CN106221817A - The device and method of high heating value gas is prepared based on double-fluidized-bed biomass pyrolytic - Google Patents
The device and method of high heating value gas is prepared based on double-fluidized-bed biomass pyrolytic Download PDFInfo
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- CN106221817A CN106221817A CN201610648712.3A CN201610648712A CN106221817A CN 106221817 A CN106221817 A CN 106221817A CN 201610648712 A CN201610648712 A CN 201610648712A CN 106221817 A CN106221817 A CN 106221817A
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—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
- C10J3/72—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
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
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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
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a kind of device and method preparing high heating value gas based on double-fluidized-bed biomass pyrolytic, the top of reformation cyclone separator (1) is connected with bubbling fluidized bed (7) by reformation fluid bed (2), the bottom of bubbling fluidized bed is by the bottom Lian Liantong of the second U-shaped material returning device (11) with calcining fluid bed (12), the top of calcining fluid bed connects calcining cyclone separator (15), the bottom of calcining cyclone separator connects storage tank (14), the bottom of storage tank is provided with the 3rd U-shaped material returning device (13) and connects with the bottom of reformation fluid bed simultaneously；The bottom of reformation cyclone separator is connected with bubbling fluidized bed by the first U-shaped material returning device (4)；The bottom of hopper (3) connects screw feeder (5), the inner chamber of the output termination bubbling fluidized bed of screw feeder；This device prepares synthesis gas, can reduce tar yield and pipeline by tar stopping state, extension device service life, improves flow rate and gasification efficiency.
Description
Technical field
The present invention relates to a kind of device producing high heating value gas and preparation method thereof, it particularly relates to one based on
Double-fluidized-bed biomass pyrolytic device preparing high heating value gas and preparation method thereof.
Background technology
Currently, facing mankind economic growth and the dual-pressure of environmental conservation, change the production and consumption mode of the energy, use
Modern technologies develop regenerative resource including biomass energy, to setting up the energy resource system of sustainable development, promote
Socio-economic development and Improvement of Ecological Environment and break away from the dependence to fossil energy tool be of great significance.
One of important energy source that the biomass energy always mankind depend on for existence, including energy forest, energy crop, aquatic plants
Thing, various debirs etc., the Renewable Energy Resources that they are transformed by photosynthesis, is organic storage of solar energy
Depositing, biomass energy is most common a kind of regenerative resource, enormous amount on the earth, be only second to coal, oil, natural gas and arrange
The energy of the 4th.According to estimates, the annual water of the earth, the heat equivalent of terrestrial substance production are 3 × 1021About J, is that the whole world is the most total
10 times of energy consumption.China's biomass resource is the abundantest, and the stock number of the most all kinds of agricultural wastes (such as straw etc.) is every year
3.08 hundred million tons of standard coals, yule logs stock number is 1.3 hundred million tons of standard coals, adds feces, municipal refuse etc., and total resources is up to 6.5
Hundred million tons of standard coals.
Utilization for biomass energy at present has various ways, including biomass fuel burning technology, biomass gasification technology, life
Material pyrolysis technology, biomass Direct liquefaction technology, bio-fuel ethanol technology, biodiesel technology of preparing, biological hydrogen production skill
Art, biogas technology etc., wherein gasification of biomass is a kind of important biomass energy conversion regime.Biomass have volatile component and contain
Amount height, the characteristics such as content is low of carbon activity height, sulfur, nitrogen and ash, be the preferable gasified raw material of one.
After gasification of biomass refers to that biomass material is through processing, in gasification furnace, react gasification cracking with gasifying agent,
Obtaining fuel gas, purified treatment further to output gas obtains required product gas as required.Its principle is to be situated between in gasification
Under the effect of matter, biomass fermentation heat solution, aoxidize, reduce, reforming reaction, with the generation of tar in pyrolytic process, tar can
Thermal cracking or catalytic pyrolysis become little molecular carbon hydrogen compound further, thus obtain the combustible gases such as hydrogen, carbon monoxide, methane
Body.
The most domestic used biomass gasifying furnace is generally fixed-bed gasification furnace or fluidized-bed gasification furnace.But it is wherein solid
The application of fixed bed gasification furnace is less, because it has production capacity little, tar yield is big, and gasification efficiency is low waits shortcomings, and fluidizes
Bed gasification furnace becomes the first-selected type of furnace of gasification of biomass because its gasification efficiency is high, adaptability to raw material is wide, can large-scale industry
Change utilization and synthesis gas tar content is relatively low.
The subject matter that the biomass gasification device put into operation exists has structure complicated, and operating cost is high, gasification efficiency
Low, biomass undergoes adaptation is poor, but the problem of maximum is still that tar yield is big, and secondary pollution is serious.In order to make coke tar cracking,
Normal practice is to use two-step method, it is simply that biomass first pass through fluidized-bed gasification furnace gasification and generate pyrolysis gas, the most again by urging
Changing reformation and coke tar cracking makes product gas be converted into synthesis gas, being pyrolyzed and reforming is to carry out in the reactor of two series connection.
Summary of the invention
Technical problem: the technical problem to be solved is: provide a kind of based on double-fluidized-bed biomass pyrolytic system
The device and method of standby high heating value gas, utilizes this device to prepare high heating value gas, reduces the yield of tar simultaneously, reduces in bed
Line clogging situation, extension device service life, tar produces because of thermal cracking and catalytic pyrolysis simultaneously carbon monoxide and hydrogen
The calorific value of product coal gas can be improved, thus also improve the gasification efficiency of biomass.
Technical scheme: for solving above-mentioned technical problem, the present invention prepares high combustion value coal based on double-fluidized-bed biomass pyrolytic
The technical scheme that the device of gas uses is as follows:
The top of reformation cyclone separator is connected with bubbling fluidized bed by reformation fluid bed, and the bottom of bubbling fluidized bed leads to
Crossing the bottom Lian Liantong of the second U-shaped material returning device and calcining fluid bed, the top of calcining fluid bed connects calcining cyclone separator, forges
The bottom burning cyclone separator connects storage tank, the bottom of storage tank be provided with the 3rd U-shaped material returning device simultaneously with reformation fluid bed
Bottom connects；The bottom of reformation cyclone separator is connected with bubbling fluidized bed by the first U-shaped material returning device；The bottom of hopper connects spiral shell
Rotation dispenser, the inner chamber of the output termination bubbling fluidized bed of screw feeder；
The top of reformation cyclone separator is provided with syngas outlet and connects tar cracker, and the top of calcining cyclone separator sets
Having exhanst gas outlet to connect air preheater, the import input air of economizer bank in air preheater, outlet connects tar cracker；
The bottom of described bubbling fluidized bed is provided with steam entry and scum pipe, and the bottom of the second U-shaped material returning device is provided with the second deslagging
Pipe, the bottom of calcining fluid bed is provided with air intake and the 3rd scum pipe.
The described bottom in bubbling fluidized bed is provided with wind-cowl air distribution plate.
Pyrolysis of the present invention is prepared the method for high heating value gas and is included procedure below:
Putting into biomass material in hopper, biomass material is sent into the bubble flow being preinstalled with limestone by screw feeder
Changing in bed, meanwhile, the steam entry bottom bubbling fluidized bed is passed through steam, when bubbling fluidized bed is heated to 750
When 850 DEG C, biomass material is pyrolytic gasification in bubbling fluidized bed, generates pyrolysis gas and solid residue, comprises one in pyrolysis gas
Carbonoxide, hydrogen, carbon dioxide, methane and tar, solid residue comprises coke, and pyrolysis gas rises to, in reformation fluid bed, add
Thermal reforming fluid bed, makes the temperature of reformation fluid bed be maintained at 900 DEG C, and solid residue is deposited on the bottom of bubbling fluidized bed, Gu
Body residue and limestone are in the second U-shaped material returning device enters calcining fluid bed, and heating and calcining fluid bed, in making calcining fluid bed
Temperature is maintained at 950 DEG C, and the air intake to calcining fluid bed is passed through air, and the coke in solid residue and oxygen combustion are put
Going out substantial amounts of heat, making the Decomposition of Calcium Carbonate in limestone is solid particulate oxidation calcium and atmospheric carbon dioxide, in calcining fluidisation
The top of bed, calcium carbonate is completely decomposed into calcium oxide and carbon dioxide, forms gas-particle two-phase product, and this gas-particle two-phase product is through forging
After burning cyclone separator separation, flue gas enters air preheater preheating and enters the air of tar cracker, and calcium oxide passes through storing
Tank, returns to the bottom of reformation fluid bed through the 3rd U-shaped material returning device, and in reformation fluid bed, pyrolysis gas carries calcium oxide and rises,
Carbon dioxide in absorbent lime pyrolysis gas, forms calcium carbonate, promotes water gas shift reaction and methane reforming reaction, with
Time, calcium oxide, nickel oxide etc. are as the catalyst of coke tar cracking, and catalytic cracking of tar generates hydrogen and CO (carbon monoxide converter) gas, weight
Rectification height of bed temperature promotes tar to produce thermal cracking, and catalytic pyrolysis and thermal cracking promote tar yield to reduce, thus reduce pipeline
Stopping state, extension device maintenance period, improves production efficiency；Pyrolysis gas obtains reformation gas after reforming in reformation fluid bed,
Reformation gas is after reformation cyclone separator gas solid separation, and the isolated calcium carbonate of reformation cyclone separator is through the first U-shaped material returning device
Sending back in bubbling fluidized bed, it is achieved heat transfer medium circuit utilizes, discharging gas from the syngas outlet of reformation cyclone separator is
Synthesis gas, enters tar cracker and makes residu tar crack further by high temperature, finally give coal gas.
Reformation fluid bed is preheated by bubbling fluidized bed, and temperature reaches 900 degrees centigrade, makes internal tar produce height
Warm cracking, simultaneously because there is the compound such as calcium oxide, nickel oxide, catalytic tar generation catalytic cracking reaction, two kinds of cracking
Reaction promotes tar yield in bed to reduce, thus reduces pipeline by tar stopping state, and can produce volume after coke tar cracking
Outer heat.
The calcining isolated high-temperature flue gas of cyclone separator can be used for air preheater preheated air, reformation cyclone separator
Isolated synthesis gas is rich in gases such as the hydrogen of a large amount of high heating values, carbon monoxides, and tar cracker can further be removed
Tar, produces high heating value gas, and can be used for gas turbine, diesel power generation, heating, thus realizes thermoelectricity gas connection
Supply.
Beneficial effect: compared with prior art, present invention have the advantage that
(1) reduce the yield of tar, improve the calorific value of synthesis gas, improve gasification of biomass efficiency.In apparatus of the present invention,
In reformation fluid bed, tar, by thermophore granule calcium oxide and nickel oxide catalytic pyrolysis, decomposites hydrogen and carbon monoxide etc.
Fuel gas, is gone out hydrogen and carbon monoxide by high temperature pyrolysis simultaneously, promotes tar yield to reduce, thus reduce line clogging feelings
The fuel gas such as condition, extension device maintenance period, raising production efficiency, and hydrogen increase so that calorific value of gas improves, overall
Gasification efficiency improve.
(2) circular regeneration of thermophore catalyst is achieved.As a example by limestone thermophore, in calcining fluid bed, burnt
The heat of charcoal burning makes limestone main composition-calcium carbonate at high temperature be decomposed into CaO and CO2, CaO carries heat and enters weight
In rectification fluidized bed reactor, provide heat for reforming reaction.In the process, the CO during CaO absorbs pyrolysis gas2, promote water coal
Gas transformationreation CO+H2O=H2+CO2And methane reforming reaction, the tar that CaO makes pyrolysis produce as catalyst simultaneously is sent out rapidly
Raw catalytic pyrolysis, generates H2With micro-molecular gas such as CO, making the tar content in pyrolysis gas reduce, the yield of synthesis gas carries significantly
High.CaO is absorbing CO2After regenerate CaCO3, return in fluidized-bed gasification furnace, it is achieved that the circulation of thermophore catalyst
Utilize.
(3) staged conversion of biomass energy is achieved.In the present invention, biomass material first gasifies in pyrolysis fluid bed
Obtain pyrolysis gas, tar and coke.Coke enters burning in calcining fluid bed, and its converting heat is to thermophore, and thermophore is by this
Partial heat returns to reformation fluid bed, and reforming to coke tar cracking and pyrolysis gas provides institute's calorific requirement.It addition, coke enters calcining
In fluid bed, burning, improves dust removal efficiency, can obviously reduce the impurity such as dust in synthesis gas, charcoal granule.The pyrolysis that gasification generates
Gas is follow-up to be processed through reformation again, reduces the requirement to gasification.
(4) compared with the method for conventional biomass producing synthesis gas, the present invention facilitates implementation the integrated of heat.At this
In bright, coke calcining fluid bed in burn generate heat, pyrolysis gas will be supplied to by thermophore, for the reformation of pyrolysis gas
And wherein coke tar cracking reacts offer condition.This just makes intractable coke originally be fully used.
(5) thermoelectricity gas alliance is achieved.This device while utilizing biomass energy, output high heating value synthesis gas and
High-temperature flue gas, wherein the synthesis gas of high heating value can be used for gas turbine or diesel power generation, heating etc., and produces high heating value
Product coal gas, high-temperature flue gas can add hot steam, generates electricity for steam turbine, and preheated fluidification bed required air energy-conservation subtracts
Row.
(6) application of distributed energy resource system is achieved.It is many that this device is suitable for scene, is formed mutually with centralized energy resource system
Mend, help to solve dispersion and the energy supply problem of remote districts, bed wide material sources and mostly be and do not have actually used value
Garbage, reduce while environmental pollution and also mitigate energy shortage problem.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention.
Figure has: reformation cyclone separator 1, reformation fluid bed 2, hopper the 3, first U-shaped material returning device 4, screw feeder 5,
Wind-cowl air distribution plate 6, bubbling fluidized bed the 7, first scum pipe the 8, second scum pipe the 9, the 3rd scum pipe the 10, second U-shaped material returning device
11, the calcining U-shaped material returning device 13 of fluid bed the 12, the 3rd, storage tank 14, calcining cyclone separator 15, air preheater 16 and tar
Cracker 17.
Detailed description of the invention
Below in conjunction with the accompanying drawings, technical scheme is described in detail.
Embodiment one:
As it is shown in figure 1, a kind of device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic of the present invention, including
Reformation cyclone separator 1, reformation fluid bed 2, hopper the 3, first U-shaped material returning device 4, screw feeder 5, wind-cowl air distribution plate 6, drum
Bubble fluid bed the 7, first scum pipe the 8, second scum pipe the 9, the 3rd scum pipe the 10, second U-shaped material returning device 11, calcining fluid bed 12,
3rd U-shaped material returning device 13, storage tank 14, calcining cyclone separator 15, air preheater 16 and tar cracker 17.Bubbling fluidization
The bottom of bed 7 is provided with steam entry.The bottom of calcining fluid bed 12 is provided with air intake.The top of reformation cyclone separator 1
It is provided with syngas outlet.The top of calcining cyclone separator 15 is provided with exhanst gas outlet.The bottom of the first U-shaped material returning device 4 is provided with
One returning charge air intake.First returning charge air intake is passed through air, as feedback air, promotes the carrying out of returning charge process.2nd U
The bottom of type material returning device 11 is provided with the second returning charge air intake.Second returning charge air intake is passed through air, as feedback air, promotees
Enter the carrying out of returning charge process.The bottom of the 3rd U-shaped material returning device 13 is provided with the 3rd returning charge air intake.In 3rd returning charge air intake
It is passed through air, as feedback air, promotes the carrying out of returning charge process.The feed end phase of the discharging opening of hopper 3 and screw feeder 5
Even, the discharge end of screw feeder 5 is positioned at the inner chamber of bubbling fluidized bed 7, and the second U-shaped returning charge is passed through in the bottom of bubbling fluidized bed 7
Device 11 is connected with the bottom of calcining fluid bed 12, and the top of calcining fluid bed 12 is connected with the top of calcining cyclone separator 15
Logical, the bottom of calcining cyclone separator 15 is connected with the bottom of reformation fluid bed 2 by the 3rd U-shaped material returning device 13, reformate stream
The top changing bed 2 is connected with the top of reformation cyclone separator 1, and the first U-shaped returning charge is passed through in the bottom of reformation cyclone separator 1
Device 4 is connected with the bottom of bubbling fluidized bed 7.
Further, the described device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic, also include wind-cowl
Air distribution plate 6, wind-cowl air distribution plate 6 is fixed on the bottom surface inside bubbling fluidized bed 7.Wind-cowl air distribution plate 6 is set, can be with cloth wind
Uniformly, making biomass material in bubbling fluidized bed 7 uniformly mix with steam, set up good fluidized state, meanwhile, blast cap is fixed
To the effect blown, beneficially coke and limestone in the second U-shaped material returning device 11 enters calcining fluid bed 12.
Above-mentioned prepare the method that the device of high heating value gas prepares synthesis gas based on double-fluidized-bed biomass pyrolytic, including with
Lower process:
In hopper 3, put into biomass material, biomass material is sent into by screw feeder 5 drum being preinstalled with limestone
In bubble fluid bed 7, meanwhile, the steam entry bottom bubbling fluidized bed 7 is passed through steam, when bubbling fluidized bed 7 is heated
During to 750 850 DEG C, biomass material is pyrolytic gasification in bubbling fluidized bed 7, generates pyrolysis gas and solid residue, pyrolysis gas
In comprise the products such as carbon monoxide, hydrogen, carbon dioxide, methane and tar, solid residue comprises coke, pyrolysis gas rise to weight
In whole fluid bed 2, heated reformate fluid bed 2, make the temperature of reformation fluid bed 2 be maintained at 900 DEG C, solid residue is deposited on bubbling
The bottom of fluid bed 7, solid residue and limestone enter through the second U-shaped material returning device 11 to be calcined in fluid bed 12, heating and calcining stream
Changing bed 12, make the temperature in calcining fluid bed 12 be maintained at 950 DEG C, the air intake to calcining fluid bed 12 is passed through air, Gu
Coke in body residue and oxygen combustion, release substantial amounts of heat, and making the Decomposition of Calcium Carbonate in limestone is solid particulate oxidation
Calcium and atmospheric carbon dioxide, at the top of calcining fluid bed 12, calcium carbonate is completely decomposed into calcium oxide and carbon dioxide, forms gas
Gu biphase product, this gas-particle two-phase product is after calcining cyclone separator 15 separates, and calcium oxide returns through the 3rd U-shaped material returning device 13
To the bottom of reformation fluid bed 2, in reformation fluid bed 2, pyrolysis gas carries calcium oxide and rises, in absorbent lime pyrolysis gas
Carbon dioxide, forms calcium carbonate, promotes water gas shift reaction and methane reforming reaction, meanwhile, the conduct such as calcium oxide, nickel oxide
The catalyst of coke tar cracking, catalytic cracking of tar generates hydrogen and CO (carbon monoxide converter) gas, and reformation fluid bed 2 high temperature promotes tar to produce
Heat cracks, and catalytic pyrolysis and thermal cracking promote tar yield to reduce, thus reduce line clogging situation, and extension device safeguards week
Phase, improving production efficiency, pyrolysis gas obtains reformation gas after reforming in reformation fluid bed 2, and reformation gas is through reformation cyclone separator 1
After gas solid separation, the isolated calcium carbonate of reformation cyclone separator 1 sends back in bubbling fluidized bed 7 through the first U-shaped material returning device 4,
Realizing heat transfer medium circuit to utilize, discharging gas from the syngas outlet of reformation cyclone separator 1 is synthesis gas.
Said apparatus, biomass are sent in bubbling fluidized bed 7 by screw feeder 5 after drying, and steam occurs anti-
Should, pyrolytic gasification, the pyrolysis gas of generation rises in reforming reaction bed, improves reforming reactor temperature, promotes tar thermal cracking
Reaction, reduces tar yield, and the hydrogen simultaneously produced and carbon dioxide can improve flow rate；Solid residue after pyrolysis
Predominantly coke, coke and thermophore calcium carbonate are in material returning device enters calcining fluid bed 12；Calcining fluid bed 12 is passed through oxygen,
Making coke combustion heat release in oxygen, the decomposition for calcium carbonate provides heat, and Decomposition of Calcium Carbonate is calcium oxide and carbon dioxide, warp
Calcining cyclone separator 15 gas solid separation, flue gas discharge, calcium oxide particle then returns to the bottom of reforming reaction bed, at pyrolysis gas
The effect of carrying secretly of air-flow is lower to be risen, and calcium oxide on the one hand absorbing carbon dioxide generates calcium carbonate, on the other hand promotes splitting of tar
Solving, improve the calorific value of reformation gas, reformation gas obtains synthesis gas through gas solid separation, and the calcium carbonate granule of regeneration returns to bubbling fluidization
Recycle in bed 7；The synthesis gas sensible heat utilizing a part to produce can be that biomass are dried offer heat.
In said method, select limestone as heat-carrying granule, decompose in calcining fluid bed 12 and heat up, for reformate stream
Reaction in bed 7 provides heat, and promotes water gas shift reaction, methane reforming reaction and coke tar cracking reaction, the most again
Raw, it is achieved to recycle.Heat-carrying granule also may select Ni/Al2O3Or Ca/Al2O3。
Embodiment two:
As it is shown in figure 1, a kind of device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic of the present invention, including
Reformation cyclone separator 1, reformation fluid bed 2, hopper the 3, first U-shaped material returning device 4, screw feeder 5, wind-cowl air distribution plate 6, drum
Bubble fluid bed the 7, first scum pipe the 8, second scum pipe the 9, the 3rd scum pipe the 10, second U-shaped material returning device 11, calcining fluid bed 12,
3rd U-shaped material returning device 13, storage tank 14, calcining cyclone separator 15, air preheater 16 and tar cracker 17.
From embodiment one, separate high-temperature flue gas from calcining cyclone separator 15 and reformation cyclone separator 1
After high heating value synthesis gas.High-temperature flue gas can be sent into and heat the working medium (water or steam) in heating surface in boiler, shares pot
The energy source of stove part, such that it is able to reach the purpose energy-saving and emission-reduction of energy-saving and emission-reduction, the working medium after being heated can send into steaming
Steam turbine generates electricity, and high-temperature flue gas can go successively to preheating in air preheater 16 and will enter the sky of calcining fluid bed 12
Gas, for calcining fluid bed 12 burning provide additional heat, simultaneously high-temperature flue gas after carrying out repeatedly heat exchange temperature the most under
Fall, after cleaner unit discharges, the harm and the pollution that are brought also are greatly diminished.High heating value synthesis gas is through cleaner unit
After can sell as high heating value product coal gas or use, it is also possible to send in gas turbine and generate electricity, the height wherein produced
Wet body may be used for heat supply heating.In sum, just can be implemented in the thermoelectricity gas coproduction alliance in same device, it is achieved that
The efficient utilization of biomass energy, not only solves the process problem of waste gas biomass, can also help to alleviate energy shortage simultaneously
Problem, it is achieved resource circulation utilization.
Embodiment three:
As it is shown in figure 1, a kind of device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic of the present invention, including
Reformation cyclone separator 1, reformation fluid bed 2, hopper the 3, first U-shaped material returning device 4, screw feeder 5, wind-cowl air distribution plate 6, drum
Bubble fluid bed the 7, first scum pipe the 8, second scum pipe the 9, the 3rd scum pipe the 10, second U-shaped material returning device 11, calcining fluid bed 12,
3rd U-shaped material returning device 13, storage tank 14, calcining cyclone separator 15, air preheater 16 and tar cracker 17.
This apparatus structure is simple, builds conveniently, and the scale of building can be changed according to the actual requirements, it is adaptable to multiple field
Scape place, bed wide material sources, can be the wooden fibres such as straw in addition to grain, fruit in agriculture and forestry production process, trees
Tie up the materials such as the fowl and animal excrement during element, farming industry leftover bits and pieces, agriculture and forestry organic waste material and Animal husbandry production and garbage,
It is reliable distributed energy resource system, complementation can be formed with centralized energy resource system, help to solve dispersion and remote districts
Energy supply problem.
Claims (5)
1. the device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic, it is characterised in that reformation cyclonic separation
The top of device (1) is connected with bubbling fluidized bed (7) by reformation fluid bed (2), and the 2nd U is passed through in the bottom of bubbling fluidized bed (7)
Type material returning device (11) and the bottom Lian Liantong of calcining fluid bed (12), calcine the top connection calcining cyclonic separation of fluid bed (12)
Device (15), the bottom of calcining cyclone separator (15) connects storage tank (14), and the bottom of storage tank (14) is provided with the 3rd U-shaped returning charge
Device (13) connects with the bottom of reformation fluid bed (2) simultaneously；The first U-shaped material returning device is passed through in the bottom of reformation cyclone separator (1)
(4) connect with bubbling fluidized bed (7)；The bottom of hopper (3) connects screw feeder (5), the output termination drum of screw feeder (5)
The inner chamber of bubble fluid bed (7)；
The top of reformation cyclone separator (1) is provided with syngas outlet and connects tar cracker (17), calcining cyclone separator (15)
Top be provided with exhanst gas outlet and connect air preheater (16), the import input air of economizer bank in air preheater (16),
Outlet connects tar cracker (17)；The bottom of described bubbling fluidized bed (7) is provided with steam entry and scum pipe (8), the 2nd U
The bottom of type material returning device (11) is provided with the second scum pipe (9), and the bottom of calcining fluid bed (12) is provided with air intake and the 3rd row
Slag pipe (10).
The device preparing high heating value gas based on double-fluidized-bed biomass pyrolytic the most according to claim 1, its feature exists
In, the described bottom in bubbling fluidized bed (7) is provided with wind-cowl air distribution plate (6).
3. the method that high heating value gas is prepared in a device pyrolysis as claimed in claim 1, it is characterised in that described method
Including procedure below:
Putting into biomass material in hopper (3), biomass material is sent into the bubbling being preinstalled with limestone by screw feeder (5)
In fluid bed (7), meanwhile, the steam entry to bubbling fluidized bed (7) bottom is passed through steam, when bubbling fluidized bed (7) quilt
When being heated to 750 850 DEG C, biomass material is pyrolytic gasification in bubbling fluidized bed (7), generates pyrolysis gas and solid residue,
Comprising carbon monoxide, hydrogen, carbon dioxide, methane and tar in pyrolysis gas, solid residue comprises coke, and pyrolysis gas rises to weight
In whole fluid bed (2), heated reformate fluid bed (2), make the temperature of reformation fluid bed (2) be maintained at 900 DEG C, solid residue deposits
Calcining fluid bed (12) is entered through the second U-shaped material returning device (11) at the bottom of bubbling fluidized bed (7), solid residue and limestone
In, heating and calcining fluid bed (12), make the temperature in calcining fluid bed (12) be maintained at 950 DEG C, to calcining fluid bed (12)
Air intake is passed through air, the coke in solid residue and oxygen combustion, releases substantial amounts of heat, makes the calcium carbonate in limestone
Being decomposed into solid particulate oxidation calcium and atmospheric carbon dioxide, at the top of calcining fluid bed (12), calcium carbonate is completely decomposed into oxygen
Change calcium and carbon dioxide, form gas-particle two-phase product, this gas-particle two-phase product after calcining cyclone separator (15) separates, flue gas
Entering air preheater (16) preheating and enter the air of tar cracker, calcium oxide passes through storage tank (14), through the 3rd U-shaped returning charge
Device (13) returns to the bottom of reformation fluid bed (2), and in reformation fluid bed (2), pyrolysis gas carries calcium oxide and rises, calcium oxide
Absorb the carbon dioxide in pyrolysis gas, form calcium carbonate, promote water gas shift reaction and methane reforming reaction, meanwhile, oxidation
Calcium, nickel oxide etc. generate hydrogen and CO (carbon monoxide converter) gas, reformation fluid bed as the catalyst of coke tar cracking, catalytic cracking of tar
(2) high temperature promotes tar to produce thermal cracking, and catalytic pyrolysis and thermal cracking promote tar yield to reduce, thus reduce line clogging feelings
Condition, extension device maintenance period, improves production efficiency；Pyrolysis gas obtains reformation gas after reforming in reformation fluid bed (2), reforms
Gas is after reformation cyclone separator (1) gas solid separation, and reformation cyclone separator (14) isolated calcium carbonate is through the first U-shaped returning charge
Device (4) sends back in bubbling fluidized bed (7), it is achieved heat transfer medium circuit utilizes, from the syngas outlet of reformation cyclone separator (1)
Discharge gas is synthesis gas, enters tar cracker (17) and makes residu tar crack further by high temperature, finally gives coal gas.
The method of high heating value gas is prepared in pyrolysis the most according to claim 3, it is characterised in that reformation fluid bed (2) is subject to
To the preheating of bubbling fluidized bed (7), temperature reaches 900 degrees centigrade, makes internal tar produce high temperature pyrolysis, simultaneously because
There is the compound such as calcium oxide, nickel oxide, catalytic tar generation catalytic cracking reaction, in two kinds of cracking reactions promote bed, tar produces
Amount reduces, thus reduces pipeline by tar stopping state, and can produce additional heat after coke tar cracking.
The method of high heating value gas is prepared in pyrolysis the most according to claim 3, it is characterised in that calcining cyclone separator
(15) isolated high-temperature flue gas can be used for air preheater (16) preheated air, reformation cyclone separator (1) isolated conjunction
Becoming gas rich in gases such as the hydrogen of a large amount of high heating values, carbon monoxides, tar cracker (17) can further remove tar removing, raw
Output high heating value gas, and can be used for gas turbine, diesel power generation, heating, thus realize thermoelectricity gas alliance.
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| CN109735370A (en) * | 2019-01-24 | 2019-05-10 | 东南大学 | Pyrolysis is with gasification zoning for the device and method of hydrogen-rich synthetic gas |
| CN110760343A (en) * | 2019-10-15 | 2020-02-07 | 武汉丰盈能源技术工程有限公司 | Method for reducing tar content in biomass fluidized bed gasification furnace synthesis gas |
| WO2020082377A1 (en) * | 2018-10-23 | 2020-04-30 | 西安华大骄阳绿色科技有限公司 | Process for using garbage to prepare liquid-state fuel and chemical products, and garbage catalytic pyrolysis system |
| CN112899032A (en) * | 2021-01-18 | 2021-06-04 | 北京交通大学 | Two-section type double bubbling bed hydrogen production device |
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Inventor after: Xiang Wenguo Inventor after: Liu Yijun Inventor after: Chen Shiyi Inventor after: Zhang Lei Inventor after: Li Meng Inventor before: Xiang Wenguo Inventor before: Liu Yijun Inventor before: Chen Shiyi |
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Application publication date: 20161214 |