CN111229026B - Device and method for efficiently converting volatile organic compounds - Google Patents
Device and method for efficiently converting volatile organic compounds Download PDFInfo
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- CN111229026B CN111229026B CN202010085860.5A CN202010085860A CN111229026B CN 111229026 B CN111229026 B CN 111229026B CN 202010085860 A CN202010085860 A CN 202010085860A CN 111229026 B CN111229026 B CN 111229026B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/44—Organic components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/10—Nitrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/18—Noble gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention discloses a device and a method for efficiently converting volatile organic compounds, wherein the lower section of the device is a fluidized bed section, the upper section of the device is a fixed bed section, the lower section of the device is separated by a porous distribution plate, and a wire mesh layer for preventing solids of the fluidized bed section from moving upwards, inlets of volatile organic compounds, water vapor and catalysts and outlets of carbon products and gas products are arranged at the same time; the method comprises the step of filling nano metal supported catalysts with different particle sizes in a fluidized bed section and a fixed bed section respectively. Conversion energy is provided by external heating, and heat is supplied to the catalyst in the fixed bed section through the gas in the fluidized bed section; the steam is introduced into the middle part of the reaction device to control the fluidized bed section to produce a large amount of carbon products, and the carbon deposition is avoided in the fixed bed section, so that the long service life of the catalyst is maintained. By using the method, the volatile organic compounds are efficiently converted and directly discharged; and the carbon nano material is prepared at the same time, so that the additional value is improved. Has the advantages of compact equipment structure, small investment and easy amplification.
Description
Technical Field
The invention relates to the technical field of volatile organic compound conversion, in particular to a device and a method for efficiently converting volatile organic compounds.
Background
Volatile organic compounds are a particularly large type in waste gas and have the characteristics of complex components, low content and large environmental impact effect. Current methods for treating volatile organic compounds include pre-cooling followed by enrichment by absorption or adsorption. Part of the volatile organics can become liquid after enrichment. A small amount of liquid with simple components can be recycled as a product. However, most of the liquid components are complex and difficult to separate continuously, and can only be reprocessed by incineration or catalytic oxidation. In addition, there are also volatile components with very low boiling points, often in gaseous form, which still have the potential to continue to be vented to the atmosphere. So that it can be changed into carbon dioxide and water only by means of incineration or catalytic oxidation. A large amount of fuel is needed in the incineration process, expensive reagents or catalysts are needed in the catalytic oxidation, and the product has no added value and is unfavorable in economic aspect.
The organic matter can be used as a raw material for preparing carbon nano materials (carbon nano tubes or graphene and carbon nano fibers). The products have large specific surface area, good electrical conductivity, thermal conductivity, mechanical strength and the like, and have good application in the aspects of composite materials, catalysts, adsorbing materials and energy storage and high added value. However, in many published reports, only quality, structure and purity control of carbon products is concerned, and conversion efficiency of carbon sources is rarely concerned. For example, in the production process of carbon nanotubes used as a conductive agent of a lithium ion battery, the conversion rate of the carbon source rarely exceeds 80%. By using the method, even if the enriched volatile organic compounds are changed into carbon products, the tail gas still belongs to the volatile organic compounds and does not meet the emission standard.
Generally, the concentration of the enriched volatile organic compounds is 0.1-100%, and the total hydrocarbon content except methane in the discharged gas after conversion is required not to exceed 50-100mg/Nm3. This corresponds to a conversion efficiency of more than 99.99%, even 99.999%, of the volatile organic compounds in the reaction apparatus. Obviously, the current technology is not satisfactory.
In addition, the volatile organic compound is an industry with large processing capacity, and the scale of the volatile organic compound is much larger than that of the current carbon nano material preparation industry. Therefore, a complex engineering problem is generated, namely the reaction device needs to meet the requirements of continuous conversion and standard conversion all the time. The technology has not been reported.
Disclosure of Invention
Aiming at the defects of the conventional volatile organic compound treatment method and the defects of the carbon nano material preparation technology, the invention provides a device and a method for efficiently converting volatile organic compounds.
In order to achieve the purpose, the invention adopts the following technical scheme:
a device for efficiently converting volatile organic compounds comprises a fluidized bed section 1 at the lower section and a fixed bed section 2 at the upper section, which are separated by a porous distribution plate 3; a steam jet pipe 5 and a metal wire mesh layer 4 are sequentially arranged below the porous distribution plate 3; the bottom of the fluidized bed section 1 is provided with a volatile organic compound inlet 6, the top of the fixed bed section 2 is provided with a gas product outlet 7, the fluidized bed section 1 is provided with a fluidized bed section catalyst inlet 8 and a carbon product outlet 9, and the fixed bed section 2 is provided with a fixed bed section catalyst inlet 10.
The porosity of the porous distribution plate 3 is 30-70%, and the diameter of a single hole is smaller than the minimum size of the catalyst in the fixed bed section 2.
A metal wire mesh layer 4 with the thickness of 1-3cm is arranged on the cross section of the fluidized bed section 1 which is 0.5-1m below the porous distribution plate 3; the void ratio of the metal wire mesh layer 4 is 90-95%, and the diameter of a single hole of the metal wire mesh is less than 0.01 mm; the wire mesh is made of stainless steel, nickel or platinum.
The water vapor injection pipe 5 is positioned at the center of the porous distribution plate 3 and the metal wire mesh layer 4; the number of the steam injection pipes 5 is one or more, and the openings thereof are directed downward, being opposed to the wire mesh layer 4.
The height of the fluidized bed section 1 is 2-5 times of the height of the fixed bed section 2.
The catalyst in the fluidized bed section 1 and the fixed bed section 2 is a nano metal supported catalyst, the metal component of the catalyst is one or more of Fe, Co, Ni, W, Cu, Mo and Mn, and the grain size is 1-20 nm; the carrier is one or more of alumina, silica, zirconia and magnesia, the mass fraction of the carrier is 10-90%, and the rest is metal; the nano metal-supported catalyst used in the fluidized bed section 1 has an average particle diameter of 0.05 to 0.5 mm, and the nano metal-supported catalyst used in the fixed bed section 2 has an average diameter of 2 to 10 mm. .
The method for converting the volatile organic compound by the device for efficiently converting the volatile organic compound comprises the following steps:
step 1: respectively filling the nano metal supported catalyst in the fluidized bed section 1 and the fixed bed section 2, heating the device to 500-1000 ℃, and controlling the absolute pressure of the gas product outlet (7) to be 0.1-2 MPa;
step 2: volatile organic compound gas is introduced from a volatile organic compound inlet 6 at the bottom of the fluidized bed section 1 and is cracked on a catalyst in the fluidized bed section 1 to generate carbon products, methane and hydrogen gas; the carbon product moves upwards along with the gas, and after the carbon product meets the wire mesh layer 4, most of the carbon product is rebounded and returns to the fluidized bed section 1;
and step 3: methane, hydrogen and unreacted volatile organic gas pass through the wire mesh layer 4 and the porous distribution plate 3 and enter the fixed bed section 2 to continue to react;
and 4, step 4: opening a water vapor injection pipe 5, and introducing water vapor with the total amount of volatile organic compounds being 1-10%; the carbon product adhered on the wire mesh layer 4 is back blown by the water vapor and returns to the fluidized bed section 1, so that the wire is back blownThe pressure drop of the net layer 4 is stable, and the void ratio is unchanged; after being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section 2, and reacts with volatile organic gas and carbon products on the catalyst; the final gas product has less than 50mg/Nm of non-methane total hydrocarbons3The gas product is discharged through a gas product outlet 7 after reaching the standard; the catalyst on the fixed bed section 2 does not deposit carbon and can be used for a long time;
and 5: when the carbon product of the fluidized bed section 1 is excessive, the carbon product is discharged out of the device through a carbon product outlet 9; and fresh catalyst is added through a fluidized bed section catalyst inlet 8; the above process is repeated.
The volatile organic gas is 0.01-90% of organic gas with molecular weight of 26-150, and the rest is one or more of inert gas such as nitrogen, argon and water vapor; in the conversion process, the space velocity of the volatile organic gas is 0.1-20 g/gcat/h.
The inert gas is one or more of nitrogen, argon and water vapor.
The carbon product is one or more of carbon nano tube, graphene and carbon nano-fiber.
Compared with the prior art, the invention has the following advantages:
(1) the fluidized bed and the fixed bed are integrated together, so that the requirement of high conversion rate of volatile organic compounds is met, and the requirement of solid volume expansion is met. In contrast, any single device does not meet this requirement.
(2) The water vapor is introduced, so that the back blowing effect of the fluidized bed section is ensured, and the cyclone separation device is not needed, so that the cost of the device is reduced by 30 percent. Meanwhile, the catalyst in the fixed bed section can not deposit carbon, and the reaction life is long. Compared with the case of no water, the service life of the catalyst in the solid bed section is prolonged by 5-50000 times.
(3) The high-temperature gas in the fluidized bed section is used for heating the catalyst in the fixed bed section, the defect of poor heat transfer effect of the fixed bed catalyst bed layer is overcome, and the energy can be saved by 50-80%.
Drawings
FIG. 1 is a schematic view of an apparatus for efficiently converting volatile organic compounds according to the present invention.
Wherein 1, a fluidized bed section; 2. a fixed bed section; 3. a porous distribution plate; 4. a wire mesh layer; 5. a water vapor injection pipe; 6. a volatile organic inlet; 7. a gaseous product outlet; 8. a fluidized bed section catalyst inlet; 9. a carbon product outlet; 10. and a catalyst inlet of the fixed bed section.
Detailed Description
The present invention will be described in further detail below with reference to the accompanying drawings and specific embodiments, including but not limited to the following examples and effects.
Example 1
An apparatus as shown in FIG. 1 is used in which the height of the fluidized bed section 1 is 2 times the height of the fixed bed section 2. The porosity of the porous distribution plate 3 is 30%, and the diameter of a single hole is 1 mm. A wire mesh layer 4 (platinum, the void ratio is 90%, and the single-hole diameter of the wire mesh is less than 0.01mm) with the thickness of 1cm is arranged on the cross section of the fluidized bed section 1 which is 0.5m below the porous distribution plate 3. A steam injection pipe 5 is provided at the center of the perforated distribution plate 3 and the mesh layer 4 (opening downward, facing the mesh layer 4).
A nano metal supported catalyst (10% Fe-90% alumina, 1nm grain) having an average particle size of 0.05 mm was charged into the fluidized bed section 1 through the fluidized bed section catalyst inlet 8. A nano metal supported catalyst (90% Ni-10% silica, 1-20nm in crystal grain) having an average diameter of 2mm was charged into the fixed bed section 2 through the fixed bed section catalyst inlet 10. The apparatus was heated to 500 ℃ and the absolute pressure at the product gas outlet 7 was controlled to 0.1 MPa.
Volatile organic gas (volatile organic gas composition: 0.01% of organic gas with molecular weight of 26-60, 1% of water vapor, and the balance of nitrogen) is introduced from a volatile organic gas inlet 6 at the bottom of the fluidized bed section 1. In the conversion process, the space velocity of the volatile organic compound gas is 0.1g/gcat/h, and carbon products (carbon nano tubes) and products such as methane, hydrogen and the like are generated by cracking on the catalyst. The carbon products travel upwards with the gas and, after hitting the wire mesh layer 4, are bounced back mostly back to the fluidized bed section 1. Methane, hydrogen and unreacted volatile organic gas pass through the wire mesh layer 4 and enter the fixed bed section 2 to continue reaction.
And opening a water vapor injection pipe 5 arranged above the wire mesh 4, and introducing water vapor with the total amount of volatile organic compounds of 1%. The carbon product adhered on the wire mesh layer 4 is reversely blown by the water vapor and returns to the fluidized bed section 1, so that the pressure drop of the wire mesh layer 4 is stable and the void ratio is unchanged. After being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section 2, and reacts with volatile organic gas and carbon products on the catalyst. The total non-methane hydrocarbons in the final gas is less than 30mg/Nm3And the gas product is discharged through a gas product outlet 7 after reaching the standard. The catalyst on the fixed bed section 2 does not deposit carbon and can be used for a long time.
When the carbon product of the fluidized bed section 1 is excessive, the apparatus is discharged from the carbon product outlet 9. And fresh catalyst is added through the fluidized bed section catalyst inlet 8. The above process is repeated.
Example 2
An apparatus as shown in FIG. 1 is used in which the height of the fluidized bed section 1 is 5 times the height of the fixed bed section 2. The porosity of the porous distribution plate is 70%, and the diameter of a single hole is 8 mm. A wire mesh layer 4 (stainless steel, the void ratio is 95%, and the diameter of a single hole of the wire mesh is less than 0.01mm) with the thickness of 3cm is arranged on the cross section of the fluidized bed section 1m below the porous distribution plate 3. Five steam injection pipes 5 (opening downward, facing the wire mesh layer 4) are provided at the center of the porous distribution plate 3 and the wire mesh layer 4.
A nano metal supported catalyst (10% Fe-90% alumina, crystal grain of 20nm) having an average particle size of 0.5 mm was charged into the fluidized bed section 1 through the fluidized bed section catalyst inlet 8. A nano metal supported catalyst (20% Fe-5% Co-10% Cu-65% silica, grain size 3nm) having an average diameter of 10 mm was charged into the fixed bed section 2 through the fixed bed section catalyst inlet 10. The apparatus was heated to 1000 ℃ and the absolute pressure at the product gas outlet 7 was controlled to 2 MPa.
Volatile organic gas (volatile organic gas composition: 50% organic gas with molecular weight of 60-150, 50% argon) is introduced from a volatile organic gas inlet 6 at the bottom of the fluidized bed section. In the conversion process, the space velocity of the volatile organic compound gas is 20g/gcat/h, and the volatile organic compound gas is cracked on a catalyst to generate carbon products (a mixture of carbon nano tubes and carbon nano fibers) and products such as methane, hydrogen and the like. The carbon products travel upwards with the gas and, after hitting the wire mesh layer 4, are bounced back mostly back to the fluidized bed section 1. Methane, hydrogen and unreacted volatile organic gas pass through the wire mesh layer 4 and enter the fixed bed section 2 to continue reaction.
And opening a steam injection pipe 5 arranged above the metal wire mesh layer 4, and introducing steam accounting for 10% of the total amount of the volatile organic compounds. The carbon product adhered on the wire mesh layer 4 is reversely blown by the water vapor and returns to the fluidized bed section 1, so that the pressure drop of the wire mesh layer 4 is stable and the void ratio is unchanged. After being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section 2, and reacts with volatile organic gas and carbon products on the catalyst. The total non-methane hydrocarbons in the final gas is less than 18mg/Nm3And the gas product is discharged through a gas product outlet 7 after reaching the standard. The catalyst on the fixed bed section 2 does not deposit carbon and can be used for a long time.
When the carbon product of the fluidized bed section 1 is excessive, the apparatus is discharged from the carbon product outlet 9. And fresh catalyst is added through the fluidized bed section catalyst inlet 8. The above process is repeated.
Example 3
An apparatus as shown in FIG. 1 was used in which the height of the fluidized bed section 1 was 3 times the height of the fixed bed section 2. The porosity of the porous distribution plate 3 is 60%, and the diameter of a single hole is less than 3 mm. A wire mesh layer 4 (nickel, the porosity is 92%, and the single-hole diameter of the wire mesh is less than 0.01mm) with the thickness of 2cm is arranged on the cross section of the fluidized bed section 1 which is 0.8m below the porous distribution plate 3. Four steam injection pipes 5 (opening downward, facing the wire mesh layer 4) are provided at the center of the porous distribution plate 3 and the wire mesh layer 4.
A nano metal supported catalyst (30% Fe-30% Co-10% Mo-30% magnesia, 5nm grain size) with an average particle size of 0.1-0.3 mm was charged into the fluidized bed section 1 through the fluidized bed section catalyst inlet 8. A nano metal supported catalyst (68% Ni-20% Mn-2% W-10% zirconia, crystal grain 10nm) having an average diameter of 5 mm was charged into the fixed bed section 2 through the fixed bed section catalyst inlet 10. The apparatus was heated to 800 ℃ and the absolute pressure at the product gas outlet 7 was controlled to 0.5 MPa.
Volatile organic gas (volatile organic gas composition: 20% of organic gas with molecular weight of 78-102, 20% of water vapor, and the balance of nitrogen) is introduced from a volatile organic gas inlet 6 at the bottom of the fluidized bed section. In the conversion process, the space velocity of volatile organic gas is 3g/gcat/h, and carbon products (graphene) and products such as methane, hydrogen and the like are generated by cracking on a catalyst. The carbon products travel upwards with the gas and, after hitting the wire mesh layer 4, are bounced back mostly back to the fluidized bed section 1. Methane, hydrogen and unreacted volatile organic gas pass through the wire mesh layer 4 and enter the fixed bed section 2 to continue reaction.
And opening a water vapor injection pipe 5 arranged above the wire mesh, and introducing water vapor accounting for 5% of the total amount of the volatile organic compounds. The carbon product adhered on the wire mesh layer 4 is reversely blown by the water vapor and returns to the fluidized bed section 1, so that the pressure drop of the wire mesh layer 4 is stable and the void ratio is unchanged. After being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section 2, and reacts with volatile organic gas and carbon products on the catalyst. The total hydrocarbons other than methane in the final gas are less than 50mg/Nm3 and are discharged from the gas product outlet 7 on a standard basis. The catalyst on the fixed bed section 2 does not deposit carbon and can be used for a long time.
When the carbon product of the fluidized bed section 1 is excessive, the apparatus is discharged from the carbon product outlet 9. And fresh catalyst is added through the fluidized bed section catalyst inlet 8. The above process is repeated.
Example 4
An apparatus as shown in FIG. 1 was used in which the height of the fluidized bed section 1 was 2.5 times the height of the fixed bed section 2. The porosity of the porous distribution plate 3 is 65%, and the diameter of a single hole is less than 2 mm. A wire mesh layer 4 (stainless steel, porosity 91%, single-hole diameter of wire mesh less than 0.01mm) with a thickness of 1.5cm is arranged on the cross section of the fluidized bed section 1 0.7m below the porous distribution plate 3. A steam jet pipe 5 (with opening direction downward, facing the wire mesh layer 4) is arranged at the center of the porous distribution plate 3 and the wire mesh layer 4.
A nano metal supported catalyst (70% Fe-2% Mo-28% alumina, grain size 6nm) having an average particle size of 0.05-0.25 mm was charged into the fluidized bed section 1 through the fluidized bed section catalyst inlet 8. A nano metal supported catalyst (80% Ni-10% Mo-10% silica, crystal grain 4nm) having an average diameter of 4 mm was charged into the fixed bed section 2 through the fixed bed section catalyst inlet 10. The apparatus was heated to 850 ℃ and the absolute pressure at the product gas outlet 7 was controlled to 1.2 MPa.
Volatile organic gas (volatile organic composition: 1% of organic substance having a molecular weight of 26 to 100, 49% of nitrogen, 50% of argon) is introduced from a volatile organic inlet 6 at the bottom of the fluidized bed section 1. In the conversion process, the space velocity of the volatile organic compound gas is 0.4g/gcat/h, and carbon products (carbon nano fibers) and products such as methane, hydrogen and the like are generated by cracking on a catalyst. The carbon products travel upwards with the gas and, after hitting the wire mesh layer 4, are bounced back mostly back to the fluidized bed section 1. Methane, hydrogen and unreacted volatile organic gas pass through the wire mesh layer 4 and enter the fixed bed section 2 to continue reaction.
The steam injection pipe 5 is opened, and steam with 5 percent of the total amount of volatile organic compounds is introduced. The carbon product adhered on the wire mesh layer 4 is reversely blown by the water vapor and returns to the fluidized bed section 1, so that the pressure drop of the wire mesh layer 4 is stable and the void ratio is unchanged. After being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section 2, and reacts with volatile organic gas and carbon products on the catalyst. The total non-methane hydrocarbons in the final gas is less than 45mg/Nm3And the gas product is discharged from a gas product outlet 7 after reaching the standard. The catalyst on the fixed bed section 2 does not deposit carbon and can be used for a long time.
When the carbon product of the fluidized bed section 1 is excessive, the apparatus is discharged from the carbon product outlet 9. And fresh catalyst is added through the fluidized bed section catalyst inlet 8. The above process is repeated.
Claims (10)
1. The device for efficiently converting the volatile organic compounds is characterized in that the lower section of the device is a fluidized bed section (1), the upper section of the device is a fixed bed section (2), and the fluidized bed section and the fixed bed section are separated by a porous distribution plate (3); a steam jet pipe (5) and a metal wire mesh layer (4) are sequentially arranged below the porous distribution plate (3); the bottom of the fluidized bed section (1) is provided with a volatile organic compound inlet (6), the top of the fixed bed section (2) is provided with a gas product outlet (7), the fluidized bed section (1) is provided with a fluidized bed section catalyst inlet (8) and a carbon product outlet (9), and the fixed bed section (2) is provided with a fixed bed section catalyst inlet (10).
2. The apparatus for converting volatile organic compounds (voc) according to claim 1, wherein the porosity of the porous distribution plate (3) is 30-70%, and the diameter of the single hole is smaller than the minimum size of the catalyst in the fixed bed section (2).
3. The device for converting volatile organic compounds with high efficiency according to claim 1, characterized in that a wire mesh layer (4) with the thickness of 1-3cm is arranged on the cross section of the fluidized bed section (1) 0.5-1m below the porous distribution plate (3); the void ratio of the metal wire mesh layer (4) is 90-95%, and the diameter of a single hole of the metal wire mesh is less than 0.01 mm; the wire mesh is made of stainless steel, nickel or platinum.
4. The apparatus for converting volatile organic compounds (voc) according to claim 1, wherein the steam injection pipe (5) is located at the center of the perforated distribution plate (3) and the wire mesh layer (4); the number of the steam injection pipes (5) is one or more, and the openings of the steam injection pipes are downward and are opposite to the wire mesh layer (4).
5. An apparatus for converting volatile organic compounds with high efficiency as claimed in claim 1, characterized in that the height of said fluidized bed section (1) is 2-5 times the height of said fixed bed section (2).
6. The apparatus for converting volatile organic compounds (voc) according to claim 1, wherein the catalyst in the fluidized bed section (1) and the fixed bed section (2) is a nano-metal supported catalyst, the metal component is one or more of Fe, Co, Ni, W, Cu, Mo and Mn, and the grain size is 1-20 nm; the carrier is one or more of alumina, silica, zirconia and magnesia, the mass fraction of the carrier is 10-90%, and the rest is metal; the nano metal supported catalyst used in the fluidized bed section (1) has an average particle diameter of 0.05 to 0.5 mm, and the nano metal supported catalyst used in the fixed bed section (2) has an average diameter of 2 to 10 mm.
7. The method for converting volatile organic compounds using the apparatus for converting volatile organic compounds according to any one of claims 1 to 6, comprising the steps of:
step 1: respectively filling the nano metal supported catalyst in the fluidized bed section (1) and the fixed bed section (2), heating the device to 500 ℃ and 1000 ℃, and controlling the absolute pressure of the gas product outlet (7) to be 0.1-2 MPa;
step 2: introducing volatile organic compound gas from a volatile organic compound inlet (6) at the bottom of the fluidized bed section (1), and cracking on a catalyst in the fluidized bed section (1) to generate a carbon product, methane and hydrogen gas; the carbon products move upwards along with the gas and are rebounded to return to the fluidized bed section (1) after encountering the wire mesh layer (4);
and step 3: methane, hydrogen and unreacted volatile organic gas pass through a wire mesh layer (4) and a porous distribution plate (3) and enter a fixed bed section (2) to continue to react;
and 4, step 4: opening a steam jet pipe (5), and introducing steam with the total amount of volatile organic compounds of 1-10%; the carbon product adhered on the wire mesh layer (4) is reversely blown by the water vapor and returns to the fluidized bed section (1), so that the pressure drop of the wire mesh layer (4) is stable and the void ratio is unchanged; after being sprayed downwards, the water vapor can automatically turn over and move upwards, enters the fixed bed section (2), and reacts with volatile organic gas and carbon products on the catalyst; the final gas product has less than 50mg/Nm of non-methane total hydrocarbons3The gas product is discharged through a gas product outlet (7) after reaching the standard; the catalyst on the fixed bed section (2) does not deposit carbon and can be used for a long time;
and 5: when the carbon product of the fluidized bed section (1) is excessive, discharging the carbon product out of the device through a carbon product outlet (9); and fresh catalyst is added through a fluidized bed section catalyst inlet (8); the above process is repeated.
8. The method according to claim 7, wherein the volatile organic gas is 0.01% -90% of organic gas with molecular weight of 26-150, and the rest is inert gas; in the conversion process, the space velocity of the volatile organic gas is 0.1-20 g/gcat/h.
9. The method of claim 8, wherein the inert gas is one or more of nitrogen, argon and water vapor.
10. The method of claim 7, wherein the carbon product is one or more of carbon nanotubes, graphene and carbon nanofibers.
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| US8845988B2 (en) * | 2007-05-23 | 2014-09-30 | Wyoming Research Products Center | Carbon-rich sorbent filters |
| CN203955014U (en) * | 2014-05-30 | 2014-11-26 | 浙江大学 | A kind of device that removes dioxin in high-temperature flue gas |
| CN107760377B (en) * | 2016-08-23 | 2021-03-30 | 中国石油化工股份有限公司 | Fluidized bed and fixed bed combined coal catalytic gasification reaction device and method thereof |
| CN106474910A (en) * | 2016-10-14 | 2017-03-08 | 黄华丽 | A kind of preparation of purifying agent for harmful gases and purification method and device |
| CN106390681A (en) * | 2016-11-15 | 2017-02-15 | 东莞市佳明环保科技有限公司 | Double-fluidized bed adsorption and desorption device and method for continuous treatment of organic waste gas |
| CN110002932B (en) * | 2019-04-18 | 2020-12-01 | 清华大学 | Method and device for preparing aromatic hydrocarbon by using synthesis gas |
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