CN104629786B - A kind of method utilizing biomass castoff to produce liquid fuel - Google Patents
A kind of method utilizing biomass castoff to produce liquid fuel Download PDFInfo
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- CN104629786B CN104629786B CN201510067790.XA CN201510067790A CN104629786B CN 104629786 B CN104629786 B CN 104629786B CN 201510067790 A CN201510067790 A CN 201510067790A CN 104629786 B CN104629786 B CN 104629786B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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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
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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Abstract
The invention discloses a kind of method utilizing biomass castoff to produce liquid fuel, belong to field of renewable energy technology.The fast pyrolysis method of the present invention includes: by feedstock transportation to reaction unit, heat through heat carrier, thermal cracking occurs in the reactor, generate thermal cracking steam and charcoal.It is transported in heater after heat carrier is separated.After the separated device of charcoal separates, it is delivered to arrange charcoal system by pipeline, thermal cracking steam passes through condenser system, condensable partial coagulation is liquid bio-oil, condensation portion can not be delivered to heat carrier heating system through combustion heating heat carrier through pipeline, heat carrier is delivered in ball storage chamber after reaching predetermined temperature continue to recycle, and this device can be used for large-scale industrial production.
Description
Technical field
The present invention relates to a kind of method utilizing biomass castoff to produce liquid fuel, especially a kind of lignocellulosic
Biolobic material castoff heat cleavage method, belongs to renewable resource technical field.
Background technology
Along with the development of human civilization, the consumption of the energy constantly rises, and the reserves of fossil energy are limited,
Thus result in energy crisis.Simultaneously because fossil energy use time produce substantial amounts of oxysulfide, nitrogen oxides, two
The gases such as carbonoxide, create serious environmental crisis.Solve one of method of the two crisis, it is simply that finding can be again
Raw clean energy resource.
Bioenergy is due to its abundant raw material source, renewable, and during whole utilization, carbon emission amount is the advantage such as zero,
It it is the focus in current regenerative resource research.The Application way of bioenergy has a lot, and biomass through pyrolysis produces liquid
Fluid fuel technology is the one that bioenergy utilizes technology, and this technology can be wooden low heat value, low value-added solid-state
Cellulose series biomass discarded object is converted into the liquid fuel of high heating value, high added value, produces charcoal and can not simultaneously
Condensed gas.Due to its simple process, requiring low to environmental condition, the advantages such as adaptability to raw material is wide are just each by the world
The highest attention of ground researcher.
Agricultural crop straw, wood chip, rice husk etc. all can be as the raw materials of thermal cracking preparing bio-oil.China is Rice Production
Big country, produces nearly 200,000,000 tons of paddy per year.As the Main By product rice husk during paddy processing, account for Seed weight
The 20% of amount, is a kind of important regenerative resource.The method utilized about rice husk both at home and abroad is a lot, as directly burnt,
Compression forming and be used as feed etc., these Land use systems come with some shortcomings part, as polluted environment, Energy harvesting
Rate is low.By biomass fast pyrolysis technology, solid rice husk being converted into liquid fuel is that one has DEVELOPMENT PROSPECT very much
Land use systems.
The core of research on biomass flash pyrolysis for liquid fuel is reactor.According to the motion mode of reaction raw materials, instead
The type answering device is broadly divided into: fixed bed reactors, fluidized-bed reactor, circulating fluid bed reactor etc.；According to adding
Hot mode, the type of reactor is broadly divided into: direct heating type reactor and indirect heating type reactor；According to material
The type of flow: up bed reactor and descending-bed reactor.
In prior art, Chinese Patent Application No. is: 200520013147, entitled: biomass flash thermal cracking system
Take in the technology of pure bio oil device and mention: in the lower port of quartz glass tube, be connected to feed air-valve mouth and purging wind
The three-way pipe of valve port, purging air-valve mouth be positioned at above feed air-valve mouth, the upper end horizontal branch pipe of quartz glass tube built with
Filter, equipped with carborunbum tube outside quartz glass tube, its cold end is connected with power supply, in a termination carborunbum tube of thermocouple
Between heating tape, another terminates control panel, and carborunbum tube is outer equipped with asbestos heat-insulation layer.The weak point of this technology exists
In: device is fed by three-way pipe feed wind, it is impossible to persistently charging and it cannot be guaranteed that reaction temperature；Device is excessively simple,
It is only suitable for the research in laboratory.
And Chinese Patent Application No. is: 200510112221.9, entitled: organic waste in agricultural and forest industries fast pyrolysis
Produce in the technology of fuel oil equipment and mention: device includes Poor oxygen gas generating means, feeding unit, fluidized-bed reaction
Device, collection of products device, Temperature-controlled appliance.Annexation is: Poor oxygen gas generating means is connected with fluid bed,
Feeding unit by extend vertically through with fluidized-bed reactor wall bottom pipe be welded on fluidized-bed reactor, fluidisation
Bed reactor is welded on a pedestal jointly with feeding unit, and collection of products device and fluidized-bed reactor pass through flange
Dish connects, and Temperature-controlled appliance passes through circuit and fluidized-bed reactor, and Poor oxygen gas generating means is connected.This technology
It is disadvantageous in that: device needs extra Poor oxygen gas generating means, adds device cost of manufacture；Tail gas without
Method recycles, and directly discharge causes the waste of resource and the pollution of environment；Device is only applicable to grinding of laboratory
Study carefully.
Therefore, those skilled in the art is devoted to develop a kind of novel biomass castoff that utilizes and produces liquid fuel
And the method for charcoal, it is achieved large-scale industrial production, to overcome the defect of prior art.
Summary of the invention
Because the drawbacks described above of prior art, the technical problem to be solved is to provide a kind of novel utilization
Biomass castoff produces liquid fuel and the method for charcoal.Heat carrier of the present invention is with biomass castoff in gas-solid also
Row directly contacts during flowing downward, and heat transfer rapidly and sufficiently, is suitable for the temperature-rise period of flash；Temperature in reactor
Degree is evenly distributed, and improves product stability；Reaction temperature is easily controlled；Only need burning raw device startup stage
Thing oil heat supply, enters normal operating phase and need not outside energy input, only utilize the burning of not condensable gases with regard to energy
Energy needed for heat scission reaction is provided；Utilize the large-scale thermal cracker that the method makes, can reach to produce biology per year
The scale of oil ton.
The present invention is the method for the fast pyrolysis utilizing lignocellulose-like biomass discarded object production liquid fuel.This
The raw material sources of method are of a great variety, and stock number is big.Agricultural crop straw, wood chip, rice husk etc. all can be as thermal cracking systems
Take the raw material of bio oil.This method currently mainly utilizes powdered rice hulls, by biomass fast pyrolysis technology by solid rice
Shell is converted into liquid fuel.
This liquid fuel, is also known as bio oil, and calorific value is at about 16MJ/Kg, and current Land use systems is mainly
Burning, this advantage directly burnt with solid fuel is: energy density is big, and the dust of generation is few, and burning is abundant.
Bio oil can also further carry out upgrading process, is transformed into substitute Fuel of Internal Combustion Engine and produces multiple high added value
Industrial chemicals.
The present invention is a kind of method utilizing biomass castoff to produce fuel, comprises the following steps:
A), crushed biomass discarded object, and will pulverize after biomass castoff send into reaction unit；
B), make the biomass castoff after described pulverizing and the heat carrier heat exchange in described reaction unit, make biology
Matter discarded object generation heat scission reaction, generates charcoal and thermal cracking steam；
C), the thermal cracking steam of gained in step (b) is separated with charcoal, and heat carrier is separated with charcoal；
D), the charcoal that is mixed in further separating step (c) thermal cracking steam, and separating step (c) heat carrier
In the charcoal that is mixed into；
E), by the thermal cracking steam condensation of gained in step (d), bio oil and non-condensable gas are generated.
The device that wherein reaction unit refers to realize needed for reaction is overall.Reaction unit includes reactor, separator,
Condenser, heater, arrange charcoal device, ball storage chamber and the heat carrier circulated in systems.Reactor is indirect
Hot type downlink cycle fluidized-bed reactor, ball storage chamber is the heat carrier after temporary heating, in case carrying for heat scission reaction
The device of heat carrier.
Step (b) occurs in the reactor of reaction unit, and after heat carrier exchanges with biomass thermal, biomass castoff is sent out
Heat cracking reaction, forms thermal cracking steam and charcoal, subsequently enters and realizes heat carrier and charcoal in separator
Separate, and the gas solid separation of thermal cracking steam and charcoal.
Further, before step (a), also include that step (f), described step (f) are: start described instead
Answer device, heat the heat carrier in described reaction unit.
Further, after step (e), also include that step (g), described step (g) are: in step (e)
Non-condensable gas and step (d) in heat carrier after carbon removal all enter heater, non-condensable gas combustion heating heat carries
Body, it is standby that the heat carrier after heating enters ball storage chamber, continues and biomass castoff heat exchange, makes living beings matter discard
Thing generation heat scission reaction.
Further, in described step (b), the biomass castoff after pulverizing directly is contacted and adds by heat carrier
Heat.
Further, heat carrier circulates in reaction unit.
Further, described heat carrier is sand, Ceramic Balls or flyash inert solid particle.
Further, in step (a), the biomass castoff after pulverizing can use spiral shell when sending into reaction unit
Bar feeding or negative pressure feeding technique, feed rate is 1-3t/h.Screw rod feeding uses screw feeding machine, and negative pressure feeding makes
Use negative pressure feeder.
Further, described step (b) particularly as follows: biomass castoff after Fen Suiing and heat carrier gas-solid parallel to
Contact heat-exchanging during lower flowing, heat carrier and pulverize after biomass castoff mixing, and impart heat to pulverize after
Biomass castoff；Biomass castoff after pulverizing is heated to more than 500 DEG C in 1-2s, and thermal cracking occurs
Reaction, the volatile ingredient of the biomass castoff after pulverizing and moisture form thermal cracking steam, and the ash content of living beings is with solid
Determine carbon and form charcoal.The course of reaction that gas-solid flows downward parallel has that gas-solid contact time is short, gas-solid speed and dense
Radial distribution is more uniformly distributed degree, gas-solid axial backmixing greatly reduces, easily realize the features such as high solid-gas ratio operation.
Further, described step concrete (e) is: by the thermal cracking steam of gained in step (d) through being positioned at institute
Stating in reaction unit one group or organize condenser more, the condensable partial coagulation in thermal cracking steam is described bio oil.
Further, described method also include by step (b) and step (d) produce charcoal utilize pipeline
Discharge described reaction unit, maintain the continuous operation of system.
Wherein, burning bio oil when heat carrier heating is device startup, when device normally transports dress in combustion heat cracking process
The not condensable gases heating heat carrier generated, supplies the energy needed for biomass castoff thermal cracking, saves the energy,
Free from environmental pollution.First in cyclone separator, charcoal is separated with the heat carrier after living beings heat exchange, be then passed through
Pipeline is transported in heat carrier heating system, and the heat carrier reaching predetermined temperature (560 DEG C) is transported in ball storage chamber circulation
Utilize.Heat carrier total amount is 7t, and heat carrier internal circulating load is 70t/h.
Separation process is to utilize one or more groups cyclone separator, isolates in the carbon dust in thermal cracking steam and heat carrier
Carbon dust, carbon dust be pipelined to arrange charcoal system.
Condensation process is that the thermal cracking steam of high temperature through one group or organizes condenser more, condensable in thermal cracking steam
Partial coagulation be liquid bio-oil, it is achieved gaseous material is changed into the system of liquid.Condensable gases is not passed through
Pipeline is transported in heat carrier heating system, wherein combustible constituent burning, the energy needed for supply heat scission reaction, no
Condensible gas reusable edible, normal operating phase need not outside energy input, only utilizes the combustion of not condensable gases
Burning provides for energy needed for heat scission reaction.
Below with reference to accompanying drawing, the technique effect of design, concrete structure and the generation of the present invention is described further, with
It is fully understood from the purpose of the present invention, feature and effect.
Accompanying drawing explanation
Fig. 1 is the process chart of the inventive method implementation process
Detailed description of the invention
As it is shown in figure 1, device startup stage, use bio oil combustion heat supplying, heat heat carrier, make whole system
Start.Heat carrier can use sand, the inert solid particle such as Ceramic Balls and flyash.When heat carrier is heated to suitably
Temperature (560 DEG C), starts feed system, in biomass castoff feedstock transportation to reaction unit, exists with heat carrier
Gas-solid flow downward parallel during contact heat-exchanging, make biomass castoff generation heat scission reaction, produce thermal cracking and steam
Gas.It is transported in heater after heat carrier is separated.Solid matter in thermal cracking steam is made by piece-rate system
Gas solid separation, obtains accessory substance charcoal.Thermal cracking steam travels further into condenser system, condensable heat therein
Cracking steam is condensed into liquid fuel: bio oil, remaining not condensable gases, is transported to heater via pipeline
Middle combustion heating heat carrier.
Material is accounted: according to material balance principle, the productivity of bio oil, the productivity of charcoal and non-condensable gases
Productivity sum is equal to 1.In actual test, biomass castoff consumption, bio oil yield, charcoal yield are direct
Weighing and record, thus obtain the productivity of the productivity of bio oil, charcoal, condensable gases productivity does not uses back balance side
Method is calculated.
Bio oil measures its moisture content after collecting, viscosity, density, pH, calorific value, solid content, ash grade characteristic.Contain
Water rate mensuration employing Karl-Fischer method (KFT TITRINO plus 870 moisture teller, Wan Tong instrument company of Switzerland,
ASTM D1744), bioassay standard sees ASTM D1744.Viscosity measurement uses capillary viscometer method (SYD-265H
Dynamic viscosity analyzer, Shanghai Changji Geological Instrument Co., Ltd.), bioassay standard sees ASTM D445.Density measurement
Use U-tube concussion method (DMA 4100M Density Measuring Instrument, Anton Paar Co., Ltd of Austria, GB/T1884-2000).
PH measures and uses pH meter method (PHS-3CT precision pH meter, Shanghai Lei Ci instrument plant, GB11165-1989).Calorific value is surveyed
Surely measuring instrument is used: oxygen bomb calorimeter, XRY-1B, Shanghai Changji Geological Instrument Co., Ltd., bioassay standard is joined
See GB GB/T283 and ASTM D3286-91a.The measurement of solid particulate matter content uses ethanol dissolution method.Ash content
Measuring the minusing of weight after using 775 DEG C to be heated to measure, instrument is Muffle furnace, and bioassay standard sees GB GB/T
508-85 and ASTM D482.All of mensuration all uses three repetitions, calculates average and variance.
Embodiment 1
Start reaction unit, bio oil of burning, heats heat carrier, reaches predetermined temperature (560 DEG C), make with powdered rice hulls
Physical obsolescence of making a living raw material, is transported in reaction unit by feed system, and the feed rate of biomass castoff is
2.33t/h。
Biomass castoff and heat carrier direct contact heat transfer during descending, heat carrier and biomass castoff are abundant
Mixing, and its heat is passed to biomass castoff.Biomass castoff instantaneous (1-2s) be heated to 500 DEG C with
On, biomass castoff generation heat scission reaction, the volatile matter of biomass castoff and moisture major part form thermal cracking
Steam.The ash content of biomass castoff and fixed carbon major part form charcoal.
After heat scission reaction, it is transported in heater after heat carrier is separated.Utilize one or more groups cyclone separator,
Isolate the carbon dust in thermal cracking steam, it is achieved gas phase and the separation of solid phase, carbon dust is pipelined to arrange charcoal system
System.
The thermal cracking steam of high temperature through one group or organizes condenser more, partial coagulation condensable in thermal cracking steam
For liquid bio-oil, it is achieved gaseous material is changed into liquid.Condensable gases is not transported to heat carrier through pipeline
In heating system, wherein combustible constituent combustion heating heat carrier, not condensible gas reusable edible, normal operating phase
Need not outside energy input, only utilize the heat of not condensable gases to provide for energy needed for heat scission reaction.
First in cyclone separator, charcoal is separated with the heat carrier after biomass castoff heat exchange, be then passed through pipe
Road is transported in heat carrier heating system, and the heat carrier reaching predetermined temperature (560 DEG C) is transported in ball storage chamber circulation profit
With.The combustible constituent of the not condensable gases generated in thermal cracking processes burns in heating system, heats heat carrier,
Energy needed for supply biomass through pyrolysis reaction.
Row's charcoal system utilizes pipeline that isolated carbon dust in carbon dust isolated in thermal cracking steam and heat carrier is discharged dress
Put, maintain the continuous operation of system.
In the present embodiment, device duration of runs is 4.42h, and the productivity of bio oil is 48.1%, and the productivity of charcoal is
26.0%, uncondensable gas yield is 25.9%.Concrete bio oil specificity analysis the results are shown in Table 1.
Embodiment 2
Start reaction unit, bio oil of burning, heats heat carrier, reaches predetermined temperature (560 DEG C), make with powdered rice hulls
Physical obsolescence of making a living raw material, is transported in reaction unit by feed system, and the feed rate of living beings is 2.17t/h.
Biomass castoff and heat carrier direct contact heat transfer during descending, heat carrier and biomass castoff are abundant
Mixing, and its heat is passed to biomass castoff.Biomass castoff instantaneous (1-2s) be heated to 500 DEG C with
On, biomass castoff generation heat scission reaction, the volatile matter of biomass castoff and moisture major part form thermal cracking
Steam.The ash content of biomass castoff and fixed carbon major part form charcoal.
After heat scission reaction, it is transported in heater after heat carrier is separated.Utilize one or more groups cyclone separator,
Isolate the carbon dust in thermal cracking steam, it is achieved gas phase and the separation of solid phase, carbon dust is pipelined to arrange charcoal system
System.
The thermal cracking steam of high temperature through one group or organizes condenser more, partial coagulation condensable in thermal cracking steam
For liquid bio-oil, it is achieved gaseous material is changed into liquid.Condensable gases is not transported to heat carrier through pipeline
In heating system, wherein combustible constituent combustion heating heat carrier, not condensible gas reusable edible, normal operating phase
Need not outside energy input, only utilize the heat of not condensible gas to provide for energy needed for heat scission reaction.
First in cyclone separator, charcoal is separated with the heat carrier after biomass castoff heat exchange, be then passed through pipe
Road is transported in heat carrier heating system, and the heat carrier reaching predetermined temperature (560 DEG C) is transported in ball storage chamber circulation profit
With.The combustible constituent of the not condensable gases generated in thermal cracking processes burns in heating system, heats heat carrier,
Energy needed for supply biomass through pyrolysis.
Row's charcoal system utilizes pipeline that isolated carbon dust in carbon dust isolated in thermal cracking steam and heat carrier is discharged dress
Put, maintain the continuous operation of system.
In the present embodiment, device duration of runs is 80.42h, and the productivity of bio oil is 46.3%, and the productivity of charcoal is
29.0%, uncondensable gas yield is 24.7%.Concrete bio oil specificity analysis the results are shown in Table 1.
Embodiment 3
Start reaction unit, bio oil of burning, heats heat carrier, reaches predetermined temperature (560 DEG C), make with powdered rice hulls
Physical obsolescence of making a living raw material, is transported in reaction unit by feed system, and the feed rate of living beings is 2.19t/h.
Biomass castoff and heat carrier direct contact heat transfer during descending, heat carrier and biomass castoff are abundant
Mixing, and its heat is passed to biomass castoff.Biomass castoff instantaneous (1-2s) be heated to 500 DEG C with
On, biomass castoff generation heat scission reaction, the volatile matter of biomass castoff and moisture major part form thermal cracking
Steam.The ash content of biomass castoff and fixed carbon major part form charcoal.
After heat scission reaction, it is transported in heater after heat carrier is separated.Utilize one or more groups cyclone separator,
Isolate the carbon dust in thermal cracking steam, it is achieved gas phase and the separation of solid phase, carbon dust is pipelined to arrange charcoal system
System.
The thermal cracking steam of high temperature through one group or organizes condenser more, partial coagulation condensable in thermal cracking steam
For liquid bio-oil, it is achieved gaseous material is changed into liquid.Condensable gases is not transported to heat carrier through pipeline
In heating system, wherein combustible constituent combustion heating heat carrier, not condensible gas reusable edible, normal operating phase
Need not outside energy input, only utilize the heat of not condensible gas to provide for energy needed for heat scission reaction.
First in cyclone separator, charcoal is separated with the heat carrier after biomass castoff heat exchange, be then passed through pipe
Road is transported in heat carrier heating system, and the heat carrier reaching predetermined temperature (560 DEG C) is transported in ball storage chamber circulation profit
With.The combustible constituent of the not condensable gases generated in thermal cracking processes burns in heating system, heats heat carrier,
Energy needed for supply biomass through pyrolysis.
Row's charcoal system utilizes pipeline that isolated carbon dust in carbon dust isolated in thermal cracking steam and heat carrier is discharged dress
Put, maintain the continuous operation of system.
In the present embodiment, device duration of runs is 9.60h, and the productivity of bio oil is 47.6%, and the productivity of charcoal is
31.0%, uncondensable gas yield is 21.4%.Concrete bio oil specificity analysis the results are shown in Table 1.
Embodiment 4
Start reaction unit, bio oil of burning, heats heat carrier, reaches predetermined temperature (560 DEG C), make with powdered rice hulls
Physical obsolescence of making a living raw material, is transported in reaction unit by feed system, and the feed rate of living beings is 3t/h.
Biomass castoff and heat carrier direct contact heat transfer during descending, heat carrier and biomass castoff are abundant
Mixing, and its heat is passed to biomass castoff.Biomass castoff instantaneous (1-2s) be heated to 500 DEG C with
On, biomass castoff generation heat scission reaction, the volatile matter of biomass castoff and moisture major part form thermal cracking
Steam.The ash content of biomass castoff and fixed carbon major part form charcoal.
After heat scission reaction, it is transported in heater after heat carrier is separated.Utilize one or more groups cyclone separator,
Isolate the carbon dust in thermal cracking steam, it is achieved gas phase and the separation of solid phase, carbon dust is pipelined to arrange charcoal system
System.
The thermal cracking steam of high temperature through one group or organizes condenser more, partial coagulation condensable in thermal cracking steam
For liquid bio-oil, it is achieved gaseous material is changed into liquid.Condensable gases is not transported to heat carrier through pipeline
In heating system, wherein combustible constituent combustion heating heat carrier, not condensible gas reusable edible, normal operating phase
Need not outside energy input, only utilize the heat of not condensible gas to provide for energy needed for heat scission reaction.
First in cyclone separator, charcoal is separated with the heat carrier after biomass castoff heat exchange, be then passed through pipe
Road is transported in heat carrier heating system, and the heat carrier reaching predetermined temperature (560 DEG C) is transported in ball storage chamber circulation profit
With.Combustible constituent combustion heating heat carrier in heating system of the not condensable gases generated in thermal cracking processes, supplies
Answer the energy needed for biomass through pyrolysis.
Row's charcoal system utilizes pipeline that isolated carbon dust in carbon dust isolated in thermal cracking steam and heat carrier is discharged dress
Put, maintain the continuous operation of system.
In the present embodiment, device duration of runs is 6.17h, and the productivity of bio oil is 53.2%, and the productivity of charcoal is
30.0%, uncondensable gas yield is 16.8%.Concrete bio oil specificity analysis the results are shown in Table 1.
The specificity analysis of table 1 bio oil
The preferred embodiment of the present invention described in detail above.Should be appreciated that the ordinary skill of this area is without wound
The property made work just can make many modifications and variations according to the design of the present invention.Therefore, all technology in the art
Personnel can be obtained by logical analysis, reasoning, or a limited experiment the most on the basis of existing technology
The technical scheme arrived, all should be in the protection domain being defined in the patent claims.
Claims (7)
1. one kind utilizes the method that biomass castoff produces fuel, it is characterised in that comprise the following steps:
A), crushed biomass discarded object, and will pulverize after biomass castoff send into reaction unit, use screw rod
Feeding or negative pressure feeding technique, feed rate is 1-3t/h；
B), make the biomass castoff after described pulverizing the most downward in gas-solid with the heat carrier in described reaction unit
Direct contact heat transfer during flowing, makes described biomass castoff generation heat scission reaction, generates biology
Charcoal and thermal cracking steam；
C), the thermal cracking steam of gained in step (b) is separated with charcoal, and heat carrier is separated with charcoal；
D), the charcoal that is mixed in further separating step (c) thermal cracking steam, and separating step (c) heat carrier
In the charcoal that is mixed into；
E), by the thermal cracking steam condensation of gained in step (d), bio oil and non-condensable gases are generated；
It is described that described method also includes utilizing pipeline to discharge the charcoal of the generation in step (b) and step (d)
Reaction unit, maintains the continuous operation of system.
Utilize the method that biomass castoff produces fuel the most as claimed in claim 1, it is characterised in that in step
A before (), also including that step (f), described step (f) are: start described reaction unit, heating is described
Heat carrier in reaction unit.
Utilize the method that biomass castoff produces fuel the most as claimed in claim 1, it is characterised in that in step
After (e), also include that step (g), described step (g) are: the non-condensable gas in step (e) and
In step (d), the heat carrier after carbon removal all enters heater, and non-condensable gas combustion heating heat carrier, after heating
Heat carrier enter ball storage chamber standby, continue with biomass castoff heat exchange, make biomass castoff occur
Heat scission reaction.
Utilize the method that biomass castoff produces liquid fuel the most as claimed in claim 3, it is characterised in that heat
Carrier circulates in reaction unit.
Utilize the method that biomass castoff produces liquid fuel the most as claimed in claim 1, it is characterised in that institute
Stating heat carrier is sand, Ceramic Balls or flyash inert solid particle.
Utilize the method that biomass castoff produces liquid fuel the most as claimed in claim 1, it is characterised in that institute
State step (b) particularly as follows: the mistake that flows downward parallel in gas-solid of biomass castoff after Fen Suiing and heat carrier
Contact heat-exchanging in journey, heat carrier and the biomass castoff mixing after pulverizing, and after heat is passed to pulverizing
Biomass castoff；Biomass castoff after pulverizing is heated to more than 500 DEG C in 1-2s, and heat occurs
Cracking reaction, the volatile ingredient of the biomass castoff after pulverizing and moisture form thermal cracking steam, living beings
Ash content and fixed carbon in discarded object form charcoal.
Utilize the method that biomass castoff produces liquid fuel the most as claimed in claim 1, it is characterised in that institute
State step (e) particularly as follows: passed through by the thermal cracking steam of gained in step (d) and be positioned at described reaction unit
In one group or organize condenser more, the condensable partial coagulation in thermal cracking steam is described bio oil.
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| CN105238432B (en) * | 2015-10-20 | 2017-04-12 | 江西金糠新材料科技有限公司 | Method and device for preparing high-quality bio-oil and white carbon black through self-heating acid pickling-pyrolysis-combustion integration |
| CN105665418B (en) * | 2016-01-28 | 2018-01-30 | 罗红杰 | A kind of rubbish anaerobic cracking apparatus |
| CN106147818B (en) * | 2016-07-29 | 2017-12-29 | 上海交通大学 | One kind utilizes biomass castoff production liquid fuel device and application method |
| CN107892931B (en) * | 2017-11-10 | 2020-07-14 | 东南大学 | Device and method for preparing biochar through mobile pyrolysis |
| CN111363569B (en) * | 2020-03-04 | 2021-05-18 | 华中科技大学 | System for co-production of gas-liquid fuel, chemicals and carbon materials by catalytic pyrolysis of biomass |
| CN115820277A (en) * | 2022-11-22 | 2023-03-21 | 吉林省秸源新能源科技有限公司 | Preparation method of biomass liquid fuel |
| CN115725329A (en) * | 2022-11-27 | 2023-03-03 | 吉林省秸源新能源科技有限公司 | Method for separating biochar from heat carrier |
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| CN101328416A (en) * | 2007-06-18 | 2008-12-24 | 郭君涛 | Method for preparing biofuel oil with agronomic crop straw thermal cracking |
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