, air sprays into vapourizing furnace body (1) via aditus laryngis air jet (14) again.
3. low-tar biomass gasifying power generation system according to claim 2, it is characterized in that, described aditus laryngis air jet (14) is a circle ring structure, enter air scoop and be two and be arranged symmetrically with, and internal structure contains inverted trapezoidal loop buffer air chamber composition.
4. low-tar biomass gasifying power generation system according to claim 1 or 2, it is characterized in that, described system also comprises steam turbine decompressor (3), service pump (4), condenser (5), the amount of heat that circulating fluidized bed main body (2) discharges is converted into steam through water wall, export promotion turbo-expander (3) from circulating fluidized bed main body (2) to do work, and providing circulation power by service pump (4), condenser (5) provides low-temperature receiver, forms independent loops.
5. low-tar biomass gasifying power generation system according to claim 2, it is characterized in that, described system also comprises organic rankine cycle system, organic working medium recycle pump (130) provides circulation power for organic rankine cycle system, adopt the using and the reserved, organic working medium condenser (160) cools for finishing the exhaust steam of merit organic working medium, container for storing liquid (120) is entered to form phlegma, normal temperature organic working medium sends into two waste-heat recoverers (9 serving as vaporizer respectively from container for storing liquid (120) via organic working medium recycle pump (130), 170), finally converge and enter ORC decompressor (180) and do work, exhaust steam is condensed into liquid working substance by organic working medium condenser (160), be back to container for storing liquid (120) again and form circulation.
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