CN106281375A - Low temperature continuous pyrolysis biomass prepare fixed bed reactors and the method for activated carbon - Google Patents
Low temperature continuous pyrolysis biomass prepare fixed bed reactors and the method for activated carbon Download PDFInfo
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- CN106281375A CN106281375A CN201610653795.5A CN201610653795A CN106281375A CN 106281375 A CN106281375 A CN 106281375A CN 201610653795 A CN201610653795 A CN 201610653795A CN 106281375 A CN106281375 A CN 106281375A
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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
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
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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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/32—Other processes in ovens with mechanical conveying means
- C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
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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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
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- Oil, Petroleum & Natural Gas (AREA)
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- Combustion & Propulsion (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The present invention relates to low temperature continuous pyrolysis biomass and prepare fixed bed reactors and the method for activated carbon.Reactor of the present invention includes charging aperture, response system, discharging opening, and charging aperture is on discharging opening, and response system includes collection chamber, plenum zone, reative cell from top to bottom；Reative cell has feed auger, discharging spiral, flitch, flitch includes feed end and discharge end, feed auger is under charging aperture, feed end top, discharging spiral is on discharge end top, discharge end is on discharging opening, and feed auger includes center bolt and left and right helical blade, and left and right helical blade is crossed by center bolt, and the centrage being perpendicular to center bolt becomes axial symmetry, 1/3～1/2 that distance is charging aperture bore；Reative cell has reative cell dividing plate, and two ends connect steam inlet and steam jet respectively, for spraying into steam in reative cell.Reactor of the present invention can realize the pyrolysis of biomass and the preparation of activated carbon simultaneously, can continuous feeding and discharging, remarkable in economical benefits.
Description
Technical field
The present invention relates to biomass processes field, the fixed bed particularly relating to a kind of low temperature continuous pyrolysis process biomass is anti-
Answer device, and utilize the method that this reactor prepared activated carbon by biomass.
Background technology
China's biomass resource enriches, about 6.5 hundred million tons of agricultural stalks of annual generation, adds fuel wood and forestry waste
Deng, reduced energy and 4.6 hundred million tons of standard coals are suitable, it is contemplated that will be added to 9.04 hundred million tons to the year two thousand fifty, are equivalent to more than 600,000,000 ton of standard
Coal.The annual forest consumptive material of China reaches 2.1 billion cubic meters, the energy of equivalent 1.2 hundred million tons of standard coals.It addition, National urban is raw
Material annual production more than 1.5 hundred million tons, will reach 2.1 hundred million tons to the year two thousand twenty annual production, and the content of organic matter in rubbish is averagely about
40%.Producing per year in " municipal refuse " of 1.5 hundred million tons, " Renewable resource " being dropped is worth up to 25,000,000,000 yuan.If these resources
Directly burn without improvement, enter water body or accumulation, not only cause the wasting of resources, also can cause air, soil, surface water and ground
The pollution of lower water and the deterioration of environment for human survival.If but carried out carbonization produce oil, gas and solid carbon, can partly replace
For resources such as coal, oil, natural gass.
Activated carbon has highly developed pore structure, and the surface functional group of uniqueness, preferable chemical stability, machine
Tool intensity, and acidproof, alkaline-resisting, heat-resisting, is a kind of excellent adsorbent, is widely used in environmental protection, chemical industry, food add
The every field such as work, hydrometallurgy, medicine are refined, military chemistry protection, are the daily lifes of national economy, national defense construction and people
Requisite product alive.
Along with the development of national economy, growing to even greater heights of cry of curbing environmental pollution the most in recent years, the city of activated carbon
Field prospect and economic benefit are day by day notable, have promoted its research, development and utilization further.World Activated Carbon annual production exceedes
600000 tons, 1992 domestic has reached 70,000 tons, and within 1993, Japan reaches 80,000 tons.At present, activated carbon in China development is very fast, averagely
Annual rate of growth is up to 15%, and export volume has exceeded Japan and the U.S., occupies first place in the world.
Prior art CN101863468A discloses a kind of rotary type microwave oven preparing activated carbon and preparation activity
The system and method for charcoal.This system selects two rotary type microwave ovens, and the material of pretreatment is carried out pyrolysis processing, material
In a rotary type microwave oven, complete carbonization process, enter another rotary type microwave oven and activate, activation
After carbonization admittedly stay thing enter cooling chamber seal cooling, be processed as primary activity charcoal product, then proceed to active-carbon finely system of processing.
But, the raw material limitation that the method uses is big, and microwave heating equipment energy consumption is high, the Dust Capacity that material carbonization process produces
Greatly, temperature of charge and mobility are difficult to monitor, and the imflammable gas of generation is not obtained by, and cause economic benefit low, it is difficult to real
Existing industrialization.
Prior art CN102559222A discloses the method for a kind of low temperature distillation stove pyrolysis material.This method for pyrolysis uses
Horizontal gas retort, before pyrolysis starts each time, first needs to stop unloading reaction after reactor heat supply, question response device cooling down
Device fire door or bell, the solid product of a collection of pyrolysis residual before taking out, needs are artificial adds next batch heat in reactor
The material solved.Therefore the method cannot realize material hot under the conditions of continuous feeding and discharging, without automatic distributing and discharging functions, real
Existing high temperature pyrolysis fixed gas is from for providing heat.Input and output material process need to rise gentleness cooling to reactor, reduces the place of device
Reason ability and efficiency, add fault rate.
Summary of the invention
In view of the deficiencies in the prior art, it is desirable to provide a kind of low cost, the thermal efficiency are high, and high-quality can be produced
The industrialized pyrolysis that is suitable for of activated carbon activates device and method.
The present invention proposes a kind of low temperature continuous pyrolysis biomass and prepares the fixed bed reactors of activated carbon, described reactor
Including charging aperture, response system, discharging opening, the horizontal level of described charging aperture sets high than the horizontal position of described discharging opening；
Described response system includes collection chamber, plenum zone, reative cell the most successively；Described reative cell has
Feed auger, discharging spiral, flitch, described flitch includes that feed end and discharge end, described feed auger are arranged on described charging
Under Kou, it is positioned at described feed end top；Described discharging spiral is arranged on described discharge end top, and described discharge end is positioned at described
On discharging opening；
Described feed auger includes center bolt, left-hand screw blade, right-hand screw blade；Described center bolt crosses a described left side
Helical blade and right-hand screw blade, the centrage that described left-hand screw blade is perpendicular to described center bolt with right-hand screw blade becomes axle
Symmetry, distance between the two is the 1/3～1/2 of described charging aperture bore；
Described reative cell has reative cell dividing plate, and described reative cell dividing plate two ends connect steam inlet and steam spray respectively
Mouth.
Further, the lower limb of described left-hand screw blade and right-hand screw blade and the vertical dimension of described flitch be 50～
150, preferably 80；Described left-hand screw impeller clearance and right-hand screw impeller clearance are placed equidistant or displacement is arranged.
Further, described plenum zone is prismatoid, and described reative cell is cube, the end of described plenum zone
Portion connects with the top of described reative cell；The top of described plenum zone is 1000～1500 with the vertical dimension of described flitch
㎜。
Further, the angle of the vertical plane of the trapezoidal oblique section of described plenum zone and described reative cell be 120 °～
150 °, preferably 135 °；Described trapezoidal oblique section is made up of steel plate, is provided with circular hole thereon.
Further, feed end and the discharge end of described flitch are provided with drive bearing, are used for driving described flitch continuous
Rotate；Described drive bearing has two or more.
Further, described reactor also includes that housing, described housing include reactor wall, support platform, support；
Described reactor wall is used for sealing described reative cell；
Described support platform is arranged under described flitch；
Described support is fixed in described support platform, is used for connecting described drive bearing.
Further, described reative cell includes radial canal；
Described radial canal is heat accumulation type radiant tube, is arranged on described flitch top parallel with described flitch；
Vertical dimension between described radial canal and described flitch is 400～550, preferably 400.
The invention allows for a kind of method utilizing above-mentioned reactor to be prepared activated carbon by biomass, described method includes
Following steps:
Charging stage: biomass material is transported to via described charging aperture the interlude of described feed auger；
Pyrolysis phase: described biomass material is uniformly distributed along the flitch both sides of described continuous rotation, and in described reaction
Room occur pyrolytic reaction generate carbonization material；
Activation stage: be passed through steam by described steam inlet, described steam enters described reative cell dividing plate and heats up,
Steam after intensification, after described intensification, steam enters in described reative cell via described steam jet, described carbonization material
Activation obtains activated carbon.
In said method, described pyrolysis phase radial canal temperature is 600～850 DEG C；Described activation stage radial canal temperature
Being 650～1100 DEG C, after described intensification, steam temperature is 700～950 DEG C.
In said method, the particle diameter of described biomass material is 0.3～12, and it is distributed in the height on described flitch and is
100～1500；
Described reaction chamber temperature is 350～1200 DEG C, and pressure is-2～5kPa.
The present invention, by using unique feed auger to construct, can realize biomass material being uniformly distributed on flitch.
Being evenly arranged many radial canals above flitch, raw material is static relative to flitch and radial canal in pyrolytic process, it is ensured that its
Thermally equivalent.During pyrolysis processing, by flitch, feed auger, the joint operation of discharging spiral, can be at the bar of not blowing out
Under part, it is achieved the continuous feed of reactor and discharging, and the classification of thermal decomposition product is reclaimed.
In the present invention, the setting of plenum zone and collection chamber can be substantially reduced the dustiness of pyrolysis gas, it is achieved high temperature pyrolysis
Directly recycling of gas, reduces heat loss, improves heat utilization efficiency.At inside reactor, activation gas import pipe is set,
Pyrolysis biomass while prepare high quality active carbon, it is achieved that multi-use, improve whole device disposal ability and
Efficiency.
Accompanying drawing explanation
Fig. 1 is the left view that low temperature continuous pyrolysis biomass prepare the fixed bed reactors of activated carbon.
Fig. 2 is the top view that low temperature continuous pyrolysis biomass prepare the fixed bed reactors of activated carbon.
Fig. 3 is the front view that low temperature continuous pyrolysis biomass prepare the fixed bed reactors of activated carbon.
Reference in accompanying drawing is as follows:
1-housing；
2,2a, 2b, 2c-radial canal；
3-center bolt；3a-discharging spiral；3b-feed auger；
4-flitch；
5-feeding warehouse；5a-charging aperture；
6-push-pull valve；
7-support；
8-reative cell；
9-drive bearing；
10-substrate；
11-support platform；
12-solid collecting bin；12a-discharging opening；
13-plenum zone；
14-collection chamber；
15-steam jet；
16-steam inlet；
17-reative cell dividing plate.
Detailed description of the invention
Below in conjunction with drawings and Examples, the detailed description of the invention of the present invention is described in more details, in order to energy
The advantage being enough more fully understood that the solution of the present invention and various aspects thereof.But, specific embodiments described below and enforcement
Example is only descriptive purpose rather than limitation of the present invention.
These fixed bed reactors can be not only used for resource and recycle organic compound, can be used for again harmless treatment and discard
Thing, for being prepared activated carbon by biomass in the embodiment of the present invention.Reactor includes four parts: feed system, response system,
Discharge system, housing.The left view of fixed bed reactors that shows respectively below in conjunction with Fig. 1, Fig. 2, Fig. 3, top view, main regard
Figure, illustrates the structure between these four parts and relation thereof.
1. housing: as shown in Figure 1, the housing 1 of fixed bed reactors includes reactor wall, support 7, substrate 10, supports and put down
Platform 11.
Reactor wall includes furnace roof, sidewall, furnace bottom, is used for sealing whole reative cell 8 so that the reaction gas in reative cell 8
Atmosphere is sufficiently spaced from ambient atmosphere.
2. feed system: shown in Fig. 1 and Fig. 3, feed system include the most successively feeding warehouse 5, push-pull valve 6,
Charging aperture 5a.The quantity of feeding warehouse 5 can be one or more.
3. discharge system: as shown in Figure 1, discharge system is made up of discharging opening 12a and solid collecting bin 12.Discharging opening 12a
Under charging aperture 5a, and it is both provided with feeding chute, for charging and the discharging of reactor.The quantity of solid collecting bin 12 can
For one or more.
4. response system: response system includes collection chamber 14, plenum zone 13, reative cell 8 the most successively.
As seen from Figure 3, the bottom of reative cell 8 is provided with flitch 4, is positioned on support platform 11.For the ease of describing,
The two ends of flitch 4 are respectively designated as feed end and discharge end.As seen from Figure 1, discharge end is collected with solid by discharging opening 12a
Storehouse 12 connects.
By Fig. 1, it is respectively provided with a drive bearing 9 at feed end and discharge end.One end of support 7 is fixed on support platform
On 11, the other end connects drive bearing 9.In drive bearing 9, one is drivewheel, and one is driven pulley, for driving flitch 4
Rotate continuously.As required, can arrange several driven pulleys at the interlude of flitch 4, driven pulley upper end contacts with flitch 4 and plays
Supporting role, lower end is fixed in support platform 11.
As shown in Figure 1, feed auger 3b is arranged on the top of flitch 4 feed end, is positioned under charging aperture 5a；Discharging spiral
3a is arranged on the top of flitch 4 discharge end, and discharge end is positioned on discharging opening 12a.In embodiments of the present invention, feed auger
It is additionally provided with level-sensing device between 3b and push-pull valve 6.
Shown in Fig. 2 and Fig. 3, feed auger 3b and discharging spiral 3a are formed by helical blade and center bolt 3, center
Screw rod 3 crosses helical blade.In the embodiment of the present invention, the gap between helical blade is placed equidistant, its lower limb and flitch 4
Vertical dimension is 50～150, and wherein preferred distance is 80.
In other embodiments, the gap between helical blade can use the mode that displacement is arranged, and near mid portion
Helical blade gap, helical blade gap-ratio center bolt two ends is little so that material distribution on flitch 4 is more uniform.
As shown in Figure 2, feed auger 3b is positioned under charging aperture 5a, and helical blade includes left-hand screw blade and right-hand screw leaf
Sheet, center bolt 3 crosses left-hand screw leaf and right-hand screw blade.Left-hand screw blade and right-hand screw blade are perpendicular to center bolt 3
Centrage becomes axial symmetry.In the embodiment of the present invention, the distance between left-hand screw blade and right-hand screw blade is charging aperture 5a bore
1/3～1/2.
In the embodiment of the present invention, the special tectonic of feed auger 3b so that biomass material is from the centre of feed auger 3b
Part is to two end motions, it is possible to reduce material is with the operating distance of feed auger 3b, and realizes the equal of material on wider flitch 4
Even distribution, preferred implementation is for using single feed auger.
In other embodiments, deflector can be set up at the feeding chute of charging aperture 5a, contribute to uniformly dividing of material
Cloth.
As shown in Figure 2, reative cell 8 is provided with 3 radial canals, respectively 2a, 2b, 2c, is denoted as in Fig. 1 and Fig. 3
Radial canal 2.In other embodiments, the quantity of radial canal 2 can be any amount in addition to 3.In the embodiment of the present invention.
Radial canal 2 is evenly arranged in reative cell 8, and parallel with flitch 4, and the vertical height of its distance flitch 4 is 400～550, this
Inventive embodiments is 400.
As seen from Figure 1, being provided with 3 reative cell dividing plates 17 in reative cell 8, reative cell dividing plate 17 is positioned at 3 radial canals
Between and be arranged in parallel, its two ends are connected with steam inlet 16 and steam jet 15 respectively.Steam inlet 16 is tubular structure, position
On 3 radial canals and horizontally disposed, it has 3 gas outlets, and the upper end with 3 reative cell dividing plates 17 connects respectively.Steam
Vapour nozzle 15 has multiple, and the lower end being arranged at reative cell dividing plate 17 communicates therewith, and it is positioned on flitch 4, flat with flitch 4
OK.In other embodiments, the quantity of reative cell dividing plate 17 can be any amount in addition to 3, and corresponding steam inlet 16 goes out
The quantity of QI KOU is identical with the quantity of reative cell dividing plate 17.
In the embodiment of the present invention, plenum zone 13 is a prismatoid, and reative cell is a cube, plenum zone 13
Bottom connects with the top of reative cell 8.Top levels and the trapezoidal oblique section of plenum zone 13 are made by steel plate, thus
Separate with collection chamber 14.The steel plate making trapezoidal oblique section is provided with circular hole, for the circulation of pyrolysis gas.
Collection chamber 14 has vertical plane sidewall and inclined plane sidewall, and the vertical plane sidewall of upright side walls and reative cell 8 connects；
The trapezoidal oblique section sidewall of inclined plane sidewall and plenum zone 13 connects.
Vertical dimension between top and the flitch of plenum zone 13 is 1000～1500, in the embodiment of the present invention,
Preferred distance is 1000～1200mm.Between trapezoidal oblique section and the vertical plane of reative cell 8 of plenum zone 13, angle is
120 °～150 °, optimized angle is 135 °.
The preferred square of whole reactor wall of embodiment of the present invention reactor, it is possible to be designed as cylinder or other shape
Shape.The structure of employing square reactor wall is advantageously in the setting of radial canal 2, so that material is heated evenly, it is ensured that heat
That vents one's spleen uniformly produces and flowing.
The process flow process of the embodiment of the present invention is as follows:
1. ingredient requirement
The fixed bed reactors of the embodiment of the present invention to raw material without be strict with, for obtain higher quality activated carbon, excellent
The particle diameter selecting biomass material is 0.3～12.
2. fill process
Close push-pull valve 6, biomass material is transported in feeding warehouse 5.Stirring rod can be set in feeding warehouse 5, be used for
Prevent the fluffy material phenomenon of material.Opening push-pull valve 6, material under gravity, enters via the feeding chute at charging aperture 5a
The middle part of reative cell 8 leading portion.
Biomass material is continuously conveyed the mid portion to feed auger 3b, along flitch under the effect of feed auger 3b
The both sides of 4 are distributed uniformly.Flitch 4, under the operating of drive bearing 9, can drive biomass to be fed forward, and makes whole flitch 4 equal
Even cloth full with substance.
Level-sensing device can be used for detection and enters the height of materials of reative cell 8, thus controls single inlet amount, it is possible to by regulation
Feed auger 3b, changes the distributed effect of material on flitch 4.
Noble gas access port can be set at push-pull valve 6, in reactor, add biomass material opening push-pull valve 6
Time, it being passed through noble gas, raw material enters in reative cell 8 under the assistance of inert gas flow.Noble gas may select nitrogen, or
For other non-oxidizing gas, meet the anoxybiotic requirement of pyrolytic reaction in reative cell 8.
Fixed bed reactors of the present invention can use the mode that single feeds, it is possible to uses the mode of continuous feed.When required
When the inventory of process is less, the fixed bed reactors in the embodiment of the present invention can be used to operate.If the material processed
Amount is relatively big, can increase the area of flitch 4, keeps the continuous rotation of flitch 4, make material on flitch 4 during pyrolytic reaction
Pyrolytic reaction is completed, it is ensured that charging and the seriality of discharging from feed end to discharge end.
3. entry level
In order to ensure the seriality of biomass material pyrolysis in reative cell 8, the single material storage storage of feeding warehouse 5 must not be lacked
Single material abundance in flitch 4.During pyrolytic reaction, feeding warehouse 5 stores a certain amount of biomass material, protect
On card flitch 4, the height of material is 100～150.
4. pyrolytic process and activation process
Pyrolytic process: fixed bed reactors run within the temperature range of 350～1200 DEG C, biomass material enters reaction
After room 8, under the radiant heat transfer effect of radial canal 2, progressively heat up pyrolysis, is first dried dehydration, then removes volatilization
Point, generate pyrolysis gas and carbonization material.
Activation process: after being pyrolyzed, improves the temperature of every radial canal, is passed through water via steam inlet 16 simultaneously and steams
Vapour.Steam enters heat temperature raising in the reative cell dividing plate 17 being made up of high temperature resistant stainless steel, then is sprayed into by steam jet 15
In reative cell 8.Steam is fully contacted with carbonization material, and under the radiant heat transfer effect of radial canal, carbonization material is activated, from
And prepare activated carbon.
On flitch 4, the low boiling organic matter in upper materials is first pyrolyzed, lower floor's material and high pyrolysis organic compound
After be pyrolyzed, it is ensured that the uniformity that on whole flitch 4, material is heated.
During pyrolytic reaction, reative cell 8 to be controlled is in anoxybiotic atmosphere, and whole activation process is complete under steam atmosphere
Become, maintain the pressure of reative cell 8 in the range of-2～5kPa.
5. mode of heating
The mode of heating of these fixed bed reactors may select Electric heating, fuel mode of heating, high-temperature plasma add
Hot mode etc., the embodiment of the present invention preferred heat accumulation type radiant tube mode of heating, meet combustion heating system and material heat in device
The isolation of solution system.
In pyrolytic process when temperature of charge is less than 280 DEG C, the heating rate of radial canal 2 controls at 40～60 DEG C/min；
When temperature of charge is at 280～450 DEG C, the heating rate of radial canal 2 controls at 20～40 DEG C/min；When temperature of charge exceedes
When 450 DEG C, the heating rate of radial canal 2 controls at 20～60 DEG C/min.
It is 600～850 DEG C that whole pyrolytic process controls the temperature of radial canal 2, and ensures charcoal before carrying out activation process
Minimum temperature >=600 DEG C of compound material.
It is 20～80 DEG C/min that activation process controls the heating rate of radial canal 2, and temperature is 650～1100 DEG C, material temperature
Degree is 600～1000 DEG C.
6. discharging process
Discharging spiral 3a, under the operating of discharging spiral 3a, the activity of preparation is started while starting feed auger 3b
Charcoal enters in solid collecting bin 12 via the feeding chute at discharging opening 12a.
This discharging process can meet flitch 4 while being uniformly distributed biomass material, goes out the activated carbon of preparation
Material, thus ensure charging and the seriality of discharging in reactor.
7. the recycling of pyrolysis gas
The pyrolysis gas that pyrolysis produces expands and is pooled in plenum zone 13, heats up wherein and accelerates cracking, then warp
By the circular hole on the steel plate of trapezoidal oblique section, enter in collection chamber 14.
Circular hole on plenum zone 13 oblique section, the flowing velocity that can make pyrolysis gas is slack-off, causes dust therein to sink
Form sediment and land, thus being lowered into the dustiness of collection chamber 14 pyrolysis gas.Collection chamber 14 both can store pyrolysis gas, in turn, ensures that heat
Vent one's spleen and be in the condition of high temperature, fully reclaim the heat of pyrolysis gas, improve heat utilization efficiency.
The prismatoid structure of plenum zone 13 contributes to collecting pyrolysis gas, and trapezoidal oblique section and reative cell 8 is perpendicular
The size of angle between facing directly, can directly affect flow direction and the time of staying of pyrolysis gas.
These fixed bed reactors discharging required time after being fed to pyrolysis activation is 3～5h, and this time can be subject to
The impact of the physical property of biomass, single inlet amount, heating rate etc..
The fixed bed reactors of the embodiment of the present invention are with one of difference of conventional fixed bed reactor: the present invention consolidates
Fixed bed reactor is after having processed the biomass of single batch, it is not necessary to lower the temperature, and just can carry out the charging of next group biomass
Discharging with activated carbon.Therefore, the radial canal 2 in reactor of the present invention only need to carry out the igniting that goes into operation when feeding first, is connecing
In the whole continuous running got off, only need to maintain the normal heating temperature of radial canal 2.Thus, run at reactor
During, it is to avoid because the liter gentleness of reactor is lowered the temperature by charging each time and discharging, reduce the fault rate of reactor；Difference
Two be: the fixed bed reactors of the present invention can be by controlling the operating between feed auger 3b, flitch 4, discharging spiral 3a
Speed, it is achieved continuous print charging and discharging in pyrolytic process.
Embodiment
Thered is provided the biomass of granularity 0.3～0.6mm as raw material (Biomass aiialysis data are shown in Table 1), material by Manzhouli
First being stored in feeding warehouse 5, open push-pull valve 6, under gravity, the feeding chute at feeding warehouse 5 is slipped to anti-material
Answer in room 8.
Under feed auger 3b rotates and under drive bearing 9 drive, biomass material is evenly distributed on flitch 4, simultaneously
Move horizontally to discharge end.Control feed auger 3b and the speed of drive bearing 9, make the material thickness on whole flitch 4 be
100mm, is then shut off push-pull valve 6.Open radial canal combustion system, when temperature of charge is less than 280 DEG C, control radial canal 2 liters
Temperature speed is 45 DEG C/min；When temperature of charge is higher than 280 DEG C, controlling radial canal 2 heating rate is 25 DEG C/min.Pyrolytic process
Producing pyrolysis gas and carbonization material, reactor pressure controls within 800Pa.
After pyrolytic process does not produces pyrolysis gas, improve every radial canal temperature to 700～950 DEG C, simultaneously by
Steam inlet 16 is passed through water vapour, after the water vapour being passed through is heated up in reative cell dividing plate 17, by steam jet 15
Spraying in reative cell 8, be fully contacted with carbonization material, carbonization material activating obtains activated carbon.After prepared by activated carbon, carry out
The charging of second batch secondary substance, the activated carbon while charging prepared the reaction of fixed bed reactors last time carries out discharging,
Keep the seriality of charging and discharging.The activated carbon transferred out is sent in solid collecting bin 12 and is stored.
Process of the present invention can long-term smooth operation, the productivity of obtained more stable thermal decomposition product is shown in Table 2.
Table 1 biomass material analysis result
Table 2 activated carbon data result
(remarks: M in table 1adRepresent air-dried moisture, AadRepresent empty dry basis ash content, VadRepresent empty butt volatile matter, FCad
Represent empty butt fixed carbon, St,adRepresent empty butt sulfur, CadRepresent empty butt carbon, HadRepresent empty butt hydrogen, QNet.arUnit be
MJ/kg, % are mass percent)
Process described in the embodiment of the present invention can long-term smooth operation, and prepare the activated carbon of high-quality, reactor therefore
Barrier rate is extremely low.
It should be noted that each embodiment above by reference to described by accompanying drawing is only in order to illustrate rather than restriction originally
The scope of invention, it will be understood by those within the art that, the most right
Amendment that the present invention is carried out or equivalent, all should contain within the scope of the present invention.Additionally, indication unless the context
Outward, the word occurred in the singular includes plural form, and vice versa.It addition, unless stated otherwise, then any embodiment
All or part of can use in conjunction with all or part of of any other embodiments.
Claims (10)
1. low temperature continuous pyrolysis biomass prepare fixed bed reactors for activated carbon, and described reactor includes charging aperture, anti-
System, discharging opening, the horizontal level of described charging aperture is answered to set high than the horizontal position of described discharging opening；
Described response system includes collection chamber, plenum zone, reative cell the most successively；Described reative cell has charging
Spiral, discharging spiral, flitch, described flitch include feed end and discharge end, described feed auger be arranged on described charging aperture it
Under, it is positioned at described feed end top；Described discharging spiral is arranged on described discharge end top, and described discharge end is positioned at described discharging
On Kou；
Described feed auger includes center bolt, left-hand screw blade, right-hand screw blade；Described center bolt crosses described left-hand screw
Blade and right-hand screw blade, the centrage that described left-hand screw blade is perpendicular to described center bolt with right-hand screw blade becomes axle pair
Claiming, distance between the two is the 1/3～1/2 of described charging aperture bore；
Described reative cell has reative cell dividing plate, and described reative cell dividing plate two ends connect steam inlet and steam jet respectively, uses
In spraying into steam in described reative cell.
Reactor the most according to claim 1, it is characterised in that described left-hand screw blade and the lower limb of right-hand screw blade
It is 50～150 with the vertical dimension of described flitch, preferably 80；Described left-hand screw impeller clearance and right-hand screw impeller clearance
It is placed equidistant or displacement is arranged.
Reactor the most according to claim 1, it is characterised in that described plenum zone is prismatoid, described reative cell
For cube, the bottom of described plenum zone connects with the top of described reative cell；The top of described plenum zone and institute
The vertical dimension stating flitch is 1000～1500.
Reactor the most according to claim 3, it is characterised in that the trapezoidal oblique section of described plenum zone with described instead
The angle answering the vertical plane of room is 120 °～150 °, preferably 135 °；Described trapezoidal oblique section is made up of steel plate, arranges thereon
There is circular hole.
Reactor the most according to claim 1, it is characterised in that feed end and the discharge end of described flitch are provided with transmission
Bearing, is used for driving described flitch to rotate continuously；Described drive bearing has two or more.
Reactor the most according to claim 5, it is characterised in that also include that housing, described housing include reactor wall, prop up
Support platform, support；
Described reactor wall is used for sealing described reative cell；
Described support platform is arranged under described flitch；
Described support is fixed in described support platform, is used for connecting described drive bearing.
Reactor the most according to claim 1, it is characterised in that described reative cell includes radial canal；
Described radial canal is heat accumulation type radiant tube, is arranged on described flitch top parallel with described flitch；
Vertical dimension between described radial canal and described flitch is 400～550, preferably 400.
8. the method being prepared activated carbon with the reactor one of claim 1-7 Suo Shu by biomass, described method includes
Following steps:
Charging stage: biomass material is transported to via described charging aperture the interlude of described feed auger；
Pyrolysis phase: described biomass material is uniformly distributed along the flitch both sides of described continuous rotation, and in described reative cell
Pyrolytic reaction is occurred to generate carbonization material；
Activation stage: be passed through steam by described steam inlet, described steam enters described reative cell dividing plate and heats up, and is risen
Steam after temperature, after described intensification, steam enters in described reative cell via described steam jet, described carbonization material activating
Obtain activated carbon.
Method the most according to claim 8, it is characterised in that described pyrolysis phase radial canal temperature is 600～850 DEG C；
Described activation stage radial canal temperature is 650～1100 DEG C, and after described intensification, steam temperature is 700～950 DEG C.
Method the most according to claim 8, it is characterised in that the particle diameter of described biomass material is 0.3～12, its
Being distributed in the height on described flitch is 100～1500；
Described reaction chamber temperature is 350～1200 DEG C, and pressure is-2～5kPa.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106744939A (en) * | 2017-02-06 | 2017-05-31 | 成都新火环保科技有限公司 | The method that leaf is converted to activated carbon using plasma combination activator |
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2016
- 2016-08-10 CN CN201610653795.5A patent/CN106281375A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106744939A (en) * | 2017-02-06 | 2017-05-31 | 成都新火环保科技有限公司 | The method that leaf is converted to activated carbon using plasma combination activator |
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