CN115337918A - Activated carbon regeneration system and method - Google Patents
Activated carbon regeneration system and method Download PDFInfo
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- CN115337918A CN115337918A CN202210976339.XA CN202210976339A CN115337918A CN 115337918 A CN115337918 A CN 115337918A CN 202210976339 A CN202210976339 A CN 202210976339A CN 115337918 A CN115337918 A CN 115337918A
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- B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract
The invention discloses an active carbon regeneration system and method, wherein the system comprises: the system comprises a raw material pretreatment and feeding system, a vertical multi-stage regenerative furnace and a waste heat recovery system which are sequentially connected; the raw material pretreatment and feeding system comprises a drying furnace, and the vertical multi-section regeneration furnace comprises a distributor, a carbonization bin, an activation bin and a regenerated carbon cooler in an up-down arrangement sequence. The activated carbon regeneration method comprises the following steps: preliminarily drying the activated carbon to be activated; activating the preliminarily dried activated carbon to be activated to obtain activated carbon and activated tail gas, and generating combustion flue gas; respectively recovering the activated tail gas and heat generated by the activated tail gas, wherein the recovered activated tail gas is used as fuel gas after being dedusted, and the recovered heat is used for heating desalted water to generate steam which is respectively used as cloth steam and activated steam; and (3) using the combustion flue gas as a heat source for primarily drying the activated carbon to be activated, performing environment-friendly treatment on the cooling flue gas, and then discharging the cooled flue gas, and repeating the steps until the activated carbon to be activated is treated.
Description
Technical Field
The invention relates to the technical field of activated carbon regeneration, in particular to an activated carbon regeneration system and method.
Background
The activated carbon has a highly developed pore structure, a high specific surface area and stable chemical properties, has strong adsorption capacity on organic substances, and is widely applied to various fields such as medicine, metallurgy, food, chemical industry, military, environmental protection and the like as an excellent adsorbent. However, on one hand, the production resources of the activated carbon are more and more scarce, and the price is higher; on the other hand, activated carbon after saturation adsorption is difficult to regenerate, and a common activated carbon regeneration method is complex in regeneration operation and high in regeneration cost, so that a large amount of waste activated carbon is treated in ways of incineration, landfill and the like, and resource waste and environmental hazards are caused. Therefore, the regeneration of activated carbon is of great importance from the economical and environmental viewpoints.
At present, the technologies for regenerating activated carbon mainly include: chemical regeneration, thermal regeneration, biological regeneration, electrochemical regeneration, and the like. Among them, the thermal regeneration method is most commonly used, and is suitable for saturated activated carbon in which almost all adsorbates are organic substances. However, the conventional thermal regeneration method generally has the problems of high regeneration cost, low thermal efficiency and large pollutant discharge amount, and the yield of the obtained regenerated activated carbon is relatively low. For example, a vertical fluidized bed furnace is adopted to regenerate powdered activated carbon, the equipment structure is simpler, continuous production is realized, but high-temperature tail gas is cooled by water spraying, and the calcined carbon powder is collected by a bag type dust collector or is directly collected by a wet type dust collector, so that the obtained product is in a slurry state, and the heat energy is not fully utilized. Other main regeneration methods such as a smoldering furnace method, a flat furnace method, a groove furnace method and a forming, granulating and activating method (a vertical furnace) are all used for carrying out batch production, and have the advantages of high energy consumption, low yield, environmental pollution, poor product quality and high labor intensity.
Disclosure of Invention
In view of the above, the present invention provides a system and a method for regenerating activated carbon, which have the advantages of high production efficiency, low energy consumption, continuous production, stable performance of regenerated activated carbon, high yield, no pollution, low labor intensity, etc., and are directed to the problems of the activated carbon regeneration technology. The technical scheme of the invention is as follows:
in a first aspect, the present invention provides an activated carbon regeneration system comprising: the system comprises a raw material pretreatment and feeding system, a vertical multi-section regenerating furnace and a waste heat recovery system which are connected in sequence;
the raw material pretreatment and feeding system comprises a drying furnace, wherein a hot flue gas inlet of the drying furnace is connected with a flue gas main pipe of a combustion heating mechanism of the vertical multi-section regenerating furnace; the air inlet of the drying furnace is connected with the air outlet of the hot blast stove, and the air inlet of the hot blast stove is connected with the air outlet of the tail gas dust remover of the waste heat recovery system; the discharge port of the drying furnace is connected with the inlet of a dry carbon bin, and the outlet of the dry carbon bin is connected with the feed port of the vertical multi-section regenerating furnace; the waste gas outlet of the drying furnace is connected to a flue gas purification device;
the vertical multi-section regenerative furnace comprises a furnace body, the furnace body comprises a distributor, a carbonization bin, an activation bin and a regenerated carbon cooler which are arranged in sequence from top to bottom, the distributor is connected with a feed inlet of the furnace body, and a distributor steam inlet is arranged on the distributor; at least one tail gas outlet is arranged between the carbonization bin and the activation bin or in the activation bin and is communicated with a tail gas cooler air inlet of the waste heat recovery system; the activation bin is provided with an activation bin steam inlet; at least one combustion heating mechanism is respectively arranged in the carbonization bin and the activation bin; the regenerated carbon cooler is connected with a discharge hole of the furnace body; and the distributor steam inlet and the activation bin steam inlet are connected with a heat exchange liquid outlet of a tail gas cooler of the waste heat recovery system.
Furthermore, each combustion heating mechanism comprises two burners, the two burners are connected through a connecting body, a heat transfer element is arranged in the connecting body, the burners are arranged outside the furnace body, and the connecting body is positioned inside the furnace body; two the combustor communicates respectively through 3 three-way valves flue gas house steward, gas house steward and compressed air house steward, the hot flue gas import of drying furnace is still connected to the flue gas house steward, waste heat recovery system's tail gas dust remover gas outlet is still connected to the gas house steward, compressed air pump is still connected to the compressed air house steward.
Preferably, the material of the connecting body is heat-resistant alloy steel.
Alternatively, the connecting body may be arranged in parallel and/or perpendicular to the furnace body.
Further, the heat transfer element is formed by filling a plurality of porous ceramic heat accumulators.
Further, the waste heat recovery system comprises a tail gas cooler, a tail gas dust remover, a steam distribution drum and a dust collection tank, wherein a gas outlet of the tail gas cooler is connected with a gas inlet of the tail gas dust remover, a dust outlet of the tail gas dust remover is connected with the dust collection tank, and a gas outlet of the tail gas dust remover is respectively connected with a gas main pipe of the combustion heating mechanism and a gas inlet of the hot blast stove; the steam outlet of the steam distribution drum is respectively connected with the steam inlet of the activation bin and the steam inlet of the distributor, the liquid inlet of the steam distribution drum is connected with a desalted water pipeline, the liquid outlet of the steam distribution drum is connected to the inlet of a desalted water circulating pump, the outlet of the desalted water circulating pump is connected to the circulating liquid inlet of the regenerated carbon cooler, the circulating liquid outlet of the regenerated carbon cooler is connected with the heat exchange liquid inlet of the heat exchanger, and the heat exchange liquid outlet of the heat exchanger is connected to the steam inlet of the steam distribution drum.
Preferably, the hot blast stove is also provided with a combustion fan, and the combustion fan is connected to a combustion air inlet of the hot blast stove and used for providing combustion air for the hot blast stove.
In a second aspect, the present invention provides a method for regenerating activated carbon, comprising:
primarily drying the activated carbon to be activated in a drying furnace;
introducing the preliminarily dried activated carbon to be activated into a vertical multi-stage regeneration furnace for activation to obtain activated carbon and activated tail gas, and generating combustion flue gas;
respectively recovering the activated tail gas and heat generated by the activated tail gas through a waste heat recovery system, wherein the recovered activated tail gas is used as fuel gas after being dedusted, and the recovered heat is used for heating desalted water to generate steam which is respectively used as cloth steam and activated steam;
and (3) using the combustion flue gas as a heat source for primarily drying the activated carbon to be activated, performing environment-friendly treatment on the cooling flue gas, and then discharging, wherein the steps are repeated in such a circulating way until the activated carbon to be activated is treated.
Further, the activated carbon to be activated is primarily dried in a drying furnace, wherein the temperature of the drying furnace is controlled to be 130-200 ℃, and preferably 150-190 ℃; the water content of the dry carbon is 5-15%, preferably 5-10%.
Further, the control parameters for activating the preliminarily dried activated carbon to be activated are as follows: the pressure in the hearth of the vertical multi-section regenerative furnace is-0.01 MPaG-0.2MPaG, preferably-0.01 MPaG-0.1MPaG; the temperature of the carbonization bin is controlled to be 440-600 ℃, preferably 500-550 ℃, and the temperature of the activation bin is controlled to be 600-1100 ℃, preferably 700-900 ℃.
Further, the preliminarily dried activated carbon to be activated is introduced into a vertical multi-stage regeneration furnace for activation, one part of steam participating in the activation reaction is cloth steam, and the other part of the steam is activated steam.
Further, in the process of introducing the preliminarily dried activated carbon to be activated into a vertical multi-stage regenerating furnace for activation, the total consumption Q of the material distribution steam and the activated steam is calculated according to the following formula:
q = W (Fc multiplied by eta-, Q: total steam flow, kg/h; W: dry carbon flow, kg/h; fc: fixed carbon content of dry carbon,%; eta: steam coefficient, 10% -15%; M: total water content of dry carbon,%, wherein the cloth steam accounts for 20% -50% of the total steam.
Further, the dust content control after the dust removal of the activated tail gas<5mg/m 3 . Compared with the prior art, the invention can obtain the following technical effects:
(1) The method is suitable for all media from powder activated carbon to granular activated carbon, and can be used for regenerating waste activated carbon with various specifications from biomass activated carbon to coal-based activated carbon, the yield of the regenerated carbon can reach 50% -95%, and the performance of the regenerated carbon can reach 92% -130% of that of new carbon.
(2) According to the invention, through the circular matching of the raw material pretreatment and feeding system, the vertical multi-stage regeneration furnace and the waste heat recovery system, the high-temperature carbon after the activation reaction and the steam produced by recovering the waste heat of the high-temperature tail gas are used as the activating agent, the activated tail gas after the waste heat recovery is deeply filtered and purified and then returns to the regeneration furnace to burn and maintain the temperature required by activation, the flue gas after the combustion of the activated tail gas is used for drying the wet waste active carbon raw material, the heat required by activation can basically reach self balance, and the method has the advantages of high production efficiency, low energy consumption, continuous production, stable performance of the regenerated active carbon, high yield, no pollution, low labor intensity and the like.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiment(s) of the application and together with the description serve to explain the application and not to limit the application. In the drawings:
fig. 1 is a schematic view of the structure of an activated carbon regeneration system of the present invention.
Fig. 2 is a schematic structural view of a combustion heating mechanism of the activated carbon regeneration system of the present invention.
FIG. 3 shows the iodine value of the fresh charcoal and the iodine value of the regenerated charcoal in example 2 of the present invention.
FIG. 4 is a graph showing the yield of the regenerated carbon relative to each regeneration in example 2 of the present invention.
FIG. 5 is a graph showing the change in the regeneration rate of the wet oxidation process in comparative example 2 of the present invention.
In fig. 1 and 2, 1 raw material pretreatment and feeding system, 101 drying furnace, 102 drying furnace tail gas blower, 103 dry char conveying mechanism, 104 dry char bin, 105 feeder; 2, a vertical multi-section regenerative furnace, 201 distributing devices, 202 carbonization bins, 203 activation bins, 204 tail gas outlets, 206 combustion heating mechanisms, 207 burners, 208 connecting bodies, 209 porous ceramic heat accumulators, 210 flue gas pipes, 211 flue gas three-way valves, 212 flue gas main pipes, 213 gas pipes, 214 gas three-way control valves, 215 gas main pipes, 216 compressed air pipes, 217 compressed air three-way control valves, 218 compressed air main pipes and 219 furnace bodies; 3 waste heat recovery system, 301 tail gas cooler, 302 tail gas dust remover, 303 dust collection tank, 304 regenerated carbon cooler, 305 steam-dividing drum, 306 forced circulation pump, 307 hot-blast furnace, 308 cloth steam pipe, 309 activation steam pipe, 310 hot-blast furnace fan, 4 regenerated carbon feed bins, a make-up gas, B waste activated carbon, C compressed air, D steam header, E desalted water, F make-up gas.
Detailed Description
In the description of the present invention, the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "parallel", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of describing the present invention but do not require that the present invention must be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
In the description of the present invention, it is to be noted that those whose specific conditions are not specified in the examples are carried out according to the conventional conditions or the conditions recommended by the manufacturers. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
The present invention will now be described in further detail with reference to the following figures and specific examples, which are intended to be illustrative, but not limiting, of the invention.
As shown in fig. 1 and 2, an embodiment of the present invention provides an activated carbon regeneration system, including: the system comprises a raw material pretreatment and feeding system 1, a vertical multi-section regenerative furnace 2 and a waste heat recovery system 3 which are connected in sequence.
The raw material pretreatment and feeding system 1 comprises a drying furnace 101, a dry charcoal conveying mechanism 103 and a dry charcoal bin 104. The drying furnace 101 is used for heating and drying the activated carbon to be activated by using the residual heat of the flue gas, and the drying furnace 101 can be a boiling drying furnace or a rotary drying furnace. The air inlet of the drying furnace 101 is connected with a flue gas manifold 212 of the combustion heating mechanism 206 of the vertical multi-section regenerating furnace 2; the discharge port of the drying furnace 101 is connected to the inlet at the bottom of the dry charcoal conveying mechanism 103, the outlet at the top of the dry charcoal conveying mechanism 103 is connected to the dry charcoal bin 104, the dry charcoal bin 104 is connected to the feeder 105 of the vertical multi-stage regeneration furnace 2, and the outlet of the feeder 105 is connected to the feed port of the vertical multi-stage regeneration furnace 2. The air inlet of the drying furnace 101 is connected with the air outlet of the hot blast stove 307. The drying furnace 101 is provided with a drying furnace tail gas fan 102, the drying furnace tail gas fan 102 is connected to a flue gas purification device for purification treatment and then is discharged, and the drying furnace tail gas purification adopts a conventional flue gas desulfurization and dust removal technology.
The vertical multi-section regenerative furnace 2 comprises a furnace body 219, the furnace body 219 comprises a distributor 201, a carbonization bin 202, an activation bin 203 and a regenerated carbon cooler 304 in the vertical arrangement sequence, the distributor 201 is connected with a feed inlet of the furnace body 219, and a distributor steam inlet is arranged on the distributor 201; a tail gas outlet 204 is arranged in the activation bin 203, and the tail gas outlet 204 is communicated with a tail gas cooler 301 air inlet of the waste heat recovery system 3; the activation bin 203 is provided with an activation bin steam inlet. The carbonization bin 202 and the activation bin 203 are respectively provided with a combustion heating mechanism 206, the combustion heating mechanism 206 comprises two burners 207, the two burners 207 are connected through a connecting body 208, and the connecting body 208 is made of heat-resistant alloy steel which can work at 1200 ℃ for a long time. The connector 208 is internally provided with a heat transfer element, the heat transfer element is formed by sequentially filling a plurality of refractory material porous ceramic heat accumulators 209, and the inside of each porous ceramic heat accumulator has certain porosity and can circulate high-temperature flue gas. The burner 207 is arranged outside the furnace body 219, and the connecting body 208 is positioned inside the furnace body 219; the two burners 207 are respectively communicated with a flue gas manifold 212, a fuel gas manifold 215 and a compressed air manifold 218 through 3 three-way valves (211, 214, 217). The flue gas main pipe 212 is also connected with a hot flue gas inlet of the drying furnace, and hot flue gas generated by the burner is used for drying the activated carbon to be activated. The gas main pipe 215 is further connected to an air outlet of a tail gas dust remover 302 of the waste heat recovery system 3, and tail gas generated by the waste heat recovery system is used as a part of gas. The compressed air manifold 218 is also connected to a compressed air pump. In the present embodiment, the combustion heating mechanism 206 is arranged perpendicular to the furnace body 219. In addition, a plurality of combustion heating means 206 may be provided according to the specification of the vertical multi-stage regenerator 2. The regenerated carbon cooler 304 is connected with a discharge port of the furnace body 219, and the discharge port of the furnace body 219 is connected with a regenerated carbon bin 4.
The waste heat recovery system 3 comprises a tail gas cooler 301, a tail gas dust remover 302, a steam distribution drum 305 and a dust collection tank 303, wherein a gas outlet of the tail gas cooler 301 is connected with a gas inlet of the tail gas dust remover 302, a dust outlet of the tail gas dust remover 302 is connected with a feed inlet of the dust collection tank 303, a gas outlet of the tail gas dust remover 302 is connected with a gas main 215 of the combustion heating mechanism 206, a gas outlet of the tail gas dust remover 302 is also connected with a gas inlet of a hot blast stove 307, a gas outlet of the hot blast stove 307 is connected with a gas inlet of the drying furnace 101, the hot blast stove 307 is also provided with a combustion-supporting fan 310, and the combustion-supporting fan 310 is connected to a combustion-supporting air inlet of the hot blast stove 307 to provide combustion-supporting air for the hot blast stove. The steam outlet of the steam-distributing drum 305 is respectively connected with the steam inlet of the activation bin 203 and the steam inlet of the distributor 201, the liquid inlet of the steam-distributing drum 305 is connected with a desalted water pipeline, the other end of the desalted water pipeline is connected with a desalted water device, and the preparation of desalted water is a conventional means in the field and is not explained in detail here. A liquid outlet of the steam-separating drum 305 is connected with a circulating liquid inlet of the regenerated carbon cooler 304 through a forced circulating pump 306, a circulating liquid outlet of the regenerated carbon cooler 304 is connected with a heat exchange liquid inlet of the tail gas cooler 301, and a heat exchange liquid outlet of the tail gas cooler 301 is connected with a steam inlet of the steam-separating drum 305 to form steam-water circulation. In this embodiment, the outlet steam pipeline at the top of the steam-splitting drum 305 is divided into three paths, one path is the distribution steam 308, and is connected to the steam interface of the distributor 201 of the vertical multi-stage regenerator 2; the other path is activated steam 309 which is connected to the furnace body between the position above the activated material outlet and the position below the activation bin of the vertical multi-section regeneration furnace 2; the third path is adjusting steam which is connected to an external steam pipe network, and the steam pipes are provided with corresponding steam flow meters and steam flow control valves.
In the system, the waste activated carbon is directly contacted with the flue gas sent from the vertical multi-section regeneration furnace in the raw material pretreatment and feeding system for heat exchange and is dried, and then the waste activated carbon enters the vertical multi-section regeneration furnace and is subjected to activation reaction with the steam sent from the waste heat recovery system at high temperature to obtain regeneration. On one hand, the waste heat recovery system removes dust and purifies the high-temperature activated tail gas generated by the vertical multi-section regenerative furnace and returns the high-temperature activated tail gas to the combustion heating mechanism of the vertical multi-section regenerative furnace for combustion, and the flue gas generated by combustion enters a drying furnace to dry wet waste activated carbon; on the other hand, desalted water is used for heat exchange to recover high-temperature regenerated carbon waste heat of the vertical multi-stage regeneration furnace and byproduct steam of activated tail gas waste heat of the vertical multi-stage regeneration furnace, and the byproduct steam is used for material dispersion and gasification pore-forming of the vertical multi-stage regeneration furnace.
The specific embodiment of the invention also provides a regeneration method of biomass activated carbon powder, which adopts the system and specifically comprises the following steps:
And 2, drying: feeding the materials to a drying furnace 101 through a screw feeder, blowing the waste activated carbon in the furnace through flue gas to carry out boiling heat transfer, controlling the temperature in the furnace to be 140-220 ℃, selecting the residence time of the materials in the furnace according to different material properties, discharging the dried materials from the drying furnace 101, and lifting the materials to a dried carbon bin 104 through a dried carbon conveying mechanism 103. The total water content of the dried material is 5-15%.
And 3, carbonizing and activating: the dry carbon in the dry carbon bin 104 is sent to a distributor 201 of the vertical multi-stage regenerating furnace through a feeder 105, and the distributor 201 is communicated with distribution steam to scatter the powder to achieve uniform distribution. The materials enter a regeneration furnace and then sequentially pass through the carbonization bin 202 and the activation bin 203 from top to bottom, and then enter a regenerated carbon cooler 304 for cooling and then are sent to a regenerated carbon bin 4. The steam participating in the activation reaction is partly the cloth steam from cloth steam pipe 308 and partly the activation steam from activation steam pipe 309. The operation temperature of the carbonization bin 202 is between 440 and 600 ℃, and the operation temperature of the activation bin 203 is between 600 and 1100 ℃. The residence time and the operation temperature of the materials in the furnace are selected according to different material properties, and the residence time of the waste carbon in the carbonization bin 202 and the activation bin 203 is determined according to the source and the properties of the waste carbon.
The iodine value of the active carbon regenerated by the steps is recovered to 950 mg/g-1100 mg/g, the total water content is less than 2 percent, and the specific surface area is 1100m 2 /g——1300m 2 The yield of the regenerated carbon can reach 50 to 95 percent, and the performance of the regenerated carbon can reach 92 to 130 percent of that of new carbon.
In the step 2, the temperature of the drying furnace is controlled to be 130-200 ℃, preferably 150-190 ℃; the water content of the dried carbon is 5-15%, preferably 5-10%.
In step 3, the pressure in the hearth of the vertical multi-section regenerating furnace 2 is-0.01 MPaG-0.2MPaG, preferably-0.01 MPaG-0.1MPaG; the temperature of the carbonization bin of the vertical multi-stage regeneration furnace 2 is controlled to be 440-600 ℃, preferably 500-550 ℃, and the temperature of the activation bin is controlled to be 600-1100 ℃, preferably 700-900 ℃; the retention time of the activated carbon in the carbonization bin is controlled according to different raw material particle sizes and pollutant types, and one excellent control index is shown in table 1:
TABLE 1 index for controlling regeneration of waste activated carbon of typical particle size
Note: the particle size classifications in Table 1 are classified according to commercially available columnar activated carbon, granular activated carbon, and powdered activated carbon.
In step 3, the total consumption Q of the distribution steam and the activation steam is calculated according to the following formula:
Q＝W(Fc×η-，
q: total steam flow, kg/h;
w: drying carbon flow rate, kg/h;
fc: fixed carbon content of dry carbon,%;
η: steam coefficient, 10% -15%;
m: total water content of dry charcoal,%;
wherein the cloth steam accounts for 20-50% of the total amount of the steam.
In step 4, the temperature of the activated tail gas at the outlet of the tail gas cooler is controlled to be 100-300 ℃, and preferably 120-150 ℃; control of dust content in activated tail gas at outlet of tail gas dust remover<5mg/m 3 (ii) a The operating pressure of the steam-dividing drum is 0.1MPa-0.3MPa, preferably 0.15MPa-0.2MPa;
example 1
This example provides a method for regenerating activated carbon from powdered activated carbon for chemical wastewater treatment, the main performance data of the new carbon being shown in table 2:
table 2 analysis data of new carbon performance of certain water treatment powdered activated carbon:
the powdered activated carbon is used for chemical wastewater treatment, the water content of the dehydrated waste carbon after adsorption saturation is about 50%, and the particle size distribution is less than 200 meshes (the main index analysis data is shown in table 3).
Table 3 water treatment waste activated carbon performance analysis data:
the activated carbon regeneration method specifically comprises the following steps:
And 2, drying: the material is fed into a drying furnace 101 through a screw feeder, the waste activated carbon is blown by smoke in the furnace to carry out boiling heat transfer, the temperature in the furnace is controlled to be 150-190 ℃, the retention time of the activated carbon in the furnace is 25-35 seconds, and the dried material is discharged from the drying furnace 101 and lifted to a dried carbon bin 104 through a dried carbon conveying mechanism 103. The total water content of the dried material is 5% -10%.
The temperature of the activated tail gas at the outlet of the activated tail gas heat collector is controlled to be 130-150 ℃; the activated tail gas dust content at the outlet of the activated tail gas dust remover is less than 5mg/m 3 (ii) a The operating pressure of the steam-splitting drum is 0.2MPaG; the total consumption amount of the cloth steam and the activated steam is 25Kg to 60Kg per ton of dry carbon feeding requirement, and the cloth steam accounts for 45 percent to 50 percent of the total amount of the steam.
The yield of the regenerated carbon (based on fixed carbon) of the waste activated carbon treated by the regeneration equipment and the regeneration method reaches 77-85 percent. The quality index analysis thereof is shown in Table 4.
Table 4 analytical data for regenerated activated carbon of example 1
Example 2
The waste activated carbon of example 1 was subjected to a plurality of adsorption-regeneration cycles under the regeneration conditions of example 1, and the changes in the performance and yield of the regenerated carbon after the treatment of 5 adsorption-regeneration cycles were shown in fig. 1 and 2, respectively.
From the performance and yield data of the regenerated carbon after 5 times of adsorption-regeneration cycle treatment, the performance of the regenerated carbon after the regeneration treatment of the waste active carbon is stable, and the repeated cyclic utilization can not be obviously reduced; the relative stability is maintained in terms of the yield of the regenerated carbon, and the loss of each regeneration is about 20 percent.
Example 3
This example takes the same regeneration steps as example 1, but changes are made to the regeneration operating conditions as follows, specifically:
and 3, in the carbonization and activation, the operation temperature of the carbonization bin 202 is controlled to be 440-490 ℃, and the operation temperature of the activation bin 203 is controlled to be 950-1100 ℃. The residence time of the waste carbon in the carbonization bin 202 is 40-60 seconds, and the residence time of the waste carbon in the activation bin 202 is 20-35 seconds.
The total consumption amount of the cloth steam and the activated steam is 45Kg to 73Kg per ton of dry carbon feeding requirement, and the cloth steam accounts for 40 percent to 50 percent of the total amount of the steam.
The yield of the activated carbon regenerated under the conditions reaches 70-74 percent. The mass analysis data are shown in table 4:
table 5 analysis data of the properties of the regenerated carbon of example 2
As the activation temperature and the activation residence time are increased in example 2, the adsorption capacity of the obtained regenerated carbon is improved, but the burnout rate is increased and the yield of the regenerated carbon is reduced. Therefore, the temperature of the carbonization bin of the vertical multi-stage regenerating furnace is controlled to be 440-600 ℃, preferably 500-550 ℃, and the temperature of the activation bin is controlled to be 600-1100 ℃, preferably 700-900 ℃; and the residence time is moderate.
Example 4
In this example, a columnar coal-based activated carbon was obtained by removing tar and naphthalene from coke oven gas in deep purification and saturated with naphthalene as raw materials, and the performance parameters are shown in Table 6.
Table 6 analysis data of a certain adsorption-saturated spent columnar coal-based activated carbon:
| particle size distribution of waste carbon | All water | Ash content | Volatile component(s) | Carbon tetrachloride adsorption Rate (%) | Specific surface area |
| 2mm—4mm | ≈32％ | 1.4％ | 31.1％ | 13％ | 352m 2 /g |
The activation was carried out as in example 1, with the following specific process specifications:
and 2, in the drying process, the temperature of the drying furnace is between 150 and 190 ℃, and the retention time of the drying furnace is between 11 and 15 minutes.
In the step 3, during carbonization and activation, the operation temperature of the carbonization bin 202 is controlled to be 460-520 ℃, and the operation temperature of the activation bin 203 is controlled to be 800-850 ℃. The retention time of the waste carbon in the carbonization bin 202 is 20 minutes to 25 minutes, and the retention time of the waste carbon in the activation bin 202 is 20 minutes to 24 minutes.
The yield of the activated carbon regenerated under the conditions reaches 78-82%. The mass analysis data are shown in table 7:
TABLE 7 regenerated carbon Industrial analysis and elemental analysis data of example 3
Example 5
The embodiment provides a regeneration method of granular activated carbon in VOC adsorption treatment, the specific raw material is husk granular activated carbon with saturated adsorption in VOC treatment, and the performance parameters are shown in Table 8.
Table 8 certain adsorption saturated husk granular activated carbon analytical data:
| particle size distribution of waste carbon | All-water | Ash content | Volatile component(s) | Carbon tetrachloride adsorption Rate (%) | |
| 10 to 50 meshes | ≈9％ | 1.6％ | 21.1％ | 18.6％ | 413m 2 /g |
The activation was carried out as in example 1, with the following specific process specifications:
and 2, in the drying process, the temperature of a drying furnace is 130-150 ℃, and the retention time of the drying furnace is 6-11 minutes.
And 3, in the carbonization and activation, the operation temperature of the carbonization bin 202 is controlled to be 440-500 ℃, and the operation temperature of the activation bin 203 is controlled to be 800-850 ℃. The retention time of the waste carbon in the carbonization bin 202 is 10-15 minutes, and the retention time of the waste carbon in the activation bin 202 is 7-12 minutes.
The yield of the activated carbon regenerated under the conditions reaches 75-80 percent. The mass analysis data are shown in table 9:
TABLE 9 regenerated carbon Industrial analysis and elemental analysis data of example 4
Comparative example 1
The spent activated carbon of example 1 was regenerated by a Fenton reagent oxidation wet regeneration process under the following operating conditions:
h in Fenton reagent 2 O 2 /Fe 2+ Is 20 2 O 2 The concentration of the regenerated carbon is approximately equal to 20mmol/L, the regeneration temperature is 60 ℃, the regeneration time is 1 hour, the yield of the regenerated carbon is more than 96 percent, and the performance analysis data of the regenerated carbon is shown in a table 10:
TABLE 10 analysis of regenerated activated carbon Performance data for comparative example 1
| Dry basis ash | Volatile component of drying base | Packing density | Methylene blue adsorption number | Iodine number |
| 1.94％ | 4.62％ | 0.53 | 113mg/g | 682mg/g |
From the data of the regenerated carbon, the loss of the fixed carbon regenerated by the wet oxidation method is small, the yield of the regenerated carbon is high, but the problem of incomplete regeneration exists, the regeneration time is long, and the regeneration performance can be recovered by about 70 percent.
Comparative example 2
As shown in fig. 5, it can be seen that the wet regeneration method cannot completely regenerate activated carbon, and the performance of the regenerated carbon after 5 regeneration cycles is less than 60% of the performance of new carbon.
In conclusion, the method is suitable for all media from powder activated carbon to granular activated carbon, and can be used for regenerating waste activated carbon with various specifications from biomass activated carbon to coal-based activated carbon, the yield of the regenerated carbon can reach 50-95%, and the performance of the regenerated carbon can reach 92-115% of that of new carbon.
As used in the specification and claims, certain terms are used to refer to particular components or methods. As one skilled in the art will appreciate, different regions may refer to a component by different names. The present specification and claims do not intend to distinguish between components that differ in name but not in name. In the following description and in the claims, the terms "include" and "comprise" are used in an open-ended fashion, and thus should be interpreted to mean "include, but not limited to. "substantially" means within an acceptable error range, that a person skilled in the art can solve the technical problem within a certain error range to substantially achieve the technical effect. The following description is of the preferred embodiment for carrying out the present application, but is made for the purpose of illustrating the general principles of the application and is not to be taken in a limiting sense. The scope of the present application is to be considered as defined by the appended claims.
It is also noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a good or system that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such good or system. Without further limitation, an element defined by the phrases "comprising one of 8230; \8230;" 8230; "does not exclude the presence of additional like elements in articles of commerce or systems including such elements.
While the foregoing description shows and describes several preferred embodiments of the invention, it is to be understood, as noted above, that the invention is not limited to the forms disclosed herein, but is not to be construed as excluding other embodiments and is capable of use in various other combinations, modifications, and environments and is capable of changes within the scope of the inventive concept as expressed herein, commensurate with the above teachings, or the skill or knowledge of the relevant art. And that modifications and variations may be effected by those skilled in the art without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. An activated carbon regeneration system, comprising: the system comprises a raw material pretreatment and feeding system, a vertical multi-section regenerating furnace and a waste heat recovery system which are connected in sequence;
the raw material pretreatment and feeding system comprises a drying furnace, wherein a hot flue gas inlet of the drying furnace is connected with a flue gas main pipe of a combustion heating mechanism of the vertical multi-section regenerating furnace; the air inlet of the drying furnace is connected with the air outlet of the hot blast stove, and the air inlet of the hot blast stove is connected with the air outlet of the tail gas dust remover of the waste heat recovery system; the discharge port of the drying furnace is connected with the inlet of a dry carbon bin, and the outlet of the dry carbon bin is connected with the feed port of the vertical multi-section regenerating furnace; the waste gas outlet of the drying furnace is connected to a flue gas purification device;
the vertical multi-section regenerating furnace comprises a furnace body, wherein the furnace body comprises a distributing device, a carbonization bin, an activation bin and a regenerated carbon cooler which are arranged in sequence from top to bottom, the distributing device is connected with a feed inlet of the furnace body, and a distributing device steam inlet is arranged on the distributing device; at least one tail gas outlet is arranged between the carbonization bin and the activation bin or in the activation bin and is communicated with a tail gas cooler air inlet of the waste heat recovery system; the activation bin is provided with an activation bin steam inlet; at least one combustion heating mechanism is respectively arranged in the carbonization bin and the activation bin; the regenerated carbon cooler is connected with a discharge hole of the furnace body; and the distributor steam inlet and the activation bin steam inlet are connected with a heat exchange liquid outlet of a tail gas cooler of the waste heat recovery system.
2. The activated carbon regeneration system of claim 1, wherein each of the combustion heating mechanisms comprises two burners connected by a connecting body, the connecting body having a heat transfer element therein, the burners being mounted outside the furnace body, the connecting body being located inside the furnace body; two the combustor communicates respectively through 3 three-way valves flue gas house steward, gas house steward and compressed air house steward, the hot flue gas import of drying furnace is still connected to the flue gas house steward, waste heat recovery system's tail gas dust remover gas outlet is still connected to the gas house steward, compressed air pump is still connected to the compressed air house steward.
3. The activated carbon regeneration system of claim 2, wherein the connecting body is disposed parallel to and/or perpendicular to the furnace body.
4. An activated carbon regeneration system according to claim 2 or 3 wherein the heat transfer element is comprised of a plurality of porous ceramic heat accumulator packs.
5. The activated carbon regeneration system of claim 1, wherein the waste heat recovery system comprises a tail gas cooler, a tail gas dust remover, a steam separation drum and a dust collection tank, wherein an air outlet of the tail gas cooler is connected with an air inlet of the tail gas dust remover, a dust outlet of the tail gas dust remover is connected with the dust collection tank, and an air outlet of the tail gas dust remover is respectively connected with a gas main pipe of the combustion heating mechanism and an air inlet of the hot blast stove; the steam outlet of the steam distribution drum is respectively connected with the steam inlet of the activation bin and the steam inlet of the distributor, the liquid inlet of the steam distribution drum is connected with a desalted water pipeline, the liquid outlet of the steam distribution drum is connected to the inlet of a desalted water circulating pump, the outlet of the desalted water circulating pump is connected to the circulating liquid inlet of the regenerated carbon cooler, the circulating liquid outlet of the regenerated carbon cooler is connected with the heat exchange liquid inlet of the heat exchanger, and the heat exchange liquid outlet of the heat exchanger is connected to the steam-water inlet of the steam distribution drum.
6. A method for regenerating activated carbon, which comprises using the regeneration system according to any one of claims 1 to 5, the method comprising:
primarily drying the activated carbon to be activated in a drying furnace;
introducing the preliminarily dried activated carbon to be activated into a vertical multi-stage regeneration furnace for activation to obtain activated carbon and activated tail gas, and generating combustion flue gas;
respectively recovering the activated tail gas and heat generated by the activated tail gas through a waste heat recovery system, wherein the recovered activated tail gas is used as fuel gas after being dedusted, and the recovered heat is used for heating desalted water to generate steam which is respectively used as cloth steam and activated steam;
and (3) using the combustion flue gas as a heat source for primarily drying the activated carbon to be activated, performing environment-friendly treatment on the cooling flue gas, and then discharging the cooled flue gas, and repeating the steps until the activated carbon to be activated is treated.
7. The activated carbon regeneration method of claim 6, wherein the activated carbon to be activated is preliminarily dried in a drying furnace, and the temperature of the drying furnace is controlled to be 130 ℃ to 200 ℃, preferably 150 ℃ to 190 ℃; the water content of the dried carbon is 5-15%, preferably 5-10%.
8. The activated carbon regeneration method according to claim 6, wherein the control parameters for activating the preliminarily dried activated carbon to be activated are as follows: the pressure in the hearth of the vertical multi-section regenerative furnace is-0.01 MPaG-0.2MPaG, preferably-0.01 MPaG-0.1MPaG; the temperature of the carbonization bin is controlled to be 440-600 ℃, preferably 500-550 ℃, and the temperature of the activation bin is controlled to be 600-1100 ℃, preferably 700-900 ℃.
9. The activated carbon regeneration method as claimed in claim 6, wherein the activated carbon to be activated after primary drying is introduced into a vertical multi-stage regeneration furnace for activation, and a part of the steam participating in the activation reaction is cloth steam and a part of the steam is activated steam.
10. The activated carbon regeneration method according to claim 9, wherein the total amount Q of the cloth steam and the activated steam consumed during the activation is calculated as follows: q = W (Fc multiplied by eta-, Q is the total steam flow, kg/h, W is the dry carbon flow, kg/h, fc is the fixed carbon content of the dry carbon, eta is the steam coefficient, 10-15%, M is the total water content of the dry carbon, wherein the cloth steam accounts for 20-50% of the total steam.
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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 | On-line regeneration equipment and process of decoloration adsorption activated carbon for lactic acid production |
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