CN106395791A - Spray type kiln of carbon nanotubes and production method thereof - Google Patents
Spray type kiln of carbon nanotubes and production method thereof Download PDFInfo
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- CN106395791A CN106395791A CN201610740258.4A CN201610740258A CN106395791A CN 106395791 A CN106395791 A CN 106395791A CN 201610740258 A CN201610740258 A CN 201610740258A CN 106395791 A CN106395791 A CN 106395791A
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Abstract
Belonging to the technical field of chemical equipment, the invention provides a spray type kiln of carbon nanotubes. The spray type kiln of carbon nanotubes comprises: a feeding system, which is used for conveying a catalyst and a carbon source gas; a reactor, which is used for receiving the catalyst and carbon source gas sent from the feeding system and make them react to react carbon nanotubes; and a bin, which is used for receiving the carbon nanotubes produced by the reactor. The spray type kiln of carbon nanotubes provided by the invention has the advantages of reliable work and high production efficiency.
Description
Technical field
The invention belongs to technical field of chemical, it is related to atomizing kiln and its production method of a kind of CNT,
The atomizing kiln of particularly a kind of achievable large-scale production CNT and its production method.
Background technology
CNT, as a kind of monodimension nanometer material being made up of the coaxial curling of graphite flake, has many exceptions
Mechanics, electricity and chemical property, have more and more important application in the industrial production.The industrialized production of CNT is carbon
The premise that nanotube is applied in the industry.In the production method of CNT, vapour deposition process has that reaction condition is gentle, produces
Amount is big, low cost and other advantages, is the method most possibly realizing industrialized production.
The growth pattern of CNT is affected and restriction by multiple growth conditions, with distribution on carrier for the catalyst,
The factors such as the species of carbon source, growth temperature, hydrogen content are closely related.The design of CNT industrialized production reactor is right
The characteristic of above impact carbon nano tube growth is targetedly designed and is optimized, and could obtain preferable effect.
In prior art, Zhai Meizhen et al. discloses a kind of tower reactor (Application No. CN1454838), this reactor
It is made up of parts such as catalyst container, catalyst quantitative slot, reaction tower, crude product outlet, offgas outlet, unstripped gas outlets,
Set polylith column plate between reactor, control catalyst speed in the reactor.Further, Zhai Meizhen et al. have also been devised one kind
Moving-burden bed reactor (Application No. CN1317446), in this reactor, catalyst continuously dispenses to conveyer belt,
Catalyst reaction is deviate from after generating CNT from conveyer belt, it is achieved thereby that the continuous production of CNT.Wei Fei et al.
Disclose a kind of reactor design (Application No. CN1327943) of fluid bed, in that patent, gas enters from bottom distributor
Enter, by gas fluidized catalyst in reactor and CNT, the industrialized production of CNT can be obtained.Further,
In order to improve the conversion ratio of raw material, Wei Fei et al. have also been devised a kind of multi-stage countercurrent reactor (Application No. CN101049927),
After CNT agglomerate volumetric expansion to a certain extent, from upper level reactor, overfall enters the continuation of next stage reactor instead
Should, gas and solid material counter current contacting between each stage reactor, thus improve the conversion ratio of raw material.And in Application No.
In the patent application of CN102502589, hold high up big in et al. disclose a kind of dress continuously preparing high-purity single/double-wall carbon nano tubes
Put, this device reaction device is made up of down-flow fluidized bed using ECT and riser, and down-flow fluidized bed using ECT is inserted in riser, gas-solid outlet and the lifting of down-flow fluidized bed using ECT
The lower end of the pyramidal structure in pipe or dividing plate is adjacent.
In the prior art it can be seen that foregoing invention is made that beneficial exploration to the industrialized production of CNT,
But with the further investigation to CNT reaction mechanism, the governing factor of the growth course of CNT be there has also been deeper
Understand.Generally believe now that gas-liquid-solid pattern is followed in the vapour deposition process growth of CNT, in this mode, transition gold
Metal catalyst particle is in molten condition, and carbon-source gas molecule produces single carbon atom after decomposing at high temperature, and carbon atom exists
Molten metal particles surface is dissolved, and enters inside metallic particles, then saturation separates out again, generates CNT.
The diameter of CNT is closely related with supported catalyst granular size, and for minor-diameter carbon nanotube,
Its catalyst granules is greatly influenced by temperature, and when catalyst enters reaction zone, generally will experience one section of temperature-rise period, if this
The section heating-up time is long, can cause growing up of catalyst granules.In the industrial production, be usually used methane, ethene, acetylene, third
The organic molecule containing hydrogen atom such as alkene, natural gas is as carbon source, with the carrying out of carbon nano tube growth, carbon atom in carbon source
Cracking deposition generates CNT, and hydrogen atom precipitation in carbon source becomes hydrogen and retains in the reactor, causes hydrogen in reactor
Concentration rising slows down with carbon nanometer tube growth speed.In addition, when using catalyst carrier, because CNT is extremely high
Draw ratio, generates pencil CNT from carrier surface and is mutually wound around, generate agglomerate shape CNT, at the initial stage of growth, urge
Agent and carbon nanotube by volume start to expand, density reduces rapidly, but the latter stage in growth, when length of carbon nanotube reach certain
After degree, agglomerate shape CNT becomes strong due to the inside effect of mutually tangling, and volume cannot expand, and CNT can only be in group
Poly- growth inside, causes density to increase again, soft-agglomerated is changed into rigid agglomerate；Finally, supported catalyst work one section when
Between after can lose activity, lose catalysis, at this moment need will inactivation after CNT removal reactor, carbon could be obtained and receive
The continuous production of mitron.
With going deep into of research, the performance of carbon nano-tube catalyst, the speed of growth of CNT and length all obtain huge
Big lifting, more and more stronger to the demand of minor diameter, superelevation length CNT.By to above carbon nanotube growth process
Governing factor analysis, need to design the consersion unit of new CNT industrialized production, with mate CNT production
Characteristic.
In sum, for solving the deficiency in existing CNT production equipment structure, need to design a kind of reliable operation,
The atomizing kiln of the CNT of efficiency high.
Content of the invention
The purpose of the present invention is to there are the problems referred to above for existing technology it is proposed that a kind of reliable operation, production efficiency
The atomizing kiln of high CNT.
The purpose of the present invention can be realized by following technical proposal：A kind of atomizing kiln of CNT, including：
Feed system, for conveying catalyst and carbon-source gas；
Reactor, for receiving the catalyst that feed system sends and carbon-source gas and making the two react to generate carbon nanometer
Pipe；
Feed bin, for receiving the CNT of reactor generation.
As a further improvement on the present invention, described feed system includes at least one the powder feeding machine for conveying catalyst
Structure, the mechanism of supplying gas for conveying carbon-source gas.
As the further improvement of the present invention, supplying gas, mechanism exit is provided with heat exchanger, and described carbon-source gas are through changing
Reactor is entered after hot device preheating.
As the further improvement of the present invention, the CNT that described reactor generates is accommodated in material after gas solid separation
Storehouse.
As a further improvement on the present invention, described feed system also includes the atomizer matching with powder feeding mechanism, institute
State catalyst to spray in reactor after corresponding atomizer atomization.
As a further improvement on the present invention, described reactor includes the reaction cavity being vertically arranged, and described atomizer is put
In reaction cavity inner upper, it is additionally provided with the gas distribution being connected with heat exchanger and be located at below atomizer in reaction cavity
Device, described atomizer opening down, described carbon-source gas pass through this gas distributor gas distribution in reaction cavity.
As a further improvement on the present invention, described gas distributor is single-row or many along reaction cavity axial direction distribution
Row wireway.
As a further improvement on the present invention, described reactor includes the reaction cavity being vertically arranged, and described atomizer is put
In the internal medium position of reaction cavity, it is provided with the gas distributor being connected with heat exchanger, described carbon-source gas in reaction cavity
By this gas distributor in reaction cavity gas distribution, be additionally provided with reaction cavity be connected with atomizer and be placed in gas distribution
Mozzle in device, described atomizer opening up.
As a further improvement on the present invention, described reactor includes horizontally disposed reaction cavity, described reaction cavity
It is provided with the discharging opening for CNT being discharged into feed bin, described atomizer corresponds setting, described atomization with powder feeding mechanism
Device is connected with corresponding powder feeding mechanism by entering powder passage, and described atomizer is placed in the one end inside reaction cavity away from discharging opening,
Towards discharging opening, described heat exchanger is respectively connected to respectively to enter powder passage and by carbon source gas by inlet channel to the opening of described atomizer
Body imports and respectively enters powder passage so that the catalyst respectively entering in powder passage enters back into corresponding atomizer with after carbon-source gas mixing.
As another improvement of the present invention, the production method of the atomizing kiln of this CNT comprises the following steps：
Catalyst sends into the reaction zone of reactor by powder feeding mechanism；
Carbon-source gas enter the reaction zone of reactor by mechanism of supplying gas after heat exchanger preheating, and carbon-source gas are anti-with catalyst
CNT should be generated；
The CNT generating is accommodated in feed bin after gas solid separation.
Based on technique scheme, the embodiment of the present invention at least can produce following technique effect：Atomizing kiln is overall
Reasonable in design, compact in design and reliable operation, catalyst and carbon-source gas are imported the reaction zone of reactor by feed system
Domain, the production of CNT is to start in the gas phase to grow in catalyst distribution, and catalyst is uniformly dispersed, and reduces and grew
Tangle degree between CNT in journey, the higher speed of growth and higher length of carbon nanotube, the carbon of generation can be obtained
Nanotube sends into feed bin in time, and production efficiency is high, can meet high speed, large-scale production demand.
Brief description
Below in conjunction with the accompanying drawings the specific embodiment of the present invention is described in further detail, wherein：
Fig. 1 is the structural representation of a preferred embodiment of the present invention.
Fig. 2 is the structural representation of second embodiment of the invention.
Fig. 3 is the structural representation of third embodiment of the invention.
In figure, 10, powder feeding mechanism；11st, powder bucket；12nd, fluidized plate；13rd, powder absorbing pipe；14th, pump core；20th, reactor；21st, anti-
Answer cavity；22nd, material survey meter；23rd, components and parts are heated；24th, heat-barrier material；25th, hygrosensor；26th, temperature controller；
30th, feed bin；40th, heat exchanger；50th, atomizer；60th, discharge system；61st, discharge screw；62nd, motor；63rd, mechanical sealing member；70、
Gas distributor；80th, deduster；90th, mozzle；100th, enter powder passage；110th, inlet channel.
Specific embodiment
The following is the specific embodiment of the present invention and combine accompanying drawing, technical scheme is further described,
But the present invention is not limited to these embodiments.
In the prior art, with research going deep into, the performance of carbon nano-tube catalyst, the speed of growth of CNT and
Length all obtains huge lifting, more and more stronger to the demand of minor diameter, superelevation length CNT, needs design a kind of new
The consersion unit of type CNT industrialized production, to mate the characteristic of CNT production.
The present invention protects a kind of atomizing kiln and its production method of CNT, can achieve large-scale production carbon nanometer
Pipe.
Illustrated in more detail with reference to the technical scheme that Fig. 1 to Fig. 3 provides to the present invention.
As shown in Figure 1 to Figure 3, the atomizing kiln of this CNT includes：
Feed system, for conveying catalyst and carbon-source gas；
Reactor 20, for receiving the catalyst that feed system sends and carbon-source gas and making the two react to generate carbon nanometer
Pipe；
Feed bin 30, for receiving the CNT of reactor 20 generation.
According to metallic particles in the position of carbon pipe, the growth pattern of CNT can be divided into apical growth pattern and bottom
Two kinds of growth pattern.Apical growth pattern refers to that catalyst granules is located at CNT top in the growth course of CNT
End, drives CNT constantly to grow under the guiding of air-flow；Bottom growth pattern refers in the growth course of CNT
Catalyst granules is maintained at the top that motionless in substrate, newly-generated CNT is located at catalyst.
Because CNT maintains the higher speed of growth to need in gas phase a large amount of carbon source molecules in catalyst in growth
Surface cracks, and in this process, catalyst granules can carry out high-speed rotation around CNT.In such growth course
In, catalyst surface has violent quality, heat transfer and needs huge rotary inertia, therefore apical growth pattern more
It is beneficial to prepare Seedling height speed, the CNT of high length and perfect structure.The atomizing kiln of the present invention is applied to processing
Speed of growth catalyst faster, is particularly well-suited to apical growth pattern to produce CNT, and this pattern CNT is given birth to
Long speed higher it is ensured that efficient produce and work reliability.
The atomizing kiln overall construction design of this CNT rationally, compact in design and reliable operation, feed system will
Catalyst and the conversion zone of carbon-source gas importing reactor 20, the production of CNT is to be in the gas phase in catalyst distribution
Start to grow, catalyst is uniformly dispersed, reduce in growth course and to tangle degree between CNT, higher life can be obtained
Long speed and higher length of carbon nanotube, the CNT of generation sends into feed bin 30 in time, and production efficiency is high, can meet height
Speed, large-scale production demand.
In the present case, the contact with carbon-source gas for the catalyst can occur can also occur before entering reactor 20
After entering reactor 20, flexibly, versatility is wide for application.
Further, feed system include for convey catalyst at least one powder feeding mechanism 10, be used for conveying carbon source
Mechanism's (not shown) of supplying gas of gas.It is suitable that the setting of powder feeding mechanism 10 can provide before entering reaction zone for catalyst
The temperature-rise period of time, more abundant to ensure catalyst granules reaction；Mechanism of supplying gas then facilitates the importing of carbon-source gas, reduces
Interference with catalyst transport passage.
As further improving, supplying gas, mechanism exit is provided with heat exchanger 40, and carbon-source gas preheat through heat exchanger 40
Enter reactor 20 afterwards.Further, the CNT that reactor 20 generates is accommodated in feed bin 30, gas-solid after gas solid separation
After separating, tail gas draws off, and solid matter is accommodated in feed bin 30.
Present invention also offers the production method of the atomizing kiln of above-mentioned CNT, it comprises the following steps：
Catalyst sends into the reaction zone of reactor 20 by powder feeding mechanism 10；
Carbon-source gas enter reaction zone, carbon-source gas and the catalysis of reactor 20 by mechanism of supplying gas after being preheated through heat exchanger 40
Agent reaction generates CNT；
The CNT generating is accommodated in feed bin 30 after gas solid separation.
Such topology layout, equipment reliable operation and enable the efficient production operation of CNT.
Preferably, feed system also includes the atomizer 50 matching with powder feeding mechanism 10, preferably atomizer 50 and powder feeding
Mechanism 10 correspond setting it is ensured that connect compactness and catalyst transmission reliability, stationarity；Catalyst is through corresponding mist
Spray in reactor 20 after changing device 50 atomization, such catalyst enters atomization during the reaction zone of reactor 20, and uniformly gas powder mixes
Compound.
During work, catalyst is delivered to reactor 20 one end through pneumatic powder feed system (i.e. powder feeding mechanism 10) carrier gas, through mist
It is injected into reactor 20, the catalyst after atomization is directly entered reaction zone, reduces the heating of catalyst after changing device 50 atomization
Time, reduce the coalescence of metal nanoparticle in catalyst, be particularly suited for minor-diameter carbon nanotube, such as single wall, double-walled carbon
The growth of nanotube.In the present invention, the production of CNT is that catalyst distribution starts to grow in the gas phase, and catalyst divides
Dissipate uniformly, reduce in growth course and to tangle degree between CNT, the higher speed of growth and higher carbon can be obtained
Nanotube length.
In the present invention, as the preferred or optional embodiment of one kind, as shown in figure 1, preferred reactor 20 includes erecting
The reaction cavity 21 of straight setting, atomizer 50 is placed in reaction cavity 21 inner upper, is additionally provided with and heat exchange in reaction cavity 21
Device 40 is connected and the gas distributor 70 positioned at atomizer 50 lower section, opening down (preferably straight down) of atomizer 50,
Carbon-source gas pass through this gas distributor 70 gas distribution in reaction cavity 21.
Further, for lifting gas distribution effect and feed stock conversion, preferably gas distributor 70 is along reaction cavity 21 axle
Single-row or multiple row wireway to distribution.
Fig. 1 of the present invention discloses a kind of vertical downstream atomizing kiln it is adaptable to carbon nanometer tube growth speed is higher
Situation, gained CNT tangles low degree each other, and CNT has higher length.Especially, carbon-source gas
By gas distributor 70 in reactor 20 gas distribution, compensate for the density of hydrogen that CNT causes in growth course and increase
Plus, be conducive to improving feed stock conversion.
The powder feeding mechanism 10 of preferably above-mentioned atomizing kiln includes powder bucket 11, the fluidized plate 12 being arranged in powder bucket 11, inserts
The powder absorbing pipe 13 that is located in powder bucket 11, for connecting powder absorbing pipe 13 and the pump core 14 of corresponding atomizer 50, preferably fluidized plate 12 is in
Cellular arranges and is placed in powder bucket 11 near bottom position, and pump core 14 rear also can connect another road-load gas, to adjust powder sending quantity.
Further preferably powder feeding mechanism 10 is single, and atomizer 50 is also configured as corresponding single, and the going out of atomizer 50
Mouth-shaped is horn-like in what Open Side Down.The CNT being also preferably generated passes through discharge system 60 through heat exchanger 40 heat exchange heel row
Enter in (i.e. material collection storehouse) in feed bin 30, above-mentioned atomizing kiln also includes deduster 80 (preferably impulse bag), deduster
80 are connected with feed bin 30, and the tail gas in feed bin 30 enters this deduster 80, and then realizes gas solid separation, and the tail gas after filtration is permissible
Directly discharge or recycling are processed.
In the present case, the inner chamber of reaction cavity 21 is the reaction zone of reactor 20, and the inner chamber of reaction cavity 21 is provided with
For drawing off the discharging opening of CNT, and the material that above-mentioned reactor 20 preferably also includes being inserted on reaction cavity 21 detects
Instrument 22, the heating components and parts 23 being built on reaction cavity 21 side wall, be filled on reaction cavity 21 side wall and with heating unit device
Hygrosensor 25 that the close-fitting heat-barrier material 24 of part 23 is connected with reaction cavity 21 inner chamber, it is placed in outside reaction cavity 21
And the temperature controller 26 with hygrosensor 25 electrical connection.
Corresponding, preferably above-mentioned discharge system 60 include the discharge screw 61 connecting with the discharging opening of reaction cavity 21 and
The motor 62 that discharge screw 61 head end is connected, the head end of discharge screw 61 seals also by mechanical sealing member 63, discharge screw 61
End be connected with feed bin 30, above-mentioned heat exchanger 40 is contacted with the middle part of discharge screw 61, during realizing discharge system 60 discharging
The heat exchange of CNT.
Specifically, the production process of the kiln of vertical downstream atomizing shown in Fig. 1 is as follows：On the one hand, at catalyst upon activation
Put into after reason in sealing powder bucket 11；Bottom of the barrel sets a cellular fluidized plate 12, and carrier gas enters powder bucket 11 top after fluidized plate 12
And top material is fluidized；Catalyst after fluidisation enters pump core 14 through powder absorbing pipe 13, terminates another road-load after pump core 14
Gas is to adjust powder sending quantity；Catalyst enters atomizer 50 through duff pipe, and atomizer 50 surface is provided with multiple micropores, in the height of gas
Under speed belt moves, catalyst is uniformly sprayed in whole reaction cavity 21 from reaction cavity 21 top.
On the other hand, carbon-source gas enter heat exchanger 40 after proportioning and preheat, and enter gas distributor through pipeline after preheating
70, gas distributor 70 be along reaction cavity 21 axially arranged (preferably axially be arrangeding in parallel) multiple row wireway (preferably
Pipe), have multiple steam vents in air guide pipe surface, the gas after preheating enters in reaction cavity 21 through steam vent.
In reaction cavity 21, catalyst is reacted with carbon-source gas, and newly-generated CNT is settled down to reaction chamber
The CNT material section top of reaction in body 21, continues reaction in this stage CNT；Above-mentioned material survey meter 22, reaction
Cavity 21, heating components and parts 23, heat-barrier material 24, hygrosensor 25, temperature controller 26 constitute anti-in this embodiment
Answer device 20；Height in reactor 20 for the CNT is measured by material survey meter 22.
Above-mentioned motor 62, mechanical sealing member 63 and discharge screw 61 constitute discharge system 60, react gained CNT
Discharged by screw rod, arranged material, after heat exchanger 40 heat exchange, falls into feed bin 30, tail gas is discharged after sack cleaner 80 purification.
In Fig. 1 disclosed embodiment, because catalyst is brought directly to reaction zone by air-flow, reduce the heating of catalyst
Time, reduce the coalescence of metal nanoparticle in catalyst, be particularly suited for minor-diameter carbon nanotube, such as single wall, double-walled carbon
The growth of nanotube.
In the present invention, also disclose the second embodiment of atomizing kiln, as shown in Fig. 2 preferred reactor 20 is wrapped
Include the reaction cavity 21 being vertically arranged, atomizer 50 is placed in the internal medium position of reaction cavity 21, is provided with reaction cavity 21
The gas distributor 70 being connected with heat exchanger 40, carbon-source gas pass through this gas distributor 70 gas distribution in reaction cavity 21,
It is additionally provided with the mozzle 90 being connected with atomizer 50 and being placed in gas distributor 70, the opening of atomizer 50 in reaction cavity 21
Upward (preferably straight up).
Further, for lifting gas distribution effect and feed stock conversion, the gas distributor 70 of preferably this embodiment is also edge
The single-row or multiple row wireway that reaction cavity 21 is axially distributed.
It is also a kind of vertical downstream atomizing kiln disclosed in Fig. 2 of the present invention, this second embodiment is real disclosed in Fig. 1
Increased a mozzle 90 on the basis of applying example, increased the catalyst time of staying in the gas flow, and have adjusted atomizer 50
With the topology layout of gas distributor 70, reduce further and tangle degree between carbon pipe, be particularly suited for overlength carbon nanometer
The production of pipe.Likewise, carbon-source gas pass through gas distributor 70 gas distribution in reactor 20, compensate for CNT in growth
During the density of hydrogen that causes increase, be conducive to improving feed stock conversion.
Preferably disclosed in second embodiment of the invention, above-mentioned atomizing kiln also includes discharge system 60 and deduster 80, and
Powder feeding mechanism 10 structure of this atomizing kiln, discharge system 60, deduster 80 and reactor 20 structure all real with first
Apply example identical, no longer excessively repeat herein.Corresponding, the atomizer 50 of this embodiment opening up.
Specifically, the production process of the kiln of vertical downstream atomizing shown in Fig. 2 is as follows：On the one hand, at catalyst upon activation
Put into after reason in sealing powder bucket 11, bottom of the barrel sets a cellular fluidized plate 12, and carrier gas enters powder bucket 11 top after fluidized plate 12
Top material is fluidized；Catalyst after fluidisation enters pump core 14 through powder absorbing pipe 13, terminates another road-load gas after pump core 14
To adjust powder sending quantity；Catalyst enters atomizer 50 through duff pipe, and there are multiple micropores on atomizer 50 surface, in the hyper tape of gas
Under dynamic, catalyst enters reaction cavity 21, and under the high speed of gas drives, catalyst sprays from dispersive nozzle, enters mozzle
90；In mozzle 90, gas carries catalyst and travels upwardly, and in mozzle 90 end, catalyst enters reaction cavity 21 inner chamber
Overhead simultaneously slowly settles under gravity, falls into CNT material section top.Herein it is worth mentioning at this point that：Led by controlling
The diameter of flow tube 90 and carrier gas flux, adjustable CNT time of staying in mozzle 90.
On the other hand, reacting gas (i.e. carbon-source gas) enters heat exchanger 40 after proportioning and preheats, and enters through pipeline after preheating
Enter gas distributor 70, gas distributor 70 is along the axially in parallel multiple row wireway of reaction cavity 21 (preferably pipe),
Air guide pipe surface has multiple steam vents, and the gas after preheating enters in reactor 20 through steam vent and catalyst reaction, reaction
CNT afterwards is deposited in reaction cavity 21 bottom；Height in reactor 20 for the CNT is surveyed by material survey meter 22
Fixed；Reaction gained CNT is discharged by discharge screw 61, and arranged material, after heat exchanger 40 (i.e. heat exchanger) heat exchange, falls into
Feed bin 30, tail gas is discharged after sack cleaner 80 purification.
In the present invention, also disclose the third embodiment of atomizing kiln, as shown in figure 3, preferred reactor 20 is wrapped
Include horizontally disposed reaction cavity 21, reaction cavity 21 is provided with the discharging opening for CNT is discharged into feed bin 30, atomizer
50 correspond setting with powder feeding mechanism 10, and atomizer 50 is connected with corresponding powder feeding mechanism 10 by entering powder passage 100, atomizer
50 are placed in the one end inside reaction cavity 21 away from discharging opening, and the opening of atomizer 50 (is set to level court towards discharging opening
To preset direction), heat exchanger 40 is respectively connected to respectively to enter powder passage 100 by inlet channel 110 and imports respectively to enter by carbon-source gas
Powder passage 100 is so that the catalyst respectively entering in powder passage 100 enters back into corresponding atomizer 50 with after carbon-source gas mixing.
Further, it is improve production efficiency it is ensured that the reliably working of internal-response；Preferably powder feeding mechanism in this embodiment
10 are set to multiple, and that is, atomizer 50 is also configured as multiple (can be more preferably three, such topology layout not only can be expired
Foot is actually needed, and also makes the space layout more reasonable, compact), and it is preferably multiple and opening direction vertically arranged in parallel
Unanimously.
Fig. 3 of the present invention discloses a kind of horizontal concurrent spray formula kiln, and in this third embodiment, reaction cavity 21 is
Horizontal, adopt multiple atomizers 50 (spraying nozzle) at top, take product out of reaction using reacting gas itself air-flow
Area is it is adaptable to the production of ultra-large CNT.
Preferably disclosed in third embodiment of the invention, above-mentioned atomizing kiln also includes deduster 80 but eliminates similar
Discharge system 60 structure, and in the present embodiment, after the CNT that reactor 20 is sent is directly over heat exchanger 40 heat exchange
Enter deduster 80, after reduster 80 gas solid separation, solid matter (solid-phase material) falls in feed bin 30.Additionally, this spraying
Powder feeding mechanism 10 structure of formula kiln, deduster 80 and the structure of reactor 20 and first embodiment are essentially identical, herein not
After repeating more.
Specifically, shown in Fig. 3, the production process of horizontal concurrent spray formula kiln is as follows：Catalyst upon activation is put into after processing
In sealing powder bucket 11, bottom of the barrel sets a cellular fluidized plate 12, and carrier gas enters powder bucket 11 top to headpiece after fluidized plate 12
Material is fluidized, and the catalyst after fluidisation enters pump core 14 through powder absorbing pipe 13；Terminate another road-load gas after pump core 14 to send to adjust
Powder amount, catalyst air-flow enters atomizer 50 after mixing with carbon-source gas, and there are multiple micropores on atomizer 50 surface, in the height of gas
Under speed belt moves, catalyst enters reaction cavity 21；Reactor 20 is by reaction cavity 21, heating components and parts 23, heat-barrier material 24, temperature
Degree detector 25, temperature controller 26 are constituted；Reacted CNT is taken out of from the discharging opening of afterbody under airflow function, then
Enter heat exchanger 40 (heat exchanger), enter sack cleaner 80 after heat exchanger 40 heat exchange, carry out gas-solid in deduster 80 and divide
From rear, solid-phase material falls into feed bin 30, discharges after tail gas clean-up.
Specific embodiment described herein is only explanation for example to present invention spirit.The affiliated technology of the present invention is led
The technical staff in domain can be made various modifications or supplement or replaced using similar mode to described specific embodiment
Generation, but the spirit without departing from the present invention or surmount scope defined in appended claims.
Claims (10)
1. a kind of CNT atomizing kiln it is characterised in that：Including：
Feed system, for conveying catalyst and carbon-source gas；
Reactor, for receiving the catalyst that feed system sends and carbon-source gas and making the two react to generate CNT；
Feed bin, for receiving the CNT of reactor generation.
2. a kind of CNT according to claim 1 atomizing kiln it is characterised in that：Described feed system includes
For conveying at least one powder feeding mechanism, the mechanism of supplying gas for conveying carbon-source gas of catalyst.
3. a kind of CNT according to claim 2 atomizing kiln it is characterised in that：In mechanism exit of supplying gas
It is provided with heat exchanger, described carbon-source gas enter reactor after heat exchanger preheating.
4. a kind of CNT according to claim 3 atomizing kiln it is characterised in that：Described reactor generates
CNT is accommodated in feed bin after gas solid separation.
5. a kind of CNT according to claim 4 atomizing kiln it is characterised in that：Described feed system is also wrapped
Include the atomizer matching with powder feeding mechanism, described catalyst sprays in reactor after corresponding atomizer atomization.
6. a kind of CNT according to claim 5 atomizing kiln it is characterised in that：Described reactor includes erecting
The reaction cavity of straight setting, described atomizer is placed in reaction cavity inner upper, is additionally provided with and heat exchanger phase in reaction cavity
Even and be located at gas distributor below atomizer, described atomizer is opening down, and described carbon-source gas are divided by this gas
Cloth device gas distribution in reaction cavity.
7. a kind of CNT according to claim 6 atomizing kiln it is characterised in that：Described gas distributor is
The single-row or multiple row wireway being axially distributed along reaction cavity.
8. a kind of CNT according to claim 5 atomizing kiln it is characterised in that：Described reactor includes erecting
The reaction cavity of straight setting, described atomizer is placed in the internal medium position of reaction cavity, is provided with and heat exchanger in reaction cavity
Connected gas distributor, described carbon-source gas pass through this gas distributor gas distribution in reaction cavity, in reaction cavity also
Be provided with the mozzle being connected with atomizer and being placed in gas distributor, described atomizer opening up.
9. a kind of CNT according to claim 5 atomizing kiln it is characterised in that：Described reactor includes water
The reaction cavity of flat setting, described reaction cavity is provided with the discharging opening for CNT is discharged into feed bin, described atomizer with
Powder feeding mechanism corresponds setting, and described atomizer is connected with corresponding powder feeding mechanism by entering powder passage, and described atomizer is placed in
Away from one end of discharging opening inside reaction cavity, towards discharging opening, described heat exchanger passes through air inlet and leads to the opening of described atomizer
Road is respectively connected to respectively enter powder passage and carbon-source gas importing is respectively entered powder passage so that respectively entering the catalyst in powder passage and carbon source
Corresponding atomizer is entered back into after gas mixing.
10. a kind of atomizing kiln of the CNT described in claim 4 production method it is characterised in that：It include with
Lower step：
Catalyst sends into the reaction zone of reactor by powder feeding mechanism；
Carbon-source gas enter the reaction zone of reactor by mechanism of supplying gas after heat exchanger preheating, and carbon-source gas are given birth to catalyst reaction
Become CNT；
The CNT generating is accommodated in feed bin after gas solid separation.
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| CN201610740258.4A CN106395791A (en) | 2016-08-26 | 2016-08-26 | Spray type kiln of carbon nanotubes and production method thereof |
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| CN108455569A (en) * | 2018-04-18 | 2018-08-28 | 复旦大学 | A kind of feed liquor system of the continuous extensive preparation facilities of carbon nano-tube fibre |
| CN108467024A (en) * | 2018-05-30 | 2018-08-31 | 合肥百思新材料研究院有限公司 | A kind of fluid bed preparing carbon nanotube based on chemical vapour deposition technique batch |
| CN111282763A (en) * | 2019-09-10 | 2020-06-16 | 沈健民 | Atomization device for carbon nanotube film production equipment |
| CN113490638A (en) * | 2019-02-22 | 2021-10-08 | 住友电气工业株式会社 | Method for producing carbon nanotube, method for producing carbon nanotube assembly line bundle, carbon nanotube production apparatus, carbon nanotube assembly line production apparatus, and carbon nanotube assembly line bundle production apparatus |
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| CN113490638A (en) * | 2019-02-22 | 2021-10-08 | 住友电气工业株式会社 | Method for producing carbon nanotube, method for producing carbon nanotube assembly line bundle, carbon nanotube production apparatus, carbon nanotube assembly line production apparatus, and carbon nanotube assembly line bundle production apparatus |
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