CN116422311A - Thermal regeneration device and regeneration method for activated carbon - Google Patents
Thermal regeneration device and regeneration method for activated carbon Download PDFInfo
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- CN116422311A CN116422311A CN202310236268.4A CN202310236268A CN116422311A CN 116422311 A CN116422311 A CN 116422311A CN 202310236268 A CN202310236268 A CN 202310236268A CN 116422311 A CN116422311 A CN 116422311A
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 308
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- 230000008929 regeneration Effects 0.000 title claims abstract description 67
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 97
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- 238000001035 drying Methods 0.000 claims abstract description 62
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- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
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- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
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Images
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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
- B01J20/34—Regenerating or reactivating
- B01J20/3483—Regenerating or reactivating by thermal treatment not covered by groups B01J20/3441 - B01J20/3475, e.g. by heating or cooling
-
- 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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- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of activated carbon regeneration, and discloses a thermal regeneration device and a regeneration method of activated carbon. The invention is improved based on the most widely applied oxidation regeneration method, adopts an internal heat regeneration method, utilizes the drying of a feeding system to desorb and convert part of volatile organic matters adsorbed in the hazardous waste activated carbon into waste gas at high temperature, utilizes the carbonization and activation of a regeneration system to char most of the organic matters in the hazardous waste activated carbon, recovers the original pores and makes new pores, achieves the aim of regenerating the waste activated carbon, has the advantages of high regeneration rate, high quality recovery of the activated carbon and short time, and solves the problems of high auxiliary heat source, high investment and operation cost, difficult tail gas treatment and the like by the combination of a combustion system, a waste heat utilization system and a flue gas purification system.
Description
Technical Field
The invention relates to the technical field of activated carbon regeneration, in particular to a thermal regeneration device and a regeneration method of activated carbon.
Background
Along with the development of scientific economy, the country encourages industries to attach importance to and strengthen recycling of wastes produced in production and life, activated carbon is used as an adsorbent widely used, the annual usage amount of various industries is considerable, and the recycling of regenerated saturated activated carbon has strong economic and environmental benefits and is supported and encouraged by national policies.
1. Is beneficial to recycling economy: the application range of the activated carbon is becoming wider, but the activated carbon is easy to saturate and lose adsorption capacity in the use process, so that the use effect is required to be achieved through frequent replacement, the activated carbon is high in price, and the operation cost of enterprises is increased when the new carbon is replaced each time, so that the saturated activated carbon is required to be recycled, and the purpose of recycling economy is achieved.
2. Is beneficial to energy conservation and emission reduction: if 1 ton of saturated activated carbon is burnt as waste, 0.128 ton of carbon dioxide is released to the atmosphere, and 1 ton of high-quality activated carbon is prepared, 8 tons of wood or 8 tons of raw coal are required to be consumed, and the consumption of coal resources can be greatly reduced by regenerating the activated carbon, so that the atmospheric pollution is reduced, and the energy waste is reduced.
With the intensive research of mainstream technology, the ways of regenerating saturated activated carbon are as follows: the most widely used regeneration method is an oxidation regeneration method as a current stage, and the best regeneration condition of activated carbon obtained in a laboratory under the conditions of high temperature and high pressure is as follows: the regeneration temperature is 230 ℃, the regeneration time is 1h, the oxygenation amount is 20.6MPa, the charcoal adding amount is 15g, the water adding amount is 300mL, the regeneration efficiency reaches (45+/-5)%, the regeneration efficiency is only reduced by 3% after 5 times of cyclic regeneration, and the method is put into production based on test data.
However, the existing oxidation regeneration method for regenerating the saturated activated carbon still has some defects that the regeneration temperature can be reached by the auxiliary investment of a heat source when the regeneration is carried out, the investment and the operation cost are high, and the regenerated tail gas has the problems of difficult treatment and low treatment. Accordingly, a person skilled in the art provides a thermal regeneration device and a regeneration method for activated carbon to solve the problems set forth in the background art.
Disclosure of Invention
The invention aims to provide a thermal regeneration device and a regeneration method of active carbon, which are used for solving the problems in the background technology.
In order to achieve the above purpose, the present invention provides the following technical solutions: the device comprises a feeding system, a regeneration system, a screening and packaging system, a combustion system, a waste heat utilization system and a flue gas purification system;
the feeding system comprises a raw material hoister and a drying furnace, wherein a feeding port and a discharging port of the raw material hoister are sequentially communicated with a hoister bin and a first scraper machine, and a feeding port and a discharging port of the drying furnace are sequentially communicated with a drying feeder and a spiral discharging machine;
the regeneration system comprises a semi-finished product lifting machine and a regeneration furnace, wherein a feeding port and a discharging port of the semi-finished product lifting machine are respectively provided with a semi-finished product bin, and the feeding port and the discharging port of the regeneration furnace are sequentially communicated with a spiral feeder and a cooling carbon outlet machine;
the screening and packaging system comprises two groups of screening elevators and a drum screening machine, wherein the feed inlets of the two groups of screening elevators are communicated with the second scraper machine, the discharge outlets of the two groups of screening elevators are communicated with the drum screening machine, and the two groups of screening elevators are communicated through a impurity removing machine;
the combustion system comprises a second cyclone dust collector and a secondary combustion chamber which are connected through a pipeline, and the second cyclone dust collector is also communicated with the regenerating furnace;
the waste heat utilization system comprises a waste heat boiler communicated with the secondary combustion chamber, and the waste heat boiler is also communicated with the drying furnace;
the flue gas purification system is characterized in that the flue gas purification system is sequentially connected with an SNCR denitration reactor, a quenching tower, a dry deacidification tower, a second bag-type dust remover, a basic washing tower, a demister, an activated carbon adsorption box, a flue gas whitening device and a chimney through pipelines, and the SNCR denitration reactor is arranged between a secondary combustion chamber and a communicating pipeline of a waste heat boiler.
As still further aspects of the invention: the discharge opening of the first scraper is communicated with the feed inlet of the drying feeder through a raw material bin.
As still further aspects of the invention: one end of the furnace body of the drying furnace is provided with a burner along the direction of the discharging end of the furnace body.
As still further aspects of the invention: the two groups of semi-finished product bins are respectively communicated with the spiral discharging machine and the spiral feeding machine.
As still further aspects of the invention: the two groups of screening elevators are divided into A, B groups along the discharging direction, wherein the feeding inlet and the discharging outlet of the group A are respectively provided with a finished product bin communicated with the second scraper and the impurity remover, and the feeding inlet of the group B is communicated with the discharging outlet of the impurity remover.
As still further aspects of the invention: the feeding system also comprises a drying cyclone dust collector and a drying condenser which are connected through pipelines, and the drying cyclone dust collector is also communicated with the drying furnace.
As still further aspects of the invention: the screening and packaging system further comprises a first cyclone dust collector and a first cloth bag dust collector which are connected through pipelines, and the first cyclone dust collector is also communicated with the impurity remover and the drum screening machine.
As still further aspects of the invention: the inner wall of the secondary combustion chamber is built with a high-alumina refractory material, and a heat insulation layer is lined between the refractory material and the inner wall of the secondary combustion chamber.
As still further aspects of the invention: the second bag-type dust collector is communicated with the basic washing tower through a main induced draft fan, and the activated carbon adsorption box is communicated with the flue gas whitening device through a secondary induced draft fan.
A method for thermally regenerating activated carbon, comprising the steps of:
s1, raw materials enter a field, waste activated carbon enters a field for testing, qualified products enter a qualified warehouse for temporary storage, unqualified products enter an unqualified warehouse for temporary storage and then return, and qualified products are stored in a classified mode according to powder and particle states;
s2, charging into a rotary kiln for compatibility, and before charging into the rotary kiln, according to the detection result of the waste activated carbon, mixing the waste activated carbon with relatively high chlorine and fluorine content with the waste activated carbon with relatively low chlorine and fluorine content or without chlorine and fluorine content, and charging into the kiln after uniformly mixing the materials so as to ensure that the chlorine and fluorine content in the waste activated carbon charged into the kiln is relatively stable;
s3, feeding, namely placing the mixed waste activated carbon in a ton bag or ton barrel, placing the waste activated carbon in a feed hopper by using a crane, a forklift and the like, and conveying the waste activated carbon into a storage hopper of an internal heat dryer by using a closed lifter and a scraper;
s4, drying, namely slowly moving the waste granular activated carbon forwards under the action of the inclination angle of an internal heating type drying furnace and gravity, wherein the temperature of saturated steam in the drying furnace is in the range of 150-170 ℃, and collecting the dried material from the bottom of the internal heating type drying machine, and conveying the material to a granular carbon regeneration bin for temporary storage through a screw conveyor;
s5, regenerating the activated carbon, feeding the dried material in a regeneration bin into a rotary kiln through a screw feeder for regeneration, introducing a small amount of air and steam, resolving waste gas adsorbed by waste activated carbon at a high temperature, precipitating the regenerated activated carbon at the bottom of the rotary kiln, cooling, packaging and recycling to obtain finished granular activated carbon, and purifying regenerated flue gas through a secondary combustion chamber, and then entering a flue gas purification system for purification, and discharging the regenerated flue gas through a 35-meter high-exhaust barrel;
s6, cooling, wherein the regenerated granular activated carbon enters a water-cooling carbon outlet machine through a closed conveying pipeline to be cooled and discharged, and the cooled material is conveyed to a screening hoist bin for storage through a ground scraper;
s7, screening and packaging, namely cooling the regenerated granular activated carbon, then enabling the cooled regenerated granular activated carbon to enter a screening system, directly packaging the regenerated carbon with the mesh number of more than 80 meshes, and crushing and packaging a small amount of the regenerated carbon with the mesh number of less than 80 meshes by a pulverizer;
s8, warehousing the finished product, and directly selling the packaged activated carbon serving as the finished product.
Compared with the prior art, the invention has the beneficial effects that:
feeding system, regeneration system, screening and packaging system, combustion system, waste heat utilization system and flue gas purification system
1. The invention is based on the most widely used oxidation regeneration method for improvement, adopts an internal heat regeneration method, utilizes the drying of a feeding system to desorb and convert part of volatile organic matters adsorbed in the hazardous waste activated carbon into waste gas at high temperature, volatilizes the waste gas together with water vapor, and utilizes the carbonization and activation of a regeneration system to carbonize most of the organic matters in the hazardous waste activated carbon, activates the hazardous waste activated carbon in the presence of a quantitative oxidant, recovers the original pores and makes new pores, thereby achieving the aim of regenerating the hazardous waste activated carbon, and having the advantages of high regeneration rate, high quality recovery of the activated carbon and short time.
2. According to the invention, through the combination of the combustion system and the waste heat utilization system, the waste gas is combusted and recycled, and the smoke purification system is used for SNCR denitration, quenching, dry deacidification, dry dioxin removal, cloth bag dust removal, wet deacidification, water separation, activated carbon adsorption treatment and smoke reheating of the combusted waste gas, on one hand, the heat can be recycled, so that the waste gas is used as the heat energy source of the regenerating furnace to supply, the energy loss is saved, on the other hand, the dangerous waste gas can be subjected to integral and synchronous purification work, the discharged smoke reaches the standard, and then the problems of auxiliary heat source requirement, higher investment and operation cost, difficult tail gas treatment and the like are solved.
Drawings
FIG. 1 is a schematic structural view of a thermal regeneration device for activated carbon;
FIG. 2 is a schematic process flow diagram of a thermal regeneration device for activated carbon;
FIG. 3 is a schematic diagram of a flue gas purification flow of a thermal regeneration device for activated carbon;
FIG. 4 is a schematic flow chart of a thermal regeneration method of activated carbon.
In the figure: 1. a raw material hoister; 2. a raw material bin; 3. a drying feeder; 4. a hoister bin; 5. a first scraper; 6. a drying furnace; 7. a combustion machine; 8. a spiral discharging machine; 9. a semi-finished product elevator; 10. a semi-finished product bin; 11. a screw feeder; 12. a regenerator; 13. cooling the carbon outlet machine; 14. a second scraper; 15. a screening elevator; 16. a impurity removing machine; 17. a roller screen grader; 18. a first cyclone dust collector; 19. a first bag-type dust collector; 20. a drying cyclone dust collector; 21. drying the condenser; 22. a second cyclone dust collector; 23. a secondary combustion chamber; 24. a waste heat boiler; 25. an SNCR denitration reactor; 26. a quenching tower; 27. a dry deacidification tower; 28. a second bag-type dust collector; 29. a main induced draft fan; 30. a basic wash column; 31. a demister; 32. an activated carbon adsorption tank; 33. a secondary induced draft fan; 34. a flue gas whitening device; 35. and (5) a chimney.
Detailed Description
Referring to fig. 1 to 3, in an embodiment of the present invention, a thermal regeneration device for activated carbon includes a feeding system, a regeneration system, a screening and packaging system, a combustion system, a waste heat utilization system, and a flue gas purification system.
The feeding system comprises a raw material lifting machine 1 and a drying furnace 6, wherein a feeding port and a discharging port of the raw material lifting machine 1 are sequentially communicated with a lifting machine bin 4 and a first scraper machine 5, a discharging port of the first scraper machine 5 is communicated with a feeding port of a drying feeder 3 through a raw material bin 2, and the combination of the raw material lifting machine 1, the first scraper machine 5 and the drying feeder 3 in the system is used for quantitatively feeding dangerous waste activated carbon raw materials and quantitatively feeding the dangerous waste activated carbon into the drying furnace 6;
the feed inlet and the discharge outlet of the drying furnace 6 are sequentially communicated with the drying feeder 3 and the spiral discharge machine 8, a burner 7 is arranged at one end of a furnace body of the drying furnace 6 along the direction of the discharge end of the furnace body, the drying furnace 6 in the system is used for drying dangerous waste activated carbon, the dangerous waste activated carbon is subjected to heat exchange with steam in a steam pipe in the drying furnace 6 by utilizing a saturated steam heat source generated by a waste heat boiler 24, if the heat value of the steam is insufficient, hot air is supplemented by the burner 7 in the form of natural gas at the tail of the furnace for drying, and the dried dangerous waste activated carbon is conveyed out by the spiral discharge machine 8;
the design theoretical parameters of the drying furnace 6 are as follows:
the feeding system further comprises a drying cyclone 20 and a drying condenser 21 which are connected through a pipeline, the drying cyclone 20 is also communicated with the drying furnace 6, the combination of the drying cyclone 20 and the drying condenser 21 in the system is used for treating dry waste gas G2 in the drying furnace 6, most of water vapor is removed after the dry waste gas is dried and condensed by the drying cyclone 20 and the drying condenser 21, and the dry waste gas is introduced into a secondary combustion chamber 23 for combustion treatment by a fan and is discharged outside after being purified by a flue gas purifying system.
The regeneration system comprises a semi-finished product lifting machine 9 and a regeneration furnace 12, wherein a feeding port and a discharging port of the semi-finished product lifting machine 9 are respectively provided with a semi-finished product bin 10, the feeding port and the discharging port of the regeneration furnace 12 are sequentially communicated with a spiral feeder 11 and a cooling carbon outlet 13, and two groups of semi-finished product bins 10 are respectively communicated with the spiral discharger 8 and the spiral feeder 11;
the combination of the semi-finished product lifting machine 9 and the screw feeder 11 in the system is used for quantitatively feeding the raw materials after the hazardous waste activated carbon is dried, and quantitatively feeding the hazardous waste activated carbon into the regenerating furnace 12 for regeneration;
the regeneration furnace 12 in the system is divided into a waste activated carbon feeding section, a carbonization section, an activation section and an activated carbon discharging section, wherein in the feeding section, dangerous waste activated carbon is kept in a certain storage quantity in a screw feeder 11 above a gap feeding hole of the regeneration furnace 12 to form natural sealing, furnace gas is isolated from the outside, in the carbonization section, temperature of each section is automatically controlled to be about 600 ℃, in the activation section, the distance between the temperature control facilities is 3-4 m on average, the temperature of each section is automatically controlled to be about 900 ℃, and in the discharging section, dangerous waste activated carbon is cooled and discharged by a cooling carbon discharging machine 13 after being subjected to preliminary cooling in the regeneration furnace 12;
in the regenerating furnace 12, the waste heat boiler 24 conveys part of the generated vapor to the position about 25 cm above the hazardous waste active carbon material through a vapor conveying pipeline, the material is fully contacted with the vapor through high-pressure injection, necessary oxygen, fuel gas and vapor are provided, the active carbon flows from the furnace end to the furnace tail under the pulling of a subsequent fan, the active carbon firstly starts to be a carbonization section, the adsorbed volatile substances and high-boiling-point organic matters remained in the pores of the active carbon are carbonized, the high-boiling-point organic matters are decomposed and carbonized in an adsorption state, and remain in the form of fixed carbon, the residual carbon generated in the carbonization process is decomposed by using gases such as carbon dioxide, oxygen and the like at 900 ℃, the oxidizing property of the oxygen is strong, the active carbon body is easily consumed excessively, the project is not generally adopted, the project is selected to decompose the oxidizing gas by adopting the vapor under the anaerobic environment, the material is gradually opened through the aperture of the vapor under the high-temperature effect, the regeneration process is the high-temperature anaerobic process, the organic elements and halogen are mainly oxidized and reacted to generate stable oxides, the heavy metals exist in the form of the active carbon ash in the end product,
the following reactions were carried out on the activated carbon surface:
C+O 2 ＝CO 2 2C+O 2 ＝2CO
2CO+O 2 ＝2CO 2 N+O 2 ＝NO 2 C+O 2 ＝CO 2
C+2HO 2 ＝2H 2 +CO 2 C+HO 2 ＝H 2 +CO C+CO 2 ＝2CO
azo compound=n 2 +radical 2H 2 +O 2 ＝2H 2 O S+O 2 ＝SO 2
Cl-+H + ＝HCl
F-+H + ＝HF
The chemical reaction is carried out, so that carbon atoms on the surfaces of capillary holes of the active carbon are gasified, the capillary holes are expanded to form a new active surface, a large amount of combustible gas is released in the process, the combustible gas reacts with the introduced oxygen to release a large amount of heat energy which is used as a heat source for maintaining the furnace temperature, the adsorbed substances are carbonized, activated or burnt out at high temperature to complete the regeneration process, if the heat energy is insufficient in the regeneration process, a burner is added at the tail part of the furnace to supplement the heat energy, and the regenerated tail gas G3 generated in the process is introduced into a secondary combustion chamber 23 to burn and is recovered by a waste heat boiler 24 and then is purified by a flue gas purification system to be discharged outside;
the theoretical parameters for the regenerator 12 design are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Regeneration temperature | ℃ | 950 |
| 2 | Residence time in rotary kiln | s | 3600 |
| 3 | Design of treatment scale | t/h | 1.3 |
| 4 | Internal pressure of furnace | / | Micro |
| 5 | Rotary kiln size | mm | Φ2600×17000 |
| 6 | Inclination angle of rotary kiln | Degree of | 1.5 |
| 7 | Total thickness of refractory material | mm | 300 |
| 8 | Air supplementing quantity | Nm3/h | 1500 |
The cooling carbon outlet machine 13 in the system is used for water cooling operation of activated carbon particles, and conveys the cooled material to the screening hoist 15 through the second scraper machine 14 for storage, the cooling carbon outlet machine 13 is in a water cooling mode, reuse water is used as cooling water to flow in a jacket of the carbon outlet machine to take away heat of the activated carbon, the temperature of the activated carbon is reduced, the cooling water is recycled, and the waste water is periodically discharged to a wastewater treatment facility for treatment and then impurity removal recycling.
The screening and packaging system comprises two groups of screening elevators 15 and a drum screening machine 17, wherein the feed inlets of the two groups of screening elevators 15 are communicated with the second scraper 14, the discharge outlets of the two groups of screening elevators 15 are communicated with the drum screening machine 17, the two groups of screening elevators 15 are communicated through a impurity removing machine 16, the two groups of screening elevators 15 are divided into A, B groups along the discharging direction, the feed inlets and the discharge outlets of the A group are respectively provided with a finished product bin communicated with the second scraper 14 and the impurity removing machine 16, the feed inlets of the B group are communicated with the discharge outlets of the impurity removing machine 16, the two groups of screening elevators 15 and the impurity removing machine 16 in the system are used for impurity removing operation on regenerated active carbon particles, after cooled materials are subjected to impurity removing, the materials are lifted and conveyed into the drum screening machine 17, the particle sizes of the regenerated carbon are screened, the mesh sizes of the drum screening machine 17 are 80 meshes, the mesh sizes of the regenerated carbon with meshes of more than 80 meshes are directly packaged, and the mesh sizes of the regenerated carbon with meshes of less than 80 meshes are packaged after being crushed by the grinding machine.
The screening and packaging system further comprises a first cyclone dust collector 18 and a first cloth bag dust collector 19 which are connected through pipelines, the first cyclone dust collector 18 is also communicated with the impurity remover 16 and the roller screening machine 17, and the combination of the first cyclone dust collector 18 and the first cloth bag dust collector 19 in the system is used for dust removal work of dust and waste gas G4 particles generated in the screening, grinding and packaging processes.
The combustion system comprises a second cyclone dust collector 22 and a second combustion chamber 23 which are connected through a pipeline, wherein the second cyclone dust collector 22 is also communicated with the regenerating furnace 12, the inner wall of the second combustion chamber 23 is built with a high-alumina refractory material, a heat insulation layer is lined between the refractory material and the inner wall of the second combustion chamber 23, the second cyclone dust collector 22 in the system is used for treating particles in the flue gas in the regenerating furnace 12, the treated flue gas is burnt at a high temperature of over 1100 ℃ in the second combustion chamber 23, the burning residence time is longer than 2s, harmful odor and polychloride are fully decomposed, the generation of dioxins is inhibited, the full burning of harmful substances contained in the flue gas is ensured, wherein,
description of the combustion time in the secondary combustion chamber 23: t=273×3600×v/G/(273+t), smoke amount: g, effective volume of the secondary combustion chamber: v, combustion temperature: t, flue gas residence time: t is;
the inner wall of the secondary combustion chamber 23 is built with high-alumina refractory materials, the refractory materials and the shell are lined with heat insulation layers, the temperature rise of the outer wall and the environment is ensured to be less than 60 ℃, the outer wall is made of steel materials, the rust removal effect is ensured to be good by adopting high-temperature anti-corrosion paint for brushing, and the top of the secondary combustion chamber 23 is provided with an emergency opening, which mainly has the effects of emergency opening when unexpected conditions such as deflagration or power failure occur in the rotary kiln, avoiding malignant accidents such as equipment explosion and subsequent equipment damage, keeping the air tightness at ordinary times for the emergency discharge opening, and preventing smoke from directly escaping;
the theoretical design parameters of the secondary combustion chamber 23 are as follows:
the waste heat utilization system comprises a waste heat boiler 24 communicated with a secondary combustion chamber 23, the waste heat boiler 24 is also communicated with a drying furnace 6, the waste heat boiler 24 in the system is used for recovering combustion heat of the secondary combustion chamber 23, and steam generated by heat exchange is conveyed into a steam pipe of the drying furnace 6 in a water bath heat exchange mode to perform heat exchange and drying with dangerous waste activated carbon.
The flue gas purification system sequentially connects an SNCR denitration reactor 25, a quenching tower 26, a dry deacidification tower 27, a second bag-type dust remover 28, an alkali washing tower 30, a demister 31, an active carbon adsorption box 32, a flue gas whitening device 34 and a chimney 35 through pipelines, the SNCR denitration reactor 25 is arranged between a secondary combustion chamber 23 and a communicating pipeline of a waste heat boiler 24, the second bag-type dust remover 28 is communicated with the alkali washing tower 30 through a main induced draft fan 29, the active carbon adsorption box 32 is communicated with the flue gas whitening device 34 through a secondary induced draft fan 33, the system utilizes the dual wind pumping of the main induced draft fan 29 and the secondary induced draft fan 33 to pump the flue gas generated by burning the secondary combustion chamber 23 into various reactors for purification, the purification process sequentially comprises SNCR denitration, quenching, dry deacidification, bag dust removal, wet deacidification, water separation, active carbon adsorption treatment and flue gas reheating, wherein,
the SNCR denitration reactor 25 is a selective non-catalytic reduction technology, belongs to a post-combustion control technology, and is characterized in that amino substances are injected into a furnace by a pump under the condition of no catalyst, and react with NOx in combustion flue gas to generate nontoxic and harmless nitrogen and water under certain conditions, the amino substances select urea solution, the temperature of the injection point is a 'temperature window' in the SNCR reaction process, a proper range of the injection point is 900-1100 ℃, and a chemical reaction equation of the urea solution for reducing NOx is as follows:
CO(NH 2 )+H 2 O→2NH 3 +CO 2 (1)
4NH 3 +4NO+O 2 →4N 2 +6H 2 O (2)
8NH 3 +6NO 2 →7N 2 +12H 2 O (3)
at the same time as urea reduces NOx, NH volatilizes from the urea solution 3 Molecules and O 2 Is a reaction of (a).
4NH 3 +5O 2 →4NO+6H 2 O (4)
4NH 3 +3O 2 →2N 2 +6H 2 O (5)
When the temperature is highWhen the degree is higher than the temperature window, NH 3 The oxidation reaction of urea solution will be dominant, ammonia decomposed from urea solution does not reduce NOx, but reacts with oxygen to form NOx, so the reaction temperature is a main factor affecting SNCR process;
the theoretical parameters for the design of the SNCR denitration reactor 25 are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Inlet flue gas temperature | ℃ | 1050 |
| 2 | Temperature of the outlet flue gas | ℃ | 950 |
| 3 | Inlet smoke volume | Nm3/h | 14500 |
| 4 | Outlet smoke volume | Nm3/h | 14700 |
| 5 | Consumption of urea solution (10%) | Kg/h | 51 |
The denitration process flow comprises the following steps: water, solid urea at 1:1 ratio is 2m 3 The urea preparation tank is internally configured into urea solution with the concentration of 50%, then high-concentration urea is conveyed into a urea storage tank, the urea solution with the concentration of 10% is diluted by water according to the use requirement of equipment, and is conveyed by a urea injection pump, automatically and continuously injected into a flue gas pipeline by a denitration atomizer, and the flue gas in the pipeline is subjected to denitration;
the quench tower 26 is mainly used for rapidly cooling the flue gas by utilizing water, the temperature of the flue gas after SNCR denitration and waste heat recovery is about 550 ℃, in order to avoid regeneration of dioxin substances in a temperature range of 250-500 ℃, the system is required to shorten the residence time of the flue gas in the temperature range as much as possible, so the quench tower 26 is arranged for rapidly cooling the flue gas, the quench tower 26 adopts a quench injection device to spray water into the flue gas, the flue gas in a pipeline is directly contacted with the sprayed water after atomization, the mass transfer speed and the heat transfer speed are faster, the sprayed water is rapidly gasified to take away a large amount of heat, the temperature of the flue gas is rapidly reduced to about 200 ℃, thereby the regeneration of dioxin substances is avoided, the water used for contact absorption quenching with the flue gas is recycled water, most of impurities are basically removed by the water base of RO/evaporation condensation treatment, the relevant standard limit value in the industrial water quality of urban sewage regeneration (GB/T19923-2005) can be met, and the recycled water is pumped to a spray head at the top of the quench tower by a pressure atomization, and the process of fully atomizing the water in the flue gas state is completed.
The theoretical parameters for quench tower 26 design are as follows:
the dry deacidification tower is respectively connected to 2 dry spray devices, one is provided with quicklime powder for acid removal, the other is provided with powdered activated carbon for dioxin removal, and the main equipment of the dry reactor comprises an activated carbon powder storage tank, a calcium oxide storage tank, a rotary high-pressure fan and a venturi dry reactor, so that the purpose is to adopt the active carbon powder and the calcium oxide powder to be respectively sprayed into the venturi dry reactor in front of the second bag-type dust remover 28, remove acidic substances in flue gas and adsorb most of harmful substances such as dioxin and the like, and the main reaction formula is as follows:
CaO+H 2 O→Ca(OH) 2
2HCl+Ca(OH) 2 →CaCl 2 +2H 2 O
SO 2 +Ca(OH) 2 →CaSO 3 +H 2 O
the dry deacidification tower 27 is provided with an active carbon jet reactor, the active carbon is conveyed by a rotary fan under high pressure, the powdery active carbon is added into the flue gas by adjusting the input air quantity, the particle size is about 170 meshes, and the jet quantity is 50mg/m 3 Dioxin substances are easy to be adsorbed by activated carbon at low temperature (180 ℃), the activated carbon is mixed with flue gas in a flue after being phase-cut and sprayed by a venturi tube, preliminary adsorption is carried out, the mixed flue gas enters a second bag-type dust collector 28, activated carbon powder is adsorbed on the surface of a filter bag, harmful substances are continuously adsorbed on the surface of the filter bag, the removal rate of the dioxin substances is obviously improved, and the removal rate of the dioxin substances can reach more than 90% by controlling the temperature and the adsorption of the activated carbon;
the dry deacidification tower 27 is provided with a quicklime dry powder deacidification jet reactor, the quicklime dry powder is conveyed by high-pressure air through a rotary fan, the lime dry powder added into the flue gas is controlled by adjusting the input air quantity, the quicklime dry powder is added into the flue gas, the quicklime dry powder is mixed with the flue gas in a flue after being jetted into the flue gas, the primary neutralization absorption reaction is carried out, the mixed flue gas enters the second bag-type dust remover 28, the quicklime powder is adsorbed on the surface of a filter bag, the surface of the filter bag is continuously subjected to neutralization reaction with trace acidic substances, the removal rate of the acidic gases is improved, and a calcium oxide storage tank for storing the lime dry powder adopts a closed structure to prevent water vapor in the adsorption air from agglomerating;
the venturi dry reactor is arranged on a flue of the dry deacidification tower 27, the quicklime powder and the activated carbon powder are sprayed into the reactor through a rotary high-pressure fan, gas and solid are mutually met, and when the quicklime powder and the activated carbon powder pass through a throat, the sectional area is reduced, the speed of flue gas is increased, high turbulence and gas and solid mixing are generated, so that residual harmful substances in the flue gas are fully contacted with the quicklime powder and the activated carbon for reaction and adsorption, and the purposes of complete neutralization reaction and adsorption are achieved;
the design theoretical parameters of the dry deacidification tower 27 are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Inlet smoke volume | Nm3/h | 15500 |
| 2 | Outlet smoke volume | Nm3/h | 15800 |
| 3 | Inlet flue gas temperature | ℃ | 195 |
| 4 | Temperature of the outlet flue gas | ℃ | 180 |
| 5 | Compressed air quantity | Nm3/min | 2.5 |
| 6 | Feeding capacity | kg/ |
5～30 |
| 7 | Specification and size | mm | Φ1800*6000 |
The second bag-type dust collector 28 is a dry dust filtering device, a filter bag of the second bag-type dust collector is made of PTFE (polytetrafluoroethylene) film, the aperture is 800 meshes, the filter bag is of an irregular blade-shaped section, the surface area of the filter bag is increased by 80% compared with that of a general cylindrical section, when dust-containing gas enters the bag-type dust collector, the granularity of fly ash is about 300 meshes-450 meshes, dust is accumulated on the surface of the filter bag to form a dust cake, the dust cake falls down due to the action of gravity in a dust hopper in a pulse mode, the dust is blocked when the gas containing finer dust passes through a filter material, the gas is purified, the second bag-type dust collector 28 periodically discharges the dust collector to collect dust, the dust is cooled in a collecting container and then packaged, the dust is collected by a ton bag and is transported to a secondary dangerous waste storehouse by a forklift to be stored, and the damaged bag after long-term operation is entrusted with a qualification unit for disposal as dangerous waste;
the theoretical parameters for the design of the second bag house 28 are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Inlet smoke volume | Nm3/h | 15800 |
| 2 | Outlet smoke volume | Nm3/h | 16500 |
| 3 | Inlet flue gas temperature | ℃ | 180 |
| 4 | Temperature of the outlet flue gas | ℃ | 175 |
| 5 | Air filtering speed | m/min | 0.8-1.2 |
| 6 | Filtration area | m2 | 500 |
The alkali type washing tower 30 adopts three sets of wet type alkali liquid washing towers to wash the flue gas, alkali liquid spraying is carried out, the flue gas is sprayed through a special nozzle, the flue gas enters from the bottom of the tower, the gas and the filler in the tower are in countercurrent contact with the alkali liquid, so that residual gaseous pollutants are effectively washed, the temperature is further reduced, the generation of dioxin is controlled, finally, the purified flue gas is connected to a subsequent treatment procedure from the top of the tower, and most of spray water returns to an alkali liquid pool and is influenced by the temperature of the flue gas, and a small amount of spray water is gasified;
the basic wash column 30 design theoretical parameters are as follows:
the demister 31 is arranged behind the basic washing tower 30 and internally comprises two water-gas separators and has main functions
| Sequence number | Project | Unit (B) | |
| 1 | Inlet smoke volume | Nm3/h | 16600 |
| 2 | Outlet smoke volume | Nm3/h | 18600 |
| 3 | Inlet flue gas temperature | ℃ | 175 |
| 4 | Temperature of the outlet flue gas | ℃ | 60 |
| 6 | Ratio of gas to liquid | / | 1:1.4 |
| 7 | External dimension | mm | Φ2300×6000 |
In order to remove the moisture in the flue gas, the interference of water vapor to the subsequent process is reduced, the generation of white smoke is reduced, the condensed and separated water is partially recycled after being filtered by an RO membrane, and the partially discharged water is discharged to a sewage pipe network, and the filtered concentrated water is recycled for production after being evaporated and condensed by an evaporator.
The theoretical parameters for the design of the mist eliminator 31 are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Inlet smoke volume | Nm3/h | 18600 |
| 2 | Outlet smoke volume | Nm3/h | 18900 |
| 3 | Inlet flue gas temperature | ℃ | 60 |
| 4 | Temperature of the outlet flue gas | ℃ | 55 |
| 5 | External dimension | mm | Φ2500×6000 |
The activated carbon adsorption box 32 is arranged behind the demister 31, organic matters in the waste gas are further absorbed and treated, when the flue gas enters the activated carbon adsorption box 32, the wind speed is instantaneously reduced, larger particle impurities in the gas naturally settle into the bottom of the tower, and the organic gas part dissolved into the gas flows into the activated carbon filter layer along with the gas flow direction, when the organic gas enters the carbon layer, the organic gas is adsorbed into the carbon by the activated carbon, and clean flue gas passes through the carbon layer to enter the gas outlet bin.
The theoretical parameters for the design of the activated carbon adsorption tank 32 are as follows:
| sequence number | Project | Unit (B) | |
|
| 1 | Inlet smoke volume | Nm3/h | 18900 | |
| 2 | Outlet smoke volume | Nm3/h | 19100 | |
| 3 | Inlet flue gas temperature | ℃ | 55 | |
| 4 | Dosage of | m3 | 8 | |
| 5 | External dimension | mm | 3900×3400×3300 |
The flue gas heater of the flue gas whitening device 34 is arranged in front of the chimney 35, and the tail gas is reheated before entering the chimney 35, so that the vapor and the water mist which are not separated in the flue gas are gasified at high temperature, and the effect of flue gas whitening is achieved;
the theoretical parameters for the design of the flue gas whitening device 34 are as follows:
| sequence number | Project | Unit (B) | |
| 1 | Inlet smoke volume | Nm3/h | 19100 |
| 2 | Outlet smoke volume | Nm3/h | 19500 |
| 3 | Inlet flue gas temperature | ℃ | 55 |
| 4 | Temperature of the outlet flue gas | ℃ | 120 |
| 5 | Area of heating | m2 | 150 |
| 6 | External dimension | mm | Φ15000*6000 |
Referring to fig. 4, in an embodiment of the present invention, a thermal regeneration method of activated carbon includes the following steps:
s1, raw material entering, waste activated carbon entering test, test feeding requirements: heavy metals (mercury, cadmium, chromium, arsenic and lead) cannot be detected, the chlorine content (wet basis) is less than or equal to 2 percent, the fluorine content (wet basis) is less than or equal to 0.05 percent, the bromine content (wet basis) is less than or equal to 0.02 percent, and the ash content is less than 15 percent; the qualified products enter a qualified warehouse for temporary storage, the unqualified products enter an unqualified warehouse for temporary storage and then return, the qualified products are stored in a classified mode according to powder and particle states, and an activated carbon adsorption box is arranged in the warehouse for adsorbing malodorous pollutants G1 in the volatilized part of the waste activated carbon;
s2, charging into a rotary kiln for compatibility, and before charging into the rotary kiln, according to the detection result of the waste activated carbon, mixing the waste activated carbon with relatively high chlorine and fluorine content with the waste activated carbon with relatively low chlorine and fluorine content or without chlorine and fluorine content, and charging into the kiln after uniformly mixing the materials so as to ensure that the chlorine and fluorine content in the waste activated carbon charged into the kiln is relatively stable;
s3, feeding, namely placing the mixed waste activated carbon in a ton bag or ton barrel, placing the waste activated carbon in a feed hopper by using a crane, a forklift and the like, and conveying the waste activated carbon into a storage hopper of an internal heat dryer by using a closed lifter and a scraper;
s4, drying, namely slowly moving the waste granular activated carbon forwards under the action of the inclination angle of an internal heating type drying furnace and gravity, wherein the temperature of saturated steam in the drying furnace is in the range of 150-170 ℃, and collecting the dried material from the bottom of the internal heating type drying machine, and conveying the material to a granular carbon regeneration bin for temporary storage through a screw conveyor;
s5, regenerating the activated carbon, feeding the dried material in a regeneration bin into a rotary kiln through a screw feeder for regeneration, introducing a small amount of air and steam, resolving waste gas adsorbed by waste activated carbon at a high temperature, precipitating the regenerated activated carbon at the bottom of the rotary kiln, cooling, packaging and recycling to obtain finished granular activated carbon, and purifying regenerated flue gas through a secondary combustion chamber, and then entering a flue gas purification system for purification, and discharging the regenerated flue gas through a 35-meter high-exhaust barrel;
s6, cooling, wherein the regenerated granular activated carbon enters a water-cooling carbon outlet machine through a closed conveying pipeline to be cooled and discharged, and the cooled material is conveyed to a screening hoist bin for storage through a ground scraper;
s7, screening and packaging, namely cooling the regenerated granular activated carbon, then enabling the cooled regenerated granular activated carbon to enter a screening system, directly packaging the regenerated carbon with the mesh number of more than 80 meshes, and crushing and packaging a small amount of the regenerated carbon with the mesh number of less than 80 meshes by a pulverizer;
s8, warehousing finished products, wherein the packaged activated carbon is used as a finished product and is directly sold;
the flue gas purification process generated after regeneration is as follows: the regenerated flue gas after combustion in the secondary combustion chamber is subjected to SNCR denitration at the temperature of 1100 ℃, heat is recovered by a waste heat boiler, the temperature of the flue gas is reduced to 550 ℃, then the flue gas enters a quenching tower, the quenching tower is atomized and quenched by using recycled water, the quenching in the temperature range of 550-200 ℃ is ensured, the regeneration of dioxins is prevented, then the flue gas enters a dry deacidification tower, the absorbents such as quicklime, powdered activated carbon and the like are sprayed, the absorbents are deposited on the bag wall of the bag-type dust collector to form a filter cake, the deposited absorbents continuously absorb gaseous pollutants and dioxins in the flue gas, the purpose of deacidifying and removing the polluted dioxins is achieved, the absorbents are deposited on the bag wall of the bag-type dust collector to form a filter cake, the deposited absorbents continuously absorb the gaseous pollutants in the flue gas, the flue gas after dust removal by the bag-type dust collector is pulled into the wet deacidification tower by using a draught fan, the flue gas enters the demister for further deacidification treatment after the deacidification treatment is completed, the flue gas is further absorbed by the activated carbon absorption box to remove residual trace harmful components in the flue gas, and finally enters the exhaust gas after the flue gas is heated to 120 ℃ by the flue gas heating device to remove the white.
The foregoing description is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical solution of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (10)
1. The heat regeneration device of the activated carbon is characterized by comprising a feeding system, a regeneration system, a screening and packaging system, a combustion system, a waste heat utilization system and a flue gas purification system;
the feeding system comprises a raw material lifting machine (1) and a drying furnace (6), wherein a feeding port and a discharging port of the raw material lifting machine (1) are sequentially communicated with a lifting machine bin (4) and a first scraper machine (5), and a feeding port and a discharging port of the drying furnace (6) are sequentially communicated with a drying feeder (3) and a spiral discharging machine (8);
the regeneration system comprises a semi-finished product lifting machine (9) and a regeneration furnace (12), wherein a semi-finished product storage bin (10) is arranged at a feed inlet and a discharge outlet of the semi-finished product lifting machine (9), and the feed inlet and the discharge outlet of the regeneration furnace (12) are sequentially communicated with a spiral feeder (11) and a cooling carbon outlet (13);
the screening and packaging system comprises two groups of screening elevators (15) and a drum screening machine (17), wherein the feed inlets of the two groups of screening elevators (15) are communicated with a second scraper machine (14), the discharge outlets of the two groups of screening elevators (15) are communicated with the drum screening machine (17), and the two groups of screening elevators (15) are communicated through a impurity removing machine (16);
the combustion system comprises a second cyclone dust collector (22) and a secondary combustion chamber (23) which are connected through a pipeline, and the second cyclone dust collector (22) is also communicated with the regenerating furnace (12);
the waste heat utilization system comprises a waste heat boiler (24) communicated with the secondary combustion chamber (23), and the waste heat boiler (24) is also communicated with the drying furnace (6);
the flue gas purification system is characterized in that the flue gas purification system is sequentially connected with an SNCR denitration reactor (25), a quenching tower (26), a dry deacidification tower (27), a second bag-type dust remover (28), a basic washing tower (30), a demister (31), an activated carbon adsorption box (32), a flue gas whitening device (34) and a chimney (35) through pipelines, and the SNCR denitration reactor (25) is arranged between a secondary combustion chamber (23) and a communicating pipeline of a waste heat boiler (24).
2. The device for thermally regenerating activated carbon according to claim 1, characterized in that the discharge opening of the first scraper (5) is communicated with the feed opening of the drying feeder (3) through a raw material bin (2).
3. A device for thermal regeneration of activated carbon according to claim 1, characterized in that one end of the body of the drying oven (6) is provided with a burner (7) in the direction of its discharge end.
4. A device for thermal regeneration of activated carbon according to claim 1, characterized in that two sets of said semi-finished product silos (10) are respectively in communication with a screw discharger (8) and a screw feeder (11).
5. The device for thermal regeneration of activated carbon according to claim 1, wherein the two groups of sieving and lifting machines (15) are divided into two groups A, B along the discharging direction, wherein the feeding port and the discharging port of group a are respectively provided with a finished product bin communicated with the second scraper (14) and the impurity removing machine (16), and the feeding port of group B is communicated with the discharging port of the impurity removing machine (16).
6. A device for thermal regeneration of activated carbon according to claim 1, characterized in that the feed system further comprises a drying cyclone (20), a drying condenser (21) connected by a pipe, and that the drying cyclone (20) is also in communication with the drying oven (6).
7. The device for thermally regenerating activated carbon according to claim 1, characterized in that the screening and packaging system further comprises a first cyclone (18) and a first bag-type dust collector (19) connected by a pipeline, and the first cyclone (18) is further communicated with the impurity remover (16) and the drum screening machine (17).
8. The device for thermal regeneration of activated carbon according to claim 1, characterized in that the inner wall of the secondary combustion chamber (23) is lined with a high alumina refractory material, and a heat insulating layer is lined between the refractory material and the inner wall of the secondary combustion chamber (23).
9. The activated carbon heat regeneration device according to claim 1, wherein the second bag-type dust collector (28) is communicated with the basic washing tower (30) through a main induced draft fan (29), and the activated carbon adsorption box (32) is communicated with the flue gas whitening device (34) through a secondary induced draft fan (33).
10. A method for the thermal regeneration of activated carbon according to any one of claims 1 to 9, characterized by the steps of:
s1, raw materials enter a field, waste activated carbon enters a field for testing, qualified products enter a qualified warehouse for temporary storage, unqualified products enter an unqualified warehouse for temporary storage and then return, and qualified products are stored in a classified mode according to powder and particle states;
s2, charging into a rotary kiln for compatibility, and before charging into the rotary kiln, according to the detection result of the waste activated carbon, mixing the waste activated carbon with relatively high chlorine and fluorine content with the waste activated carbon with relatively low chlorine and fluorine content or without chlorine and fluorine content, and charging into the kiln after uniformly mixing the materials so as to ensure that the chlorine and fluorine content in the waste activated carbon charged into the kiln is relatively stable;
s3, feeding, namely placing the mixed waste activated carbon in a ton bag or ton barrel, placing the waste activated carbon in a feed hopper by using a crane, a forklift and the like, and conveying the waste activated carbon into a storage hopper of an internal heat dryer by using a closed lifter and a scraper;
s4, drying, namely slowly moving the waste granular activated carbon forwards under the action of the inclination angle of an internal heating type drying furnace and gravity, wherein the temperature of saturated steam in the drying furnace is in the range of 150-170 ℃, and collecting the dried material from the bottom of the internal heating type drying machine, and conveying the material to a granular carbon regeneration bin for temporary storage through a screw conveyor;
s5, regenerating the activated carbon, feeding the dried material in a regeneration bin into a rotary kiln through a screw feeder for regeneration, introducing a small amount of air and steam, resolving waste gas adsorbed by waste activated carbon at a high temperature, precipitating the regenerated activated carbon at the bottom of the rotary kiln, cooling, packaging and recycling to obtain finished granular activated carbon, and purifying regenerated flue gas through a secondary combustion chamber, and then entering a flue gas purification system for purification, and discharging the regenerated flue gas through a 35-meter high-exhaust barrel;
s6, cooling, wherein the regenerated granular activated carbon enters a water-cooling carbon outlet machine through a closed conveying pipeline to be cooled and discharged, and the cooled material is conveyed to a screening hoist bin for storage through a ground scraper;
s7, screening and packaging, namely cooling the regenerated granular activated carbon, then enabling the cooled regenerated granular activated carbon to enter a screening system, directly packaging the regenerated carbon with the mesh number of more than 80 meshes, and crushing and packaging a small amount of the regenerated carbon with the mesh number of less than 80 meshes by a pulverizer;
s8, warehousing the finished product, and directly selling the packaged activated carbon serving as the finished product.
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| CN117101634A (en) * | 2023-09-21 | 2023-11-24 | 宁夏启玉生物新材料有限公司 | A kind of decolorization adsorption activated carbon online regeneration equipment and process for lactic acid production |
| CN117101634B (en) * | 2023-09-21 | 2024-02-06 | 宁夏启玉生物新材料有限公司 | A kind of online regeneration equipment and process of decolorizing adsorption activated carbon for lactic acid production |
| JP2025073943A (en) * | 2023-10-27 | 2025-05-13 | 青▲島▼冠宝林活性炭有限公司 | Powdered activated carbon non-oxidizing continuous regenerative cooling production line |
| JP7720896B2 (en) | 2023-10-27 | 2025-08-08 | 青▲島▼冠宝林活性炭有限公司 | Powdered activated carbon non-oxidizing continuous regenerative cooling production line |
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