CN116550286A - Light-heat synergistic low-carbon green modified biochar-based CO adsorption 2 Apparatus and method of (a) - Google Patents
Light-heat synergistic low-carbon green modified biochar-based CO adsorption 2 Apparatus and method of (a) Download PDFInfo
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
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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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
- B01J20/0259—Compounds of N, P, As, Sb, Bi
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/0203—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of metals not provided for in B01J20/04
- B01J20/0262—Compounds of O, S, Se, Te
- B01J20/0266—Compounds of S
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/3085—Chemical treatments not covered by groups B01J20/3007 - B01J20/3078
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
Light-heat synergistic low-carbon green modified biochar-based CO adsorption 2 The device and the method adopt a modifying reagent to induce and release hydroxyl free radicals, sulfate radical and nitrogen-hydrogen free radicals under the synergistic effect of ultraviolet light and temperature to jointly modify the biochar to generate high active sites. The modified biochar enters a mixing reaction tower and contains CO from a combustion device 2 The flue gas is subjected to adsorption reaction in the tower, and the reacted biochar is separated by a cloth bag separator and then is sent into a photochemical-thermochemical synergistic modification tower again for modification and regeneration, so that CO is separated 2 The combustion flue gas is discharged into the atmosphere. The biochar in the device and the method can be recycled, and the gas-solid mass transfer rate of the mixed reaction tower is high, so that CO can be efficiently adsorbed 2 。
Description
Technical Field
The invention relates to the CO in the combustion flue gas 2 In particular to a photo-thermal coordination-based trapping fieldCO adsorption with low-carbon green modified biochar 2 Is provided.
Background
Since the industrial revolution, fossil fuels have been an irreplaceable energy source to provide continuous energy for humans. Greenhouse gases are inevitably generated in the process of using fossil fuels by human beings, so that natural disasters such as warm weather, rising sea level, flood, drought, waterlogging and the like frequently occur, and the ecological balance of the earth is seriously damaged. Thus, CO 2 Trapping, utilizing and sequestering (CCUS) are becoming research hotspots in the scientific and industrial world, actively studying and developing CO in combustion flue gases 2 Has important strategic significance in emission reduction technology.
Up to now, the mainstream CO developed at home and abroad 2 The trapping technology mainly comprises a membrane separation method, a liquid phase absorption method, an adsorption method, an oxygen-enriched combustion method, a low-temperature separation method, a chemical-looping combustion method, a hydrothermal method and a photo/electrochemical method.
The membrane separation method has the advantages of simple process, no waste generation and the like, and is a CO with better development prospect 2 Trapping technology, however, currently has practical problems of short membrane life and low separation purity. The low-temperature separation method has the advantages of simple and environment-friendly process, suitability for large-scale treatment and the like, but has the defects of high energy consumption and high-pressure operation, and is mainly used for treating high-concentration CO 2 Is separated from the other components. The liquid phase absorption method mainly utilizes various alcohol amine organic solvents/ammonia water/ionic liquid and the like to realize CO 2 Is absorbed and trapped by liquid phase, and then realizes the activation regeneration of the liquid phase absorbent and CO through processes such as heating and desorption 2 The method can realize the recycling of the absorbent theoretically, but the practical application finds that the defects of serious reagent loss, large regeneration energy consumption and the like exist, and part of the reagent also has the problem of corroding equipment. The oxygen-enriched combustion method and the chemical looping combustion method mainly realize CO by constructing novel combustion conditions and combustion modes 2 But will affect the existing combustion device and working condition, and is not suitable for treating the existing and huge-keeping boiler/kiln and other traditional combustion devices. Emerging carbon emission reduction technologies such as hydrothermal method, photo/electrochemical method and the like are still in experimentThe chamber exploration phase is still a distance from industrial applications. The adsorption and removal method has been concerned with the academic world and engineering world at home and abroad because of the advantages of the regenerable adsorbent and no waste liquid in the removal process, and has become the CO with the most development prospect at present 2 One of the trapping techniques. Adsorption separation of CO 2 The technology is most applied to the adsorption of CO in the flue gas by adopting activated carbon as an adsorbent 2 Regeneration of the adsorbent and CO is then achieved by thermal desorption 2 Is recovered. However, the technology has the defects of huge consumption of active carbon, high application cost and the like, and cannot realize large-scale industrial application, wherein the development of the adsorbent with low cost is a key ring for realizing the application of the technology.
Biochar (Biochar) is a pyrolysis product from agricultural and forestry waste or organic industrial waste, has the advantages of wide raw material source, low cost, environmental protection and the like, but the original Biochar without activation modification generally has the defects of small specific surface area and poor active site, and is difficult to obtain satisfactory CO 2 Adsorption capacity. To improve CO of biochar 2 The adsorption performance can be improved by scholars at home and abroad through various physicochemical activation/modification means, or active sites are induced on the surface of the biochar, so that the biochar has a special high-activity surface. The pore structure and specific surface area of the biochar can be effectively improved by activating the biochar at high temperature or under a special atmosphere by microwaves, but the improvement on vital active sites is very limited. Most research work is currently focused on improving the surface active sites of biochar by various chemical means, and the most studied ideas mainly include: (1) Activating and modifying by adopting reagents such as organic alcohol ammonium, ammonia gas or ionic liquid; (2) Doping modification is carried out by adopting various metal or nonmetal elements; and (3) adopting strong acid and strong oxidant to carry out oxidation modification. Although the modification of the activated modification method on the biochar can effectively increase the specific surface area or the surface active site of the biochar, the method has the problems of high cost, poor treatment effect, secondary pollution or higher energy consumption. Therefore, the development of a novel efficient green biochar modification method is actively explored, and the method has important scientific significance and practical significance.
Disclosure of Invention
In order to overcome the development bottleneck, the invention discloses a light-heat synergistic low-carbon green modified biochar-based CO adsorption method 2 Is provided. The biochar used in the invention has wide sources, low cost and recycling, can effectively solve the problem of high cost in other methods, and secondly, the photochemical-thermochemical synergistic modification tower in the device has an internal gas-solid nozzle array which can effectively promote the rate of activating modified biochar; the suspension type combustion flue gas nozzle positioned at the top of the mixed reaction tower and the bottom combustion flue gas nozzle positioned at the bottom of the mixed reaction tower can accelerate the gas-solid mass transfer rate, thereby improving the capture of CO 2 The invention uses dry method removing technique, without waste water and waste liquid, and reagent leakage risk, so that it has no secondary pollution.
The invention is realized by the following technical scheme:
light-heat synergistic low-carbon green modified biochar-based CO adsorption 2 Is characterized in that: comprises a biochar feeding device, a modifying reagent container, a photochemical-thermochemical synergistic modifying tower, a modified biochar quantitative feeder, a cloth bag separator, a mixed reaction tower, a combustion flue gas temperature regulator and a combustion device;
the charcoal feeding device is communicated with the upper part of the photochemical-thermochemical synergistic modification tower, the modification reagent container is communicated with the lower part of the photochemical-thermochemical synergistic modification tower, and a gas-solid nozzle array positioned at the bottom, a plurality of gravity heat pipes and ultraviolet lamp tubes which are hoisted on the inner wall of the top are arranged in the photochemical-thermochemical synergistic modification tower; one end of the side of the photochemical-thermochemical synergistic modification tower is communicated with the gas-solid nozzle array, and the other end of the side of the photochemical-thermochemical synergistic modification tower is communicated with a circulating bypass of the photochemical-thermochemical synergistic modification tower from the top; the circulating bypass is provided with a first fan, and the circulating direction provided by the circulating bypass is from top to bottom in a circulating flow mode; the outlet of the photochemical-thermochemical synergistic modification tower is communicated with the modified biochar quantitative feeder and the second fan;
the mixed reaction tower is internally provided with a suspended combustion flue gas nozzle suspended at the top and a bottom combustion flue gas nozzle positioned at the bottom, flue gas in the combustion device is divided into two paths of pipelines after being subjected to temperature adjustment by a combustion flue gas temperature regulator, the two paths of pipelines are respectively communicated with the suspended combustion flue gas nozzle and the bottom combustion flue gas nozzle, and an outlet of the mixed reaction tower is communicated with the cloth bag separator.
In the scheme, a first outlet and a second outlet are arranged on the cloth bag separator, the first outlet is communicated with the photochemical-thermochemical synergistic modification tower, the second outlet is communicated with the atmosphere, and a fourth fan is arranged on a pipeline of the second outlet.
In the scheme, the photochemical-thermochemical synergistic modification tower is a modification reactor with a rectangular section or a circular section, and all the nozzles in the ultraviolet lamp tube, the gravity heat pipe and the gas-solid nozzle array are arranged in a rectangular array or a circular array.
In the scheme, the ultraviolet lamp tube and the gravity heat tube are both hoisted at the top of the photochemical-thermochemical synergistic modification tower and extend in the up-down direction, and are alternately arranged between the ultraviolet lamp tube and the gravity heat tube; the ultraviolet lamp tubes and the gravity heat pipes are arranged at equal intervals, the interval between every two adjacent ultraviolet lamp tubes is 5cm-80cm, the gravity heat pipes are arranged at the center of the ultraviolet lamp tubes, the central lines of the ultraviolet lamp tubes and the gravity heat pipes are parallel to the axial central line of the photochemical-thermochemical synergistic modification tower, the effective wavelength of ultraviolet light is 150nm-290nm, the length of the ultraviolet lamp tubes is 40cm-450cm, and the length of the gravity heat pipes is the same as that of the ultraviolet lamp tubes; the spacing between the individual nozzles in the gas-solid nozzle array is in the range of 5cm to 30cm.
In the scheme, the distance range between the bottom combustion flue gas nozzles is 10cm-60cm, the distance between the suspension type combustion flue gas nozzles is 2 times of the distance between the bottom combustion flue gas nozzles, the length range of the vertical suspension pipe of the suspension type combustion flue gas nozzles in the mixing reaction tower is 100cm-1500cm, and the combustion device is communicated with the combustion flue gas temperature regulator through the third fan.
In the above scheme, the device adsorbs CO 2 The method is characterized by comprising the following steps:
(1) The smoke waste heat and ultraviolet light are utilized to cooperatively induce a modifying reagent, and the modifying reagentContains hydrogen peroxide (H) 2 O 2 ) Persulfates (S) 2 O 8 2- ) Ammonia (NH) 3 ·H 2 O), the modifying reagent generates hydroxyl radical (OH) and sulfate radical (SO) after ultraviolet light induction 4 - ) And/or active free radicals of nitrogen-hydrogen free radicals (NH), wherein the active free radicals attack the surface of the Biochar (Biochar) to generate active sites, and the activated modification of the Biochar is completed in a photochemical-thermochemical synergistic modification tower, and the specific process is represented by the following equations (1) - (6):
n·OH+Biochar——→Biochar-active sites (4)
nSO 4 · - +Biochar——→Biochar-active sites (5)
nNH·+Biochar→Biochar-active sites (6)
(2) The modified biochar enters a mixing reaction tower and contains CO from a combustion device 2 The flue gas in the mixing reaction tower is subjected to adsorption reaction, and CO in the flue gas is adsorbed and trapped by utilizing active sites 2 Desorption of CO by heating 2 And realize the sealing or utilization after recycling, the specific process is as shown in equations (7) and (8):
the biochar which loses active sites after adsorption is led into a cloth bag separator to be separated, and CO is removed 2 The combustion flue gas is discharged into the atmosphere.
The adsorption of CO 2 In the method, the biochar separated in the cloth bag separator is introduced into a photochemical-thermochemical synergistic modification tower again through a first outlet for recycling, and then modified regeneration is realized through equations (1) - (6) so as to recover the adsorbed CO 2 Is provided).
The adsorption of CO 2 According to the difference of the loss rate of the biochar in use, the modification time of the biochar in the photochemical-thermochemical synergistic modification tower is 10min-180min, the modification temperature of the biochar is required to be kept at 30-150 ℃, and the circulation rate of a circulation bypass is 20m 3 /h-600m 3 And/h, the ultraviolet radiation intensity is 30 mu W/cm 2 -300μW/cm 2 The heat radiation intensity of the gravity assisted heat pipe is 50W/m 2 -600 W/m 2 。
The adsorption of CO 2 In the method, the reaction temperature in the mixed reaction tower is kept at 25-140 ℃, and CO in the flue gas from the combustion device 2 The inlet concentration of the catalyst is not more than 60 percent, and the biochar in the mixed reaction tower is used for removing CO 2 The residence time of the gas is 10s-180s, the combustion flue gas quantity entering the bottom combustion flue gas nozzle accounts for 20% -30% of the total combustion flue gas quantity, and the combustion flue gas quantity entering the suspension combustion flue gas nozzle accounts for 70% -80% of the total combustion flue gas quantity.
The adsorption of CO 2 In the method, the used biochar is the biochar obtained by cracking agricultural straws or the biochar obtained by cracking municipal sludge, fruit shells and industrial organic wastes; the agricultural straw is one or more of rice straw, wheat straw, cotton straw, corn straw, rice hull and corncob; the adding amount of the biochar is 0.4kg-16kg per cubic meter of the volume of the photochemical-thermochemical synergistic modification tower, and the particle size of the biochar is required to be kept between 0.02 mu m and 1.2 mu m.
The adsorption of CO 2 In the method of (2), the modifying reagent hydrogen peroxide (H 2 O 2 ) Concentration of (2) addedTo be maintained at 0.02mol/L to 8.0mol/L, the modifying agent persulfate (S 2 O 8 2- ) The adding concentration of the modified reagent ammonia water (NH) is required to be kept between 0.01mol/L and 5.0mol/L 3 ·H 2 The adding concentration of the O) is required to be kept between 0.01mol/L and 5.0mol/L, and the adding amount of the modifying reagent is 100g to 5000g per cubic meter according to the volume of the photochemical-thermochemical synergistic modifying tower.
Compared with the prior art, the invention has the following beneficial effects:
firstly, the invention adopts the low-cost agricultural straw or organic waste to crack and prepare the biochar, and adopts the technical scheme of modifying the biochar in real time to realize the recycling of the biochar, compared with a catalytic method and a membrane separation method, the technology has extremely low cost, the process is green and environment-friendly, and compared with other adsorption methods, the technology has more advantages, and is the CO with low cost 2 Adsorption apparatus and method.
Secondly, the light-heat synergistic low-carbon green modified biochar-based CO adsorption method 2 CO 2 The adsorption process is to utilize biochar to adsorb CO in the combustion flue gas in a mixed reaction tower 2 The mixed reaction tower has extremely strong gas-solid mass transfer rate, which is improved by one order of magnitude compared with the mass transfer rate of the traditional fixed bed and the fluidized bed, and can greatly improve CO 2 And reduces the volume of the reactor.
And the dry removal technology used in the invention does not generate any waste water or waste liquid in the whole process, does not leak reagent, and avoids the treatment difficulty of a large amount of solid waste generated by membrane separation and catalysis methods due to membrane material and catalyst deactivation, so that the method has no secondary pollution and accords with the green sustainable development strategy proposed by the current country.
Finally, the invention utilizes the flue gas waste heat and ultraviolet light to cooperatively induce the high-activity free radical modified biochar, and adopts a low-energy-consumption mixed reaction tower to adsorb CO 2 Because the ultraviolet radiation intensity is very low, and the gravity assisted heat pipe rapidly absorbs the waste heat in the flue gas, then radiates heat on the surface of the gravity assisted heat pipe, and forms photo-thermal synergistic activation with ultraviolet light, the energy consumption of the method is reducedCompared with the low-temperature separation technology, the energy consumption required by the operation of the whole device is extremely low by more than 3 orders of magnitude, and the device has the beneficial effects of energy conservation and low carbon.
Drawings
FIG. 1 is a schematic diagram of a photochemistry-thermochemical CO-modification tower modified biochar CO adsorption 2 The overall schematic of the device.
FIG. 2 is a schematic diagram of a rectangular arrangement of ultraviolet lamps, gravity assisted heat pipes and nozzles in a photochemical-thermochemical co-modification tower.
FIG. 3 is a schematic view of a circular arrangement of ultraviolet lamps, gravity assisted heat pipes and nozzles in a photochemical-thermochemical co-modification tower.
FIG. 4 is a schematic diagram of a rectangular arrangement of suspended and bottom combustion flue gas nozzles in a mixing reaction tower.
FIG. 5 is a schematic view of a circular arrangement of a suspended combustion flue gas nozzle and a bottom combustion flue gas nozzle in a mixing reaction tower.
In the figure: 1. the device comprises a biochar feeding device 2, a first fan, 3, a circulating bypass, 4, a gas-solid nozzle array, 5, a modifying reagent container, 6, a photochemical-thermochemical synergistic modifying tower, 7, a gravity heat pipe, 8, an ultraviolet lamp tube, 9, a modified biochar quantitative feeder, 10, a cloth bag separator, 10-1, a first outlet, 10-2, a second outlet, 11, a suspended combustion flue gas nozzle, 12, a mixing reaction tower, 13, a bottom combustion flue gas nozzle, 14, a combustion flue gas temperature regulator, 15, a combustion device, 16, a second fan, 17, a third fan, 18 and a fourth fan.
Detailed Description
The present invention will be described in further detail with reference to the drawings, but the scope of the invention is not limited thereto.
As shown in figure 1, the light-heat synergistic low-carbon green modified biochar based CO adsorption method of the invention 2 The device comprises a biochar feeding device 1, a modifying reagent container 5, a photochemical-thermochemical synergistic modifying tower 6, a modified biochar quantitative feeder 9, a cloth bag separator 10, a mixing reaction tower 12, a combustion flue gas temperature regulator 14 and a combustion device 15.
The biochar feeding device 1 is communicated with the upper part of the photochemical-thermochemical synergetic modification tower 6 and is used for conveying biochar into the photochemical-thermochemical synergetic modification tower 6; the modifying reagent container 5 is communicated with the lower part of the photochemical-thermochemical synergetic modifying tower 6 to provide modifying reagent for the photochemical-thermochemical synergetic modifying tower 6;
the photochemical-thermochemical synergistic modification tower 6 is internally provided with a gas-solid nozzle array 4 positioned at the bottom, a plurality of gravity heat pipes 7 hung on the inner wall of the top and an ultraviolet lamp tube 8, as shown in fig. 2 or 3, the distance range between the nozzles in the gas-solid nozzle array 4 is 5cm-30cm, the ultraviolet lamp tubes 8 and the gravity heat pipes 7 are equally spaced, the distance between the ultraviolet lamp tubes 8 is 5cm-80cm, the gravity heat pipes 7 are arranged at the center of the ultraviolet lamp tubes 8, the central lines of the ultraviolet lamp tubes 8 and the gravity heat pipes 7 are parallel to the axial central line of the photochemical-thermochemical synergistic modification tower 6, the effective wavelength of ultraviolet light is 150nm-290nm, the length of the ultraviolet lamp tubes 8 is 40cm-450cm, and the length of the gravity heat pipes 7 is the same as that of the ultraviolet lamp tubes 8.
One end of the side of the photochemical-thermochemical synergistic modification tower 6 is communicated with the gas-solid nozzle array 4, and the other end of the side is introduced into the circulation bypass 3 of the photochemical-thermochemical synergistic modification tower 6 from the top; the circulating bypass 3 is provided with a first fan 2 for accelerating the flow velocity in a circulating bypass pipeline; the circulation direction provided by the circulation bypass 3 is from top to bottom in a circulating way, and on the basis of the circulation direction, the modifying reagent and the biochar are continuously sprayed upwards from the gas-solid nozzle array 4, so that the activated modifying efficiency of the biochar is further accelerated;
in fig. 1, an outlet of the photochemical-thermochemical synergistic modification tower 6 is communicated with the mixed reaction tower 12 through a modified biochar quantitative feeder 9, a second fan 16, and activated modified biochar enters the mixed reaction tower 12 from the outlet, wherein the second fan 16 is used for accelerating the speed of the activated modified biochar gas-solid mixture entering the modified biochar quantitative feeder 9;
the mixing reaction tower 12 is internally provided with a suspension type combustion flue gas nozzle 11 suspended at the top and a bottom combustion flue gas nozzle 13 positioned at the bottom, the distance between the bottom combustion flue gas nozzles 13 is 10cm-60cm, the distance between the suspension type combustion flue gas nozzles 11 is 2 times of the distance between the bottom combustion flue gas nozzles 13, and the length of a vertical suspension pipe of the suspension type combustion flue gas nozzle 11 in the mixing reaction tower 12 is 100cm-1500cm;
in fig. 1, the combustion device 15 is communicated with the combustion flue gas attemperator 14 through a third fan 17, and the third fan 17 is used for accelerating the flue gas velocity; the flue gas in the combustion device 15 is divided into two paths of pipelines after being subjected to temperature adjustment by the combustion flue gas temperature adjuster 14, and is respectively communicated with the suspension type combustion flue gas nozzle 11 and the bottom combustion flue gas nozzle 13;
the outlet of the mixing reaction tower 12 is communicated with a cloth bag separator 10, a first outlet 10-1 and a second outlet 10-2 are arranged on the cloth bag separator 10, the first outlet 10-1 is communicated with a photochemical-thermochemical synergistic modification tower 6, and after the used biochar is separated in the cloth bag separator 10, the biochar is sent to the photochemical-thermochemical synergistic modification tower 6 again through the first outlet 10-1 for reactivation modification; the second outlet 10-2 is opened to the atmosphere, a fourth fan 18 is arranged on the pipeline of the second outlet 10-2, and CO is treated 2 Is accelerated to the atmosphere by the fourth fan 18.
As shown in fig. 4 or fig. 5, the bottom combustion flue gas nozzles 13 in the mixing reaction tower 12 are arranged in a rectangular or circular shape to spray the gas-solid mixture upwards, while the suspension type combustion flue gas nozzles 11 at the top of the mixing reaction tower 12 can spray the gas-solid mixture transversely, and the two cooperate to form a mixed or cross-spray diffusion gas-solid mixture, so as to further enhance the gas-solid mixing and mass transfer diffusion reaction rate.
CO adsorption device based on the device 2 A method comprising the steps of:
(1) The flue gas waste heat and ultraviolet light are utilized to cooperatively induce a modifying reagent, and the modifying reagent contains hydrogen peroxide (H) 2 O 2 ) Persulfates (S) 2 O 8 2- ) Ammonia (NH) 3 ·H 2 O), the modifying reagent generates hydroxyl radical (OH) and sulfate radical (SO) after ultraviolet light induction 4 - ) And/or active radicals of nitrogen-hydrogen radicals (NH), which attack biochar (Bioc)har) surface generating active sites (active sites), and completing activated modification of biochar in a photochemical-thermochemical co-modifying tower 6, wherein the specific process is represented by equations (1) - (6):
n·OH+Biochar——→Biochar-active sites (4)
nSO 4 · - +Biochar——→Biochar-active sites (5)
(2) The modified biochar enters the mixing reaction tower 12 and contains CO from the combustion device 15 2 The flue gas in the mixing reaction tower 12 is subjected to adsorption reaction, and CO in the flue gas is adsorbed and trapped by utilizing active sites 2 Desorption of CO by heating 2 And realize the sealing or utilization after recycling, the specific process is as shown in equations (7) and (8):
the biochar which loses active sites after adsorption is led into a cloth bag separator 10 to be separated, and CO is removed 2 The combustion flue gas is discharged into the atmosphere.
The adsorption of CO 2 In the method of (2), the clothThe biochar separated in the bag separator 10 is introduced into the photochemical-thermochemical synergetic modification tower 6 again through the first outlet 10-1 for recycling, and then modified regeneration is realized through the equations (1) - (6) so as to recover the adsorbed CO 2 Is provided).
The adsorption of CO 2 According to the difference of the loss rate of the biochar in use, the modification time of the biochar in the photochemical-thermochemical synergistic modification tower 6 is 10min-180min, the modification temperature of the biochar is required to be kept at 30-150 ℃, and the circulation rate of the circulation bypass 3 is 20m 3 /h-600m 3 And/h, the ultraviolet radiation intensity is 30 mu W/cm 2 -300μW/cm 2 The heat radiation intensity of the gravity assisted heat pipe is 50W/m 2 -600 W/m 2 。
The adsorption of CO 2 In the method (2), the reaction temperature in the mixed reaction tower 12 is kept at 25-140 ℃, and CO in the flue gas from the combustion device 15 is needed to be kept 2 The inlet concentration of (2) is not more than 60%, and the biochar in the mixed reaction tower 12 is used for removing CO 2 The residence time of (2) is 10s-180s, the combustion flue gas quantity entering the bottom combustion flue gas nozzle 13 accounts for 20% -30% of the total combustion flue gas quantity, and the combustion flue gas quantity entering the suspension combustion flue gas nozzle 11 accounts for 70% -80% of the total combustion flue gas quantity.
The adsorption of CO 2 In the method, the used biochar is the biochar obtained by cracking agricultural straws or the biochar obtained by cracking municipal sludge, fruit shells and industrial organic wastes; the agricultural straw is one or more of rice straw, wheat straw, cotton straw, corn straw, rice hull and corncob; the adding amount of the biochar is 0.4kg-16kg per cubic meter of the volume of the photochemical-thermochemical synergistic modification tower 6, and the particle size of the biochar is required to be kept between 0.02 mu m and 1.2 mu m.
The adsorption of CO 2 In the method of (2), the modifying reagent hydrogen peroxide (H 2 O 2 ) The addition concentration of the modified agent persulfate (S) is required to be kept between 0.02 and 8.0mol/L 2 O 8 2- ) The adding concentration of the modified reagent ammonia water (NH) is required to be kept between 0.01mol/L and 5.0mol/L 3 ·H 2 The adding concentration of the O) is required to be kept between 0.01mol/L and 5.0mol/L, and the modifying reagentThe adding amount is 100g-5000g per cubic meter according to the volume of the photochemical-thermochemical synergistic modification tower 6.
Example 1:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation are 20 mu W/cm respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.05mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.1mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.05mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 60g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 120g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 60g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 35.7%.
Example 2:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation are 40 mu W/cm respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.05mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.1mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.05mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 60g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the catalyst is per cubic meter of photochemical-thermochemical synergistic modification tower120g of modifying reagent H is added 2 O 2 The adding amount of the catalyst is 60g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) was 42.2%.
Example 3:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation are 40 mu W/cm respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.1mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.2mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.1mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 60g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 120g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 60g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 56.8%.
Example 4:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation were 60. Mu.W/cm, respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.1mol/L 2 O 2 The addition concentration of (C) is 0.2mol/L, and the modification test is carried outAgent Na 2 S 2 O 8 The adding concentration of the modified reagent H is 0.1mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 60g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 120g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 60g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 64.9%.
Example 5:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation were 60. Mu.W/cm, respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.3mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 60g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 120g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 60g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) was 76.0%.
Example 6:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation were 80. Mu.W/cm, respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.3mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 100g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 180g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 100g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 0.5kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 84.5%.
Example 7:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation were 80. Mu.W/cm, respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.3mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 100g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 180g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 100g per cubic meter of photochemical-thermochemical synergistic modification tower, and the biochar is microWave steam activated rice straw charcoal, the concentration of the biochar is 1.0 kg/cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 89.6%.
Example 8:
the modification temperature of the photochemical-thermochemical synergistic modification tower is 55 ℃, and the heat radiation intensity of the gravity heat pipe is 100W/m 2 The intensity and wavelength of the ultraviolet radiation were 80. Mu.W/cm, respectively 2 And 254nm, modifying reagent NH 3 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent Na is 0.3mol/L 2 S 2 O 8 The adding concentration of the modified reagent H is 0.2mol/L 2 O 2 The adding concentration of the modified reagent NH is 0.1mol/L 3 The adding amount of the modified reagent Na is 100g per cubic meter of photochemical-thermochemical synergistic modification tower 2 S 2 O 8 The adding amount of the modified reagent H is 180g per cubic meter of photochemical-thermochemical synergistic modification tower 2 O 2 The adding amount of the catalyst is 100g per cubic meter of photochemical-thermochemical synergistic modification tower, the biochar is microwave steam activated rice straw charcoal, the concentration of the biochar is 1.0kg per cubic meter of mixed reaction tower, and CO is adsorbed in the mixed reaction tower 2 The operating temperature of (2) was 25 ℃. Simulating CO in combustion flue gas 2 The concentration of (2) was 10%. The test results on the small experiment system are: CO in combustion flue gas 2 The adsorption removal efficiency of (2) is 92.8%.
In summary, in the eight embodiments, the embodiment 8 has the best simultaneous removal effect, and can be used as a preferred scheme.
The examples are embodiments of the present invention, but the present invention is not limited to the above-described embodiments, and any obvious modifications, substitutions or variations that can be made by one skilled in the art without departing from the spirit of the present invention are within the scope of the present invention.
Claims (10)
1. BaseCO adsorption by light-heat synergistic low-carbon green modified biochar 2 Is characterized in that: comprises a biochar feeding device (1), a modifying reagent container (5), a photochemical-thermochemical synergetic modifying tower (6), a modified biochar quantitative feeder (9), a cloth bag separator (10), a mixing reaction tower (12), a combustion flue gas temperature regulator (14) and a combustion device (15);
the charcoal feeding device (1) is communicated with the upper part of the photochemical-thermochemical synergistic modification tower (6), the modification reagent container (5) is communicated with the lower part of the photochemical-thermochemical synergistic modification tower (6), and a gas-solid nozzle array (4) positioned at the bottom, a plurality of gravity heat pipes (7) hung on the inner wall of the top and an ultraviolet lamp tube (8) are arranged in the photochemical-thermochemical synergistic modification tower (6); one end of the side of the photochemical-thermochemical synergistic modification tower (6) is communicated with the gas-solid nozzle array (4), and the other end of the side is introduced into the circulation bypass (3) of the photochemical-thermochemical synergistic modification tower (6) from the top; the circulating bypass (3) is provided with a first fan (2), and the circulating direction provided by the circulating bypass (3) is from top to bottom in a circulating way; the outlet of the photochemical-thermochemical synergistic modification tower (6) is communicated with the modified biochar quantitative feeder (9) and the second fan (16) through the mixing reaction tower (12);
the mixed reaction tower (12) is internally provided with a suspended combustion flue gas nozzle (11) suspended at the top and a bottom combustion flue gas nozzle (13) positioned at the bottom, flue gas in the combustion device (15) is subjected to temperature adjustment by a combustion flue gas temperature regulator (14) and then is divided into two paths of pipelines, the two paths of pipelines are respectively communicated with the suspended combustion flue gas nozzle (11) and the bottom combustion flue gas nozzle (13), and an outlet of the mixed reaction tower (12) is communicated with the cloth bag separator (10).
2. The CO-adsorption based on photo-thermal synergistic low-carbon green modified biochar according to claim 1 2 Is characterized in that: the cloth bag separator (10) is provided with a first outlet (10-1) and a second outlet (10-2), the first outlet (10-1) is communicated with the photochemical-thermochemical synergistic modification tower (6), the second outlet (10-2) is communicated with the atmosphere, and a fourth fan (18) is arranged on a pipeline of the second outlet (10-2).
3. According to claimThe light-heat synergy low-carbon green modified biochar adsorption CO as described in the item 1 2 Is characterized in that: the photochemical-thermochemical synergistic modification tower (6) is a modification reactor with a rectangular section or a circular section, and all nozzles in the ultraviolet lamp tube (8), the gravity heat tube (7) and the gas-solid nozzle array (4) are arranged in a rectangular array or a circular array;
the ultraviolet lamp tube (8) and the gravity heat tube (7) are both hoisted at the top of the photochemical-thermochemical synergistic modification tower (6), extend in the up-down direction and are alternately arranged between the two; the ultraviolet lamp tubes (8) and the gravity heat pipes (7) are arranged at equal intervals, the interval between every two adjacent ultraviolet lamp tubes (8) is 5cm-80cm, the gravity heat pipes (7) are arranged at the center of the ultraviolet lamp tubes (8), the central lines of the ultraviolet lamp tubes (8) and the gravity heat pipes (7) are parallel to the axial central line of the photochemical-thermochemical synergetic modification tower (6), the effective wavelength of ultraviolet light is 150nm-290nm, the length of the ultraviolet lamp tubes (8) is 40cm-450cm, and the length of the gravity heat pipes (7) is the same as that of the ultraviolet lamp tubes (8); the distance between the nozzles in the gas-solid nozzle array (4) is in the range of 5cm-30cm.
4. The CO-adsorption based on photo-thermal synergistic low-carbon green modified biochar according to claim 1 2 Is characterized in that: the range of the interval between the bottom combustion flue gas nozzles (13) is 10cm-60cm, the interval between the suspension type combustion flue gas nozzles (11) is 2 times of the interval between the bottom combustion flue gas nozzles (13), the length range of the vertical suspension pipe of the suspension type combustion flue gas nozzles (11) in the mixing reaction tower (12) is 100cm-1500cm, and the combustion device (15) is communicated with the combustion flue gas temperature regulator (14) through the third fan (17).
5. Adsorption of CO based on the device of any one of claims 1-4 2 The method is characterized by comprising the following steps:
(1) The flue gas waste heat and ultraviolet light are utilized to cooperatively induce a modifying reagent, and the modifying reagent contains hydrogen peroxide (H) 2 O 2 ) Persulfates (S) 2 O 8 2- ) Ammonia (NH) 3 ·H 2 One of O)Or more of the modifying agents generate hydroxyl radical (OH) and sulfate radical (SO) after ultraviolet light induction 4 - ) And/or active free radicals of nitrogen-hydrogen free radicals (NH), wherein the active free radicals attack the surface of the Biochar (Biochar) to generate active sites, and the activated modification of the Biochar is finished in a photochemical-thermochemical synergistic modification tower (6), and the specific process is expressed as the following equations (1) - (6):
n·OH+Biochar→Biochar-active sites (4)
nSO 4 · - +Biochar→Biochar-active sites (5)
nNH·+Biochar→Biochar-active sites (6)
(2) The modified biochar enters a mixing reaction tower (12) and contains CO from a combustion device (15) 2 The flue gas of (2) is subjected to adsorption reaction in a mixed reaction tower (12), and CO in the flue gas is adsorbed and trapped by utilizing active sites 2 Desorption of CO by heating 2 And realize the sealing or utilization after recycling, the specific process is as shown in equations (7) and (8):
biochar quilt with active sites lost after adsorptionSeparating by passing through a cloth bag separator (10) to remove CO 2 The combustion flue gas is discharged into the atmosphere.
6. The CO-adsorbing of claim 5 2 The method is characterized in that: the biochar separated in the cloth bag separator (10) is re-introduced into the photochemical-thermochemical synergistic modification tower (6) for recycling through a first outlet (10-1), and then modified and regenerated through equations (1) - (6) to recover adsorbed CO 2 Is provided).
7. The CO-adsorbing of claim 5 2 The method is characterized in that: according to the difference of loss rate of biochar in use, the time for modifying the biochar in the photochemical-thermochemical synergistic modification tower (6) is 10min-180min, the modification temperature of the biochar is required to be kept at 30-150 ℃, and the circulation rate of the circulation bypass (3) is 20m 3 /h-600m 3 And/h, the ultraviolet radiation intensity is 30 mu W/cm 2 -300μW/cm 2 The heat radiation intensity of the gravity assisted heat pipe is 50W/m 2 -600 W/m 2 。
8. The CO-adsorbing of claim 5 2 The method is characterized in that the reaction temperature in the mixed reaction tower (12) is kept at 25-140 ℃, and CO in the flue gas from the combustion device (15) 2 The inlet concentration of (2) is not more than 60%, and the biochar in the mixed reaction tower (12) is used for removing CO 2 The residence time of the gas is 10s-180s, the combustion flue gas quantity entering the bottom combustion flue gas nozzle (13) accounts for 20% -30% of the total combustion flue gas quantity, and the combustion flue gas quantity entering the suspension combustion flue gas nozzle (11) accounts for 70% -80% of the total combustion flue gas quantity.
9. The CO-adsorbing of claim 5 2 The method is characterized in that the used biochar is the biochar obtained by cracking agricultural straws or the biochar obtained by cracking municipal sludge, fruit shells and industrial organic wastes; the agricultural straw is one or more of rice straw, wheat straw, cotton straw, corn straw, rice hull and corncob; biochar (biochar)The adding amount is 0.4kg-16kg of the charcoal is added per cubic meter of the volume of the photochemical-thermochemical synergistic modification tower (6), and the grain size of the charcoal is required to be kept between 0.02 mu m and 1.2 mu m.
10. The CO-adsorbing of claim 5 2 The method is characterized in that the modifying agent hydrogen peroxide (H 2 O 2 ) The addition concentration of the modified agent persulfate (S) is required to be kept between 0.02 and 8.0mol/L 2 O 8 2- ) The adding concentration of the modified reagent ammonia water (NH) is required to be kept between 0.01mol/L and 5.0mol/L 3 ·H 2 The adding concentration of the O) is kept between 0.01mol/L and 5.0mol/L, and the adding amount of the modifying reagent is 100g to 5000g per cubic meter according to the volume of the photochemical-thermochemical synergistic modifying tower (6).
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| CN115888649A (en) * | 2022-11-16 | 2023-04-04 | 江苏大学 | Method and device for adsorbing VOCs (volatile organic compounds) by using modified charcoal based on high-energy radiation induced active components |
| CN115888648A (en) * | 2022-11-16 | 2023-04-04 | 江苏大学 | CO adsorption and removal based on free radical induction multi-element modified porous carbon 2 Method and system for generating a response to a user |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115888649A (en) * | 2022-11-16 | 2023-04-04 | 江苏大学 | Method and device for adsorbing VOCs (volatile organic compounds) by using modified charcoal based on high-energy radiation induced active components |
| CN115888648A (en) * | 2022-11-16 | 2023-04-04 | 江苏大学 | CO adsorption and removal based on free radical induction multi-element modified porous carbon 2 Method and system for generating a response to a user |
| CN115888649B (en) * | 2022-11-16 | 2024-03-19 | 江苏大学 | Method and device for adsorbing VOCs (volatile organic compounds) by using active component modified biochar based on high-energy radiation induction |
| CN115888648B (en) * | 2022-11-16 | 2024-04-09 | 江苏大学 | Multi-element modified porous carbon adsorption CO removal based on free radical induction 2 Method and system of (2) |
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