CN111517300B - Production process of carbon nanomaterial - Google Patents
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- CN111517300B CN111517300B CN201910109000.8A CN201910109000A CN111517300B CN 111517300 B CN111517300 B CN 111517300B CN 201910109000 A CN201910109000 A CN 201910109000A CN 111517300 B CN111517300 B CN 111517300B
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Abstract
The invention discloses a production process of a carbon nanomaterial, which comprises the following steps: the carbon source enters one or more groups of super-current reactors in a gas form through a carbon source air inlet pipe to be decomposed; the mixture obtained by decomposition enters a separator, the carbon nano material is obtained by collection, and the gas is discharged from an outlet. The invention adopts the super-electric current to discharge the carbon source, has large treatment capacity, low energy consumption, high production efficiency, high product quality, small defects and capability of expanding the production scale, and meets the industrial requirements.
Description
Technical Field
The invention provides a production process of a carbon nanomaterial.
Background
The carbon nanomaterial mainly comprises fullerene, carbon nanotube, graphene and the like, and has wide application prospect due to unique structure and excellent mechanical, electrical, chemical and other properties. Wherein Graphene is a polymer of carbon atomsspThe two-dimensional carbon nanomaterial with hexagonal lattice and honeycomb lattice is excellent in optical, electrical and mechanical properties, has important application prospects in the aspects of materialization, micro-nano processing, energy, biomedicine, drug delivery and the like, and is considered as a revolutionary material in the future. Common methods for producing graphene powder are a micromechanical lift-off method, an orientation attached growth method, an epitaxial growth method, a graphite oxide reduction method and a Chemical Vapor Deposition (CVD) method.
Among them, the micro-mechanical exfoliation method is the simplest one, namely, separating graphene or graphene nanoplatelets from a graphite crystal by applying mechanical force to the graphite crystal. The method has the advantages of simple process, low preparation cost and high sample quality, but the method has some disadvantages, such as the obtained product is not easy to control in size, and graphene with enough length cannot be reliably prepared, so that the method cannot meet the industrial requirement.
Peter w.sutter et al used rare metal ruthenium as a growth substrate by an epitaxy method, and "seeded" with graphene using the growth substrate atomic structure. The single-layer graphene obtained by the method has satisfactory performance, but the graphene sheet produced by the method is often uneven in thickness, and the adhesion between the graphene and the matrix can influence the characteristics of the prepared graphene sheet.
The epitaxial growth method is to epitaxially grow a graphite layer on the surface of a single crystal and then peel the graphite layer from a substrate by chemical etching. There are two common methods, one is SiC surface decomposition and one is molecular beam deposition. Graphene with the thickness of 1-2 carbon atoms can be prepared by adopting an epitaxial growth method, but large-area graphene with uniform thickness is difficult to obtain.
The graphite oxide contains epoxy groups, hydroxyl groups, carbonyl groups, carboxyl groups and other oxygen-containing groups, and can be dissolved in water and certain organic solvents. Graphene can be produced by a graphite oxide reduction method. The method has the advantages of low cost, high efficiency, environmental protection and large-scale industrial production, but has the disadvantage of easily causing loss of some physical and chemical properties.
The chemical vapor deposition method is to deposit a layer of transition metal film (such as Fe, cu, ni, pt, au) as a substrate, make use of the high temperature solid solution of the transition metal film and C, then cool and separate out the transition metal film, and reconstruct the surface to form the graphene. The method has the advantages that the method is beneficial to preparing the graphene with larger area; the defects are that the number of layers is difficult to control accurately, metal substrate stripping and substrate transferring are needed, the cost is high, and the process is complex.
It follows that the production of carbon nanomaterials is mainly faced with several problems: the method can not continuously produce a large amount of carbon nano materials, has good quality and uneven product quality, has high product cost, can not be widely applied, has long production process and low efficiency.
Disclosure of Invention
The invention aims to overcome the defects that the production efficiency of the carbon nano material is low, the product quality is good and uneven, the cost is high, the production process is long, and continuous mass production cannot be realized in the prior art, and provides the production process of the carbon nano material, which adopts the super-electric current to discharge the carbon source, has the advantages of large treatment capacity, low energy consumption, high production efficiency, high product quality, small defects, suitability for industrial requirements and expandable production scale.
The invention solves the technical problems by the following technical proposal:
the invention provides a production process of a carbon nanomaterial, comprising the following steps: the carbon source enters one or more groups of super-current reactors in a gas form through a carbon source air inlet pipe to be decomposed; the mixture obtained by decomposition enters a separator, carbon nano materials are obtained by collection, and gas is discharged from an outlet;
the carbon source is a hydrocarbon-containing gas;
each group of the super-electric current reactors consists of a positive polarity super-electric current reactor and a negative polarity super-electric current reactor which are sequentially connected in series along the air flow direction through connecting pipelines;
the positive polarity super-current reactor comprises a first insulating shell with a first inlet and a first outlet, wherein the first inlet is communicated with the carbon source air inlet pipe; at least one group of discharging components are arranged in the first insulating shell, each discharging component comprises at least one PCB (printed circuit board) with discharging needles uniformly distributed on two sides and two discharging plates arranged on two sides of the PCB, and the discharging needles are uniformly distributed on one surface of each discharging plate opposite to the PCB;
in the discharging assembly, a parallel gas channel is formed between the PCB and the discharging plate, an air inlet of the gas channel is communicated with the first inlet, and an air outlet of the gas channel is communicated with the first outlet;
the negative polarity supercurrent reactor comprises a second insulated housing having a second inlet in communication with the first outlet of the positive polarity supercurrent reactor and a second outlet in communication with the separator; and a conductive layer and at least two hollow electrodes are coaxially arranged in the second insulating shell from outside to inside.
The invention adopts the supercurrent to discharge the carbon source, the gas entering the supercurrent reactor is regarded as zero potential, the gas and the high-voltage electrode in the supercurrent reactor are subjected to micro-discharge, the adjacent supercurrent reactor is set to be heteropolarity, the voltage difference is doubled, the substance flowing out of the positive-polarity supercurrent reactor is positively charged, and the positively charged substance is decomposed into carbon nano-materials at the moment of flowing into the negative-polarity supercurrent reactor.
Preferably, the hydrocarbon is methane (CH 4 ) Benzene (C) 6 H 6 ) Toluene (C) 7 H 8 ) Xylene (C) 8 H 10 ) And acenaphthene.
More preferably, the hydrocarbon content in the carbon source is 1% by volume or more. Further, the volume percentage content of hydrocarbon in the carbon source is more than 99%, and the gas with the purity higher than 99% is used, so that the purity of the carbon nano material product is improved.
The flow rate of the carbon source can significantly influence the decomposition efficiency of the carbon source, and preferably, the flow rate of the carbon source is below 5 m/s; more preferably, the flow rate of the carbon source is 1m/s or less.
Preferably, the air inlet volume of the carbon source is 100-200000 m 3 /h。
The decomposition efficiency of the carbon source is related to the number of groups of the super-electric current reactor, and preferably the number of groups of the super-electric current reactor is 2 or more. More preferably, the number of groups of the super-electrofluid reactors is 5 or more.
When more than one set of said super-electric flow reactors are present, they may be connected in series or in parallel as desired by means of pipes, preferably by means of connecting pipes.
The number of the super-electric current reactors is also related to the type of the carbon source gas to be treated and the treatment effect, and the number of the super-electric current reactors required for high linking strength of the carbon source gas is large. For example, when the carbon source is benzene, 80% of the carbon source can be decomposed using a 2-set of super-electric flow reactors, and 95% of the carbon source can be decomposed using a 3-set of super-electric flow reactors. The length of the connecting pipe is related to the flow rate of the carbon source, and preferably, when the flow rate of the carbon source is 1m/s or less, the length of the connecting pipe is at least 2m; when the flow rate of the carbon source is more than 1m/s and less than 5m/s, the length of the connecting pipeline is at least 3m.
The decomposition efficiency of the carbon source is controlled by reasonably adjusting the group number of the super-electric current reactors and the flow rate of the carbon source, and when the group number of the super-electric current reactors is more than 3 groups, the flow rate of the carbon source is below 5m/s, and the decomposition efficiency of the carbon source is more than 45%; when the number of groups of the super-electric current reactor is more than 6, the flow speed of the carbon source is less than 5m/s, and the decomposition efficiency of the carbon source is more than 80%.
The working power of the super-current has an important influence on the morphology of the carbon nanomaterial, and preferably, the working voltage of the first high-voltage direct-current power supply and/or the second high-voltage direct-current power supply is 80 KV-300 KV, and the working current is 0.1A-8A.
In the positive polarity super-current reactor, the number of groups of the discharge components is at least 1, and when the number of groups of the discharge components is more than one group, the discharge components are connected in parallel.
In the positive polarity super-current reactor, the number of the PCB boards is at least 1. When the number of the PCB boards is more than one, the PCB boards are connected in parallel.
Preferably, the PCB board and the discharge board are connected in parallel with an anode of a first high-voltage dc power supply, and a cathode of the first high-voltage dc power supply is grounded.
In the negative polarity super-current reactor, the hollow electrodes are mutually sleeved. Preferably, any one of the hollow electrodes is connected with a negative electrode of a second high-voltage direct-current power supply, and a positive electrode of the second high-voltage direct-current power supply is grounded.
In the negative polarity super-current reactor, the hollow electrodes comprise a plurality of discharge rings connected end to end, and preferably, the discharge rings are provided with a discharge sharp edge part which is beneficial to improving the power density of the hollow electrodes for releasing super-current.
Preferably, the separator comprises at least one spray tower and a drying device, redundant gas is discharged through a gas outlet of the spray tower after the mixture enters the spray tower, a bottom outlet of the spray tower is communicated with an inlet of the drying device, and the carbon nanomaterial is obtained after drying.
The drying apparatus may be a conventional drying apparatus in the art, preferably the drying apparatus is a freeze drying apparatus or a vacuum drying apparatus.
In the separator, the spray tower sprays with deionized water.
Controlling the gas discharge amount of the spray tower to ensure that the pressure of the carbon source gas is 0.5kg/cm higher than the pipeline pressure 2 Above, in order to ensure that the carbon source gas intake is normal.
When the number of the spray towers is plural, the spray towers can be connected in series or in parallel as required. More preferably, in order to ensure continuous production, the number of the spray towers is 2, and the spray towers are connected in parallel, so that switching is performed when material is taken out, and continuous production is maintained.
The gas outlet of the spray tower is also connected with a gas separation device for separating and collecting hydrogen generated by decomposition of the super-electric current reactor, and the residual gas is subjected to waste gas treatment or returned to the super-electric current reactor.
The gas separation device may be a gas separation device conventional in the art, preferably the gas separation device separates and collects hydrogen by pressure swing adsorption or molecular sieves.
Preferably, the carbon nanomaterial is of a single-layer sheet structure, the sheet diameter is 0.1-50 μm, and the thickness is 0.4-1.2 μm.
On the basis of conforming to the common knowledge in the field, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the invention.
In the present invention, unless otherwise specified, "decomposition efficiency" of a carbon source refers to the percentage of the carbon source that enters the super-electric current reactor of the present invention to be decomposed,
wherein, the method comprises the steps of, wherein,VOL 1 refers to the volume percent content of hydrocarbon in the carbon source entering the super-electric flow reactor of the invention,VOL 2 refers to the volume percent of hydrocarbons in the gas leaving the separator of the present invention.
The invention has the positive progress effects that:
(1) The super-current reactor has no ozone generation in the working process, has an explosion-proof function, has self-cleaning capability of the electrode in the cavity, and is easy to maintain; the production system of the invention has low energy consumption, and the power consumption is only 1/100 of that of the traditional plasma reactor.
(2) The production system can produce the carbon nano material with extremely high quality and few defects and meets the industrial requirements; the process is stable, the cost is low, and the service life of equipment is long; the production scale can be enlarged, and the process can be duplicated.
Drawings
FIG. 1 is a schematic view of the production process of the carbon nanomaterial of embodiment 1 of the present invention;
FIG. 2 is a schematic structural view of a super-current reactor according to example 1 of the present invention;
FIG. 3 is a schematic diagram of the positive polarity supersonic flow reactor of example 1 of the present invention;
FIG. 4 is a schematic diagram of the wiring of a positive polarity superconducting current reactor of example 1 of the present invention;
FIG. 5 is a schematic diagram of a negative polarity super-current reactor according to example 1 of the present invention;
FIG. 6 is a schematic cross-sectional view of a negative polarity super-current reactor according to example 1 of the present invention;
FIG. 7 is a schematic diagram showing the structure of hollow electrode of negative polarity super-current reactor in example 1 of the present invention;
FIG. 8 is an SEM image of the carbon nanomaterial prepared in example 1 of the present invention;
FIG. 9 is an AFM image of the carbon nanomaterial prepared in example 1 of the present invention, wherein (a) is an AFM topography of the carbon nanomaterial; (b) is an AFM perspective view of the carbon nanomaterial.
Reference numerals illustrate:
1-a carbon source air inlet pipe and 2-a connecting pipeline;
11-positive polarity super-electric current reactor, 12-negative polarity super-electric current reactor;
101-a first inlet, 102-a first outlet, 103-a first insulating shell, 104-a PCB (printed circuit board), 105-a discharge plate, 106-a discharge needle and 107-a first high-voltage direct current power supply;
111-second inlet, 112-second outlet, 113-second insulating housing, 114-conductive layer, 115, 116, 117 and 118-hollow electrode, 119-discharge ring;
31-spray tower, 32-drying device, 33-gas separation device.
Detailed Description
The invention is further illustrated by means of the following examples, which are not intended to limit the scope of the invention. The experimental methods, in which specific conditions are not noted in the following examples, were selected according to conventional methods and conditions, or according to the commercial specifications.
Example 1
As shown in fig. 1, the present embodiment provides a process for producing a carbon nanomaterial using benzene as a carbon source, including:
(1) At a concentration of 600mg/m 3 Benzene gas of (2) is taken as a carbon source, and enters 2 groups of super-electric current reactors connected in series through a carbon source air inlet pipe 1 at an air inlet rate of 1000 m/h at an air speed of 5m/s for decomposition; the external dimensions of the positive and negative super-current reactors 11 and 12 are 4×0.6×0.8m (long×wide×high). The length of the connecting pipe 2 between the positive and negative super-electric current reactors 11 and 12 is 3m. The positive polarity super-current reactor 11 has a simple structure, and has large contact areas of a PCB, a discharge plate and gas and large treatment capacity; the negative polarity super-current reactor 12 increases the super-current discharge area by designing a plurality of hollow electrodes coaxially arranged, so that the carbon source is intensively decomposed in the reactor.
As shown in fig. 2 to 7, each group of the super-electric current reactors is composed of a positive polarity super-electric current reactor 11 and a negative polarity super-electric current reactor 12 which are sequentially connected in series in the air flow direction through the connecting pipe 2.
The positive polarity super-current reactor 11 includes a first insulated housing 103 having a first inlet 101 and a first outlet 102; two groups of discharging assemblies are arranged in the first insulating shell 103, each discharging assembly comprises a PCB 104 with discharging needles 106 uniformly distributed on two sides and two discharging plates 105 arranged on two sides of the PCB, and the discharging needles 106 are uniformly distributed on one surface of each discharging plate 105 opposite to the PCB 104;
a parallel gas channel is formed between the PCB 104 and the discharge plate 105; the gas inlet of the gas channel is communicated with the first inlet 101, and the gas outlet of the gas channel is communicated with the first outlet 102;
the PCB 104 and the two discharge plates 105 are connected in parallel with the positive pole of a first high voltage dc power supply 107, and the negative pole of the first high voltage dc power supply 107 is grounded.
The negative polarity super-electric current reactor 12 comprises a second insulated housing 113 having a second inlet 111 and a second outlet 112, wherein the first inlet 101 of the positive polarity super-electric current reactor 11 is in communication with the carbon source inlet pipe 1, the first outlet 102 is in communication with the second inlet 111 of the negative polarity super-electric current reactor 12, and the second outlet 112 of the negative polarity super-electric current reactor 12 is in communication with the separator.
The second insulating housing 113 is coaxially provided with a conductive layer 114 and four hollow electrodes 115-118 sleeved with each other from outside to inside. Each of the hollow electrodes 115 to 118 includes a plurality of discharge rings 119 having a discharge tip portion connected end to end.
Since the voltage in the negative polarity super-current reactor 12 is high, the second insulating housing 113 is easily broken down, and in order to improve the life of the second insulating housing 113 and also improve the electronic function in the reactor, a conductive layer 114 is provided between the second insulating housing 113 and the hollow electrode 115; the materials of the second insulating housing 113 and the conductive layer 114 may be selected according to the needs, and in this embodiment, the material of the second insulating housing 113 is PVC, and the material of the conductive layer 114 is stainless steel.
The hollow electrode 116 in the middle layer is connected to the negative electrode of a second high voltage dc power supply, the positive electrode of which is grounded.
In the positive polarity super-current reactor 11, the working voltage of the first high-voltage direct-current power supply is 150KV, the working current is 0.2A, and the electrical property of the positive polarity super-current reactor 11 is reducibility, so that most of substances passing through the positive polarity super-current reactor 11 can be positively charged.
In the negative polarity super-current reactor 12, the second high-voltage DC power supply has an operating voltage of 150KV and an operating current of 0.2A. By setting the adjacent super-electric current reactors to the opposite polarity, the voltage difference is doubled, the substance flowing out of the positive polarity super-electric current reactor 11 is positively charged, the positively charged substance is decomposed at the moment of flowing into the negative polarity super-electric current reactor 12, the carbon atoms generate a single layer of carbon nanomaterial in the pipeline, and the growing carbon nanomaterial stops growing after flowing into the positive polarity super-electric current reactor.
(2) The decomposed mixture enters a separator which comprises two spray towers 31 connected in parallel and a drying device 32 communicated with the spray towers, wherein the drying device 32 is a freeze drying device, and the separation can be selected according to the needs when the freeze drying device is specifically manufactured.
Spraying deionized water in a spray tower 31, entraining carbon nano materials in the mixture to the bottom of the spray tower 31, conveying the entrained carbon nano materials to a drying device 32 for drying, enabling redundant gas to enter a gas separation device 33 through a gas outlet of the spray tower 31, separating and collecting hydrogen through a molecular sieve, compressing, condensing and bottling for standby, carrying out waste gas treatment on one part of the rest gas, returning the other part of the rest gas to a super-electric elementary stream reactor for continuous reaction, and controlling the flow rate of the rest gas and the flow rate of the rest gas to ensure that the pressure of carbon source gas is higher than the pipeline pressure by 0.5kg/cm 2 Above, in order to ensure that the carbon source gas intake is normal.
The decomposition efficiency of the carbon nanomaterial production system is 80%, the equipment month power consumption is 63.4KW (calculated by 24 hours a day and 30 days a month production time), and the month yield of the carbon nanomaterial is 0.32 ton.
The carbon nanomaterial dried by the freeze drying device is characterized by adopting a scanning electron microscope, and the result is shown in fig. 8, wherein the obtained carbon nanomaterial is a single-layer sheet-shaped film material with uniform thickness, the sheet diameter is 0.4-1.5 mu m, and the carbon nanomaterial is sheet-shaped carbon nanomaterial with excellent quality.
The atomic force microscope is adopted to characterize the carbon nano material dried by the freeze drying device, the result is shown in fig. 9, wherein (a) in fig. 9 is an AFM morphology diagram of the carbon nano material; fig. 9 (b) is an AFM perspective view of the carbon nanomaterial, and it can be seen from the figure that the surface of the carbon nanomaterial bar is relatively smooth, and only a small amount of impurities adhere, and the height difference between the corresponding two points in fig. 9 (a) is 0.945 and nm.
Example 2
Compared with example 1, the only difference is that: and decomposing by adopting 2 groups of super-current reactors connected in series, wherein the working voltage of the first high-voltage direct-current power supply and the working voltage of the second high-voltage direct-current power supply are both 150KV, and the working current is both 0.2A. At a concentration of 1000mg/m 3 The benzene gas of (2) was used as a carbon source, the air inlet amount was 100 m/h at a wind speed of 5m/s, and the other parameters and operations were the same as those of example 1.
The decomposition efficiency of the carbon nanomaterial production system is 80%, and the equipment month power consumption is 63.4KW (calculated according to 24 hours a day and 30 days a month production time).
Example 3
Compared with example 1, the only difference is that: and decomposing by adopting 2 groups of super-current reactors connected in series, wherein the working voltage of the first high-voltage direct-current power supply and the working voltage of the second high-voltage direct-current power supply are both 150KV, and the working current is both 0.2A. At a concentration of 1500mg/m 3 The methane gas of (2) is used as a carbon source, the air inlet quantity is 1000 m/h at the air speed of 5m/s, and the rest parameters and operations are the same as those of the embodiment 1.
The decomposition efficiency of the carbon nanomaterial production system is 85%, the equipment month power consumption is 63.4KW (calculated by 24 hours a day and 30 days a month production time), and the month yield of the carbon nanomaterial is 0.69 ton.
Example 4
Compared with example 1, the only difference is that: and 3 groups of super-current reactors connected in series are adopted for decomposition, the working voltage of the first high-voltage direct-current power supply and the working voltage of the second high-voltage direct-current power supply are both 200KV, and the working current is both 0.2A. At a concentration of 2000mg/m 3 Toluene gas of (2) is used as a carbon source, the air inlet quantity is 1000 m/h at the air speed of 5m/s, and the rest parameters and operation are the same as those of the example 1.
The decomposition efficiency of the carbon nanomaterial production system is 95%, the equipment month power consumption is 95KW (calculated according to 24 hours a day and 30 days a month production time), and the month yield of the carbon nanomaterial is 1.25 tons.
Claims (8)
1. A process for producing a carbon nanomaterial, comprising: the carbon source enters one or more groups of super-current reactors in a gas form through a carbon source air inlet pipe to be decomposed; the mixture obtained by decomposition enters a separator, carbon nano materials are obtained by collection, and gas is discharged from an outlet;
the carbon source is a hydrocarbon-containing gas; the hydrocarbon is one or more of methane, benzene, toluene, xylene and acenaphthene;
each group of the super-electric current reactors consists of a positive polarity super-electric current reactor and a negative polarity super-electric current reactor which are sequentially connected in series along the air flow direction through connecting pipelines;
the positive polarity super-current reactor comprises a first insulating shell with a first inlet and a first outlet, wherein the first inlet is communicated with the carbon source air inlet pipe; at least one group of discharging components are arranged in the first insulating shell, each discharging component comprises at least one PCB (printed circuit board) with discharging needles uniformly distributed on two sides and two discharging plates arranged on two sides of the PCB, and the discharging needles are uniformly distributed on one surface of each discharging plate opposite to the PCB;
in the discharging assembly, a parallel gas channel is formed between the PCB and the discharging plate, an air inlet of the gas channel is communicated with the first inlet, and an air outlet of the gas channel is communicated with the first outlet;
the negative polarity supercurrent reactor comprises a second insulated housing having a second inlet in communication with the first outlet of the positive polarity supercurrent reactor and a second outlet in communication with the separator; the second insulating shell is internally and coaxially provided with a conductive layer and at least two hollow electrodes from outside to inside;
the PCB and the discharge plate are connected in parallel with the positive electrode of a first high-voltage direct-current power supply, and the negative electrode of the first high-voltage direct-current power supply is grounded;
in the negative polarity super-current reactor, all the hollow electrodes are mutually sleeved, any one of the hollow electrodes is connected with the negative electrode of a second high-voltage direct-current power supply, and the positive electrode of the second high-voltage direct-current power supply is grounded; in the negative polarity super-current reactor, the hollow electrodes comprise a plurality of discharge rings which are connected end to end, and each discharge ring is provided with a discharge sharp edge part;
the working voltage of the first high-voltage direct current power supply and the working voltage of the second high-voltage direct current power supply are respectively 80 kV-300 kV, and the working current is respectively 0.1A-8A.
2. The process for producing a carbon nanomaterial of claim 1, wherein the hydrocarbon content of the carbon source is 1% by volume or more.
3. The process for producing a carbon nanomaterial of claim 1, wherein the hydrocarbon content of the carbon source is 99% or more by volume;
the flow rate of the carbon source is below 5 m/s; the air inlet quantity of the carbon source is 100-200000 m 3 /h；
The number of groups of the super-electric current reactors is more than 2, and the super-electric current reactors are connected in series through connecting pipelines.
4. The process for producing a carbon nanomaterial of claim 1, wherein a flow rate of the carbon source is 1m/s or less;
the number of groups of the super-electric current reactor is more than 5 groups.
5. The process for producing carbon nanomaterial of claim 1, wherein the length of the connecting pipe is at least 2m when the flow rate of the carbon source is 1m/s or less; when the flow rate of the carbon source is more than 1m/s and less than 5m/s, the length of the connecting pipeline is at least 3m.
6. The process for producing carbon nanomaterial of claim 1, wherein in the positive polarity superconducting current reactor, the number of groups of the discharge elements is at least 1, and when the number of groups of the discharge elements is more than one, the discharge elements are connected in parallel;
in the positive polarity super-current reactor, the number of the PCB boards is at least 1, and when the number of the PCB boards is more than one, all the PCB boards are connected in parallel.
7. The process for producing carbon nanomaterial according to claim 1, wherein the separator comprises at least one spray tower and a drying device, and after the mixture enters the spray tower, surplus gas is discharged through a gas outlet of the spray tower, a bottom outlet of the spray tower is communicated with an inlet of the drying device, and the carbon nanomaterial is obtained after drying.
8. The process for producing carbon nanomaterial of claim 7, wherein the number of the spray towers is 2 to be connected in parallel;
the gas outlet of the spray tower is also connected with a gas separation device for separating and collecting hydrogen generated by decomposition of the super-electric current reactor, and the residual gas is subjected to waste gas treatment or returned to the super-electric current reactor.
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| CN101912761A (en) * | 2010-07-05 | 2010-12-15 | 洪昆喨 | Dielectric discharge reactor of uniform electric field |
| CN105457423A (en) * | 2014-09-04 | 2016-04-06 | 苏州鼎德电环保科技有限公司 | Discharge reactor and exhaust gas treating method |
| CN106475029A (en) * | 2015-08-27 | 2017-03-08 | 洪昆喨 | A kind of high voltage electro-catalysis discharge reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101912761A (en) * | 2010-07-05 | 2010-12-15 | 洪昆喨 | Dielectric discharge reactor of uniform electric field |
| CN105457423A (en) * | 2014-09-04 | 2016-04-06 | 苏州鼎德电环保科技有限公司 | Discharge reactor and exhaust gas treating method |
| CN106475029A (en) * | 2015-08-27 | 2017-03-08 | 洪昆喨 | A kind of high voltage electro-catalysis discharge reactor |
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