CN115557500B

CN115557500B - A multi-chamber circulating fluidized activation integrated furnace device and method for preparing activated carbon by physical method

Info

Publication number: CN115557500B
Application number: CN202211096745.3A
Authority: CN
Inventors: 孙孝德; 范玉佼
Original assignee: Individual
Current assignee: Individual
Priority date: 2022-09-08
Filing date: 2022-09-08
Publication date: 2025-01-28
Anticipated expiration: 2042-09-08
Also published as: CN115557500A

Abstract

The invention discloses a multi-hearth circulating fluidization and activation integrated furnace device and method for preparing active carbon by a physical method, and relates to the technical fields of active carbon preparation of an activation furnace and thermal regeneration of waste active carbon. The device comprises a sealed spiral conveyor, a feed pipe, a baffling type hood, a pneumatic conveying medium inlet, a distributing device, a discharging pipe, a cold material machine, a top gas mixer, a cyclone separator, a material returning device, a slag discharging pipe, a gas machine box, a bottom gas hood and a slag cooling machine. According to the invention, carbonaceous semicoke particles with the particle size of more than 100 microns are captured by the cyclone separator, the activator gas flow is recycled from the lower hearth to the upper hearth layer through the baffling hood, the granular carbonaceous materials flow into the lower hearth layer through the blanking pipe after fluidization and activation from the upper hearth to be continuously subjected to fluidization and activation, and then the product is collected, so that the activator is saved, and meanwhile, the yield of activated carbon of carbonaceous raw materials is increased, so that the integrated furnace device has more environmental protection and economy.

Description

Multi-hearth circulating fluidization and activation integrated furnace device and method for preparing activated carbon by physical method

Technical Field

The invention relates to the technical field of activated carbon preparation of an activation furnace and waste activated carbon thermal regeneration, in particular to a multi-hearth circulating fluidization activation integrated furnace device and method for preparing activated carbon by a physical method. .

Background

Currently, there are various furnace types and activation processes for physical activation of activated carbon, and there are mainly a schlieren activation furnace, a rotary furnace, a rake furnace, and the like. The activation process is that the activating gas and the activator gas contacted with the surface of the solid particles are diffused and enter into the carbon layer, so that the existing furnace has the problems of low activation speed, long activation time, poor product quality consistency and the like, the existing furnace has huge volume and high manufacturing cost, the currently commonly used Siroper furnace has the defects of complex structure, long furnace starting and stopping time, low steam utilization rate, large consumption, high energy consumption, low unit volume yield, high manufacturing cost of the rake type furnace and long construction period, wherein the heat-resistant steel needs to be imported from abroad and has a certain dead angle during activation, and the various activation furnaces cannot activate powdery carbon raw materials.

Along with the increasing use amount of the activated carbon, the demand for regenerating the waste activated carbon is stronger, and the method has wide prospect for reducing carbon emission and regenerating the waste activated carbon. At present, the waste activated carbon is thermally regenerated in a furnace type rake type furnace, two rotary furnaces are used, the furnace type is externally supplied with fuel gas, only granular waste activated carbon can be regenerated, the waste activated carbon has high selectivity on the particle size, the energy consumption is high, and the quality of the thermally regenerated activated carbon is obviously reduced.

Disclosure of Invention

The invention aims to provide a physical method activated carbon activating and thermal regenerating device in a gas-solid fluidization contact mode, provides a multi-chamber circulating fluidization activating integrated furnace for preparing activated carbon by a physical method and a method thereof, is an activating technology in a fluidized state by directly contacting gas and solid, is also an advanced multi-chamber circulating fluidization activating integrated furnace for preparing activated carbon, and aims to solve the problems that the energy consumption of the existing furnace type for thermally regenerating waste activated carbon is high and the quality of the activated carbon after thermal regeneration is obviously reduced.

In order to achieve the above object, the present invention provides the following technical solutions:

According to an aspect of the present invention, there is provided a multi-hearth circulating fluidized activation integrated furnace apparatus for physically preparing activated carbon, the apparatus comprising:

The device comprises a sealing screw conveyor, a feeding pipe, a distributing device, a discharging pipe, a cold material machine, a top gas mixer, a cyclone separator, a material returning device, a slag discharging pipe, a gas machine box and a slag cooling machine;

The material enters a distributing device through a feed pipe by a sealed spiral conveyor, enters a first hearth material layer for fluidization activation, enters a next hearth fluidization material layer through a discharging pipe for deep fluidization activation after fluidization activation for a set residence time, and is collected after entering a cold material machine for indirect cooling after being discharged into an integrated furnace body through a discharging pipe;

the number of the partial hearths can be increased, and the total hearth number is generally ensured to be optimal in 2-4 hearths;

The bottom high-temperature mixed gas enters the bottom hearth fluidization layer of the multi-hearth furnace from the gas cabinet through the hood and is used as a fluidization medium, and a high-temperature steam activator is provided for the hearth fluidization layer;

the waste residues in each hearth waste residue zone are moved into the next hearth waste residue zone through a lower residue pipe until the waste residues are discharged from a furnace body through the lower residue pipe of the lowest hearth waste residue zone and are collected through a slag cooler;

the activated tail gas enters a cyclone separator to separate out solid and gas, and the gas enters subsequent treatment;

Specifically, the method comprises the following steps;

The device comprises a stock bin, a sealed screw conveyor, a feed pipe, a multi-hearth furnace, a discharge pipe, a cold material machine, a gas cabinet, a hood, a pneumatic conveying medium inlet, a cyclone separator, a material returning device, a distributing device, a top gas mixer, a jacket type hood, a slag discharging pipe, a feed pipe, a baffling hood and a slag cooling machine;

Each layer of the multi-hearth furnace is also provided with an ash slag zone and a fluidization working condition material layer;

after the device is started, carbonaceous materials enter a distributing device from a feed bin through a feed pipe by a sealed screw conveyor and then enter a first layer of hearth, after the first layer of hearth is fluidized and activated for a set residence time, high Wen Tanzhi solids are discharged into a working condition material layer of a next layer of hearth through a discharging pipe for further deep fluidization and activation, after the specific gravity of carbonaceous particles is reduced, the carbonaceous materials are discharged downwards through the discharging pipe and enter the next layer of hearth under the action of gas pressure and self gravity, and the carbonaceous materials continue to be fluidized and activated until the carbonaceous materials are discharged from the hearth of the set furnace layer through the discharging pipe to the outside of the furnace and are collected through a cold material machine after the carbonaceous materials are qualified for activation;

waste residues with large particle size and which cannot be fluidized by the waste residues enter an ash residue area, are transferred into the ash residue area of the next-layer hearth through a lower slag pipe, are discharged from a furnace body through a lower slag pipe of the lowest-layer hearth, and are collected through a slag cooler;

The activated tail gas discharged from the upper first-layer furnace and part of carbonaceous solid particles with small particle size enter the cyclone separator for gas-solid separation, the separated carbonaceous solid is returned to the upper furnace for continuous activation, the activated gas is cooled by a gas/gas heat exchange device and is preheated for air and steam, then the cooled gas is collected by a bag type dust collector to obtain powdery activated carbon with smaller particle size, the cooled activated tail gas enters a gas treatment flow for gas recycling or external delivery, the activated tail gas can be directly burnt, and sensible heat of high-temperature flue gas is collected by a preheater and a waste heat boiler for utilizing the purified qualified flue gas atmosphere to be discharged;

Part of the activator gas is fed in through annular steam feeding ports of furnace walls of the hearths, the bottom high-temperature mixed gas enters a fluidized bed of the bottommost hearth of the multi-hearth furnace from a gas cabinet through a blast cap, and is used as high-temperature fluidizing medium, and meanwhile, high-temperature steam is also used as the activator gas, and the high-temperature gas among the hearths enters a fluidized bed of the upper layer from the next hearth through a baffling blast cap penetrating through the bottom plate of the hearth.

The baffling type blast caps uniformly arranged at the bottom of the hearth can prevent carbonaceous solids from returning to the hearth at the lower part, ensure that high-temperature air flows uniformly and upwards pass through the fluidized bed, and the slag discharging pipes of the adjacent hearths are uniformly and crosswise arranged with the circumference when seen from the top view direction, so that uniform and smooth slag discharging is facilitated, and the slag discharging pipes are downwards inserted into slag in the slag discharging area of the hearth at the lower layer from the bottom of the hearth at the upper part.

The device further comprises a standby feed bin and a standby sealing screw conveyor, wherein before feeding, materials in the standby feed bin enter the device through the standby sealing screw conveyor, and the starting device enters a high-temperature fluidization working condition.

The device further comprises a furnace wall annular steam supplementing opening and a furnace wall annular air supplementing opening, wherein the furnace wall annular steam supplementing opening is uniformly supplemented with steam, the furnace wall annular air supplementing opening is uniformly supplemented with air, the steam is uniformly supplemented with the steam as activator gas, the activator concentration of a fluidized bed of a furnace in the upper layer is kept, oxygen in the uniformly supplemented air and the upward moving activated tail gas generate gas/gas homogeneous exothermic reaction, high-temperature gas sensible heat is provided for the activation endothermic reaction of carbonaceous solids in the material bed of the furnace in the upper layer, the continuous stable progress of the activation reaction of the furnace in the upper layer is kept, meanwhile, the formed high-temperature carbon dioxide gas is also used as a gas activator of the activation reaction in the upper layer, and the high-temperature mixed gas flows through baffling type hoods which penetrate through the furnace uniformly arranged on the bottom plate of the furnace and enters the fluidized bed of the upper layer to be fluidized and activated with carbonaceous particles of the furnace in the upper layer.

Furthermore, in the device, in the same hearth, the lower end of the upper hearth discharging pipe which is submerged in the fluidized bed is lower than the upper end of the same hearth discharging pipe, so that the mixing of the raw clinker of the carbonaceous solid particles is reduced, and the high Wen Tanzhi solid particles entering the hearth from the upper hearth can stay for a set fluidization activation reaction time.

Further, in the device, the upper ends of the slag discharging pipes are leveled with the bottoms of the corresponding hearths, the lower ends of the slag discharging pipes are immersed into ash slag areas of the hearths of the next layer, slag discharging pipes are arranged at positions, wherein slag discharging repose angles are formed by the edges of furnace walls of the horizontal air outlets of the baffling hood and slag outlets of the bottoms, the horizontal dip angle is larger than 45 degrees, the number of the slag discharging pipes of each layer exceeds 4, and the slag discharging pipes are uniformly arranged on the circumference. Thus, the slag discharging blind area of the slag area is reduced as much as possible, and slag can be discharged more smoothly when the pressure of the hearth fluctuates, so that the high-temperature air flow is kept to circulate smoothly upwards from the bottom through the baffling type hood, the continuous and stable operation of fluidization activation of each hearth is kept, and the slag discharging blind area of the slag area is cleaned and overhauled when the furnace is stopped.

Further, in the device, the distributor is arranged in the first hearth fluidization working condition material layer.

The blanking pipes (overlooking direction) of adjacent hearths are arranged in a crossed manner with the circumference, so that smooth discharging is facilitated, high-temperature carbonaceous particles flow into the next hearth fluidized bed from the upper hearth fluidized bed through the blanking pipes in sequence until the activated carbon is activated into qualified active carbon finished products, the qualified active carbon finished products are discharged out of a furnace body and are indirectly cooled by a cold material machine and then collected, and the active carbon of the second hearth can be directly discharged out of the furnace from the furnace wall or the bottom hearth through the discharging pipes at the corresponding blanking pipe height, and the finished active carbon is collected by the cold material machine.

According to the invention, the blanking pipe, the feeding pipe, the slag blanking pipe and the blast cap required by each hearth are all made of high-temperature-resistant alloy materials to provide mechanical properties, the ceramic materials with high temperature resistance, wear resistance and corrosion resistance are coated inside and outside, and the expansion joints are filled with high-temperature-resistant fibers, so that the parts can be used stably for a long time.

According to another aspect of the present invention, there is provided a method for preparing activated carbon by a physical method, the method comprising:

Step one, before feeding, materials in a standby stock bin enter a device through a standby sealing screw conveyor, and a starting device enters a high-temperature fluidization working condition;

After the device is started, materials enter a distributing device from a feed bin through a feed pipe and then enter a first hearth fluidization material layer, uniformly fall into the first hearth fluidization material layer of the integrated activation furnace under the action of the pressure of gas and the gravity of solids, after the first hearth is fluidized and activated for a set residence time, high-temperature carbonaceous particles are discharged into a next hearth working condition fluidization material layer through a discharging pipe for further deep fluidization and activation, the specific surface area of the carbonaceous particles is increased, the pore volume is increased, the specific gravity is gradually reduced, and under the action of a gas fluidization medium, the high Wen Tanzhi particles gradually flow out from the hearth to the lower hearth fluidization material layer through the discharging pipe under the action of the gravity until the carbonaceous particles are discharged from a furnace body and are indirectly cooled through a cold material machine and then are collected;

Step three, large-particle-size particles and gangue non-carbon impurities which are not easy to fluidize enter an ash residue area, move into the ash residue area of the next-layer hearth through a slag discharging pipe, finally, are discharged from a furnace body in the ash residue area of the bottom hearth through a slag discharging pipe, and are collected after being indirectly cooled through a slag cooler;

The solid carbonaceous particles with larger particle size are returned to the multi-hearth furnace through the steam returning device to be continuously fluidized and activated, and the activated tail gas is indirectly cooled and then is collected through the bag-type dust collector;

And fifthly, uniformly supplementing a part of the activator gas through annular steam supplementing openings of furnace walls of the hearths, enabling the bottom high-temperature mixed gas to enter a bottom hearth fluidized bed of the multi-hearth furnace from a gas cabinet through a connecting blast cap, taking the mixed gas as a gas fluidizing medium, simultaneously taking steam in the mixed gas as a gas activator, enabling oxygen in the air supplemented through the annular air supplementing openings of the furnace walls and hydrogen and carbon monoxide in the upward-moving activated tail gas to generate gas/gas homogeneous exothermic reaction, enabling high-temperature gas rich in steam and carbon dioxide gas to flow through baffling blast caps penetrating through the furnace bottom uniformly arranged on a hearth bottom plate, and taking the high-temperature steam and generated carbon dioxide as the gas activator of a upper hearth fluidized bed while taking the high-temperature steam and generated carbon dioxide as the fluidizing medium of the upper hearth fluidized bed.

Further, the activator gas is water vapor and carbon dioxide.

The ceramic material externally applied to various pipes is suitable for gas and solid environments of activation reaction (850-950 ℃ high temperature), and is resistant to steam corrosion and hydrogen sulfide corrosion;

The high-temperature carbonaceous particles in the hearth at the bottom are fluidized and activated, the material is kept to be continuously fluidized and activated, a gas activating agent required by activation and activated tail gas serving as energy are continuously provided for the hearth at the upper part, and the carbonaceous semicoke fine powder returned by the cyclone separator can also be continuously used for providing high-temperature solid carbonaceous material for returning to the hearth, so that the material temperature of a fluidized material layer of the hearth can be better kept, and the activation reaction is continuously and stably carried out.

The invention has the following advantages:

The invention fully utilizes the advantages of mass transfer and heat transfer of the circulating fluidized bed, the designed multi-hearth circulating fluidized activation structure ensures that the activation reaction of solid carbonaceous particles is uniform, the multi-hearth design reduces the problem of mixing carbonaceous solid particles in a fluidized bed reactor, the relative residence time of the solid particles in the hearth is consistent, the residence time of each hearth can be controlled by adjusting the flow according to the height and the diameter of a blanking pipe of the hearth, the material temperature can be controlled, the yield per unit volume is high, the activation efficiency is high, the utilization efficiency of a water vapor activator is high, the energy is saved, the environment is protected, the prepared powdery and granular activated carbon has stable and uniform quality, the conversion rate of the finished product of fixed carbon in a carbonaceous semicoke material is high, and the invention can apply granular and powdery carbonaceous raw materials, so that the circulating fluidized bed has wide prospect in the field of thermal regeneration of preparing activated carbon and waste activated carbon by the carbonaceous material.

The invention designs a carbonaceous particle circulating steam returning device, which is used for capturing carbonaceous semicoke particles with the particle size larger than 100 microns through a cyclone separator, leading the carbonaceous semicoke particles to enter a corresponding hearth for supplementary activation, discharging part of the carbonaceous semicoke particles from a discharging pipe, reducing the particle size of the rest of the carbonaceous semicoke particles, indirectly cooling the carbonaceous semicoke particles along with high-temperature activated tail gas, and collecting the carbonaceous semicoke particles through a bag-type dust collector, thereby increasing the yield of activated carbon of carbonaceous raw materials and enabling an integrated furnace system to have more environmental protection and economy.

The physical method provided by the invention has the advantages of high mass transfer and heat transfer of the fluidized bed, greatly reduced mixing of carbonaceous solid particles, high utilization rate of a gas activator, short activation time, uniform reaction, energy conservation, high yield of the activated carbon, and capability of preparing high-quality activated carbon.

The invention can also simultaneously prepare the active carbon of two different carbonaceous raw materials, and can realize the co-production of the active carbon preparation and the active carbon thermal regeneration without external fuel gas when the waste particles and the powdery active carbon are thermally regenerated.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It will be apparent to those of ordinary skill in the art that the drawings in the following description are exemplary only and that other implementations can be obtained from the extensions of the drawings provided without inventive effort.

The structures, proportions, sizes, etc. shown in the present specification are shown only for the purposes of illustration and description, and are not intended to limit the scope of the invention, which is defined by the claims, so that any structural modifications, changes in proportions, or adjustments of sizes, which do not affect the efficacy or the achievement of the present invention, should fall within the ambit of the technical disclosure.

FIG. 1 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method provided in embodiment 1 of the present invention;

FIG. 2 is an enlarged view of a deflector cap according to embodiment 1 of the present invention;

FIG. 3 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method according to example 2 of the present invention;

FIG. 4 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method according to example 3 of the present invention;

FIG. 5 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method according to example 4 of the present invention;

FIG. 6 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method according to example 5 of the present invention;

FIG. 7 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for preparing activated carbon by a physical method according to example 6 of the present invention;

FIG. 8 is a diagram of a multi-chamber circulating fluidized activation integrated furnace for physically preparing activated carbon according to example 7 of the present invention;

in the figure, 1-bin, 2-sealing screw conveyor, 3-standby bin, 4-standby sealing screw conveyor, 5-multi-hearth furnace, 51-working condition fluidized bed, 52-ash zone, 53-furnace wall annular water vapor supplementing port, 54-furnace wall annular air supplementing port, 55-hearth bottom plate and 56-slag discharging repose angle;

6-discharging pipe, 7-cold material machine, 7-1 cold material machine, 8-gas machine box, 9-feeding pipe, 10-pneumatic conveying medium inlet, 10-1-first pneumatic conveying medium inlet, 10-2-second pneumatic conveying medium inlet, 11-top gas mixer, 11-1-first mixer, 11-2-second mixer, 12-cyclone separator, 13-water vapor return device, 14-distributor, 15-jacket type hood, 16-slag discharging pipe, 16-1-upper furnace slag discharging pipe and 16-2-furnace slag discharging pipe;

17-blanking pipe, 18-baffling hood, 18-1-bottom gas hood, 19-slag cooler, 19-1-slag outlet, 20-bottom gas mixer, 21-air preheater, 22-secondary air blower, 23-steam superheater, 24-bag dust collector, 25-blower, 26-incinerator, 27-Roots blower, 28-mixer preheater, 29-waste heat steam boiler, 30-induced draft fan, 30-1-first induced draft fan, 30-2-second induced draft fan, 31-split cylinder, 32-economizer, 33-chimney, 34-high temperature high pressure gas fan, 35-lower hearth bunker, 36-lower hearth screw conveyor, 37-gas intercooler, 38-high pressure fan, 39-burner, 40-bellows, 41-gas cabinet and 42-powder collection tank.

Detailed Description

Other advantages and advantages of the present invention will become apparent to those skilled in the art from the following detailed description, which, by way of illustration, is to be read in connection with certain specific embodiments, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.

Example 1

As shown in fig. 1, the embodiment provides a multi-chamber circulating fluidization activation integrated furnace device and method for preparing activated carbon by a physical method:

The device is composed of 3 layers of hearths;

The device comprises a feed bin 1, a sealed screw conveyor 2, a feed pipe 9, a multi-hearth furnace 5, a discharge pipe 6, a cold material machine 7, a gas cabinet 8, a pneumatic conveying medium inlet 10, a cyclone separator 12, a water vapor return device 13, a distributing device 14, a top gas mixer 11, a jacket type hood 15, a slag discharging pipe 16, a feed pipe 17, a baffling hood 18 and a bottom gas hood 18-1, a slag cooler 19 and a bottom gas mixer 20;

The upper furnace layer slag discharging pipe 16-1 and the hearth slag discharging pipe 16-2 are uniformly arranged on a circumference in a top view, and each layer is provided with 4 pairs of four pipes which form a square.

Each layer of the multi-hearth furnace is also provided with an ash slag zone 52 and a working condition fluidization material layer 51;

after the device is started, materials enter a distributor 14 from a feed bin 1 through a feed pipe 9 by a sealed screw conveyor 2, then enter a first-layer hearth, after the first-layer hearth is fluidized and activated for a set residence time, high Wen Tanzhi solids flow into a second-layer hearth working condition fluidization material layer 51 through a discharging pipe 17 to be subjected to deep fluidization and activation again, after the specific gravity is reduced, the materials flow into the bottommost-layer hearth working condition fluidization material layer 51 downwards through the discharging pipe 17 to be subjected to continuous flow activation under the action of gravity, after the preset fluidization and activation time is activated, the materials are discharged from a hearth through a discharging pipe 6 to be indirectly cooled by a cold material machine 7 and then collected;

Waste residues with large particle size and difficult fluidization of waste residues such as carbonaceous particles and gangue enter a first-layer furnace ash zone 52, enter a second-layer furnace ash zone 52 through a lower slag pipe 16, are discharged from the bottom-most furnace ash zone 52, enter a slag cooler 19 for indirect cooling and are collected;

The small-particle-size carbonaceous solid particles and the waste gas enter a cyclone separator 12 to separate out solids and gases, and the gases enter subsequent treatment; the solid returns to the multi-hearth circulating furnace again through the steam returning device 13 to continue fluidization and activation, namely, the activated gas of the uppermost hearth and a part of solid particles with small particle size enter the cyclone separator 12, and the carbonaceous solid after gas-solid separation returns to the fluidized bed of the first hearth to be subjected to fluidization and activation;

The bottom gas is mixed by the bottom gas mixer 20 and then enters the gas cabinet 8 to enter the bottom working condition fluidization material layer 51 of the multi-hearth furnace through the connected bottom gas hood 18-1, and the steam gas activator enters the upper hearth working condition fluidization material layer 51 from the lower hearth sequentially along with the high-temperature gas flow through the baffling hood 18 penetrating through the hearth bottom plate 55.

The baffling type hood 18 penetrating through the hearth bottom plate 55 can prevent solids from returning to the hearth at the lower part, ensures that high-temperature air flows uniformly and upwards pass through the working condition fluidized bed 51, and the slag discharging pipes of the adjacent furnace layers are uniformly and crosswise arranged with the circumference in the overlook direction, so that uniform and smooth slag discharging is facilitated, and the slag discharging pipes 16 are downwards inserted into slag in the slag zone of the hearth at the lower layer from the bottom of the hearth at the upper part.

Furthermore, the device also comprises a standby feed bin 3 and a standby sealing screw conveyor 4, wherein before feeding, the materials in the standby feed bin 3 enter the device through the standby sealing screw conveyor 4, and the starting device enters a high-temperature fluidization working condition.

Further, the device also comprises a furnace wall annular water vapor supplementing port 53 and a furnace wall annular air supplementing port 54, wherein water vapor is supplemented as activator gas, the activator concentration in the fluidized bed of the upper furnace is kept, oxygen in the supplemented air and hydrogen and carbon monoxide in the upward moving activated tail gas generate gas/gas homogeneous exothermic reaction, gas sensible heat is provided for the activation endothermic reaction in the fluidized bed 51 of the upper furnace working condition as energy, the continuous progress of the activation reaction is kept, meanwhile, the generated high-temperature carbon dioxide gas is also used as activator gas, and the high-temperature gas rich in water vapor and carbon dioxide gas flows through the baffling hood 18 penetrating through the bottom plate 55 of the furnace to enter the fluidized bed 51 of the upper working condition to be fluidized, activated and endothermic reaction is carried out with solid carbonaceous particles.

Further, in the device, in the same hearth, the lower end of the upper layer blanking pipe 17 is lower than the upper end of the same layer blanking pipe.

Further, in the device, the upper end of the slag discharging pipe 16 is leveled with the bottom plate 55 of the hearth, the lower end of the slag discharging pipe 16 is immersed into the ash slag zone 52 of the next hearth, the upper end of the slag discharging pipe 16 is arranged according to the edge of the furnace wall with horizontal air outlet to form a slag discharging angle 56, the horizontal inclination angle is larger than 45 degrees, the number of the slag discharging pipes in each layer exceeds 4, and the slag discharging pipes are uniformly arranged on the circumference. Thus, the slag discharging blind area of the slag area 52 is reduced as much as possible, and slag can be discharged more smoothly when the pressure of the hearth fluctuates, and the slag discharging blind area of the slag area is cleaned and overhauled when the furnace is stopped.

Further, in the device, the height of the distributor 14 is required to be below the fluidized bed 51 under the first-layer furnace working condition.

The blanking pipes 17 (overlooking direction) of adjacent hearths are arranged in a crossed manner along the circumference, so that smooth discharging is facilitated, the discharged furnace body is discharged from the bottom hearth after being activated into qualified active carbon finished products, and the active carbon finished products are collected after being indirectly cooled by a cold material machine 7.

The blanking pipe 17, the feeding pipe 9, the slag discharging pipe 16, the jacket type hood 15, the baffling type hood 18 and the bottom gas hood 18-1 required by each hearth are made of high-temperature resistant alloy materials to provide mechanical properties, the inner and outer surfaces are coated with high-temperature resistant/wear-resistant/corrosion-resistant ceramic materials, and the expansion joints are filled with high-temperature resistant fibers, so that the parts can be used stably for a long time.

According to another aspect of the present invention, there is provided a method of preparing activated carbon, the method comprising:

step one, before feeding, materials in a standby feed bin 3 enter a device through a standby sealing screw conveyor 4, and a starting device enters a high-temperature fluidization working condition;

Step two, after the device is started, materials enter a distributing device 14 from a storage bin through a feeding pipe 9 by a sealing spiral conveyor 2; the high-temperature carbon particles are fluidized and activated for a set residence time in the first hearth, and then flow into the second hearth working condition fluidization material layer 51 through the blanking pipe 17 under the action of the gas pressure of the fluidizing gas medium and the gravity of the carbon solid for further deep fluidization and activation, the specific surface area of the particles is increased, the specific gravity is gradually reduced along with the deep progress of the activation reaction, the particles flow out from the hearth to the bottom hearth working condition fluidization material layer 51 through the blanking pipe 17 under the action of the gas fluidization medium and the gravity, and the particles are discharged from the bottom hearth working condition fluidization material layer 51 through the blanking pipe 17 under the action of the gravity after the preset residence time fluidization and activation of the bottom working condition fluidization material layer 51, are indirectly cooled and collected through the cold material machine 7;

step three, the waste residues with large particle size, such as carbonaceous solids, gangue and the like which are not easy to fluidize enter a slag area 52, enter the slag area 52 of the second-layer hearth through a slag discharging pipe 16, enter the slag area 52 of the bottom-layer hearth in sequence, are discharged from a furnace body through the slag discharging pipe, and enter a slag cooling machine 19 for cooling and collecting;

Step four, the carbonaceous particles with small particle size and the activated tail gas enter a cyclone separator 12 to separate out solids and gas, and the gas enters subsequent treatment;

And fifthly, the activator gas enters the bottom-layer hearth working condition fluidization material layer 51 of the multi-hearth furnace from the bottom through the gas cabinet 8 and the connected bottom gas hood 18-1, after the activation reaction, the activator gas is supplemented with water vapor through the annular water vapor supplementing inlet 53 of the furnace wall and then flows through the baffling hood 18 penetrating through the hearth bottom plate 55 along with high-temperature gas to enter the second-layer hearth working condition fluidization material layer 51 from the bottom hearth, after the activator gas is activated and reacted with the carbonaceous solid in the second-layer hearth working condition fluidization material layer 51, the activator gas is supplemented with water vapor again uniformly through the annular water vapor supplementing inlet 53 of the second-layer hearth, and then enters the first-layer hearth working condition fluidization material layer 51 through the baffling hood 18 penetrating through the hearth uniformly arranged on the first-layer hearth bottom plate 55, and the carbonaceous solid in the first-layer hearth working condition fluidization material layer is fluidized and activated.

As shown in fig. 2, in an enlarged view of the baffling hood 18, the high-temperature gas rich in steam and carbon dioxide activator flows through the baffling hood 18 which is uniformly arranged at the bottom of the hearth and penetrates through the hearth, and then uniformly and horizontally flows out to enter the working condition fluidization material layer 51.

Further, the activator gas is water vapor and/or carbon dioxide.

The ceramic material externally applied to various pipes is suitable for gas and solid environments of activation reaction (850-950 ℃ high temperature), and is resistant to steam corrosion and hydrogen sulfide corrosion.

Example 2

As shown in fig. 3, the embodiment provides a multi-hearth circulating fluidization and activation integrated furnace device and method for preparing activated carbon by a physical method, wherein the raw materials are single carbonaceous raw materials under the working condition of three hearths:

comprising the following steps:

The device comprises a bin 1, a sealing screw conveyor 2, a standby bin 3, a standby sealing screw conveyor 4, a multi-hearth furnace 5, a discharging pipe 6, a cold material machine 7, a gas cabinet 8, a feeding pipe 9, a pneumatic conveying medium inlet 10, a gas mixer 11, a cyclone separator 12, a returning device 13, a distributing device 14, a jacket type hood 15, a slag discharging pipe 16, a discharging pipe 17, a baffling hood 18, a bottom gas hood 18-1, a cold slag machine 19, a mixer 20, an air preheater 21, a secondary air blower 22, a steam superheater 23, a bag type dust remover 24, a blower 25, an incinerator 26, a Roots blower 27, a mixer preheater 28, a waste heat steam boiler 29, an induced draft fan 30, a split cylinder 31, an economizer 32 and a chimney 33;

The storage bin 1 is connected with the sealed spiral conveyor 2, the outlet of the sealed spiral conveyor 2 is connected with the feed pipe 9, the feed pipe 9 is connected with the jacket pipe type hood 15 assembly and the multi-hearth furnace 5, the jacket pipe type hood 15 is uniformly inserted into the first-layer hearth of the multi-hearth furnace 5, and the standby storage bin 3 is connected with the first-layer hearth of the multi-hearth furnace 5 through the sealed spiral conveyor 4; the discharging pipe 6 extends out of the fluidized bed of the multi-hearth furnace 5 and is connected with the cold material machine 7, the slag cooler 19 is connected with the multi-hearth furnace 5, ash in the furnace is discharged, the gas cabinet 8 is connected with the bottom gas hood 18-1 and enters the fluidized carbonaceous bed 51 of the lower hearth of the multi-hearth furnace, the inlet of the cyclone separator 12 is connected with the activated tail gas outlet of the first-layer hearth of the multi-hearth furnace 5, the lower part of the cyclone separator 12 is connected with the water vapor returning device 13, the outlet of the returning device 13 is connected with the upper-layer hearth of the multi-hearth furnace, the gas phase outlet of the cyclone separator 12 is connected with one end of the air preheater 21, the other end of the air preheater 21 is connected with the steam superheater 23, the side surface of the air preheater 21 is connected with the outlet of the secondary air blower 22, the other end of the steam superheater 23 is connected with the bag type dust collector 24, the outlet of the bag type dust collector 24 is connected with the inlet of the induced draft fan 30, the outlet of the induced fan 30 is connected with the inlet of the incinerator 26, the inlet of the incinerator 26 is also connected with the outlet of the incinerator 25, the outlet of the incinerator 26 is connected with the inlet of the mixed gas preheater 28, the outlet of the mixed gas preheater 28 is connected with the inlet of the steam boiler 29, the outlet of the mixed gas preheater 28 is connected with the inlet of the exhaust gas preheater 28, one side of the mixed gas preheater 28 is connected with the exhaust gas outlet of the boiler 31, the exhaust gas outlet of the flue gas separator is connected with the flue gas outlet of the flue gas separator 32, the flue gas outlet of the flue gas separator is connected with the flue gas outlet of the flue gas separator 32.

The device also comprises a slag discharging pipe 16 and a discharging pipe 17, wherein the discharging pipes (overlooking direction) of the adjacent hearths are arranged in a crossed manner with the circumference.

After the equipment is started, materials enter a distributor 14 in a multi-hearth furnace 5 from a feed bin 1 through a feed pipe 9, after solids enter a fluidized bed 51 in the working condition of the next hearth through pneumatic conveying, oxygen in air sent by a jacket pipe type hood 15 and hydrogen and carbon monoxide in upward activated gas are subjected to gas/gas homogeneous exothermic reaction to form high-temperature flue gas, sensible heat of the high-temperature flue gas rapidly transfers heat to carbonaceous solids in a fluidization mode, so that the carbonaceous solids rapidly carry out fluidization pyrolysis and activation with the upward high-temperature activator gas in the first hearth, after the reaction for a set residence time, the high-temperature carbonaceous particles enter the fluidized bed 51 in the working condition of the next hearth through a discharge pipe 17, are discharged into the fluidized bed 51 in the working condition of the next hearth through the discharge pipe 17 in the next hearth after the set fluidization activation time, finished active carbon is collected after being indirectly cooled through a cold material machine 7, large-particle-size carbonaceous particles which cannot be continuously fluidized and non-carbonaceous particles which are large in a similar manner are gradually moved to a bottom hearth slag zone 52, and the carbonaceous particles are discharged from the cyclone separator of the multi-hearth 12 to the upper hearth are recycled and discharged from the multi-hearth furnace 13 through the cyclone separator.

Part of the preheated air and steam uniformly enter a multi-hearth furnace bottom hearth from a bottom chassis 8 through a connected bottom gas hood 18-1 and enter a working condition fluidization layer 51, enter an upper-part hearth from bottom to top through a baffling hood 18 penetrating a hearth bottom plate 55, and enter a multi-hearth furnace from bottom to top through a pneumatic conveying medium inlet 10 and a top gas mixer 11, and are discharged from an upper-part hearth activated gas outlet of the multi-hearth furnace 5 after fluidized pyrolysis and activation reaction, enter a bag type dust collector 24 after heat exchange and cooling of an air preheater 21 and a steam superheater 23 after larger particles are removed through a cyclone separator 12, further collect fine powdery activated carbon, enter an incinerator 26 through a draught fan, activate tail gas and air burn and release heat, sequentially enter a mixed gas preheater 28, a steam waste heat boiler 29 and a coal economizer 32 for heat exchange, recover heat of high-temperature flue gas, and the cooled flue gas is discharged through a chimney 33 after desulfurization and purification;

the solid ash slag in the reaction process gradually descends into the ash slag zone 52 of the hearth at the bottom, and is periodically discharged from the slag cooler 19 through the slag outlet 19-1, so that the fluidized activation of each hearth is continuously carried out.

Further, the device also comprises a sub-cylinder 31 for respectively delivering saturated steam gas generated by the steam waste heat boiler to the mixed gas preheater 28, the steam superheater 23 and the air conveying medium inlet 10.

Further, the device also comprises a Roots blower 27, and after continuously mixing and preheating the air sent to the mixture preheater 28 and steam, the air sent to the bottom chassis 8 of the multi-hearth furnace enters the fluidized bed 51 of the working condition of the bottom hearth through the connected bottom air hood 18-1 to carry out fluidization activation reaction with carbonaceous particles.

Further, the device also comprises a secondary air blower 22, air is continuously sent to the air preheater 21 for preheating, then is sent to the annular air supplementing port 54 of the furnace wall of the multi-hearth furnace, oxygen in the air and the up-moved activated tail gas generate a gas/gas homogeneous phase exothermic reaction, and gas sensible heat of the activation endothermic reaction is provided for the upper-layer furnace working condition fluidization material layer 51.

Further, the apparatus also comprises a blower 25 for continuously supplying combustion air to the incinerator 26.

Further, the baffling hood uniformly arranged throughout the furnace bottom plate 55 has a special design structure, which not only ensures uniform gas distribution, but also prevents solid particles from blocking the gas pipeline, as shown in fig. 2.

The preparation method comprises the following steps:

Firstly, materials enter a feed pipe 9 from a feed bin 1 through a sealed spiral conveyor 2, and solids are pneumatically conveyed and uniformly enter a working condition fluidization material layer 51 of a first hearth of a multi-hearth furnace 5 through a distributor 14;

After the material enters the uppermost hearth working condition fluidization material layer 51, air enters the first hearth working condition fluidization material layer 51 of the multi-hearth furnace through the jacket type hood 15 by the top gas mixer 11, oxygen in the air and the upward moving activated tail gas generate gas/gas homogeneous exothermic reaction to form high-temperature flue gas, the high-temperature flue gas rapidly fluidizes and transfers heat to the carbonaceous solid, and simultaneously, the carbonaceous solid particles and the upward moving high-temperature activator generate activation reaction; the hearth is subjected to fluidization pyrolysis (after activation, high-temperature carbonaceous particles enter a second hearth working condition fluidization material layer 51 through a blanking pipe 17, are subjected to fluidization activation for a certain time, then are discharged into a bottom hearth working condition fluidization material layer 51 through the blanking pipe 17, are subjected to fluidization activation for a set residence time, are indirectly cooled through a cold material machine 7 and are collected into finished active carbon, non-carbonaceous particle impurities and large particles which cannot be continuously fluidized are sequentially dropped into a bottom hearth ash zone 52, are discharged out of a multi-hearth furnace through a slag discharge port 19-1 and are collected through a slag cooler 19, and carbonaceous particles separated by a cyclone separator 12 are circulated through a return pipe 13 and are returned to a upper part hearth of the multi-hearth furnace;

And thirdly, a part of preheated air and steam enter the bottom hearth working condition fluidization material layer 51 from the bottom chassis 8 through the connected bottom gas hood 18-1, the other part of preheated air and steam are uniformly fed in from the bottom and middle hearth furnace wall annular pipes, the other part of preheated air and steam are fed into the multi-hearth furnace first-layer hearth working condition fluidization material layer 51 from the pneumatic conveying medium inlet 10 and the gas mixer 11, the multi-hearth furnace first-layer furnace 5 furnace tail gas outlet is obtained after fluidized pyrolysis and activation reaction, bigger particles are removed through the cyclone separator 12, the preheated air and steam superheater 21 and the steam superheater 23 are gradually subjected to heat exchange and cooling, the preheated air and steam superheater 23 enter the bag-type dust collector 24 to further collect fine powder activated carbon, the fine powder activated carbon is then fed into the incinerator 26 through the induced draft fan, the activated tail gas and air are combusted and released, the heat of the high-temperature flue gas is recovered through heat exchange of the gas preheater 28, the steam waste heat boiler 29 and the economizer 32, and the cooled flue gas is discharged through the chimney 33 after desulfurization and purification.

The top is provided with a lower jacket type hood 15 which enters the top hearth working condition fluidization material layer 51 and is horizontally discharged, so that carbonaceous materials can be rapidly pyrolyzed and pre-oxidized, volatile matters in the carbonaceous materials and activated tail gas from the lower hearth are subjected to gas/gas combustion reaction with oxygen, heat is released, and preliminary fluidization activation reaction is carried out;

the secondary hot air and the preheated high-temperature steam of the two hearths at the lower part are uniformly fed in along the annular feeding port of the furnace wall of the hearth, the annular air feeding port 54 of the furnace wall is arranged below the annular steam feeding port 53, the oxygen in the hot air and the activated tail gas generate gas/gas homogeneous combustion reaction heat release, high-temperature flue gas is provided for the hearth at the upper part, and more gas activators are generated. The high-temperature steam can balance the temperature of the flue gas, ensure the concentration of the steam in the upper hearth and is favorable for the stable performance of the activation endothermic reaction.

The activation reaction is C+H ₂O→CO+H₂ (endothermic heat), C+CO ₂ →2CO (endothermic heat);

C+O ₂→CO₂ (exothermic), H ₂+1/2O₂→H₂ O (exothermic), CO+1/2O ₂→CO₂ (exothermic);

The inlet of the pneumatic conveying medium is high-temperature water vapor;

The high-temperature vapor is used as a part of activating agent and also used as a pneumatic conveying medium, and can preheat the entering solid particles, so that the high-efficiency energy-saving method is high in efficiency, the burst phenomenon caused by flash heating of the solid carbonaceous material can be prevented, the loss of fixed carbon is reduced, and the yield of the activated carbon is improved.

Example 3

As shown in fig. 4, in this embodiment, on the basis of embodiment 2, a high-temperature and high-pressure gas fan 34 is added, and other equipment flows are also changed, so that the working conditions of two hearths of a single carbonaceous raw material are as follows:

the material bin 1 is connected with the sealed spiral conveyor 2, the outlet of the sealed spiral conveyor 2 is connected with the feeding pipe 9, the feeding pipe 9 is connected with the jacket pipe type air cap 15 assembly through a flange and the multi-chamber furnace 5, the pipe type air cap 15 is inserted into the upper head working condition fluidization material layer 51 of the multi-chamber furnace 5, the standby material bin 3 is connected with the multi-chamber furnace 5 through the standby sealed spiral conveyor 4, the discharging pipe 6 extends out of a carbon layer of the multi-chamber furnace 5 and is connected with the cold material machine 7, the slag discharging pipe is connected with the bottom of the multi-chamber furnace 5, the pipeline of the slag outlet is connected with the slag cooler 19 and discharges slag in the furnace, the inlet of the cyclone 12 is connected with the outlet of the multi-chamber furnace 5, the lower part of the cyclone 12 is connected with the return pipe 13, the gas phase outlet of the cyclone 12 is connected with one end of the air preheater 21, the other end of the air preheater 21 is connected with the steam preheater 23, the other end of the steam preheater 23 is connected with the incinerator 26, the outlet of the incinerator 26 is connected with the inlet of the mixer preheater 28, the outlet of the mixer 28 is connected with the inlet of the waste heat steam boiler 29, the outlet of the waste heat boiler 29 is connected with the inlet of the air preheater 32, the inlet of the air preheater is connected with the inlet of the air preheater 24, the inlet of the air preheater is connected with the inlet of the air preheater 30, the inlet of the air preheater is connected with the inlet of the air preheater 30.

The device also comprises a distributor 14, a slag discharging pipe 16 and a feeding pipe 17.

The device also comprises a standby feed bin 3 and a standby sealing screw conveyor 4, so that the furnace is started to enter a high-temperature fluidization working condition and is stopped before the working condition is not entered;

The method comprises the following steps:

The single granular carbonaceous raw materials are firstly stored in a feed bin 1, are sent into a feed pipe 9 through a sealed spiral conveyor 2, are sent to a distributing device 14 under the action of gas conveyed by a pneumatic conveying medium inlet 10, uniformly fall into an upper hearth working condition fluidization material layer 51 of a multi-hearth furnace 5 under the action of the pressure of the gas and the gravity of the solid, and are pneumatically conveyed singly by adopting high-temperature activated tail gas as a conveying medium, wherein the high-temperature activated tail gas is provided by a high-temperature high-pressure gas 34 gas fan;

The side wall of the lower hearth of the circulating integrated furnace is provided with a furnace wall annular air supplementing port 54 for secondarily supplementing air and annular water vapor supplementing port 53 for uniformly supplementing an activating agent to the upper hearth fluidization layer, so as to keep the concentration of the activating agent in the activating reaction, oxygen in the air and the upward moving activated tail gas generate gas/gas homogeneous reaction heat release, the formed high-temperature gas flows through a baffling hood 18 penetrating through the hearth bottom plate and enters the upper hearth working condition fluidization layer 51 to provide energy for fluidization and activation endothermic reaction of upper carbonaceous particles, and the furnace wall annular air supplementing port 54 uniformly supplements preheated air to better control the material temperature of carbonaceous solid in the upper hearth working condition fluidization layer 51;

The high-temperature secondary air from the secondary blower 22 is uniformly fed in from an annular air feeding port 54 of the furnace wall of the lower furnace of the integrated furnace, the annular water vapor feeding port 53 of the furnace wall is uniformly fed in with high-temperature water vapor, oxygen in the air and the up-moved activated tail gas generate gas/gas homogeneous reaction heat release, and the annular uniform arrangement can better control the material temperature of the carbonaceous solid in the upper furnace working condition fluidization material layer 51;

The activated carbon particles enter the lower hearth working condition fluidization layer 51 to be deeply activated through the blanking pipe 17 under the action of a gas fluidization medium, high-temperature gas preheated through the jacket pipe type hood 15 is contacted with single granular carbonaceous raw materials in the upper working condition fluidization layer 51, wherein oxygen and hydrogen and carbon monoxide in the upward-moving activated tail gas generate gas/gas combustion reaction to emit heat, the formed high-temperature flue gas rapidly transfers heat to carbonaceous particles entering the upper hearth working condition fluidization layer 51 through fluidization, so that the carbonaceous solid particles are rapidly heated, continuous high-temperature gas sensible heat is provided for the activation and heat absorption reaction of the upper hearth working condition fluidization layer 51, the activation is continuously and stably carried out, the activated qualified activated carbon enters the cold material machine 7 to be indirectly cooled and collected as a product through the discharging pipe 6, the powdery carbonaceous particles slightly larger than the particles after the circulating fluidization activation reaction are subjected to gas-solid separation through the cyclone separator 12 and enter the returning pipe 13 to be rapidly transferred to the upper hearth of the multi-hearth working condition fluidization layer 51, and small-path dust is collected as a small-size dust collector in the small-path dust collector bag 24 after the activation of the particles are subjected to the follow-up dust removal treatment.

After the temperature of the air from the secondary air blower 22 is raised by the air preheater 21, a part of the air enters the lower hearth, and the other part of the air enters the gas mixer 11, after the air from the Roots blower 27 enters the mixed gas preheater 28 and the steam from the branch air cylinder 31 for mixed preheating, the air is sent to the multi-hearth furnace bottom gas cabinet 8, the air enters the working condition fluidized bed 51 of the lower hearth of the multi-hearth furnace through the connected bottom gas hood 18-1 for fluidization activation reaction, the air from the blower 25 enters the incinerator 26 as combustion air, the high-temperature high-pressure gas blower 34 sends the activated tail gas to the pneumatic conveying unit 10 for use as a gas conveying medium, after the steam from the branch air cylinder 31 is preheated by the steam preheater 23, a part of the steam is sent to the annular water vapor supplementing inlet 53 of the furnace wall of the lower hearth, and the other part of the steam is sent to the gas mixer 11;

The mixed gas of high-temperature preheated air and steam which is introduced into the hearth at the bottom of the circulating integrated furnace is used as a fluidization medium, so that carbonaceous solid particles in the furnace enter a fluidization state, a small part of oxygen in the air reacts with carbonaceous raw materials rapidly to release heat to provide reaction energy for deep activation endothermic reaction, meanwhile, the activation tail gas reacts with oxygen in secondary air to generate gas/gas homogeneous reaction to release heat, the temperature is kept stable and uniform, then high-temperature airflow rises to enter the upper hearth working condition fluidization material layer 51 through a baffling hood 18 penetrating through the hearth, on one hand, the mixed gas serves as a fluidization medium of the carbonaceous solid particles in the upper hearth working condition fluidization material layer 51, and meanwhile, sensible heat of high-temperature flue gas is provided for the upper working condition fluidization material layer 51 to serve as heat for fluidization activation endothermic reaction, so that continuous running of fluidization activation in the upper hearth working condition fluidization material layer 51 is kept. In the primary activation area of the upper furnace, high-temperature air and upward-moving activated tail gas are uniformly input from the jacket tubular hood 15 to generate gas/gas homogeneous combustion exothermic reaction, and as the activation reaction is endothermic, oxygen in the input air and gas/gas homogeneous exothermic reaction generated by combustible gas in the activated tail gas continuously provide energy for the rapid fluidization activation reaction of carbonaceous particles in the fluidized bed 51 under the upper furnace working condition:

the activated tail gas generated in the circulating multi-hearth integrated furnace carries a small amount of fine carbon particles, the activated tail gas firstly enters the cyclone separator 12, the larger-particle carbonaceous solid after gas-solid separation is returned to the upper hearth working condition fluidization material layer 51 through the material returning device 13, the tail gas enters the air preheater 21 and is cooled after heat exchange with air, then enters the steam preheater 23 and further exchanges heat and is cooled, then enters the incinerator 26 to burn and release heat to form high-temperature flue gas, the high-temperature flue gas enters the steam waste heat boiler 29 and water to exchange heat and cool, high-pressure saturated steam is generated at the same time, the cooled flue gas enters the economizer 32, the bag-type dust remover 24 to remove dust after further cooling, the solid dust formed by burning the small-particle carbon is removed, and then the flue gas is discharged through the chimney 33 after desulfurization and purification of the flue gas desulfurization system under the action of the induced draft fan 30.

Because the two hearths are adopted in the embodiment, the method is suitable for the working condition of single carbonaceous raw materials, the conveying medium can use the activated tail gas, and also can use water vapor, and the carbonaceous raw materials are rapidly fluidized, pyrolyzed and activated in the upper hearth. The method has the advantages of short activation time for single carbonaceous particle raw materials with good reactivity, easy operation, large-scale production, large productivity, low production and operation cost and good economy.

Example 4

As shown in fig. 5, this embodiment is a three-hearth activated co-production working condition of two different carbonaceous raw materials, and on the basis of embodiment 2, a feeding system is added to the lower hearth, so that activated carbon co-production can be realized for the carbonaceous raw materials with different components:

In comparison with example 2, a lower furnace silo 35, a lower furnace screw conveyor 36 and a second cold material machine 7-1 were added, and the bag house 24 was advanced and placed after the steam preheater 23 and before the incinerator 26.

The lower hearth bin 35 is connected with the lower hearth sealing type screw conveyor 36, the lower hearth sealing type screw conveyor 36 is connected with the side wall of the lower hearth of the multi-hearth furnace, and the other parts are the same as those in the embodiment 2;

The gas outlet of the multi-chamber furnace 5 is connected with the inlet of a cyclone separator 12, the lower part of the cyclone separator 12 is connected with a material returning device 13, the gas phase outlet of the cyclone separator 12 is connected with one end of an air preheater 21, the gas phase outlet pipeline of the cyclone separator 12 is connected with a standby high-temperature high-pressure gas fan 34 (standby) inlet, the other end of the air preheater 21 is connected with a steam superheater 23, the outlet of a secondary blower 22 is connected with one side of the air preheater 21 in a two-way mode, the other end of the steam superheater 23 is connected with the inlet of a bag type dust collector 24, the outlet of the bag type dust collector 24 is connected with the inlet of a draught fan 30, the outlet of the draught fan 30 is connected with the inlet of an incinerator 26, the outlet of the incinerator 26 is connected with the inlet of a mixed heat exchanger 28, the outlet of the mixed gas heat exchanger 28 is connected with the inlet of a steam waste heat boiler 29, one side of the mixed heat exchanger is connected with the outlet of a Roots blower 27, the outlet of the steam waste heat boiler 29 is connected with the inlet of a coal economizer 32, the steam outlet of the steam waste heat boiler 29 is connected with a coal dividing cylinder 31, the outlet of the economizer 32 is connected with the lower part of a chimney 33, and the treated qualified flue gas is discharged to the atmosphere.

The equipment principle and flow are that one of the carbonaceous raw materials a is firstly stored in a feed bin 1 and is sent into a feed pipe 9 through a sealed spiral conveyor 2, and is sent into an upper hearth working condition fluidization layer 51 under the action of a gas medium of a pneumatic conveying device 10, the other carbonaceous raw material b is stored in a lower hearth feed bin 35 and is sent into the lower hearth working condition fluidization layer 51 through a lower hearth sealed spiral conveyor 36, air from a secondary blower 22 is preheated in an air preheater 21 and then respectively enters a gas mixer 11, a middle hearth and a lower hearth annular air supplementing port 54, oxygen in the air and hydrogen and carbon monoxide in activated tail gas generate gas/gas heat release reaction, sensible heat of the formed high-temperature gas provides energy for activating and endothermic reaction for carbonaceous particles in the upper hearth and the middle hearth working condition fluidization layer 51, ash in the reaction moves into the middle hearth ash zone 52 from the upper hearth ash zone 52 through a lower hearth ash zone 16, and ash in the lower hearth ash zone 52 through a lower hearth tube 16, and is discharged through a slag cooler 19 after being moved into the lower hearth ash zone 52, and is discharged through a slag pipe 19 to be collected

The solid carbonaceous particles a flow into the middle hearth working condition fluidization layer 51 from the upper hearth through the blanking pipe 17 under the action of the gas fluidization medium along with the continuous progress of the reaction, then deep activation is carried out, activated carbon particles qualified in the middle hearth activation directly enter the second cold material machine 7-1 through the discharging pipe 6 and are collected and stored as products, powdery activated carbon carried by activated tail gas and having slightly larger particles is returned to the upper hearth through the return pipe 13 after being separated through the cyclone separator 12, and fine powdery activated carbon is collected in the bag type dust collector 24.

The air generated by the Roots blower 27 and the steam generated by the split cylinder 31 are mixed and then preheated in the mixer preheater 28, enter the gas cabinet 8, enter the lower hearth working condition fluidization material layer 51 through the connected bottom gas hood 18-1 to participate in fluidization activation reaction with the carbonaceous b raw material, and the activated carbon which is qualified in bottom hearth activation and is prepared from the carbonaceous b raw material is discharged from the multi-hearth furnace through the discharge pipe 6 of the bottom hearth and collected by the cold material machine 7;

The activated tail gas generated in the multi-hearth furnace carries a small amount of fine carbon particles, the activated tail gas firstly enters the cyclone separator 12, the carbonaceous raw material with larger particle size is returned to the fluidized bed 51 at the working condition of the upper hearth through the material returning device 13 for continuous fluidization and activation, the tail gas enters the air preheater 21 and is cooled after air heat exchange 21, then enters the steam superheater 23 for further heat exchange and cooling, then enters the bag-type dust collector 24 for collecting powdery activated carbon, then enters the mixed gas heat exchanger 28 after passing through the incinerator 26 under the action of the induced draft fan 30, enters the steam waste heat boiler 29 after preliminary cooling, then enters the economizer 32, and the cooled flue gas is purified to be qualified and then discharged to the atmosphere through the chimney 33.

The embodiment is suitable for co-production working conditions of two different carbonaceous raw materials, the lower hearth and the middle and upper hearths are used for producing the activated carbon prepared from the two carbonaceous raw materials, the lower hearth is independently pyrolyzed and activated to produce the activated carbon, and meanwhile, the middle and upper hearths are provided with fluidization medium, energy of activating endothermic reaction and high-temperature activating agent, so that the co-production of the activated carbon of the two different carbonaceous raw materials is realized, and the efficiency is high, the adjustment is flexible, and the energy consumption is low.

Example 5

As shown in fig. 6, the embodiment provides a working condition suitable for thermal regeneration of granular and powdery waste activated carbon and co-production of granular activated carbon on the basis of embodiment 4. The incinerator burner adopts a low-nitrogen combustion technology, a granular carbonaceous semicoke raw material is added into a bottom hearth to prepare active carbon, and the upper and middle hearths perform thermal regeneration of waste active carbon:

Specifically, the high-temperature high-pressure gas blower 34, a lower hearth stock bin 35, a lower hearth screw conveyor 36, a gas intercooler 37, a high-pressure gas blower 38 and a second material cooler 7-1

The storage bin 1 is connected with the sealed spiral conveyor 2, and the outlet of the sealed spiral conveyor 2 is connected with the feeding pipe 9; the spare bin 3 is connected with the upper hearth of the multi-hearth furnace 5 through the spare sealed screw conveyor 4, the lower hearth bin 35 is connected with the lower hearth of the multi-hearth furnace 5 through the lower hearth sealed screw conveyor 36, the inlet of the cyclone separator 12 is connected with the upper hearth activated tail gas outlet of the multi-hearth furnace 5, the gas phase outlet of the cyclone separator 12 is connected with the inlet of the air preheater 21, the lower part of the cyclone separator 12 is connected with the water vapor return device 13, the outlet of the return device 13 is connected with the middle hearth of the multi-hearth furnace 5, a high-temperature high-pressure gas fan 34 is arranged on the gas phase outlet pipeline of the cyclone separator 12, the outlet of the air preheater 21 is connected with the inlet of the steam superheater 23, the side surface of the air preheater 21 is connected with the outlet of the air fan 22, the outlet of the steam superheater 23 is connected with the inlet of the bag-type dust collector 24, the outlet of the bag-type dust collector 24 is connected with the inlet of the first induced fan 30-1, the outlet of the first induced fan 30-1 is connected with the inlet of the gas inter-cooler 37, the outlet of the gas inter-gas cooler 37 is connected with the inlet of the incinerator 26, one side of the inter-gas cooler 37 is connected with the inlet of the high-pressure gas fan 38, the inlet of the incinerator 26 is connected with the inlet of the incinerator 25, the outlet of the air preheater 26 is connected with the outlet of the air preheater 26 and the outlet of the air preheater 29-gas preheater 29, the air preheater is connected with the inlet of the air preheater 29-gas heater and the air preheater 2, the inlet of the air preheater is connected with the inlet of the air preheater 2, the inlet of the exhaust gas separator is connected with the inlet of the exhaust outlet of the exhaust gas separator, the exhaust outlet of the exhaust gas separator is connected with the exhaust gas outlet of the exhaust gas separator and the exhaust outlet is connected with the exhaust outlet of the exhaust gas separator and the exhaust gas separator.

The waste activated carbon is firstly stored in a storage bin 1, is sent into a feed pipe 9 through a sealed spiral conveyor 2, uniformly falls into a working condition fluidization material layer 51 of a multi-hearth furnace 5 under the action of gas medium of a pneumatic conveying unit 10 and the action of solid gravity, high-temperature carbon particles after preliminary activation enter the middle hearth working condition fluidization material layer 51 through a blanking pipe 17 of a first-layer hearth, and undergo deep activation reaction with hot flue gas and steam from a lower hearth, ash enters a middle hearth ash region 52 from an upper hearth ash region 52 through a lower slag pipe 16, enters a bottom hearth slag region 52 again through a middle hearth lower slag pipe 16, is discharged from the bottom hearth slag region 52 and is collected through a slag cooler 19; the waste activated carbon particles are discharged out of the multi-hearth furnace through a second cold material machine 7-1 after being deeply activated and regenerated in a middle hearth and are collected and stored in a second cold material machine 7-1, semicoke is firstly stored in a lower stock bin 35, is sent into a lower hearth working condition fluidization material layer 51 through a lower sealed screw conveyor 36, mixed gas from a mixed gas preheater 28 enters a lower machine box 8, then enters the lower hearth working condition fluidization material layer 51 through a connected bottom gas hood 18-1 to carry out fluidization and activation reaction with semicoke, and simultaneously, activated tail gas is provided in the middle hearth and upper hearth working condition fluidization material layer 51 as heat and high-temperature activating agent for thermal regeneration of the waste activated carbon, activated qualified granular activated carbon is sent out of the lower hearth of the multi-hearth furnace through a discharging pipe 6 and is collected and stored in the cold material machine 7, and powdery activated carbon qualified in thermal regeneration is collected through a bag-type dust collector 24 along with a gas flow after passing through a cyclone separator.

The subsequent flow setting of the embodiment 5 is basically the same as that of the first few embodiments, compared with the traditional activation process, the embodiment 5 has no particle size requirement on the waste activated carbon, the granular waste activated carbon and the powdery waste activated carbon can be thermally regenerated and simultaneously are prepared for co-production with the activated carbon, the invention does not need to consume fuel gas additionally during the thermal regeneration of the activated carbon, is an energy-saving technology and method, the burner of the incinerator adopts a low-nitrogen combustion technology, has low pollution and is environment-friendly, the lower hearth can adopt the granular carbonaceous semicoke raw material to prepare the activated carbon, the co-production of the activated carbon preparation and the waste activated carbon thermal regeneration is realized, and the invention belongs to the technology and method with multiple purposes, flexible operation, good economy and environment friendliness.

Example 6

As shown in FIG. 7, in this embodiment, on the basis of embodiment 2, burners are added, the ring-shaped burner is uniformly arranged on the side wall of the lower hearth, the lower hearth is not fed and is only used as a high-temperature gas mixing chamber, high-temperature hot flue gas and a high-temperature activating agent are provided for the fluidized bed of the middle and upper hearths, a gas intercooler and the like are added, an incinerator, a steam superheater and the like are omitted, and the equipment flow combination is also partially changed, specifically as follows:

Comprises a stock bin 1, a sealing screw conveyor 2, a standby stock bin 3, a standby sealing screw conveyor 4, a multi-hearth furnace 5, a discharging pipe 6, a cold material machine 7, a gas cabinet 8, a feeding pipe 9, a pneumatic conveying medium inlet 10, a cyclone separator 12, a steam material returning device 13, a distributing device 14, a jacket type hood 15, a slag discharging pipe 16, a discharging pipe 17, 18 baffling hood, a bottom gas hood 18-1, a slag cooling machine 19, a mixer 20, an air preheater 21, a Roots blower 27, a waste heat steam boiler 29, an induced draft fan 30, a split cylinder 31, a gas inter-cooler 37, a gas high-pressure blower 38 and uniformly arranged burner 39 of a bottom hearth.

The material bin 1 is connected with the sealed spiral conveyor 2, the outlet of the sealed spiral conveyor 2 is connected with the feed pipe 9, the feed pipe 9 is connected with the jacket pipe type hood 15 assembly and the multi-hearth furnace 5, the pipe type hood 15 is inserted into a first-layer hearth working condition fluidization material layer 51 of the multi-hearth furnace 5, the standby material bin 3 is connected with an upper hearth of the multi-hearth furnace 5 through the sealed spiral conveyor 4, the discharge pipe 6 penetrates through a high-temperature gas mixing chamber at the bottom of the multi-hearth furnace 5 and then is connected with the cold material machine 7, the middle hearth slag discharging pipe 16 penetrates through a high-temperature gas mixing chamber at the bottom of the multi-hearth furnace 5 and is connected with the cold slag machine 19 through a pipeline, and slag in the furnace is collected after being cooled by the cold slag machine 19;

The cyclone separator 12 is connected with an activated tail gas outlet of the multi-hearth furnace 5, the lower part of the cyclone separator 12 is connected with a steam returning device 13, an outlet of the returning device 13 is connected with an upper hearth of the multi-hearth furnace, a gas phase outlet of the cyclone separator 12 is connected with an inlet of an air preheater 21, an outlet of the air preheater 21 is connected with an inlet of a waste heat steam boiler 29, one side of the air preheater 21 is connected with an outlet of a Roots blower 27, an outlet of the waste heat steam boiler 29 is connected with an inlet of a bag-type dust collector 24, one side of the steam waste heat boiler 29 is connected with an inlet of a split cylinder 31, an outlet of the bag-type dust collector 24 is connected with an inlet of an induced draft fan 30, an outlet of the induced fan 30 is connected with an inlet of a gas intercooler 37, an outlet of the gas intercooler 37 is connected with an inlet of a gas high-pressure blower 38, an outlet of the gas intercooler 37 is connected with a main pipeline of an activated tail gas conveying system, an outlet of the gas high-pressure blower 38 is connected with an inlet of a burner 39, and a high-temperature flue gas outlet of the burner 39 is evenly distributed in a ring shape is connected with a side wall of a lower hearth of the multi-hearth.

The difference between the embodiment and the embodiment 2 is that a three-hearth structure is adopted, the lower hearth is not fed with carbonaceous raw materials, the lower hearth is only used as a high-temperature gas mixing chamber, the self-produced activated tail gas is matched with preheated air, the preheated air is fed into a burner which is uniformly installed in a circumferential direction for burning to form high-temperature flue gas, the high-temperature flue gas is fed into the lower hearth-high-temperature flue gas mixing chamber in a high-temperature flue gas mode, high-temperature steam from a bottom chassis is mixed to form high-temperature mixed gas, the mixed gas is used as a gas fluidization medium, and the sensible heat of the gas of the high-temperature flue gas is the heat of fluidization activation endothermic reaction of the carbonaceous raw materials in the middle and upper hearth fluidization material layers, and simultaneously, high-temperature carbon dioxide and high-temperature steam are provided for the carbonaceous raw materials of the upper middle two hearth fluidization material layers as gas activators.

Because the three hearths are adopted in the embodiment, the hearth at the bottom is used as a mixing chamber of high-temperature mixed gas, carbonaceous raw materials in the fluidized bed of the two hearths at the upper part can form a stable fluidized state and can be subjected to fluidized pyrolysis and activation reaction step by step stably, the reaction is uniform and full, the mixing of carbonaceous solid particles is reduced, the invalid burning loss of fixed carbon is avoided, the yield of the fixed carbon is improved, the use efficiency of an activating agent is improved, the productivity is higher, the production cost is low, the economy is good, the product quality is stable, and the quality is good.

Example 7

As shown in FIG. 8, the embodiment is based on the embodiment 6, the middle hearth is omitted, a two-hearth mode is adopted, a mixed gas bottom case is omitted, a gas case is additionally arranged, the lower hearth is still a high-temperature gas mixing chamber, only one activation hearth is arranged at the upper part, a return pipe is omitted, and a powder activated carbon collection tank is added, and the method specifically comprises the following steps:

Comprises a stock bin 1, a sealing screw conveyor 2, a standby stock bin 3, a standby sealing screw conveyor 4, a multi-hearth furnace 5, a discharging pipe 6, a cold material machine 7, a feeding pipe 9, a first pneumatic conveying medium inlet 10-1, a second pneumatic conveying medium inlet 10-2, a first mixer 11-1, a second mixer 11-2, a cyclone separator 12, a distributing device 14, a jacket type hood 15, a baffled hood 18, a slag cooling machine 19, an air preheater 21, a secondary air blower 22, a Roots blower 27, a waste heat steam boiler 29, an induced draft fan 30, a split cylinder 31, a high-temperature high-pressure gas blower 34, a gas intercooler 37, a high-pressure gas blower 38, a burner 39, a bellows 40, a gas cabinet 41 and a powder collecting tank 42.

The material bin 1 is connected with the sealed spiral conveyor 2, the outlet of the sealed spiral conveyor 2 is connected with the feed pipe 9, the feed pipe 9 is connected with the jacket pipe type hood 15 assembly and the multi-hearth furnace 5, the pipe type hood 15 is inserted into the upper hearth working condition fluidization material layer 51 of the multi-hearth furnace 5, the standby material bin 3 is connected with the upper hearth of the multi-hearth furnace 5 through the sealed spiral conveyor 4, the discharge pipe 6 penetrates through the hearth of the high-temperature gas mixing chamber at the bottom of the multi-hearth furnace 5 to extend out of the furnace to be connected with the cold material machine 7, the slag discharging pipe 16 is connected with the slag area 52 at the bottom of the upper hearth in the multi-hearth furnace 5, and the pipeline of the slag outlet penetrates through the high-temperature gas mixing chamber at the bottom to be connected with the cold slag machine 19 to discharge slag in the furnace;

The inlet of the cyclone separator 12 is connected with the activated tail gas outlet of the multi-hearth furnace 5, and the lower part of the cyclone separator 12 is connected with the powder collecting tank 42; the cyclone separator 12 is connected with the gas phase outlet of the air preheater 21, the upper pipeline is connected with the inlet of the high-temperature high-pressure gas fan 34, the outlet of the high-temperature high-pressure gas fan 34 is connected with the inlet of the second pneumatic conveying medium 10-2, the outlet of the air preheater 21 is connected with the outlet of the secondary air fan 22, one side of the air preheater 21 is connected with the outlet of the first mixer 11-1 and the second mixer 11-2, the other side of the air preheater 21 is connected with the outlet of the steam exhaust fan 29 and the inlet of the bag type dust collector 24, one side of the steam exhaust fan 29 is connected with the inlet of the split cylinder 31, the outlet of the split cylinder 31 is connected with the inlet of the second conveying medium 10-2, the inlet of the first mixer 11-1 and the inlet of the second mixer 11-2 respectively, the outlet of the bag type dust collector 24 is connected with the inlet of the induced draft fan 30, the outlet of the induced fan 30 is connected with the inlet of the gas intercooler 37, the outlet of the gas intercooler 37 is connected with the inlet of the high-pressure fan 38, the outlet of the main pipeline of the gas intercooler 37 is connected with the outlet of the activated tail gas system, the outlet of the gas high-pressure fan 38 is connected with one side of the gas chassis 41, the other side of the gas chassis 41 is connected with the outlet of the gas chassis 41, the multiple outlets 39 are respectively connected with the outlets of the air boxes 39 respectively, the nozzles 39 are connected with the inlets 39 through the burner nozzles and the burner nozzles 39 are connected to the lower side of the burner ring and the burner nozzles.

The embodiment adopts a two-hearth structure, respectively adopts high-pressure coal gas and water vapor as conveying media, adopts a mixture of two groups of high-temperature water vapor and air to be uniformly injected into a fluidized carbonaceous material layer 51 through a jacket pipe type hood 15 by a mixer, improves the fluidization pyrolysis and activation efficiency of an upper hearth, is beneficial to the stable progress of an activation reaction, cancels a bottom case, and allows smoke to enter a high-temperature mixing chamber from annularly and uniformly distributed burners to provide enough heat and fluidization activation media for the upper hearth, so that stable high-temperature smoke is formed for the stable combustion of the burners, and adopts a gas case form by a fuel gas system and a bellows form by an air system.

The fuel gas is preferably self-produced activated tail gas or externally supplied fuel gas, the Roots blower distributes air to each burner through the bellows, the air and the high-temperature activated tail gas are subjected to combustion exothermic reaction through the burners to generate high-temperature combustion flue gas, the high-temperature combustion flue gas uniformly enters the working condition fluidization material layer 51 from the lower hearth through the baffling hood 18 penetrating through the upper hearth, and on one hand, the high-temperature combustion flue gas serves as a gas fluidization medium of the carbonaceous raw material, and on the other hand, heat and an activating agent are provided for fluidization pyrolysis and activation endothermic reaction of the carbonaceous raw material.

According to the embodiment, through the design of the two hearths, high-temperature flue gas is generated in the hearth at the bottom, high-temperature gas fluidization medium and energy are provided for the hearth at the upper part, so that the fluidized pyrolysis and activation can be continuously and stably carried out on the hearth at the upper part, the structure is simple, the invalid burning loss of fixed carbon is reduced, the economy is good, and the unit volume yield is high.

While the invention has been described in detail in the foregoing general description and specific examples, it will be apparent to those skilled in the art that modifications and improvements can be made thereto. Accordingly, such modifications or improvements may be made without departing from the spirit of the invention and are intended to be within the scope of the invention as claimed.

Claims

1. A multi-hearth circulating fluidized activation integrated furnace apparatus for physically preparing activated carbon, the apparatus comprising:

The device comprises a sealed screw conveyor, a feed pipe, a baffling type hood, a pneumatic conveying medium inlet, a distributing device, a blanking pipe, a discharging pipe, a cold material machine, a top gas mixer, a cyclone separator, a material returning device, a slag discharging pipe, a gas machine box, a bottom gas hood and a slag cooling machine;

After the fluidization and activation of the preset residence time, high Wen Tanzhi solid enters the next layer of hearth through a blanking pipe penetrating through the hearth to carry out deep fluidization and activation, and finally qualified high-temperature activated carbon particles are discharged out of the furnace body through a discharging pipe and enter a cold material machine to be indirectly cooled and collected;

the bottom high-temperature mixed gas enters a fluidized bed of the multi-hearth furnace under the working condition of the bottommost hearth through a bottom gas hood from a gas cabinet, and is used as a gas fluidization medium on one hand, and meanwhile, high-temperature steam is used as a gas activator;

the waste residue moves into a next-layer hearth slag zone through a slag discharging pipe penetrating through the hearth bottom plate until being discharged from a bottom hearth slag zone to a furnace body and collected by a slag cooler;

The activated tail gas enters a cyclone separator from an upper hearth to separate carbonaceous solids and gas, and the gas enters subsequent treatment;

The multi-hearth furnace is characterized in that each hearth is also provided with an ash zone and a working condition fluidization layer, each hearth ash zone is connected through a slag discharging pipe penetrating through a hearth bottom plate, waste slag moves downwards from the upper hearth ash zone through a slag discharging pipe to enter the next hearth ash zone under the action of self gravity until a bottom movable discharge furnace body is collected through a slag cooler;

the device also comprises a baffling type hood penetrating through the bottom plate of the hearth and a jacketed tubular hood inserted into the fluidized bed of the first-layer hearth from the top, wherein the jacketed tubular hood uniformly supplies air for fluidization and activation of the first-layer hearth, and high-temperature gas flow among the hearths enters the upper-layer carbonaceous particle solid fluidized bed from the bottommost hearth from the baffling type hood in sequence, passes through the bed, and enters the fluidized bed of the hearth from the baffling type hood of the upper-layer hearth again until being discharged from the uppermost hearth.

2. The multi-hearth circulating fluidization and activation integrated furnace device for preparing active carbon by a physical method according to claim 1 is characterized by further comprising a standby storage bin and a standby sealing screw conveyor, wherein before feeding, carbonaceous materials in the standby storage bin enter the device through the standby sealing screw conveyor, and the starting device enters a fluidization material layer under a high-temperature working condition.

3. The multi-hearth circulating fluidized activation integrated furnace device for preparing activated carbon by a physical method according to claim 2, further comprising a furnace wall annular steam supplementing port and a furnace wall annular air supplementing port, wherein the furnace wall annular steam supplementing port uniformly supplements water vapor, and the furnace wall annular air supplementing port uniformly supplements air.

4. A multi-hearth circulating fluidized activation integrated furnace apparatus for physically producing activated carbon according to claim 3, wherein in the same layer of furnace, the lower end of the upper layer furnace discharging pipe is lower than the upper end of the same layer furnace discharging pipe.

5. The multi-hearth circulating fluidized activation integrated furnace device for preparing active carbon by a physical method according to claim 4 is characterized in that in the device, the upper ends of lower slag pipes of each layer of hearth are leveled with the bottom of the hearth, the lower ends of the lower slag pipes are immersed into ash slag areas of the next layer of hearth, slag area heights are arranged according to the furnace wall edges of horizontal air outlets of a baffling hood and slag holes at the bottom to form slag discharge repose angles, the horizontal dip angle is larger than 45 degrees, the number of the lower slag pipes of each layer exceeds 4 for smooth discharging and slag discharge, the circumferences of the lower slag pipes of each layer are uniformly arranged, and more than 2 discharge pipes of each layer are uniformly arranged.

6. The multi-hearth circulating fluidized activation integrated furnace device for preparing active carbon by a physical method according to claim 5 is characterized in that a distributor is arranged below a fluidized bed under the working condition of a first hearth, the bottom outlet of an upper discharging pipe is immersed in the fluidized bed under the working condition, and the horizontal height of the upper discharging pipe is lower than the discharging height of the lower discharging pipe.

7. A method for physically producing activated carbon, the method comprising:

step one, before feeding, materials in a standby bin enter a device through a standby sealing screw conveyor, and a starting device enters a high-temperature working condition fluidization material layer;

After the device is started, materials enter a distributing device from a feed bin through a feed pipe and then uniformly enter a first layer of hearth, uniformly fall into a first layer of hearth working condition fluidization material layer of a multi-hearth circulating fluidization and activation integrated furnace under the action of gas pressure and solid gravity, after the first layer of hearth is subjected to fluidization and activation for a set residence time, high-temperature carbonaceous particles flow into a next layer of hearth working condition fluidization material layer through a discharging pipe to perform further deep fluidization and activation, the specific surface area of the particles is increased, the pore volume is increased, the specific gravity is gradually reduced, and under the fluidization working condition, the high Wen Tanzhi particles gradually flow out from the hearth to a lower hearth material layer through the discharging pipe under the action of gas fluidization medium and gravity until the high Wen Tanzhi particles are discharged from the integrated furnace body through a discharging pipe to indirectly cool and collect the materials through a cold material machine;

step three, solid waste which cannot be fluidized enters an ash residue area, enters the ash residue area of the next layer of hearth through a slag discharging pipe, and is discharged out of the furnace through a slag cooler until being collected;

Step four, the small-particle-size granular carbonaceous solid and the activated tail gas enter a cyclone separator, the solid and the gas are separated, and the gas enters subsequent treatment; the solid is returned to the multi-hearth furnace through the steam returning device to be continuously fluidized and activated, and the powdery active carbon which is qualified in activation and has smaller particle size is collected through the bag-type dust collector after being indirectly cooled along with high-temperature airflow;

And fifthly, the bottom high-temperature mixed gas enters a fluidized bed of the bottommost hearth of the multi-hearth furnace from a gas cabinet through a bottom gas hood, and when the bottom high-temperature mixed gas serves as a fluidizing medium, water vapor is used as an activating agent to participate in a fluidization activation reaction, high-temperature activating agent gas is provided for the upper hearth by the water vapor which is not completely decomposed, the water vapor and the air are uniformly supplemented through a furnace wall annular water vapor supplementing port and a furnace wall annular air supplementing port, the concentration of the upper hearth water vapor activating agent is kept by supplementing the water vapor, oxygen in the supplemented air and the upward-moving activating gas generate gas/gas exothermic reaction, high-temperature gas rich in water vapor and carbon dioxide is formed after the oxygen in the supplemented air and the upward-moving activating gas flow through a baffling hood penetrating through a hearth bottom plate, and enters the upper laminar chemical material layer from the lower layer, gas sensible heat and activating agent gas are provided for the upper laminar material activating material layer, and the continuous stable progress of the activation endothermic reaction is kept until the high-temperature gas flows enter a cyclone separator from the uppermost hearth to be discharged into a subsequent treatment process.

8. The method of claim 7, wherein the activator gas is steam and carbon dioxide.