Porous carbon and carbon nanotube combined preparation system and method

Abstract

The invention provides a porous carbon and carbon nanotube combined preparation system and method. The system comprises an activation fluidized bed, a carbonization fluidized bed and a carbon nanotube preparation fluidized bed, the activated fluidized bed is filled with an energy supply carbon carrier, after oxygen and activated gas are introduced, the energy supply carbon carrier and the oxygen are combusted to release heat, so that the temperature of the activated fluidized bed is increased, formed first tail gas is introduced into a carbonization fluidized bed filled with a carbon particle precursor, and the carbon particle precursor is carbonized under the action of high temperature carried by the first tail gas; generating carbide particles and second tail gas containing C1-C30; the carbide particles are conveyed to an activation fluidized bed, the carbide particles are always located on the upper middle portion of the activation fluidized bed by controlling the gas inlet flow speed of a first gas inlet, the carbide particles are activated in activation gas, and porous carbon particles are formed; the second tail gas enters a carbon nanotube preparation fluidized bed, and C1-C30 in the second tail gas is converted into carbon nanotubes under the action of a nano-metal catalyst, so that low-cost co-production of the porous carbon and the carbon nanotubes is realized.

Description

Technical Field

[0001] The present invention relates to the technical field of carbon material preparation systems and methods, and in particular to a system and method for the combined preparation of porous carbon and carbon nanotubes. Background Art

[0002] Small-particle, high-quality porous carbon has a wide range of applications due to its large specific surface area, adjustable micropores and mesopores, and tunable surface chemical properties. For example, this product is primarily used as porous carbon for silicon-carbon anodes; electrode materials for supercapacitors; promoters for power-type lithium-ion batteries and power-type sodium-ion batteries; carriers for coal chemical catalysts or catalysts for pesticide fine chemicals; environmentally friendly adsorbents; coal chemical gas separation agents; and for direct capture of CO2 from air.

[0003] The preparation steps of porous carbon are generally to use organic precursor particles, and then carbonize and activate them at high temperature. When the activation gas (water and CO2) reacts with the carbonized material, the temperature is generally higher than 800 o C, and it is a strongly endothermic reaction. High-temperature engineering heating has always been a huge technical challenge. At the same time, the comprehensive utilization of high-temperature thermal energy is also an important way to reduce energy consumption and costs. Summary of the Invention

[0004] In response to the above-mentioned problems existing in the prior art, the present invention provides a system and method for the joint preparation of porous carbon and carbon nanotubes to improve the overall utilization rate of thermal energy in the porous carbon preparation process and the further resource conversion rate of carbonization tail gas.

[0005] The specific content of the invention is as follows: In a first aspect, the present invention provides a system for the combined preparation of porous carbon and carbon nanotubes, comprising: an activation fluidized bed, a carbonization fluidized bed in communication with the activation fluidized bed, and a carbon nanotube preparation fluidized bed in communication with the carbonization fluidized bed; The bottom of the activated fluidized bed is filled with an energy-supplying carbon carrier and is provided with a first gas inlet for introducing oxygen and activation gas. The energy-supplying carbon carrier and oxygen burn and release heat, making the temperature in the activated fluidized bed 850-1000°C; A first solid transmission channel and a first gas transmission channel are provided between the activation fluidized bed and the carbonization fluidized bed. The carbonization fluidized bed is filled with carbon particle precursors. The first tail gas in the activation fluidized bed is transported to the carbonization fluidized bed through the first gas transmission channel. The carbon particle precursors are carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles and C1-C 30 The second exhaust gas; The carbonized particles are transported to the activated fluidized bed through the first solid transport channel, and the inlet gas velocity of the first gas inlet is controlled so that the carbonized particles are always located in the upper middle portion of the activated fluidized bed. The carbonized particles are activated under the action of the activated gas to obtain the porous carbon particle material. A second gas transmission channel is provided between the carbon nanotube preparation fluidized bed and the carbonization fluidized bed. The second tail gas enters the carbon nanotube preparation fluidized bed through the second gas transmission channel. The C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

[0006] Optionally, the activated fluidized bed and the carbonized fluidized bed perform heat transfer through the first gas transmission channel, so that the temperature of the carbonized fluidized bed is 700-900° C.; The carbonization fluidized bed and the carbon nanotube preparation fluidized bed perform heat transfer via the second gas transmission channel, so that the temperature of the carbon nanotube preparation fluidized bed is 700-850°C.

[0007] Optionally, a third gas transmission channel is provided between the activation fluidized bed and the carbon nanotube preparation fluidized bed, and the third tail gas generated in the carbon nanotube preparation fluidized bed is transported to the activation fluidized bed through the third gas transmission channel and used as activation gas / combustion energy.

[0008] Optionally, a pressurizing device is provided on the third gas transmission channel, and the third tail gas is pressurized by the pressurizing device and then transported to the activated fluidized bed.

[0009] In a second aspect, the present invention provides a method for jointly preparing porous carbon and carbon nanotubes, the method being applicable to the system according to any one of claims 1 to 4, the method comprising: An energized carbon carrier is loaded into the activated fluidized bed, a carbon particle precursor is loaded into the carbonization fluidized bed, and a nano-metal catalyst is loaded into the carbon nanotube preparation fluidized bed. Oxygen and an activating gas are introduced into the combustion zone of the activated fluidized bed through a first gas inlet. The energized carbon carrier and oxygen combust and release heat, causing the temperature in the activated fluidized bed to be 850-1000°C. The first tail gas generated in the activated fluidized bed is introduced into the carbonized fluidized bed through the first gas transmission channel. The carbon particle precursor is carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles and C1-C 30 The second exhaust gas; The carbonized particles are introduced into the activated fluidized bed through the first solid transport channel, and the inlet gas velocity of the first gas inlet is controlled so that the carbonized particles are always located in the upper middle portion of the activated fluidized bed. The carbonized particles are activated by the activated gas to obtain the porous carbon particle material. The second tail gas is transported to the carbon nanotube preparation fluidized bed through the second gas transmission channel, and the C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

[0010] Optionally, the preparation method further comprises: transporting the third tail gas generated in the carbon nanotube preparation fluidized bed to the combustion area of the activation fluidized bed through a third transmission channel to be used as activation gas / combustion energy.

[0011] Optionally, the preparation method further includes: after the third tail gas is pressurized, it is transported to the combustion area of the activated fluidized bed through a third transmission channel to be used as activation gas / combustion energy.

[0012] Optionally, the particle size of the energy-supplying carbon carrier is larger than the particle size of the carbonized particles.

[0013] Optionally, the amount of oxygen introduced into the activated fluidized bed is such that after the energy-supplying carbon carrier burns to generate heat, the volume concentration of the remaining oxygen is no more than 0.5%.

[0014] Optionally, the nanometal catalyst comprises an active component and a carrier, wherein the mass proportion of the active component is 20%-50%, and the active component is selected from one or more of iron, cobalt, nickel, platinum, molybdenum, tungsten, copper and manganese; The carrier is one or more of aluminum oxide, silicon oxide and magnesium oxide.

[0015] Compared with the prior art, the present invention has the following advantages: The present invention provides a system for the combined preparation of porous carbon and carbon nanotubes, comprising: an activated fluidized bed, a carbonizing fluidized bed connected to the activated fluidized bed, and a carbon nanotube preparation fluidized bed connected to the carbonizing fluidized bed; the bottom of the activated fluidized bed is filled with an energy-supplying carbon carrier, and is provided with a first gas inlet for introducing oxygen and an activated gas, the energy-supplying carbon carrier and the oxygen burn and release heat, so that the temperature in the activated fluidized bed is 850-1000°C; a first solid transmission channel and a first gas transmission channel are provided between the activated fluidized bed and the carbonizing fluidized bed, the carbonizing fluidized bed is filled with a carbon particle precursor, the first tail gas in the activated fluidized bed is transported to the carbonizing fluidized bed through the first gas transmission channel, the carbon particle precursor is carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles, and C1-C30 The carbonized particles are transported to the activated fluidized bed through the first solid transmission channel, and the inlet flow rate of the first gas inlet is controlled so that the carbonized particles are always in the middle and upper part of the activated fluidized bed, and the carbonized particles are activated under the action of the activated gas to obtain the porous carbon particle material; a second gas transmission channel is provided between the carbon nanotube preparation fluidized bed and the carbonization fluidized bed, and the second tail gas enters the carbon nanotube preparation fluidized bed through the second gas transmission channel, and the C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

[0016] The preparation system provided by the present invention can simultaneously realize the carbonization of carbon particle precursors, the activation of carbonized particles, and the further resource conversion of carbonized exhaust gas, thereby achieving balanced energy supply and coordinated utilization, and improving the utilization rate of thermal energy; the activated fluidized bed not only serves as a device for activating carbonized particles, but also provides the required thermal energy for the operation of the entire system, and the activated fluidized bed adopts a self-heating fluidized bed (combustion-powered carbon carrier for heating), the fluidized bed has a simple structure, is easy to maintain, and effectively reduces the manufacturing cost of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0018] Figure 1 A schematic structural diagram of a system for jointly preparing porous carbon and carbon nanotubes provided in an embodiment of the present invention is shown; Figure 2 The flowchart of the method for jointly preparing porous carbon and carbon nanotubes provided by an embodiment of the present invention is shown. DETAILED DESCRIPTION

[0019] The technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, not all of the embodiments. The following description of at least one exemplary embodiment is actually only illustrative and is by no means a limitation on the present invention and its application or use. Based on the embodiments of the present invention, any product that is identical or similar to the present invention and is obtained by anyone under the inspiration of the present invention or by combining the features of the present invention with other prior arts falls within the scope of protection of the present invention. In addition, all other embodiments obtained by ordinary technicians in this field without carrying out creative work fall within the scope of protection of the present invention.

[0020] Where specific experimental steps or conditions are not specified in the examples, the conventional experimental steps or conditions described in the prior art in the art may be used. Reagents and other instruments used, for which the manufacturer is not specified, are commercially available conventional reagent products. Furthermore, the accompanying drawings are merely schematic illustrations of embodiments of the present invention and are not necessarily drawn to scale. Identical reference numerals in the figures denote identical or similar parts, and their repeated descriptions will be omitted. Some block diagrams shown in the accompanying drawings are functional entities and do not necessarily correspond to physically or logically independent entities.

[0021] Technologies, methods, and equipment known to those skilled in the art may not be discussed in detail, but where appropriate, such technologies, methods, and equipment should be considered part of the description of the present invention.

[0022] In the description of the present invention, it should be understood that the use of terms such as "first" and "second" to limit components is only for the convenience of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore cannot be understood as limiting the scope of protection of the present invention.

[0023] In addition, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0024] In a first aspect, the present invention provides a system for the combined preparation of porous carbon and carbon nanotubes. Figure 1 The schematic diagram of the structure of the system for preparing porous carbon and carbon nanotubes provided by the embodiment of the present invention is shown in FIG. Figure 1The system includes: an activated fluidized bed 1, a carbonized fluidized bed 2 connected to the activated fluidized bed 1, and a carbon nanotube preparation fluidized bed 3 connected to the carbonized fluidized bed 2; the bottom of the activated fluidized bed 1 is filled with an energy-supplying carbon carrier, and is provided with a first gas inlet 4 for introducing oxygen and activated gas, the energy-supplying carbon carrier and oxygen burn and release heat, so that the temperature in the activated fluidized bed is 850-1000 ℃; a first solid transmission channel 5 and a first gas transmission channel 7 are provided between the activated fluidized bed 1 and the carbonized fluidized bed 2, the carbonized fluidized bed 2 is filled with a carbon particle precursor, the first tail gas in the activated fluidized bed 1 is transported to the carbonized fluidized bed 2 through the first gas transmission channel 7, the carbon particle precursor is carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles, and C1-C 30 The carbonized particles are transported to the activated fluidized bed 1 through the first solid transmission channel 5. By controlling the inlet flow rate of the first gas inlet 4, the carbonized particles are always located in the upper middle part of the activated fluidized bed 1, and the carbonized particles are activated under the action of the activated gas to obtain the porous carbon particle material. A second gas transmission channel 8 is provided between the carbon nanotube preparation fluidized bed 3 and the carbonization fluidized bed 2. The second tail gas enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8. The C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

[0025] See also Figure 1 In the present invention, the activated fluidized bed 1 is a self-heating fluidized bed, which generates heat by burning energy-supplying carbon carriers to supply energy to the system. Compared with fluidized beds with a large number of electric heating structures, the self-heating fluidized bed has a simple structure and can effectively reduce the manufacturing cost of the device and maintenance costs. It should be noted that the combustion energy supply of the energy-supplying carbon carrier and the activation of the carbonized particles are both completed in the activated fluidized bed 1; in the present invention, the activated fluidized bed 1 can be divided into a combustion area and an activation area. The combustion area is located at the bottom of the activated fluidized bed, filled with the energy-supplying carbon carrier, and provides thermal energy to the preparation system by burning the energy-supplying carbon carrier; the activation area is located in the middle and upper part of the activated fluidized bed, and is used to receive the carbonized particles transported through the first solid transmission channel 5, so that the carbonized particles are activated under the action of the activation gas to obtain porous carbon particle materials; this division is mainly achieved by controlling the inlet gas flow rate of the first gas inlet 4 so that the carbonized particles are always in the middle and upper part of the activated fluidized bed (activation area), and the energy-supplying carbon carrier is located at the bottom of the activated fluidized bed (the particle size is large enough and not affected by the airflow), thereby avoiding the carbonized particles from being burned and lost.

[0026] Furthermore, the combustion of the energy-supplying carbon carrier requires the consumption of oxygen, and the activation of the carbonized particles requires strict control of the oxygen content introduced into the activated fluidized bed 1 to reduce the oxidation / combustion loss of the carbonized particles at high temperatures; the intake air (including oxygen and activation gas (such as CO2, H2O)) of the first gas inlet 4 is first fully contacted with the energy-supplying carbon carrier in the combustion area, and the oxygen therein participates in the combustion reaction and is consumed and removed, and the remaining gas (first tail gas) is heated and reaches the activation area along the airflow direction to be consumed by the carbonized particles for activation treatment and to provide energy for the carbonization fluidized bed 2.

[0027] Continue to see Figure 1 The first tail gas generated in the activated fluidized bed 1 is transported to the carbonizing fluidized bed 2 via the first gas transmission channel 7, where it is used as fluidizing gas. The heat energy carried by the first tail gas is used to provide energy for the carbonization of the carbon particle precursor. The carbonized particles generated in the carbonizing fluidized bed 2 are transported to the upper middle portion (activation zone) of the activated fluidized bed 1 via the first solid transmission channel 5. The carbonized particles are activated by the activation gas to obtain porous carbon particle material, which is discharged via the first product outlet 6. The combustion reaction between the energy-supplying carbon carrier and oxygen is an exothermic reaction, while the activation reaction of the carbonized particles is an endothermic reaction. Therefore, the combustion reaction involving oxygen and the endothermic reaction involving the activation gas can occur simultaneously in the activated fluidized bed 1, achieving self-heating balance in the activated fluidized bed 1.

[0028] In the present invention, the heat required for carbonization of the carbon particle precursor in the carbonization fluidized bed 2 is provided by the activation fluidized bed 1. In the initial stage of preparation, preheated oxygen is introduced into the activation fluidized bed 1 to provide energy for the carbon carrier to undergo a combustion reaction with the oxygen, causing the temperature in the activation fluidized bed to rise rapidly. Activation gas is further introduced, and the oxygen flux is controlled to maintain the temperature balance in the activation fluidized bed. After the accumulated gas (first tail gas) in the activation fluidized bed 1 is heated, it directly enters the carbonization fluidized bed as a fluidizing medium, fully contacts the carbon particle precursor, and provides the required temperature for the carbonization of the carbon particle precursor to form carbonized particles. The carbonized particles return to the activation fluidized bed 1 through the first solid transport channel and continue to undergo activation treatment. The high temperature carried by the second tail gas generated by carbonization can, after entering the carbon nanotube preparation fluidized bed 3, promote the C1-C 30 Converted into carbon nanotubes.

[0029] Furthermore, the carbonized particles activated in the activation fluidized bed 1 are supplied by the carbonizing fluidized bed 2, which is used to carbonize the carbon particle precursor at high temperature to form carbonized particles; at the same time, the carbonization process produces C1-C 30 The tail gas (second tail gas) further enters the carbon nanotube preparation fluidized bed 3. Under the action of nano metal catalyst, C1-C30 Converted into carbon nanotubes.

[0030] See also Figure 1 The oxygen introduced through the first gas inlet 4 of the activated fluidized bed 1 undergoes a combustion reaction with the energy-supplying carbon carrier to generate gases such as CO, CO2 and H2O. These gases are mixed with the activated gas (H2O and CO2) and the gases such as CO and H2 generated during the activation process to form the first tail gas which enters the carbonization fluidized bed 2 through the first gas transmission channel 7 and serves as the fluidizing gas of the carbonization fluidized bed 2. In addition, the carbon particle precursors in the carbonization fluidized bed 2 are carbonized under the residual heat of the first tail gas to form carbonized particles and C1-C 30 Therefore, the second tail gas is directly transmitted to the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8, so that the C1-C 30 Under the action of the nanometal catalyst, it is converted into carbon nanotubes, H2, CH4, etc. The preparation system provided by the present invention effectively utilizes the first tail gas as the fluidizing gas for the carbonization fluidized bed 2 and the second tail gas as the fluidizing gas and reaction medium for the carbon nanotube preparation fluidized bed 3, thereby improving the utilization rate of waste heat while reducing gas usage costs.

[0031] The preparation system provided by the present invention can simultaneously realize the carbonization of carbon particle precursors, the activation of carbonized particles, and the further resource conversion of carbonized exhaust gas, thereby achieving balanced energy supply and coordinated utilization, and improving the utilization rate of thermal energy; the activated fluidized bed not only serves as a device for activating carbonized particles, but also provides the required thermal energy for the operation of the entire system, and the activated fluidized bed adopts a self-heating fluidized bed (combustion-powered carbon carrier for heating), the fluidized bed has a simple structure, is easy to maintain, and effectively reduces the manufacturing cost of the system.

[0032] It should be noted that by controlling the flux of oxygen entering the activated fluidized bed, most of the oxygen is consumed by the combustion reaction with the energy-supplying carbon carrier. When it reaches the carbonized particle stacking / aggregation area, the volume concentration of oxygen is no more than 0.5%, so as to ensure that the dominant medium for the activation reaction of the carbonized particles is H2O, CO2 and trace oxygen; the content of oxygen entering the first gas inlet is matched by the heat required for the activation reaction of the carbonized particles in the activated fluidized bed 1.

[0033] In some embodiments, the activation fluidized bed and the carbonization fluidized bed perform heat transfer through the first gas transmission channel, so that the temperature of the carbonization fluidized bed is 700-900°C; the carbonization fluidized bed and the carbon nanotube preparation fluidized bed perform heat transfer through the second gas transmission channel, so that the temperature of the carbon nanotube preparation fluidized bed is 700-850°C.

[0034] The present invention is based on the fact that the carbonization temperature of the carbon particle precursor is lower than the temperature required for the activation of the carbonized particles, C1-C 30 The temperature required for conversion into carbon nanotubes is lower than the temperature required for carbonization of the carbon particle precursor. Therefore, the heat required for carbonization of the carbon particle precursor in the carbonization fluidized bed 2 can be provided by the activation fluidized bed 1. After an appropriate amount of oxygen and activation gas are introduced into the activation fluidized bed 1, the energy-supplying carbon carrier and the oxygen undergo combustion reaction, causing the temperature in the activation fluidized bed to rise rapidly. After the temperature reaches 850-1000°C, the gas (first tail gas) in the activation fluidized bed 1 is used as a fluidizing medium and introduced into the carbonization fluidized bed 2 through the first gas transmission channel 7. The temperature of the carbonization fluidized bed can be maintained at 700-900°C, meeting the temperature requirement for carbonization of the carbon particle precursor. The high temperature carried by the second tail gas generated by carbonization enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 7. The temperature of the carbon nanotube preparation fluidized bed 3 can be maintained at 700-850°C, and under the action of the catalyst, the C1-C 30 Thus, the preparation system provided by the present invention can provide energy for the operation of the entire preparation system by means of the combustion of the energy-supplying carbon carrier in the activated fluidized bed 1 .

[0035] In some embodiments, a third gas transmission channel 12 is provided between the activation fluidized bed 1 and the carbon nanotube preparation fluidized bed 3. The third exhaust gas generated in the carbon nanotube preparation fluidized bed 3 is transported to the combustion area of the activation fluidized bed 1 through the third gas transmission channel 12 and used as activation gas / combustion energy.

[0036] See also Figure 1 , in the carbon nanotube preparation fluidized bed 3, C1-C 30 Under the action of the nano-metal catalyst, it is converted into carbon nanotubes and generates H2 and CH4, which are discharged through the second product outlet 11; the remaining gas components (third tail gas) in the carbon nanotube preparation fluidized bed 3 also include the remaining unreacted activated gas. Therefore, by setting the third gas transmission channel 12, the third tail gas generated in the carbon nanotube preparation fluidized bed 3 is transported to the combustion area of the activation fluidized bed 1 for secondary utilization. The CO, CH4, H2, etc. therein can burn and release heat with the energy-supplying carbon carrier, and H2O and CO2 are used for the activation reaction of the carbonized particles, further improving resource utilization.

[0037] As a preferred example, a pressurizing device is provided on the third gas transmission channel 12. The third tail gas generated in the carbon nanotube preparation fluidized bed 3 is discharged through the third gas transmission channel 12, pressurized, and then fed into the activation fluidized bed 1 through the first gas inlet 4 to meet the pressure requirements of the activation reaction.

[0038] In a second aspect, the present invention provides a method for the combined preparation of porous carbon and carbon nanotubes, which is applicable to the preparation system described in the first aspect. Figure 2 The flow chart of the method for preparing porous carbon and carbon nanotubes provided by the embodiment of the present invention is shown as follows: Figure 2 As shown, the method includes: S1. Loading an energized carbon carrier into an activated fluidized bed, loading a carbon particle precursor into a carbonizing fluidized bed, loading a nano-metal catalyst into a carbon nanotube preparation fluidized bed, introducing oxygen and an activating gas into a combustion zone of the activated fluidized bed through a first gas inlet, wherein the energized carbon carrier and oxygen combust to release heat, causing the temperature in the activated fluidized bed to be 850-1000° C.; S2, the first tail gas generated in the activation fluidized bed is introduced into the carbonization fluidized bed through the first gas transmission channel, and the carbon particle precursor is carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles and C1-C 30 The second exhaust gas; S3, the carbonized particles are introduced into the activated fluidized bed through the first solid transport channel, and the inlet gas velocity of the first gas inlet is controlled so that the carbonized particles are always located in the upper middle portion of the activated fluidized bed. The carbonized particles are activated by the activated gas to obtain the porous carbon particle material; S4, the second tail gas is transported to the carbon nanotube preparation fluidized bed through the second gas transmission channel, and the C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

[0039] In a specific implementation, the activated fluidized bed is a self-heating fluidized bed that generates heat by burning the energy-supply carbon carriers to power the system. Compared with fluidized beds with a large number of electrically heated structures, the self-heating fluidized bed has a simple structure and can effectively reduce the manufacturing cost and maintenance costs of the device. The energy-supply carbon carriers are loaded into the activated fluidized bed and deposited at the bottom of the activated fluidized bed. In the initial stage of preparation, preheated oxygen is introduced into the activated fluidized bed through a first gas inlet. The energy-supply carbon carriers first undergo a combustion reaction with the oxygen, and the large amount of heat released causes the temperature in the activated fluidized bed to rapidly rise to 850-1000°C. Activating gas is further introduced, and the oxygen supply is controlled to maintain temperature equilibrium in the activated fluidized bed. After entering the activated fluidized bed, the gas (first tail gas) is heated and then enters the carbonization fluidized bed through the first gas transmission channel as a fluidizing medium, fully contacting the loaded carbon particle precursors and providing the required temperature for carbonization of the carbon particle precursors to form carbonized particles. The generated carbonized particles are returned to the activated fluidized bed through the first solid transport channel and continue to be activated by the activated gas. The high-temperature second tail gas generated by the carbonization reaction in the carbonized fluidized bed can enter the carbon nanotube preparation fluidized bed and, under the action of the loaded catalyst, promote the C1-C 30 Converted into carbon nanotubes.

[0040] The embodiment of the present invention controls the inlet gas flow rate of the first gas inlet so that the energy-supplying carbon carrier is located at the bottom of the activated fluidized bed (the particle size is large enough and is not affected by the airflow), while the carbonized particles entering the activated fluidized bed are always located in the upper middle part of the activated fluidized bed (activation area) due to their small particle size and light weight. The carbonized particles are activated under the action of the activation gas to obtain porous carbon particle material, thereby avoiding the loss of carbonized particles due to combustion.

[0041] Furthermore, the combustion of the energy-supplying carbon carrier requires the consumption of oxygen, and the activation of the carbonized particles requires strict control of the oxygen content introduced into the activated fluidized bed to reduce the oxidation / combustion loss of the carbonized particles at high temperatures; the intake air (including oxygen and activation gas (such as CO2, H2O)) of the first gas inlet is first fully contacted with the energy-supplying carbon carrier in the combustion area, and the oxygen therein participates in the combustion reaction and is consumed and removed, and the remaining gas (first tail gas) is heated and flows through the carbonized particles along the air flow direction for activation treatment and consumption, as well as to provide energy for the carbonization fluidized bed.

[0042] The method for jointly preparing porous carbon and carbon nanotubes provided by the present invention maintains the operating temperature of the activated fluidized bed by burning oxygen and an energy-supplying carbon carrier, without causing excessive loss of carbonized particles and porous carbon products used for activation treatment; by secondary utilization of the waste heat of the tail gas in the activated fluidized bed and using the tail gas formed in the carbonization process as a reaction medium to generate carbon nanotubes, the heat supply problem of the three endothermic reactions and the problem of toxic and odorous carbonization tail gas are solved, the fluidized bed structure is simplified, and it has the advantages of low energy consumption, continuous operation, high output, and cleanliness, effectively saving preparation costs, achieving balanced energy supply and coordinated utilization, and improving thermal energy utilization rate.

[0043] It should be noted that the energy carrier is continuously consumed in the activated fluidized bed. The energy carrier can be regularly added according to the temperature of the activated fluidized bed to maintain the self-heating balance of the activated fluidized bed. Similarly, the carbon particle precursor can also be added after the conversion of the carbonized particles is completed and transferred to the activated fluidized bed, so that the preparation process can be carried out continuously.

[0044] It should also be noted that the composition of the nanometal catalyst includes an active component and a carrier, the mass proportion of the active component is 20%-50%, and the active component is selected from one or more of iron, cobalt, nickel, platinum, molybdenum, tungsten, copper and manganese; the carrier is one or more of aluminum oxide, silicon oxide and magnesium oxide; the carbon particle precursor can be selected from organic particles with a particle size of not more than 200 μm, and the main components of the organic particles are carbon, hydrogen and oxygen, including but not limited to starch, lignin, cellulose, fruit shells, resins, polyesters, asphalt, etc.

[0045] It should also be noted that the carbon nanotubes prepared by the embodiment of the present invention have a diameter of 0.4-100 nm; the specific surface area of the porous carbon obtained is 1400-2600 m 2 / g, and the ratio of micropores to mesopores is 1:5~5:1.

[0046] In some embodiments, the preparation method further comprises: transporting the third tail gas generated in the carbon nanotube preparation fluidized bed to the combustion area of the activation fluidized bed via a third transmission channel to serve as activation gas / combustion energy.

[0047] In the fluidized bed for the preparation of carbon nanotubes, C1-C 30Under the action of the nano-metal catalyst, it is converted into carbon nanotubes and generates H2 and CH4, which are discharged through the second product outlet; the remaining gas components (third tail gas) in the carbon nanotube preparation fluidized bed also include the remaining unreacted activated gas. Therefore, the third tail gas generated in the carbon nanotube preparation fluidized bed is transported to the combustion area of the activation fluidized bed through the third gas transmission channel for secondary utilization. The CO, CH4, H2, etc. therein can burn and release heat with the energy-supplying carbon carrier, and the H2O and CO2 are used for the activation reaction of the carbonized particles, further improving resource utilization.

[0048] As a preferred example, the third tail gas is pressurized and then transported to the combustion area of the activated fluidized bed through a third transmission channel to be used as activation gas / combustion energy to meet the pressure requirements of the activation reaction.

[0049] In some embodiments, the particle size of the energetic carbon support is larger than the particle size of the carbonized material particles.

[0050] As a preferred example, the energy-supplying carbon carrier is selected from 0.3-0.5 mm carbon particles (ash content is less than 5 PPm), and the carbonized particles are controlled to be 2-200 μm.

[0051] In some embodiments, the amount of oxygen introduced into the activated fluidized bed is such that after the energy-supplying carbon support burns to generate heat, the volume concentration of the remaining oxygen is no more than 0.5%.

[0052] In specific implementation, by controlling the content of oxygen entering the first gas inlet, the volume concentration of the remaining oxygen after the oxygen is consumed in the combustion reaction with the energy-supplying carbon carrier is not greater than 0.5% when it reaches the carbonized particle stacking / aggregation area, so as to ensure that the dominant medium for the activation reaction of the carbonized particles is H2O, CO2 and trace oxygen; the content of oxygen introduced into the first gas inlet is matched by the heat required for the activation reaction of the carbonized particles in the activation fluidized bed 1.

[0053] In order to enable those skilled in the art to more clearly understand the present invention, the system and method for jointly preparing porous carbon and carbon nanotubes according to the present invention are now described in detail through the following examples.

[0054] The following examples are all in Figure 1 The process is carried out in the system shown, wherein the activation fluidized bed 1 is filled with an energy-supplying carbon carrier, the carbonization fluidized bed 2 is filled with a carbon particle precursor, and the carbon nanotube preparation fluidized bed 3 is filled with a nano-metal catalyst.

[0055] Example 1 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carrier carbon particles (particle size 0.3-0.35 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly raising the temperature of the activated fluidized bed 1. An activation gas consisting of 50% H₂O and 50% CO₂ is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4. The oxygen flow is controlled to maintain the temperature within the activated fluidized bed 1 at 950°C and the pressure at 0.1 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonization fluidized bed 2 through the first gas transmission channel 7, where it serves as the fluidizing gas.

[0056] The carbon particle precursor (starch, carbon, hydrogen, and oxygen contents of 45%, 6%, and 49%, respectively, and a particle size of 2-50 μm) in the carbonization fluidized bed 2 is treated at 770°C for 3 hours under the action of fluidizing gas and converted into carbonized particles (carbon content greater than 97%, and particle size of 2-50 μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.001%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 8 hours, the activated porous carbon product (2600 m 2 / g, the ratio of micropores to mesopores is 1:5, and the particle size is 2-50 μm) and discharged through the first product outlet 6.

[0057] The carbonized tail gas (second tail gas) produced in the carbonization fluidized bed 2 contains C1-C 30 Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8, serving as the fluidizing gas and reaction medium. Under the action of a nanometal catalyst (active metals: 40% Fe, 10% Mo; support: 50% silica), the reaction medium reacts at 700°C, converting the organic matter into carbon nanotubes (5-20 nm in diameter), CH4, and H2. After a 12-hour reaction, the carbon nanotubes are discharged through the second product outlet 11.

[0058] The third tail gas of the carbon nanotube preparation fluidized bed 3 leaves the carbon nanotube preparation fluidized bed 3 through the third gas transmission channel 12, and after being pressurized, is used as the fluidizing gas and combustion medium (with H2O or CO2 incorporated into it) for activating the fluidized bed 1.

[0059] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0060] Example 2 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carrier carbon particles (particle size 0.3-0.35 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly heating the activated fluidized bed 1. Activating H2O gas is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4, with the oxygen flow controlled to maintain a temperature of 850°C and a pressure of 1 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonizing fluidized bed 2 through the first gas transmission channel 7, serving as the fluidizing gas.

[0061] The carbon particle precursors (lignin and cellulose, with carbon, hydrogen and oxygen contents of 55%, 6% and 39% respectively, and a particle size of 20-40μm) in the carbonized fluidized bed 2 are treated at 800°C for 0.5 hours under the action of fluidizing gas and transformed into carbonized particles (carbon content greater than 97%, particle size of 20-40μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.5%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 2 hours, the activated porous carbon product (1400m 2 / g, the ratio of micropores to mesopores is 5:1, and the particle size is 20-40 μm) and discharged through the first product outlet 6.

[0062] The carbonized tail gas (second tail gas) produced in the carbonization fluidized bed 2 contains C1-C 30 Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8, serving as the fluidizing gas and reaction medium. Under the action of a nanometal catalyst (active metals: 40% Co, 10% Cu; support: 50% alumina), the reaction medium reacts at 760°C, converting the organic matter into carbon nanotubes (0.4-3 nm in diameter), CH4, and H2. After a two-hour reaction, the carbon nanotubes are discharged through the second product outlet 11.

[0063] The third tail gas of the carbon nanotube preparation fluidized bed 3 exits the carbon nanotube preparation fluidized bed 3 through the third gas transmission channel 12 and is pressurized to be used as the fluidizing gas and combustion medium (H2O is introduced into the activated fluidized bed 1).

[0064] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0065] Example 3 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carrier carbon particles (particle size 0.4-0.5 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly heating the activated fluidized bed 1. Activating gas consisting of 90% H₂O and 10% CO₂ is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4. The oxygen flow is controlled to maintain the temperature of the activated fluidized bed 1 at 950°C and the pressure at 0.5 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonizing fluidized bed 2 through the first gas transmission channel 7, where it serves as the fluidizing gas.

[0066] The carbon particle precursor (fruit shell, carbon, hydrogen, oxygen content of 60%, 6%, 34% respectively, and particle size of 2-15 μm) in the carbonization fluidized bed 2 is treated at 750 ° C for 2 hours under the action of fluidizing gas and transformed into carbonized particles (carbon content greater than 97%, particle size of 2-15 μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.01%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 4 hours, the activated porous carbon product (2200m 2 / g, the ratio of micropores to mesopores is 1:1, and the particle size is 2-15 μm) and discharged through the first product outlet 6.

[0067] The carbonized tail gas (second tail gas) produced in the carbonization fluidized bed 2 contains C1-C 30Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8, serving as the fluidizing gas and reaction medium. Under the action of a nanometal catalyst (active metals: 37% Ni, 2% Mn, 1% Pt; carrier: 60% MgO), the reaction medium reacts at 700°C, converting the organic matter into carbon nanotubes (10-100 nm in diameter), CH4, and H2. After a six-hour reaction, the carbon nanotubes are discharged through the second product outlet 11.

[0068] The third tail gas of the carbon nanotube preparation fluidized bed 3 leaves the carbon nanotube preparation fluidized bed 3 through the third gas transmission channel 12, and after being pressurized, is used as the fluidizing gas and combustion medium (with H2O or CO2 incorporated into it) for activating the fluidized bed 1.

[0069] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0070] Example 4 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carrier carbon particles (particle size 0.3-0.4 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly heating the activated fluidized bed 1. Activating H2O gas is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4, with the oxygen flow controlled to maintain a temperature of 960°C and a pressure of 0.6 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonizing fluidized bed 2 through the first gas transmission channel 7, serving as the fluidizing gas.

[0071] The carbon particle precursors (phenolic resin and epoxy resin, with carbon, hydrogen and oxygen contents of 45%, 13% and 33% respectively, and a particle size of 2-60 μm) in the carbonized fluidized bed 2 are treated at 800°C for 2 hours under the action of fluidizing gas and transformed into carbonized particles (carbon content greater than 97%, particle size of 2-60 μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.45%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 4 hours, the activated porous carbon product (1600 m 2 / g, the ratio of micropores to mesopores is 3:1, and the particle size is 2-60 μm) and discharged through the first product outlet 6.

[0072] The second tail gas produced in the carbonization fluidized bed 2 contains C1-C 30 Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through the second gas transmission channel 8, serving as the fluidizing gas and reaction medium. Under the action of a nanometal catalyst (active metals: 45% Ni, 5% Mo; support: 50% silica), the reaction medium reacts at 700°C, converting the organic matter into carbon nanotubes (1-10 nm in diameter), CH4, and H2. After an 8-hour reaction, the carbon nanotubes are discharged through the second product outlet 11.

[0073] The third tail gas of the carbon nanotube preparation fluidized bed 3 leaves the carbon nanotube preparation fluidized bed 3 through the third gas transmission channel 12, and after being pressurized, is used as the fluidizing gas and combustion medium (with H2O or CO2 incorporated into it) for activating the fluidized bed 1.

[0074] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0075] Example 5 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carbon particles (particle size 0.3-0.35 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly heating the activated fluidized bed 1. CO2 activating gas is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4, with the oxygen flow controlled to maintain a temperature of 920°C and a pressure of 0.8 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonizing fluidized bed 2 through the first gas transmission channel 7, serving as the fluidizing gas.

[0076] The carbon particle precursor (polyester, with carbon, hydrogen and oxygen contents of 62.5%, 4.2% and 33.3% respectively, and a particle size of 100-200 μm) in the carbonization fluidized bed 2 is treated at 900°C for 1 hour under the action of fluidizing gas and converted into carbonized particles (carbon content greater than 97%, particle size of 100-200 μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.35%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 2 hours, the activated porous carbon product (2000 m 2 / g, the ratio of micropores to mesopores is 1:3, and the particle size is 100-200μm) and discharged through the first product outlet 6.

[0077] The second tail gas produced in the carbonization fluidized bed 2 contains C1-C 30 Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through second gas transmission channel 8, serving as fluidizing gas and reaction medium. Under the action of a nanometal catalyst (active metals: 30% Fe, 3% Mo, 7% Mn; carrier: 60% MgO), the reaction medium reacts at 850°C, converting the organic matter into carbon nanotubes (5-20 nm in diameter), CH4, and H2. After 2-12 hours of reaction, the carbon nanotubes are discharged through second product outlet 11.

[0078] The third tail gas of the carbon nanotube production fluidized bed 3 exits the carbon nanotube production fluidized bed 3 through the third gas transmission channel 12. After being pressurized, it is used as the fluidizing gas and combustion medium (with H2O or CO2 incorporated) for activating the fluidized bed 1.

[0079] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0080] Example 6 Preheated oxygen-containing gas is introduced into the activated fluidized bed 1 through the first gas inlet 4. The energy-supplying carbon particles (particle size 0.3-0.5 mm, ash content less than 5 ppm) undergo an oxidation reaction with the oxygen, rapidly heating the activated fluidized bed 1. CO2 activating gas is continuously introduced into the activated fluidized bed 1 through the first gas inlet 4, with the oxygen flow rate controlled to maintain the temperature of the activated fluidized bed 1 at 1000°C and the pressure at 0.3 MPa. The post-combustion gas (first tail gas) contains no oxygen and enters the carbonizing fluidized bed 2 through the first gas transmission channel 7, serving as the fluidizing gas.

[0081] The carbon particle precursors (asphalt particles with carbon, hydrogen and oxygen contents of 95%, 4.9% and 0.1% respectively, and a particle size of 2-10μm) in the carbonization fluidized bed 2 are treated at 850°C for 1.5 hours under the action of fluidizing gas and transformed into carbonized particles (carbon content greater than 97% and particle size of 1-10μm). The carbonized particles are sent into the activated fluidized bed 1 through the first solid transmission channel 5. Due to the difference in particle size, under the action of gas velocity, the carbonized particles are located in the upper middle part of the fluidized bed; the energy carrier carbon particles are located in the lower part of the fluidized bed, and the mixing ratio of the two is less than 0.5%; and when the oxygen reaches the particle stacking area for activation and preparation of porous carbon, the volume concentration is 0.25%. Under the action of the activation gas, the carbonized particles are activated in the activated fluidized bed 1. After the activation time is 6 hours, the activated porous carbon product (1800 m 2 / g, the ratio of micropores to mesopores is 1:5~5:1, and the particle size is 1-10μm) and discharged through the first product outlet 6.

[0082] The second tail gas produced in the carbonization fluidized bed 2 contains C1-C 30 Organic matter, along with H2O, H2, CO2, and CO, enters the carbon nanotube preparation fluidized bed 3 through second gas transmission channel 8, serving as the fluidizing gas and reaction medium. Over a nanometal catalyst (active metals: 39% Fe, 1% Mo, 1% W; carrier: 59% alumina), these react with the reaction medium at 820°C, converting the organic matter into carbon nanotubes (5-20 nm in diameter), CH4, and H2. After 2-12 hours of reaction, the carbon nanotubes are discharged through second product outlet 11.

[0083] The third tail gas of the carbon nanotube production fluidized bed 3 exits the carbon nanotube production fluidized bed 3 through the third gas transmission channel 12. After being pressurized, it is used as the fluidizing gas and combustion medium (with H2O or CO2 incorporated) for activating the fluidized bed 1.

[0084] The energy carrier carbon particles are continuously consumed in fluidized bed 1. Based on the temperature of fluidized bed 1, they are periodically replenished to maintain self-heating equilibrium in the activated fluidized bed 1 (the combustion of carbon, CO, CH4, H2 with oxygen is an exothermic reaction; the activation reaction of carbon with H2O and CO2 is an endothermic reaction). These steps are repeated to ensure a continuous process.

[0085] In the description of this specification, the reference terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" mean that the specific features, structures, materials, or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present invention. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials, or characteristics described can be combined in any appropriate manner in any one or more embodiments or examples. In addition, those skilled in the art can combine and combine different embodiments or examples described in this specification.

[0086] For simplicity of description, the method embodiments are described as a series of actions. However, those skilled in the art should be aware that the present invention is not limited by the order of the actions described, as certain steps can be performed in other orders or simultaneously according to the present invention. Furthermore, those skilled in the art should also be aware that the embodiments described in this specification are preferred embodiments, and the actions and components involved are not necessarily required for the present invention.

[0087] The above is a detailed introduction to the system and method for the combined preparation of porous carbon and carbon nanotubes provided by the present invention. Specific examples are used herein to illustrate the principles and implementation methods of the present invention. The description of the above embodiments is only used to help understand the method of the present invention and its core idea. At the same time, for those skilled in the art, according to the ideas of the present invention, there will be changes in the specific implementation methods and application scopes. In summary, the content of this specification should not be understood as limiting the present invention.

Claims

1. A system for the combined preparation of porous carbon and carbon nanotubes, characterized in that: include: an activation fluidized bed, a carbonization fluidized bed in communication with the activation fluidized bed, and a carbon nanotube preparation fluidized bed in communication with the carbonization fluidized bed; The bottom of the activated fluidized bed is filled with an energy-supplying carbon carrier and is provided with a first gas inlet for introducing oxygen and activation gas. The energy-supplying carbon carrier and oxygen burn and release heat, making the temperature in the activated fluidized bed 850-1000°C; A first solid transmission channel and a first gas transmission channel are provided between the activation fluidized bed and the carbonization fluidized bed. The carbonization fluidized bed is filled with carbon particle precursors. The first tail gas in the activation fluidized bed is transported to the carbonization fluidized bed through the first gas transmission channel. The carbon particle precursors are carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles and C1-C 30 The second exhaust gas; The carbonized particles are transported to the activated fluidized bed through the first solid transport channel, and the inlet gas velocity of the first gas inlet is controlled so that the carbonized particles are always located in the upper middle portion of the activated fluidized bed. The carbonized particles are activated under the action of the activated gas to obtain the porous carbon particle material. A second gas transmission channel is provided between the carbon nanotube preparation fluidized bed and the carbonization fluidized bed. The second tail gas enters the carbon nanotube preparation fluidized bed through the second gas transmission channel. The C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

2. The system for preparing porous carbon and carbon nanotubes according to claim 1, characterized in that: The activated fluidized bed and the carbonized fluidized bed perform heat transfer through the first gas transmission channel, so that the temperature of the carbonized fluidized bed is 700-900° C.; The carbonization fluidized bed and the carbon nanotube preparation fluidized bed perform heat transfer via the second gas transmission channel, so that the temperature of the carbon nanotube preparation fluidized bed is 700-850°C.

3. The system for preparing porous carbon and carbon nanotubes according to claim 1, characterized in that: A third gas transmission channel is provided between the activation fluidized bed and the carbon nanotube preparation fluidized bed. The third tail gas generated in the carbon nanotube preparation fluidized bed is transported to the activation fluidized bed through the third gas transmission channel and used as activation gas / combustion energy.

4. The system for preparing porous carbon and carbon nanotubes according to claim 3, characterized in that: The third gas transmission channel is provided with a pressurizing device, and the third tail gas is pressurized by the pressurizing device and then transported to the activated fluidized bed.

5. A method for the combined preparation of porous carbon and carbon nanotubes, characterized in that: The method is applicable to the system according to any one of claims 1 to 4 above, and the method comprises: An energized carbon carrier is loaded into the activated fluidized bed, a carbon particle precursor is loaded into the carbonization fluidized bed, and a nano-metal catalyst is loaded into the carbon nanotube preparation fluidized bed. Oxygen and an activating gas are introduced into the combustion zone of the activated fluidized bed through a first gas inlet. The energized carbon carrier and oxygen combust and release heat, causing the temperature in the activated fluidized bed to be 850-1000°C. The first tail gas generated in the activated fluidized bed is introduced into the carbonized fluidized bed through the first gas transmission channel. The carbon particle precursor is carbonized under the action of the high temperature carried by the first tail gas to generate carbonized particles and C1-C 30 The second exhaust gas; The carbonized particles are introduced into the activated fluidized bed through the first solid transport channel, and the inlet gas velocity of the first gas inlet is controlled so that the carbonized particles are always located in the upper middle portion of the activated fluidized bed. The carbonized particles are activated by the activated gas to obtain the porous carbon particle material. The second tail gas is transported to the carbon nanotube preparation fluidized bed through the second gas transmission channel, and the C1-C 30 Under the action of nano metal catalyst, it is converted into carbon nanotubes.

6. The method for jointly preparing porous carbon and carbon nanotubes according to claim 5, characterized in that: The preparation method further includes: transporting the third tail gas generated in the carbon nanotube preparation fluidized bed to the combustion area of the activation fluidized bed through a third transmission channel to be used as activation gas / combustion energy.

7. The method for jointly preparing porous carbon and carbon nanotubes according to claim 6, characterized in that: The preparation method further includes: the third tail gas is pressurized and then transported to the combustion area of the activated fluidized bed through a third transmission channel to be used as activation gas / combustion energy.

8. The method for jointly preparing porous carbon and carbon nanotubes according to claim 5, characterized in that: The particle size of the energy-supplying carbon carrier is larger than the particle size of the carbonized material particles.

9. The method for jointly preparing porous carbon and carbon nanotubes according to claim 5, characterized in that: The amount of oxygen introduced into the activated fluidized bed is such that after the energy-supplying carbon carrier burns to generate heat, the volume concentration of the remaining oxygen is no more than 0.5%.

10. The method for jointly preparing porous carbon and carbon nanotubes according to claim 5, characterized in that: The nano metal catalyst comprises an active component and a carrier, wherein the mass proportion of the active component is 20%-50%, and the active component is selected from one or more of iron, cobalt, nickel, platinum, molybdenum, tungsten, copper and manganese; The carrier is one or more of aluminum oxide, silicon oxide and magnesium oxide.

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