CN106701197A - Tar removal structure of biomass gasifying furnace and application method of tar removal structure - Google Patents
Tar removal structure of biomass gasifying furnace and application method of tar removal structure Download PDFInfo
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- CN106701197A CN106701197A CN201611223180.5A CN201611223180A CN106701197A CN 106701197 A CN106701197 A CN 106701197A CN 201611223180 A CN201611223180 A CN 201611223180A CN 106701197 A CN106701197 A CN 106701197A
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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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
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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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/04—Cyclic processes, e.g. alternate blast and run
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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
- C10J3/74—Construction of shells or jackets
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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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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
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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
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
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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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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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
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
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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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- 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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- Chemical & Material Sciences (AREA)
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- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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Abstract
The invention discloses a tar removal structure of a biomass gasifying furnace and an application method of the tar removal structure. The tar removal structure comprises a tar removal device of the gasifying furnace, a cyclone separator, an air preheater, a Roots blower, a drum dryer and a spiral feeder, wherein the cyclone separator is arranged at one side of the tar removal device of the gasifying furnace; the air preheater is connected with the cyclone separator; the Roots fan and the drum dryer are respectively connected with the air preheater; one end of the spiral feeder is connected with the drum dryer, and the other end of the spiral feeder is connected with the tar removal device of the gasifying furnace. The tar removal structure has the beneficial effect that tar produced by the biomass gasifying is cracked and removed in a high-efficiency, energy-saving and environment-friendly way.
Description
Technical field
The invention belongs to biomass energy utilization technologies field, more particularly to a kind of biomass gasifying furnace tar removing structure and its
Application process.
Background technology
As energy scarcity, environmental degradation problem are increasingly sharpened, national governments pay much attention to new cleaning fuel exploitation profit
With biomass clean reproducible green energy resource as one kind, with good development prospect.Biomass pyrogenation gasification is a kind of
High efficiency utilizes the technology of biomass resource, and it reduces greenhouse gas emission, development green low-carbon warp for improving energy resource structure
Ji important in inhibiting.In recent years, gasification technology obtained tremendous development, and each process route and equipment are developed and are applied to engineering
Among example, but biomass pyrogenation gasification reaction is a recombination process, is inevitably produced with tar therebetween, especially
It is gas outlet temperature updraft type fixed bed not high, tar content is particularly evident in thick combustion gas；Tar is gasification of biomass skill
One of focal issue that art field is present, tar in one side biomass gasification burning (is commonly considered as 200 temperature is relatively low
Below DEG C) when can be condensed into viscous liquid state, be easily attached on pipeline, valve and equipment wall surface, combine shape with water, ash etc.
Into blocking and corroding, the stable operation of downstream gas equipment, and the tar of discharge is influenceed to be also easy to cause environmental pollution；The opposing party
Face, macromolecular organic compound contained energy accounts for the thick combustion gas gross energy 5%-15% that gasifies in tar, if the portion of energy
Can not effectively be utilized, it will reduce gasification furnace gas producing efficiency.In gasification of biomass practical application, tar processing mode master
There are Physical and the class of thermochemical method two.Physical decoking oil tech is broadly divided into wet method decoking and dry method decoking, wet method decoking
It is main to have WATER-WASHING METHOD and water filter method, simple to operate, low cost, but can produce largely containing tar and waste water, easily cause secondary pollution；It is dry
Method decoking is main by the way of mechanical force and filtration, purification, is limited to tar viscosity greatly, and is mixed with ash content and small carbon granules, sinks
Product is more serious, and filtrate is difficult, and practical application effect is not good；Additionally, new electric tar method power consumption is big, operating cost
Height, and it is very high to the requirement of thick combustion gas Control for Oxygen Content, reliability is not high in case history.Thermochemical method decoking oil tech is main
There are pyrolysis method and catalystic pyrolysis, it is intended to by certain reaction condition, macromolecular tar conversion permanently may be used for small molecule
Combustion gas body, can effectively utilize tar energy while tar harm is eliminated；Temperature needed for pyrolysis method is general at 1100 DEG C
More than, tar conversion is higher, but so general more difficult acquisition of high-temperature, and appliance arrangement is difficult to bear.Catalystic pyrolysis are
By catalyst activity, the temperature requirement of cracking reaction can be substantially reduced, tar can just have higher typically at 750 DEG C -900 DEG C
Conversion ratio, therefore, catalytic pyrolysis decoking oil process is that a kind of exploitativeness is strong and effective method.Catalytic pyrolysis devokes oil process
In actual applications, independent cat cracker is generally set, and the temperature for needed for meeting reaction need in addition add thermal source, cost
It is higher.But gasification furnace internal reaction temperature is typically designed at 700 DEG C -900 DEG C, using this thermal source to gasifying contained by thick combustion gas
Tar carries out catalytic pyrolysis treatment and is entirely capable of meeting requirement.In existing similar techniques, exist relevant using in gasification furnace
Thermal source meets the report of catalytic cracking of tar reaction condition, and Chinese invention patent is entitled：A kind of band interior circulation tar catalysis is split
The biomass gasification device of solution, Application No.：201110398188.6, disclose catalytic pyrolysis tar removing in a kind of gasification furnace
Gasification installation, the invention is designed with thick combustion gas circulation line in gasification furnace, and catalyst layer is provided with pipeline, using stove
Endogenous pyrogen realizes that catalytic cracking of tar is processed；Chinese invention patent is entitled：A kind of gasification with tar catalytic cracking structure
Stove, Application No.：201110145364.5, a kind of gasification installation of catalytic pyrolysis tar removing in gasification furnace is equally also disclosed that,
The invention is provided with the cracker containing catalyst layer in gasification stove internal wall, and the cracker is cubic frame-shaped endless tube structure, cracker
There is partial denudation in heat exchange is strengthened in burner hearth to ensure cracker interior reaction temperature, corner is provided with and protrudes from urging outside body of heater
Agent filler is easy to add more catalyst changeout；
Both the above invention all refers to set catalyst layer come performing catalytic pyrolysis on tar in gasification furnace using the thermal source in stove；
But some problem demanding prompt solutions are still present：First, by material running space in stove limited and catalyst filling with
Changing needs, and the circulation line containing catalyst can not be designed to excessively complexity, causes circulation pipe heat exchange area not enough, tar catalysis
Temperature needed for cracking is difficult to ensure that；Secondly, narrow space in pipe, loaded catalyst is excessive, and to be easily caused fuel gas pipeline crushing excessive
Even block, loadings are too small and cannot meet the time of contact of tar and catalyst, or even the phenomenon that is short-circuited, influence decoking
Oily effect；Again, blowing out or switching pipeline, even influence the decoking process continuous fortune of gasification installation are needed during catalyst change
OK, particularly when loaded catalyst is less, Renewal process is particularly frequent；Further, current traditional gasification technology application example
In, uniflow gas stove gas outlet temperature is in less than 400-500 DEG C substantially, and design exists gasification reaction temperature mostly in stove
700-900 DEG C, because gas furnace inner circulating tube belongs to gas wall-type heat exchange, the inside and outside medium temperature of pipe needs 100-200 DEG C
The temperature difference, and at least more than 750 DEG C of catalytic cracking of tar reaction temperature, therefore, circulation pipe need enough heat exchange areas with
And heat-exchange time more long, it is obvious that both the above invention is all difficult to meet these requirements.In addition, when the temperature in stove occurs
During fluctuation, temperature difficulty is given and being guaranteed needed for catalytic cracking reaction.
The content of the invention
In view of the above problems, it is an object of the invention to provide a kind of efficient and energy-conserving and environment-protective catalytic pyrolysis removal biomass
The biomass gasifying furnace tar removing structure and its application process of the tar that gasification is produced.
To achieve the above object, a kind of biomass gasifying furnace tar removing structure that the present invention is provided, wherein, including gasification furnace
The air preheat of tar-removing device, the cyclone separator being provided with gasification furnace tar-removing device side and cyclone separator connection
Device, the Roots blower and drum dryer that are connected with air preheater respectively, and one end are connected with drum dryer, the other end
The feeding screw being connected with gasification furnace tar-removing device.Gasification furnace tar-removing device includes gasification furnace, is provided with gasification furnace
The material inlet that is connected with feeding screw, the slag notch being provided with gasification furnace bottom, the gasifying agent being provided with gasification furnace
Import, it is provided with gasification furnace the thick gas outlet connected with gasification furnace, the high-temperature fuel gas being provided with thick gas outlet pressurization
Machine, gasification furnace side be provided with connected with high-temperature fuel gas pressuring machine overfire air jet device, be provided with gasification furnace and be wound in
Gasification furnace part and be connected with overfire air jet spiral coil, on spiral coil be provided with what is connected with overfire air jet device
Catalyst charge device, and be provided with one end in catalyst charge device side and connected with cyclone separator, the other end is to catalyst
The bucket elevator of feed arrangement feeding.The flow channel cross-section of above-mentioned spiral coil is rectangle, and rectangle side long is heating surface.Gasification
The vaporizer that stove includes feeding warehouse, is provided with below feeding warehouse.Gasifying agent import is arranged on vaporizer.Thick gas outlet is set
In on feeding warehouse.Overfire air jet device include one end connected with high-temperature fuel gas pressuring machine thick combustion gas interface pipe, in thick combustion gas
The coconnected tubaeform mixing tube of the mouthpiece other end, the catalyst inlet being provided with tubaeform mixing tube, and in thick combustion gas
Mouthpiece is provided with from the thick combustion gas interface pipe of outside insertion and extends to the air intake nozzle in tubaeform mixing tube.Spiral coil
Helical disk is tightly arranged on vaporizer outer side surface.The coil inlet connected with tubaeform mixing tube is provided with spiral coil,
And the coil outlets connected with cyclone separator.Catalyst charge device is connected with catalyst inlet.Roots blower output
Air carries out heat exchange in air preheater；Described air preheater is connected with gasifying agent import and air intake nozzle respectively.
Thus, tightly in gasification chamber outer wall, condition is that spiral coil possesses sufficiently long heat exchange stroke to spiral coil helical disk, fully profit
Use vaporizer reaction heat, it is ensured that temperature conditionss needed for tar catalytic cracking reaction in spiral coil.
In some embodiments, air intake nozzle extends to the lower section of correspondence catalyst inlet.
In some embodiments, catalyst charge device includes catalyst material corresponding with bucket elevator feeding position
Struggle against and the feed pipe connected with catalyst inlet is provided with catalyst hooper, and the feeding valve being provided with feed pipe.
In some embodiments, discharge valve is provided between cyclone separator and bucket elevator.
In some embodiments, vaporizer is taper bin；Described material inlet is arranged on feeding warehouse；Described
Slag notch is arranged at vaporizer bottom.
Another invention is to provide a kind of application process of biomass gasifying furnace tar removing structure, wherein, it is specific as follows：
(1) biomass material is burnt from material inlet feeding gasification furnace；
(2) reacted in vaporizer with the gasifying agent being passed through, produced the thick combustion gas containing tar, gone out from thick combustion gas afterwards
Mouth discharge；Thick fuel gas temperature now is 400-500 DEG C；
(3) spiral coil is entered after being pressurized through high-temperature fuel gas pressuring machine；
(4) the air intake nozzle on thick combustion gas interface pipe is toward spraying into secondary hot-air in thick combustion gas interface pipe, and from catalyst
The catalyst of entrance feeding, and thick combustion gas is sufficiently mixed in tubaeform mixing tube；Thick combustion gas now is partially oxidized
Reaction, temperature is promoted to 500-600 DEG C；
(5) the thick combustion gas after heating up forms uniform gas-particle two-phase conveying bed with catalyst in the runner of spiral coil, i.e.,
Catalyst carries out catalytic cracking reaction with thick combustion gas with the principle of gas-particle two-phase conveying bed, and thick combustion gas is full and uniform with catalyst to be connect
Touch；
(6) in vaporizer interior reaction temperature at 800-900 DEG C, by vaporizer outer side surface to the thick combustion in spiral coil
Gas is heated again, and now thick fuel gas temperature is further promoted to more than 750 DEG C, can reach the temperature strip of catalytic cracking of tar
Part；Tar contained by thick combustion gas in hot environment with catalyst uniform contact, fully to form small molecule permanently flammable for cracking
Gas, thus removes the tar carried in thick combustion gas, increases combustion gas quality；
(7) combustion gas for completing catalytic pyrolysis tar removing process takes catalyst together into cyclone separator, realizes gas-solid point
From；
(8) combustion gas after purifying is transported to air preheater；Then catalyst is arranged by the discharge valve of cyclone separator bottom
Go out, after be transported to catalyst hooper through bucket elevator, then be transmitted back to spiral coil recycling, realize that catalyst is repeated
Utilize, it is ensured that automatic catalyst-feeding continuously runs.
(9) after the combustion gas after above-mentioned purification is discharged through cyclone separator, the air for first being exported with Roots blower is in air
Heat exchange is carried out in preheater, the hot-air from after air preheater output intensification is delivered to gasification agent inlet and/or enters respectively
Wind nozzle；Hot combustion gas after cooling enter drum dryer, and the material to vaporized stokehold is dried, further after cooling
Downstream is delivered in combustion gas；Set respectively and air preheater and air intake nozzle between above-mentioned air preheater and gasification agent inlet
It is equipped with regulating valve；
(10) last, dried material enters gasification furnace through feeding screw by material inlet；So circulation.
In some embodiments, catalyst can be various conventional powder catalysts；Described catalyst is particle diameter
The custom catalystses, solid such as the nickel-base catalyst, or particle diameter 0.5-2mm coke, dolomite or olivine of 20-30 mesh
It is granular or powdered.
In some embodiments, gasifying agent is hot-air.
The beneficial effects of the invention are as follows with the efficient tar produced with energy-conserving and environment-protective cracking removal gasification of biomass.Specifically
It is as follows：(1) will gasify and tar removing process conformity, the thermal source reacted as catalytic cracking of tar by the use of gasification reaction heat release, together
When be passed through appropriate Secondary Air, that is, thick combustion gas carries out oxidation reaction release heat with Secondary Air, is conducted heat through the furnace wall of vaporizer
With secondary oxidation double action, the temperature conditionss needed for common guarantee catalytic cracking of tar.Above-mentioned furnace wall heat transfer and secondary oxidation
Double action is reaction release heat to be carried out in vaporizer and by vaporizer furnace wall heat transfer by gasifying agent and material, is carried
Rise thick fuel gas temperature in spiral coil；By overfire air jet device to spraying into Secondary Air in tubaeform mixing tube, and with thick combustion
Gas carries out what the partial oxidation reaction release thick fuel gas temperature of heat lift reached, is so capable of achieving efficiently to be gone with energy-conserving and environment-protective cracking
Except the tar purpose that gasification of biomass is produced.(2) bed principle is conveyed using gas-particle two-phase, combustion gas is sufficiently mixed with catalyst,
Ensure that thick combustion gas mixes with the full and uniform of tar, while the continuous charging of catalyst can be realized again, it is ensured that gasification installation and Jiao
The continuous and steady operation of oily catalytic cracking reaction.So can further realize the tar that efficiently cracking removal gasification of biomass is produced
Purpose.(3) spiral coil structure is set by gasification chamber outer wall, increases heat exchange area, increase heat exchange stroke, improve helical disk
The heat exchange efficiency of pipe, also for catalytic cracking of tar provides the sufficiently long reaction time.So can further realize efficiently cracking
The tar purpose that removal gasification of biomass is produced.Therefore, the three big key elements for possessing needed for catalytic cracking of tar reaction：Reactant with
Being fully contacted of catalyst, react needed for high temperature, duration needed for reaction be satisfied, fully ensure that tar catalytic cracking
That reacts is smoothed out；In addition, holding catalyst activity has also been taken into account, catalyst continuous charging has been realized, and combustion gas is net
Change the problems such as being reclaimed with catalyst, from structural material to operating cost, then gasify to tar removing effect, simple operation, raising
Efficiency etc. is many-sided to be optimized improvement to gasification decoking process.
Brief description of the drawings
Fig. 1 is structural representation of the invention；
Fig. 2 is the structural representation of gasification furnace tar-removing device shown in Fig. 1；
Fig. 3 is the structural representation of overfire air jet device in the present invention；
Fig. 4 is the structural representation of spiral coil in the present invention.
Specific embodiment
Invention is described in further detail below in conjunction with the accompanying drawings.
As shown in Figure 1-2, a kind of biomass gasifying furnace tar removing structure, including gasification furnace tar-removing device 01, gasification
Cyclone separator 02 that the side of stove tar-removing device 01 is provided with and the air preheater 03 of the connection of cyclone separator 02, respectively with
The Roots blower 04 and drum dryer 05 of the connection of air preheater 03, and one end are connected with drum dryer 05, the other end
The feeding screw 06 being connected with gasification furnace tar-removing device 01.
As in Figure 2-4, gasification furnace tar-removing device 01 includes the gasification furnace 11 connected with cyclone separator 02, is gasifying
Stove 11 is provided with the material inlet 12 connected with feeding screw 06, the slag notch 13 being provided with the bottom of gasification furnace 11, in gas
Change gasifying agent import 14 that stove 11 is provided with, be provided with gasification furnace 11 connected with gasification furnace 11 thick gas outlet 15, thick
High-temperature fuel gas pressuring machine 16 that gas outlet 15 is provided with, it is provided with what is connected with high-temperature fuel gas pressuring machine 16 in the side of gasification furnace 11
Overfire air jet device 17, it is provided with gasification furnace 11 helical disk for being wound in the part of gasification furnace 11 and being connected with overfire air jet
Pipe 18, the catalyst charge device 19 connected with overfire air jet device 17 is provided with spiral coil 18, and entered in catalyst
Material device 19 side is provided with one end and is connected with cyclone separator 02, and the other end is carried to the bucket type of the feeding of catalyst charge device 19
Rise machine 10.The flow channel cross-section of above-mentioned spiral coil 18 is rectangle, and rectangle side long is heating surface.Gasification furnace 11 includes feeding warehouse
111st, the vaporizer 112 being provided with below feeding warehouse 111.Gasifying agent import 14 is arranged on vaporizer 112.Thick gas outlet 15
It is arranged on feeding warehouse 111.Overfire air jet device 17 includes the thick combustion gas interface that one end connects with high-temperature fuel gas pressuring machine 16
Pipe 171, it is provided with the thick coconnected tubaeform mixing tube 172 of the other end of combustion gas interface pipe 171, on tubaeform mixing tube 172
Catalyst inlet 173, and be provided with thick combustion gas interface pipe 171 from the thick combustion gas interface pipe 171 of outside insertion and extended to
Air intake nozzle 174 in tubaeform mixing tube 172.The helical disk of spiral coil 18 is tightly arranged on the outer side surface of vaporizer 112.Spiral shell
The coil inlet 181 connected with tubaeform mixing tube 172 is provided with capstan pipe 18, and the coil pipe connected with cyclone separator 02
Outlet 182.Catalyst charge device 19 is connected with catalyst inlet 173.The air of the output of Roots blower 04 is in air preheat
Heat exchange is carried out in device 03.Air preheater 03 is connected with gasifying agent import 14 and air intake nozzle 174 respectively.The spiral shell of spiral coil 18
Capstan is tight in the outer wall of vaporizer 112, and condition is that spiral coil 18 possesses sufficiently long heat exchange stroke, makes full use of vaporizer 112
Reaction heat, it is ensured that temperature conditionss needed for tar catalytic cracking reaction in spiral coil 18.Air intake nozzle 174 extends to correspondence catalysis
The lower section of agent entrance 173.Catalyst charge device 19 includes catalyst hooper 191 corresponding with the feeding position of bucket elevator 10
Be provided with the feed pipe 192 that is connected with catalyst inlet 173 on catalyst hooper 191, and feeding of being provided with feed pipe 192
Material valve 193.Discharge valve 07 is provided between cyclone separator 02 and bucket elevator 10.Vaporizer 112 is taper bin.Material
Import 12 is arranged on feeding warehouse 111, and slag notch 13 is arranged at the bottom of vaporizer 112.Drum dryer 05 is through feeding screw
06 connects with material inlet 12.
A kind of application process for the tar removing structure of biomass gasifying furnace 11, it is specific as follows：(1) by biomass material from
Burning in the feeding gasification furnace 11 of material inlet 12；(2) reacted in vaporizer 112 with the gasifying agent being passed through, produced containing Jiao
The thick combustion gas of oil, discharges from thick gas outlet 15 afterwards；Thick fuel gas temperature now is 400-500 DEG C；(3) add through high-temperature fuel gas
Press 16 enters spiral coil 18 after being pressurized；(4) the air intake nozzle 174 on thick combustion gas interface pipe 171 is toward thick combustion gas interface pipe
Secondary hot-air is sprayed into 171, is entered in tubaeform mixing tube 172 with the catalyst sent into from catalyst inlet 173, and thick combustion gas
Row is sufficiently mixed；Thick combustion gas now is partially oxidized reaction, and temperature is promoted to 500-600 DEG C；(5) heat up after thick combustion gas with
Catalyst forms uniform gas-particle two-phase in the runner of spiral coil 18 and conveys bed, i.e. catalyst with thick combustion gas with gas-particle two-phase
The principle for conveying bed carries out catalytic cracking reaction, and thick combustion gas is full and uniform with catalyst to be contacted；(6) reaction in vaporizer 112
Temperature is heated, now again by the outer side surface of vaporizer 112 at 800-900 DEG C to the thick combustion gas in spiral coil 18
Thick fuel gas temperature is further promoted to more than 750 DEG C, can reach the temperature conditionss of catalytic cracking of tar；Tar contained by thick combustion gas
With catalyst uniform contact in hot environment, fully cracking forms the permanent fuel gas of small molecule, thus removes thick combustion gas
The tar of middle carrying, increases combustion gas quality；(7) combustion gas for completing catalytic pyrolysis tar removing process takes catalyst together into whirlwind
Separator 02, realizes gas solid separation；(8) combustion gas after purifying is transported to air preheater 03；Then catalyst is by cyclonic separation
The discharge valve 07 of the bottom of device 02 is discharged, after be transported to catalyst hooper 191 through bucket elevator 10, then be transmitted back to spiral coil
18 recyclings, realize that catalyst is reused, it is ensured that automatic catalyst-feeding continuously runs.(9) combustion after above-mentioned purification
After gas is discharged through cyclone separator 02, first the air with the output of Roots blower 04 carries out heat exchange in air preheater 03,
Hot-air from after air preheater output intensification is delivered to gasification agent inlet and/or air intake nozzle respectively；Heat combustion after cooling
Gas enters drum dryer 05, and the material before vaporized stove 11 is dried, and downstream is delivered in the further combustion gas after cooling；On
It is respectively arranged with and air preheater 03 and air intake nozzle 174 between the air preheater 03 and gasification agent inlet 112 stated
Regulating valve.(10) last, dried material enters gasification furnace 11 through feeding screw 06 by material inlet 12；So circulation.
Catalyst can be various conventional powder catalysts.Catalyst is the nickel-base catalyst, or particle diameter of particle diameter 20-30 mesh
The custom catalystses such as 0.5-2mm coke, dolomite or olivine, solid granular or powdered.Gasifying agent is hot-air.
Using when, will gasification with tar removing process conformity, reacted as catalytic cracking of tar by the use of gasification reaction heat release
Thermal source, while being passed through appropriate Secondary Air, that is, is passed through the hot blast of gasifying agent import 14 and the hot blast of air intake nozzle 174, through gas
Change furnace wall heat transfer and the secondary oxidation double action, the temperature conditionss needed for common guarantee catalytic cracking of tar of room 112.Above-mentioned two
Secondary wind and secondary oxidation double action are that the air exported by Roots blower 04 carries out heat exchange in air preheater 03
Afterwards, supplied by air preheater 03, i.e., hot air circulation is utilized；The lifting of temperature is by vaporizer 112 in threaded coiler
Furnace wall heat transfer reaches.Bed principle is conveyed using gas-particle two-phase, combustion gas is sufficiently mixed with catalyst, it is ensured that thick combustion gas and Jiao
The full and uniform mixing of oil, while the continuous charging of catalyst can be realized again, it is ensured that gasification installation and catalytic cracking of tar react
Continuous and steady operation.By jacket structured in the outer wall of vaporizer 112 setting spiral, increase heat exchange area, increase heat exchange row
Journey, improves the heat exchange efficiency of spiral, also for catalytic cracking of tar provides the sufficiently long reaction time.So can further realize
The tar purpose that efficiently cracking removal gasification of biomass is produced.Therefore, the three big key elements for possessing needed for catalytic cracking of tar reaction：
Being fully contacted of reactant and catalyst, react needed for high temperature, reaction required duration, fully ensure that tar Catalytic Cracking Unit of Measure
That answers is smoothed out；In addition, holding catalyst activity has also been taken into account, catalyst continuous charging, and gas-purification has been realized
The problems such as being reclaimed with catalyst, from structural material to operating cost, then imitates to tar removing effect, simple operation, raising gasification
Rate etc. is many-sided to be optimized improvement to gasification decoking process.In addition, while tar problem is processed, to being taken in thick combustion gas
The small carbon granules of band has been also carried out treatment, can reduce the carbon residue of combustion gas carry-over, further improves gasification efficiency：Gasification furnace 11
Thick combustion gas typically can also carry part of ash and small carbon granules, and Normal practice is to carry out high-temperature dust removal in thick gas outlet 15,
Tar removing process is carried out again, and in the present invention, the small carbon granules in belongings first enters spiral coil with thick combustion gas and catalyst
18, gas solid separation then is realized in cyclone separator 02, the small carbon granules in belongings can also again be sent with catalyst
Enter spiral coil 18, temperature is higher in spiral coil 18, small carbon granules can repeatedly carry out high-temperature gasification reaction, favorably improve gas
Change efficiency, reduce the carbon residue of carry-over.
Above-described is only some embodiments of the present invention.For the person of ordinary skill of the art, not
On the premise of departing from the invention design, various modifications and improvements can be made, these belong to the protection domain of invention.
Claims (8)
1. a kind of biomass gasifying furnace tar removing structure, it is characterised in that including gasification furnace tar-removing device, in gasification furnace decoking
Cyclone separator that oily device side is provided with and the air preheater of cyclone separator connection, it is connected with air preheater respectively
Roots blower and drum dryer, and one end is connected with drum dryer, and the other end is connected with gasification furnace tar-removing device
Feeding screw；
Described gasification furnace tar-removing device is provided with the material connected with feeding screw including gasification furnace, on gasification furnace and enters
Mouthful, the slag notch that is provided with gasification furnace bottom, the gasifying agent import being provided with gasification furnace, be provided with and gasification on gasification furnace
Stove connection thick gas outlet, be provided with thick gas outlet high-temperature fuel gas pressuring machine, be provided with and high temperature in gasification furnace side
The overfire air jet device of gas booster machine connection, it is provided with gasification furnace and is wound in gasification furnace part and connect with overfire air jet
The spiral coil that connects, the catalyst charge device connected with overfire air jet device is provided with spiral coil, and in catalyst
Feed arrangement side is provided with one end and is connected with cyclone separator, bucket elevator of the other end to catalyst charge device feeding；
The vaporizer that described gasification furnace includes feeding warehouse, is provided with below feeding warehouse；Described gasifying agent import is arranged at gas
Change on room；Described thick gas outlet is arranged on feeding warehouse；
Described overfire air jet device include one end connected with high-temperature fuel gas pressuring machine thick combustion gas interface pipe, connect in thick combustion gas
The coconnected tubaeform mixing tube of the mouth pipe other end, the catalyst inlet being provided with tubaeform mixing tube, and connect in thick combustion gas
Mouth pipe is provided with from the thick combustion gas interface pipe of outside insertion and extends to the air intake nozzle in tubaeform mixing tube；
Described spiral coil helical disk is tightly arranged on vaporizer outer side surface；It is provided with described spiral coil and loudspeaker
The coil inlet of shape mixing tube connection, and the coil outlets connected with cyclone separator；Described catalyst charge device with urge
Agent entrance is connected；
The air of described Roots blower output carries out heat exchange in air preheater；Described air preheater respectively with
Gasifying agent import is connected with air intake nozzle.
2. a kind of biomass gasifying furnace tar removing structure according to claim 1, it is characterised in that described air intake nozzle
Extend to the lower section of correspondence catalyst inlet.
3. a kind of biomass gasifying furnace tar removing structure according to claim 2, it is characterised in that described catalyst enters
Material device includes catalyst hooper corresponding with bucket elevator feeding position and is provided with to enter with catalyst on catalyst hooper
The feed pipe of mouth connection, and the feeding valve being provided with feed pipe.
4. a kind of biomass gasifying furnace tar removing structure according to claim 1, it is characterised in that described cyclonic separation
Discharge valve is provided between device bottom and bucket elevator.
5. a kind of biomass gasifying furnace tar removing structure according to claim 1, it is characterised in that described vaporizer is
Taper bin；Described material inlet is arranged on feeding warehouse；Described slag notch is arranged at vaporizer bottom.
6. a kind of application process of biomass gasifying furnace tar removing structure, it is characterised in that specific as follows：
(1) by biomass material from material inlet feeding gasification furnace；
(2) reacted in vaporizer with the gasifying agent being passed through, produced the thick combustion gas containing tar, arranged from thick gas outlet afterwards
Go out；Thick fuel gas temperature now is 400-500 DEG C；
(3) thick combustion gas interface pipe is entered after being pressurized through high-temperature fuel gas pressuring machine；
(4) the air intake nozzle on thick combustion gas interface pipe is toward spraying into secondary hot-air in thick combustion gas interface pipe, and from catalyst inlet
The catalyst of feeding, and thick combustion gas is sufficiently mixed in tubaeform mixing tube；Thick combustion gas now is partially oxidized reaction,
Temperature is promoted to 500-600 DEG C；
(5) the thick combustion gas after heating up forms uniform gas-particle two-phase conveying bed with catalyst in the runner of spiral coil；
(6) in vaporizer interior reaction temperature at 800-900 DEG C, the thick combustion gas in spiral coil is entered by vaporizer outer side surface
Row is heated again, and now thick fuel gas temperature is further promoted to more than 750 DEG C, can reach the temperature conditionss of catalytic cracking of tar；
Tar contained by thick combustion gas in hot environment with catalyst uniform contact, fully cracking forms the permanent combustible gas of small molecule
Body, thus removes the tar carried in thick combustion gas, increases combustion gas quality；
(7) combustion gas for completing catalytic pyrolysis tar removing process takes catalyst together into cyclone separator, realizes gas solid separation；
(8) combustion gas after purifying is transported to air preheater；Catalyst is discharged by the discharge valve of cyclone separator bottom, afterwards
Catalyst hooper is transported to through bucket elevator, spiral coil is entered back into and is recycled；
(9) after the combustion gas after above-mentioned purification is discharged through cyclone separator, the air for first being exported with Roots blower is in air preheat
Heat exchange is carried out in device, the hot-air from after air preheater output intensification is delivered to gasification agent inlet and/or air intake spray respectively
Mouth；Hot combustion gas after cooling enter drum dryer, and the material to vaporized stokehold is dried, further the combustion gas after cooling
Deliver to downstream gas equipment；Divide and air preheater and air intake nozzle between above-mentioned air preheater and gasification agent inlet
Regulating valve is not provided with it；
(10) last, dried material enters gasification furnace through feeding screw by material inlet；So circulation.
7. the application process of a kind of biomass gasifying furnace tar removing structure according to claim 6, it is characterised in that described
Catalyst can be various conventional powder catalysts；Described catalyst is the nickel-base catalyst of particle diameter 20-30 mesh.
8. the application process of a kind of biomass gasifying furnace tar removing structure according to claim 6, it is characterised in that described
Gasifying agent be hot-air.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111644053A (en) * | 2020-05-12 | 2020-09-11 | 江苏峰峰鸿运环保科技发展有限公司 | Flue gas SCR denitration method and device |
| CN112662435A (en) * | 2020-12-17 | 2021-04-16 | 安徽香杨新能源科技发展股份有限公司 | Biomass gas production equipment and production process thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1603388A (en) * | 2004-09-03 | 2005-04-06 | 南京工业大学 | Process and apparatus for preparing coal gas by using bulky biomass materials |
| CN102676235A (en) * | 2012-05-14 | 2012-09-19 | 安徽喜阳阳新能源科技有限公司 | Downdraft tar secondary pyrolysis gasification device |
| CN203999500U (en) * | 2014-07-21 | 2014-12-10 | 武汉海德新能源投资有限公司 | The continuous overall pyrolysis oven of biomass |
| CN204455009U (en) * | 2015-02-16 | 2015-07-08 | 山东宝塔新能源有限公司 | With the cylinder Reaktionsofen of spiral tube boiler tube |
| CN105349184A (en) * | 2015-11-09 | 2016-02-24 | 浙江大学 | Compound furnace catalysis vaporization device and method |
-
2016
- 2016-12-27 CN CN201611223180.5A patent/CN106701197A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1603388A (en) * | 2004-09-03 | 2005-04-06 | 南京工业大学 | Process and apparatus for preparing coal gas by using bulky biomass materials |
| CN102676235A (en) * | 2012-05-14 | 2012-09-19 | 安徽喜阳阳新能源科技有限公司 | Downdraft tar secondary pyrolysis gasification device |
| CN203999500U (en) * | 2014-07-21 | 2014-12-10 | 武汉海德新能源投资有限公司 | The continuous overall pyrolysis oven of biomass |
| CN204455009U (en) * | 2015-02-16 | 2015-07-08 | 山东宝塔新能源有限公司 | With the cylinder Reaktionsofen of spiral tube boiler tube |
| CN105349184A (en) * | 2015-11-09 | 2016-02-24 | 浙江大学 | Compound furnace catalysis vaporization device and method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111644053A (en) * | 2020-05-12 | 2020-09-11 | 江苏峰峰鸿运环保科技发展有限公司 | Flue gas SCR denitration method and device |
| CN111644053B (en) * | 2020-05-12 | 2022-04-19 | 江苏峰峰鸿运环保科技发展有限公司 | Flue gas SCR denitration method and device |
| CN112662435A (en) * | 2020-12-17 | 2021-04-16 | 安徽香杨新能源科技发展股份有限公司 | Biomass gas production equipment and production process thereof |
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Application publication date: 20170524 |