JPH01122913A - Production of active carbon and apparatus therefor - Google Patents

Abstract

PURPOSE:To obtain homogeneous high-quality active carbon, by carrying out heating of a fluidized bed with radiant heat from a combustion radiation region and heat transfer of heating tubes in the fluidized bed in producing the active carbon by activating a carbonaceous solid material with steam using the fluidized bed. CONSTITUTION:Steam 16 is overheated at a desired temperature with a steam heater 4 to produce overheated steam 17, which is then jetted from a distributor 15 into a fluidized activation chamber 7 to fluidize a carbonaceous solid raw material contained therein and form a fluidized bed. A volatile gas is generated from the carbonaceous solid raw material by heating the fluidized bed and water gas is simultaneously produced by reaction of the carbonaceous solid raw material with the overheated steam for forming the water gas to produce active carbon. Furthermore, the above-mentioned produced gas is made to flow into a combustion radiation chamber 8, mixed with oxygen (containing gas) 20 and burned to heat the fluidized bed with radiant heat of the combustion gas. The obtained combustion gas 23 is then introduced into heating tubes 11 to heat the fluidized bed through the tube walls.

Description

[Detailed description of the invention] [Industrial use! lIF]

The present invention relates to a method and apparatus for producing activated carbon by activating a carbonaceous solid raw material with steam.

[Prior art and its problems]

Conventionally, as a method for producing activated carbon by activating the carbonaceous solid source T1 with steam, combustion gas as a high-temperature heating medium is mixed with steam, and this high-temperature mixed gas is heated to a A direct heating method is generally used to produce activated carbon through a water gasification reaction using a carbonaceous solid raw material and water vapor, and a rotary kiln method, multistage furnace method, or fluidized bed method is used. All of these methods have drawbacks such as a decrease in the quality of the activated carbon obtained and a decrease in yield because the carbonaceous solid raw material is acidified by the oxygen contained in the combustion gas. In addition, in the water gasification reaction, the water vapor is boxed with 3"t gas and the water vapor partial pressure is lowered, so the reaction rate is low and the reaction time is long 1. Generally, the reaction time is a rotary kiln method. 〉Multi-stage furnace method〉Fluidized bed method.Furthermore, since the high-temperature combustion gas is prepared by combustion of fuel supplied from outside, fuel costs account for a large portion of the activated carbon production cost, and Since the construction cost of activated carbon VJ manufacturing equipment is high, the depreciation cost is also high, and the activated carbon wIJ manufacturing cost is high.These shortcomings have been actively improved to produce high-quality activated carbon with a good yield < wIJ3fi L, comparison Patent No. 1028105 describes a method and device for producing activated carbon that has high productivity with simple equipment, good thermal efficiency, and low fuel consumption.
It has been proposed as a number. To describe this proposed technology in 3T terms, the volatile gas and water gas from the fluidized bed are combusted in a combustion radiation chamber connected to the upper part of the fluidized activation chamber, and the fluidized bed is heated by the radiant heat of this combustion gas. , promotes the water gasification reaction of carbonaceous solid raw material and superheated steam as a fluid medium,
It is possible to produce high-quality activated carbon at a high yield and ripening efficiency, and after the operation of the activated carbon production equipment reaches a steady state, it is possible to produce activated carbon without supplying fuel from outside, and it is relatively simple. This provided a technology for producing activated carbon with a high reaction rate, high productivity, and good economic efficiency. However, according to the research of the present invention, the water gasification reaction of the carbonaceous solid raw material and superheated steam is an endothermic reaction, and the necessary heat is produced by the radiant heat of the combustion gas in the combustion radiant chamber. Since the energy is supplied by heating, the upper part of the fluidized bed is at a higher temperature than the lower part of the fluidized bed, resulting in a large temperature distribution in the downward direction of the fluidized bed. It was found that the quality of the fluidized bed was different, the quality was uneven, and the height of the fluidized bed could not be increased. In addition, if the upper part of the fluidized bed on the heat receiving surface becomes high temperature, it will inevitably be inside the combustion radiation chamber, and the combustion radiation chamber needs to be heat resistant to higher temperatures.
It has also been found that during actual operation, the refractory may melt and cause damage. Furthermore, it has been found that the extremely high temperature of the combustion gas causes a problem in the heat resistance of the steam superheater connected to the combustion gas outlet, and that troubles such as thermal damage often occur.

DISCLOSURE OF THE INVENTION 1 The purpose of the present invention is to produce activated carbon in which a carbonaceous solid raw material is activated with steam using a fluidized bed under a high partial pressure of steam. It is an object of the present invention to provide a method and apparatus capable of obtaining extremely uniform and high quality activated carbon at a high yield by heating by heat transfer through heating tubes within the fluidized bed and making the temperature distribution within the fluidized bed uniform. Another object of the present invention is to lower the combustion gas temperature in the combustion 9f1 radiation chamber by using multiple heating sources for the fluidized bed.
The purpose is to prevent troubles caused by thermal damage to activated carbon production equipment without generating extremely high temperatures. Still another object of the present invention is to provide a method for producing activated carbon that uses relatively simple equipment, has high productivity, has good thermal efficiency, and consumes very little fuel. Note that the carbonaceous solid raw material here is a solid raw material that can be converted into activated carbon by activation with water vapor, and examples of this carbonaceous solid raw material include coal, lignite, lignite, peat, pitch, and coconut shell. , rice husk, peanut husk, berm shell, wood chips, saw M, etc. The above object is achieved by the following technique. That is, the present invention forms a fluidized bed by fluidizing a carbonaceous solid raw material with an air flow of superheated steam in a fluidized activation region, generates volatile gas from the carbonaceous solid raw material by heating this fluidized bed, and In a method for producing activated carbon by generating water gas through a water gasification reaction between a solid raw material and superheated steam, carbon such as the volatile gas and the water gas is present in a combustion radiation region extending above the fluidized activation region. The produced gas from the solid solid raw material is injected and oxygen or oxygen-containing gas is introduced and combusted, and the fluidized bed is heated by the radiant heat of the combustion gas generated thereby, and the combustion gas is sent to the pipes installed in the fluidized bed. The present invention provides a method for producing activated carbon in which a fluidized bed is heated by heat transfer through the tube wall. In the combustion of produced gas from carbonaceous solid materials such as volatile gas and water gas in the combustion radiation region, the amount of combustion of the produced gas is adjusted by adjusting the amount of oxygen or oxygen Kurayoshi gas, and the temperature of the combustion radiation region is The secondary combustion chamber communicates with a tube in one wall of the fluidized activation chamber, which has an internal space for adjusting the heating plate to the fluidized bed by the radiant heat of the combustion gas, and also for forming a fluidized bed. The flammable gas in the combustion gas is combusted by introducing oxygen or oxygen-containing gas into the tube, and by adjusting the temperature of the combustion gas introduced into the tube, it is possible to create a fluidized bed by heat transfer through the tube. For example, some of the produced gases such as volatile gas and water gas from the flow activation region and near the E end to the carbonaceous solid raw material can be directly supplied to the carbonaceous solid raw material without passing through the combustion radiation region.
By controlling the temperature of the combustion gas introduced into the next combustion chamber, oxygen or oxygen-containing gas is introduced and combusted, and the combustion gas is merged with the combustion gas from the combustion radiation area and introduced into the tube, heat transfer through the tube is achieved. The fluidized bed is preferably heated to a temperature of about 800 to 1100°C, and the combustion gas is heated to a temperature of about 1300 to 155°C.
The combustion gas introduced into the pipe may have a temperature of about 1300-1650°C, and the superheated steam may have a temperature of about 500-900°C. is fed into the flow activation region at a rate of about 1.3 to 2.5 g/bicarbonaceous hardwood feedstock, and the combustion radiation ff[J! The oxygen or oxygen-containing gas fed into the secondary combustion chamber should be approximately 0.4 to 1.58 m'/K[r 2.11 m'/K of the carbonaceous solid feedstock. It will be done! The di- or oxygen-containing gas should be in a proportion of approximately 0.1 to 0.88 + l'/ of the bicarbonaceous solid feedstock, and the oxygen or The contained gas is preheated to about 300-800°C, and the superheated steam is heated by the combustion exhaust gas discharged from the pipe:
Il made by A is also preheated! *Element or 1I
f2″J: The contained gas may be heated by the combustion exhaust gas discharged from the pipe: IIMm, and in addition to the combustion of the product gas from the carbonaceous solid feedstock, another auxiliary fuel may be added to the combustion radiant region. In addition to the combustion of the produced gas from the carbonaceous solid feedstock, another auxiliary fuel may be used as a secondary combustion tn
It is preferable to burn it in a chamber. Such a method includes a fluidization activation chamber having, for example, a rectangular or elliptical planar cross section and having an internal space for forming a fluidized bed, and a carbonaceous solid raw material supply port on one of the short sides, for example. , an activated carbon VJ production device having an activated carbon recovery port on the other short side, a superheated steam spout formed at the bottom, and a distributor disposed on one side for rectifying the flow of the superheated steam. A secondary combustion chamber and a combustion gas collection chamber are provided, for example, in both long side walls of the flow activation chamber, and the flow activation chamber is connected between the secondary combustion chambers and between the secondary combustion chamber and the combustion gas aeration chamber. For example, a horizontal pipe is provided in the combustion chamber, one or more combustion gas inlets, an oxygen or oxygen-containing gas inlet, and a combustible gas inlet 11 are provided in one side of the secondary combustion chamber, and the The other side of the secondary combustion chamber is provided with one or more oxygen or oxygen-containing gas inlet and a combustible gas inlet, the combustion gas collecting chamber is provided with one or more combustion gas outlet, and the combustion gas collecting chamber is provided with one or more combustion gas outlet; One side of the activation chamber is open toward one side, and a combustion radiation chamber for generating combustion gas is provided above the flow activation chamber. connected to the internal space of the combustion chamber at its open upper end face, and the combustion chamber is provided with one or more oxygen or oxygen-containing gas inlets and a twisted gas outlet; Activated carbon production in which one or more combustible gas extraction ports are installed near the two ends of the "n-directional flow activation chamber" and one or more vertical partition walls (E) are arranged in the flow activation chamber. It can be carried out by a device. In the present invention, heating of the fluidized bed is performed by radiant heat from the combustion radiant chamber and heating by heat transfer from the tubes within the fluidized bed, and in both cases, the amount of combustible gas burned is small! 11
It is possible to adjust the heating time by the first section, and it is therefore possible to make the fluidized bed temperature, especially the temperature in the vertical direction, uniform, so that the water gasification reaction can be made uniform, and the water vapor partial pressure can be made uniform. This results in a water-based gasification reaction with high efficiencies, and extremely high-quality activated carbon can be obtained with uniform quality. In addition, compared to the case where the fluidized bed is heated only by radiant heat from the combustion radiant chamber, heat transfer from the tubes is also added, so even if the amount of radiant heat is small, the temperature of the combustion radiant chamber can be lowered. Therefore, thermal damage to the refractories in the combustion radiation chamber can be significantly reduced, and maintenance of the equipment is easy and economical. Furthermore, the oxygen or oxygen-containing gas fed into the combustion radiation chamber burns volatile gas and water gas in the combustion radiation chamber, and the resulting combustion gas has a higher temperature than the fluidized bed and therefore has a smaller amount of combustion. By providing a gas outlet at the top of the combustion radiation chamber, combustion gas can enter the flow activation chamber,
There is virtually no mixing with the fluidized bed, and the combustion gas in the pipes within the fluidized bed does not come into direct contact with the fluidized bed, so the carbonaceous solid material within the fluidized bed is in an atmosphere with a high water vapor partial pressure. It can flow and perform a uniform water gasification reaction,
Uniform, high-quality activated carbon can be produced with good yield. Further, the planar cross section of the flow activation chamber is rectangular or elliptical, N number of vertical partition walls are provided perpendicularly to the long sides, the carbonaceous solid raw material is supplied from one of the short sides, and the activated carbon is recovered from the other side. By creating a fluidized bed flow of carbonaceous solid feedstock through the top or bottom of the partition, a piston-flow flow 9h bed can be formed. By doing this, it is possible to suppress the mixing of the carbonaceous solid raw material and activated carbon due to complete mixing, which is one of the characteristics of a fluidized bed, and the carbonaceous solid raw material or reaction intermediate is mixed with the activated carbon product to improve the quality of the activated carbon. There is no so-called unevenness that reduces the quality of the activated carbon. Further, the amount of heat of combustion of combustible gases such as water gas and volatile gas caused by the water gasification reaction is about five times or more than the heat time of the water gasification reaction, which is an endothermic reaction. and,
The present invention burns these generated combustible gases in the combustion radiation chamber and further in the secondary combustion chamber within the same device, and uses the generated combustion heat to heat the fluidized bed by radiant heat and heat transfer through the tubes, thereby improving efficiency. It can be well utilized for the heat of water gasification reaction. After the operation of the activated carbon production apparatus of the present invention reaches a steady state, it can be operated without supplying auxiliary fuel or with only a small amount of supply. can be followed by 1. Therefore, the present invention can provide a very economical method and apparatus for producing activated carbon. Embodiment FIGS. 1 to 3 show an embodiment of an activated carbon manufacturing apparatus according to the present invention. The activated carbon production system shown in FIG. 1 includes an activation furnace 1,
It has a screw feeder 2, a cooler 3, a steam heater 4, an air preheater 5, and a starting burner 6. The activation furnace 1 has a fluidized activation chamber 7 and a combustion radiation chamber 8 provided continuously above the fluidized activation chamber 7. The planar cross section of the flow activation chamber 7 is rectangular or elliptical, and both lI! A secondary combustion chamber 9 and a combustion gas collection α chamber 10 are provided in the II wall, and a flow activation chamber 7 is connected between the secondary combustion chambers 9 and between the secondary combustion chamber 9 and the combustion gas collection chamber 10. It has a plurality of horizontal heating tubes 11. The screw feeder 2 is connected to the upper end of one of the short side walls of the fluidization activation chamber 7, and thereby can continuously supply the carbonaceous solid raw material into the fluidization activation chamber 7. Further, a cooler 3 is connected to the activated carbon recovery port 12 via a seal valve 13 at the lower end of the other tIl wall on the short side of the flow activation chamber 7 on the opposite side of the connecting portion of the screw feeder 2. ing. A superheated steam spout 14 is opened at the bottom of the flow activation chamber 7, and a distributor 15 for rectifying the flow of superheated steam is arranged on the other side. A starting burner 6 is attached to the side wall of the combustion radiation chamber 8. The steam is sent through the supply line 16 to the steam superheater P+ii4 where it is superheated to the desired temperature. The superheated steam generated here is sent to the superheated steam jet port 14 via the supply line 17, and is jetted from the distributor 15 into the flow activation chamber 7. The carbonaceous solid MC stone is crushed or granulated to a desired particle size. This is supplied to the fluid activation chamber 7 by the screw feeder 2. In the fluidization activation chamber 7, the carbonaceous solid raw material is fluidized by an airflow of superheated steam from below to form a fluidized bed. At this time, the carbonaceous solid raw material n is preferably crushed or granulated to a particle size of about 0.1 to 9III so that the carbonaceous solid raw material can form a good fluidized bed. Further, it is preferable that the superheated steam has a temperature of about 500 to 900°C, and its supply amount is about 1.3 to 2.5°C.
Kg/Kg carbonaceous solid raw ore is preferred. When starting up the manufacturing system, air is first fed through the supply line 18 to the air preheater 2; 5, where it is preheated to a desired temperature. This preheated air is then sent to the starting burner 6 via the supply line 19.20. This f! (Fuel f1 is sent to the z-driving burner 6 via the supply line 21, and the fuel and preheated air are mixed in the starting burner 6 and blown into the combustion radiation chamber 8, where it is ignited and combusted. The fluidized bed in the fluidized activation chamber 7 is heated to a desired temperature by the radiant heat from the high-temperature combustion gas generated in this way.At this time, the temperature of the high-temperature combustion gas is approximately 1:100°C to 1550°C.
℃, and the fluidized bed is about 800℃ to +1
Preferably, the preheated air sent to the starting burner 6 is preheated to about 300°C to 800°C.The fuel may be either gas fuel or liquid fuel. . By the above-mentioned starting operation, the carbonaceous solid raw material in the stream I) bed is itself activated by superheated steam and becomes activated carbon, and at the same time, a portion thereof reacts with steam to generate water gas, and , to volatilize the volatile substances in the carbonaceous solid raw material. Water gas and volatile gas to this flow activation chamber 7r,
It flows into the combustion radiation chamber 8. When the inside of the furnace becomes close to a steady state by the above-mentioned starting operation, the hot air supply line 20 and the fuel supply line 21 are connected to the IFL driving burner 6 to burn the fuel stone. is stopped, and preheated air is fed into the combustion radiation chamber 8 through the supply line 22 to combust the water gas and volatile gas in the chamber. By adjusting the preheated air supply tray, a 4ft radiant chamber 8
Adjust the temperature inside to the desired temperature. Combustion gas is extracted from the combustion radiation chamber 8 by an exhaust gas line 23 and sent to the secondary combustion chamber 9, and then to the heating pipe 11.
The combustion gas is sent to the combustion gas collection chamber 10 through. T'-hot air is sent to the secondary combustion chamber 9 from the lj supply line 24, combustible gas in the combustion gas is combusted, and the heating tube 11 is introduced to adjust the heating of the n gas. And the heating tube 11
Heat transfer through the tube walls also heats the fluidized bed to promote the water gasification reaction. The combustion gas in the combustion gas collection chamber 10 is extracted through the exhaust gas line 25, and a part of it is sent to the steam heater 4 through the branch line 26, where the steam is heated to a desired temperature by heat exchange, and then passed through the exhaust gas line 27. is discharged from the system through the Also, a part of the combustion gas pond is sent through the branch line 28 to the air preheating unit 2i15, and after heating the air to a desired temperature by heat exchange, it is sent out of the system through the exhaust gas line 29.
JF is released. Combustion of the combustion gas in the secondary combustion chamber 9 involves high concentration of flammable gas such as water gas and volatile gas before entering the combustion radiation chamber 8 from the flammable gas extraction pipe 30 provided at the upper part of the flow activation chamber. It is also possible to extract the air and send it to the combustible gas burner 32 provided in the secondary combustion chamber 9 via the combustible gas line 31, and send preheated air from the supply line 33 to mix and burn it. The combustible gas is extracted at this time by sending water vapor to the combustible gas burner 32 through the cofeeding line 34, and using an ejector structure inside the combustible gas burner 32 to draw in the flammable gas with the water vapor. The combustion of combustible gas in the combustion radiation chamber 8 and the combustion of combustible gas in the secondary combustion chamber 9 are performed by adjusting the amount of preheated air supplied, and the temperature of the combustion radiation chamber 8 is maintained at approximately 1300 to 1550°C.
A steady state is achieved by maintaining the temperature of the secondary combustion chamber 9 at about 1300-1650°C and the fluidized bed temperature at about 800-1100°C. At this time, the preheated air sent into the combustion radiation chamber 8 has an oxygen content of approximately 0.4 to 1.5 Nm3.
/Kg carbonaceous solid raw material, and the preheated air sent to the secondary combustion chamber 9 is preferably about 0.1 to 0.8 Nm2/Kg carbonaceous solid raw material in terms of oxygen content, and the combustion radiation chamber 8 and the secondary combustion chamber 9 The total amount of oxygen in the amount of preheated air sent to is approximately 1.2N+s/
Kg or more of carbonaceous solid feedstock and in steady operation, there is almost no need to use auxiliary fuel. At this time, the air is about 3
Preferably, the steam is superheated to about 500°C or more. The activated carbon generated in the fluidized activation chamber 7 is collected through the activated carbon recovery port 1.
2. It enters the cooler 3 via the seal pulp 13, is cooled without contacting air, is discharged from the system through the activated carbon line 35, and is collected. One embodiment of the activated furnace 1 used in the method of the present invention will be explained in more detail with reference to FIGS. 2 and 3. In FIG. 2, the inner wall of the active furnace 1 is lined with a refractory material 36. The planar cross section of the flow activation chamber 7 is rectangular or elliptical, and has a secondary combustion chamber 9 and a combustion gas collecting chamber 10 in both walls on the long side thereof. Each of the gathering rooms 10 has one or more. Between the opposing secondary combustion chambers 9 or between the secondary combustion chamber 9 and the combustion gas gathering chamber 10, there are a plurality of grooves horizontally extending across the flow activation chamber 7 in one or more stages in the height direction and one or more rows in the short side direction. heating tube 1
1 to enable heat transfer to the fluidized bed. The secondary combustion chamber 9 has a combustion gas inlet 37 and a preheated air inlet 38, so that combustible gas in the combustion gas and air can be mixed and combusted in the secondary combustion chamber 9. One or more flammable gas extraction pipes 30 are provided in the upper part of the flow activation chamber 7 to extract water gas and volatile gas at the highest concentration of flammable gases, and are provided in the secondary combustion chamber 9 via a flammable gas line 31. It is connected to a combustible gas burner 32. The combustible gas burner 32 has an ejector structure, and is designed to draw in flammable gas by injecting water vapor, mix it with preheated air, and burn the combustible gas. The heating of the combustion gas in the secondary combustion chamber 9 is controlled by combustion of flammable gas in the combustion gas by blowing preheated air from the preheated air inlet 38 or by combustion of flammable gas by the combustible gas burner 32. The heating tube 11 is heated by combustion of flammable gas by one or both of them. A superripe steam spout 14 opens at the bottom of the fluidization activation chamber 7,
A distributor 15 for rectifying and distributing the flow of superheated steam is arranged above it, so that the superheated steam can be distributed in a desired direction at a desired ratio. A screw feeder 2 is installed at the upper part of the short side wall of the flow activation chamber 7.
A carbonaceous solid raw material inlet 39 connected to the activated carbon recovery port 39 is opened, and an activated carbon recovery port 12 is opened at the lower part of the short side wall on the opposite side, and the cooler 3 is connected via a seal valve 13 . The fluidization activation chamber 7 is provided with one or more vertical partition walls 40 in parallel with the heating tube 11, so that the carbonaceous solid raw material fed into the fluidization activation chamber 7 forms a fluidized bed with superheated steam while passing through the inlet 39.
From there, toward the activated carbon recovery port 12, the compartment formed by the partition wall 40 can be sequentially passed through the upper or lower part of the partition m40. Thereby, the flow of the charcoal 5Fi solid raw material in the fluidized bed can be made into a piston flow shape. The combustion radiation chamber 8 is provided with one or more starter burners 6 . The number of starting burners may be one, but they may be provided at equal intervals on two polarities facing the long side wall, and if necessary, they may be provided at equal intervals on two polarities facing the short side wall. It is preferable that the inside of the combustion radiation chamber 8 can be heated uniformly.
Further, the combustion radiation chamber 8 has one or more preheated air inlets 41.
is placed facing upward. Although one preheated air inlet 41 may be provided, it is preferable that a plurality of preheated air inlets 41 be provided at equal intervals facing each other on both the long side l side and the short side wall side, so that flammable gas such as water gas and volatile gas in the combustion radiation chamber 8 can be removed. It is desirable to be able to burn evenly. A combustion gas outlet 42 is provided at the top of the combustion radiation chamber 8 so that the combustion gas can be introduced into the combustion gas inlet 37 of the secondary combustion chamber 9 via the exhaust gas line 23. The volume M v t of the combustion radiation chamber 8 is the volume M v 1 of the flow activation chamber 8.
This is preferably about 3 to 10 times as much as the combustible gas in the combustion radiation chamber 8, which prevents the adverse effects of oxygen-containing gas from diffusing into the fluidized bed due to the combustion of combustible gas in the combustion radiation chamber 8, and sufficiently transfers radiant heat to the fluidized bed. It is for the purpose of giving. The fluidized bed receives radiant heat from the combustion radiation chamber 8, and the upper part of the fluidized bed has a higher temperature than the lower part, and water gas and volatile gas due to the reaction between the carbonaceous solid raw material and superheated steam also increase. For this reason, the flow activation chamber 7 has a lower end cross section 6 area S
In order to form a stable fluidized bed, it is preferable that the upper end cross-sectional area S is larger than 1, for example, in the shape of an inverted pyramid or an inverted cone. is preferably in the range of about 1.2 to 2. Although the radiation efficiency for the inner floor of the combustion radiant chamber is improved, there are also disadvantages such as the furnace wall area becomes larger, heat loss increases, and the combustion of combustible gas becomes uneven. Therefore, the cross-sectional area S. is approximately 1.2 to 3 of the cross-sectional area S of the upper end of the flow activation chamber 7.
Preferably, it is about twice as large. As the height of the fluidization activation chamber 7 increases, the production amount of activated carbon per unit surface area increases, but there is a limit because the ratio of heat transfer by the heating tube 11 must be higher than that of radiant heat. Furthermore, the temperature difference between the upper and lower parts of the fluidized bed increases, making the fluidized bed unstable and reducing the uniformity of the quality of the obtained activated carbon. Therefore, the height H of the flow activation chamber 7 is preferably 2- or less.

【effect】

The present invention has been developed as described above and has the following features. ■ Since the fluidized bed is heated by combustion radiant heat and heat transfer from the heating tube, there is little variation in the temperature distribution of the fluidized bed.
Uniform and high quality activated carbon can be obtained with good yield. ■ There is no need to make the temperature inside the combustion radiation chamber higher than necessary, so there is less thermal damage to the furnace that makes up the combustion radiation chamber.
Highly durable. ■ While the fluidized bed is effectively heated, the amount of fuel required for activated carbon production is Y! The production cost of activated carbon can be reduced to that of paper stock. ■ The manufacturing equipment that provides the above features is not complicated;
The manufacturing equipment itself can also be provided at low cost.

[Brief explanation of the drawing]

Figures 1 to 3 show one embodiment of the activated carbon manufacturing apparatus according to the present invention, in which Figure 1 is a general schematic diagram, Figure 2 is a schematic diagram of an activated carbon furnace, and Figure 3 is a fluidized activated carbon production apparatus. It is a schematic diagram of a conversion room. 1...Activation P, 2...Screw feeder, 3.
... Cooler, 4 ... Steam heater, 5 ... Air preheater, 6 ... Starting burner, 7 ... Flow activation chamber,
8... Combustion radiation chamber, 9... Secondary combustion chamber, 10...
Combustion gas collection chamber, 11...heating pipe, 12...activated carbon recovery port,! 4... Superheated steam spout, 15... Distributor, 30... Flammable gas extraction pipe, 32
...Flammable gas burner, 3F...Combustion gas inlet, 38...Preheating air inlet, 40...Partition wall.

Claims (30)

[Claims] (1) In the fluidized activation region, the carbonaceous solid raw material is fluidized by an airflow of superheated steam to form a fluidized bed, and by heating this fluidized bed, volatile gas is generated from the carbonaceous solid raw material, and the carbonaceous solid raw material is In a method for producing activated carbon by generating water gas through a water gasification reaction with superheated steam, the generated gas from the carbonaceous solid raw material is introduced into a combustion radiation region extending above the flow activation region. At the same time, oxygen or an oxygen-containing gas is introduced and combusted, and the fluidized bed is heated by the radiant heat of the combustion gas generated.The combustion gas is then introduced into a pipe installed in the fluidized bed, and the combustion gas is combusted through the pipe wall. A method for producing activated carbon, characterized by heating a fluidized bed by heat transfer. (2) In the combustion of produced gas from a carbonaceous solid raw material in the combustion radiant region, the amount of combustion of this produced gas is adjusted by adjusting the amount of oxygen or oxygen-containing gas, and the combustion is performed by changing the temperature of the combustion radiant region. The method for producing activated carbon according to claim 1, wherein the amount of heating to the fluidized bed by the radiant heat of the gas is adjusted. (3) Combustion gas is introduced into a secondary combustion chamber that communicates with a pipe in one wall of a fluidized activation chamber that has an internal space for forming a fluidized bed, and the combustible gas in the combustion gas is replaced with oxygen or oxygen-containing gas. The method for producing activated carbon according to claim 1, wherein the amount of heating to the fluidized bed by heat transfer through the tubes is adjusted by feeding and combusting gas and adjusting the temperature of the combustion gas introduced into the tubes. . (4) A part of the generated gas from the carbonaceous solid raw material is directly introduced into the secondary combustion chamber without passing through the combustion radiation area, and oxygen or oxygen-containing gas is introduced and combusted, and the gas is combusted from the combustion radiation area. 2. The method for producing activated carbon according to claim 1, wherein the amount of heating to the fluidized bed due to heat transfer through the tube is adjusted by adjusting the temperature of the combustion gas that is introduced into the tube after joining with the combustion gas. (5) The method for producing activated carbon according to claim 1, wherein the fluidized bed is heated to a temperature of about 800 to 1100°C. (6) The method for producing activated carbon according to claim 1 or 2, wherein the combustion gas has a temperature of about 1300 to 1550°C. (7) The method for producing activated carbon according to claim 1, 3, or 4, wherein the combustion gas introduced into the pipe has a temperature of about 1,300 to 1,650°C. (8) The method for producing activated carbon according to claim 1, wherein the superheated steam has a temperature of about 500 to 900°C. (9) Superheated steam flows into the flow activation region by approximately 1.3 to 2.
The method for producing activated carbon according to claim 1, wherein the activated carbon is supplied at a ratio of 5Kg/Kg carbonaceous solid raw material. (10) The method for producing activated carbon according to claim 1 or 8, wherein the superheated steam is prepared by heating the steam with combustion exhaust gas discharged from a pipe. (11) The method for producing activated carbon according to claim 1, wherein in addition to combustion of the produced gas from the carbonaceous solid raw material, another auxiliary fuel is burned in the combustion radiation region. (12) Claim 1 or 2, wherein the oxygen or oxygen-containing gas introduced into the combustion radiation region has an oxygen content of about 0.4 to 1.5 Nm^3/Kg of carbonaceous solid raw material. 2. Method for producing activated carbon as described in section. (13) Claim 3 or 4, wherein the oxygen or oxygen-containing gas fed into the secondary combustion chamber has an oxygen content of about 0.1 to 0.8 Nm^3/Kg of carbonaceous solid raw material. Activated carbon manufacturing method described in section (14) The method for producing activated carbon according to claim 3 or 4, wherein in addition to combustion of the generated gas from the carbonaceous solid raw material, another auxiliary fuel is combusted in a secondary combustion chamber. (15) The method for producing activated carbon according to claim 12 or 13, wherein the oxygen or oxygen-containing gas introduced into the combustion radiation region and into the secondary combustion chamber is preheated to about 300 to 800°C. . (16) The method for producing activated carbon according to claim 15, wherein the preheated oxygen or oxygen-containing gas is heated and regulated by combustion exhaust gas discharged from a pipe. (17) A fluidized activation chamber having an internal space for forming a fluidized bed, a carbonaceous solid material supply port on one side, an activated carbon recovery port on the other side, and a superheated steam spout formed at the bottom. , an activated carbon manufacturing equipment in which a distributor is arranged above the distributor to rectify the flow of superheated steam,
A secondary combustion chamber and a combustion gas collection chamber are provided for the fluidization activation chamber, a pipe is provided that passes between the secondary combustion chamber and the combustion gas collection chamber and crosses the fluidization activation chamber, and the secondary combustion chamber is provided with one or more combustion gas inlets, an oxygen or oxygen-containing gas inlet, and a combustible gas inlet; the combustion gas collecting chamber is provided with one or more combustion gas outlets; The upper end surface of the oxidation chamber is open upward, and a combustion radiation chamber for generating combustion gas is provided above the flow activating chamber, and the internal space of the radiant chamber is located above the flow activating chamber. one or more oxygen or oxygen-containing gas inlets and a combustion gas outlet are connected to the interior space at its open upper end, and the combustion radiant chamber is provided with one or more oxygen or oxygen-containing gas inlets and a combustion gas outlet; 1. An activated carbon manufacturing apparatus, characterized in that one or more combustible gas extraction ports are provided in the flow activation chamber, and one or more vertical partitions are arranged in the flow activation chamber. (18) The activated carbon production apparatus according to claim 17, wherein the combustion gas outlet of the combustion radiation chamber and the combustion gas inlet of the secondary combustion chamber are connected by a duct. (19) Flammable gas extraction port near the upper end of the flow activation chamber and 2
18. The activated carbon manufacturing apparatus according to claim 17, wherein the activated carbon production apparatus is connected to the combustible gas inlet of the next combustion chamber by a duct. (20) The activated carbon production apparatus according to claim 17, wherein an activated carbon cooler is connected to the activated carbon recovery port. (21) The activated carbon manufacturing apparatus according to claim 17, wherein a steam superheater is connected to the combustion gas outlet of the combustion gas collecting chamber. (22) The activated carbon manufacturing apparatus according to claim 17, wherein an air preheater is connected to the combustion gas outlet of the combustion gas collecting chamber. (23) Claim 1, in which a superheated steam supply line passing through a steam superheater is connected to the superheated steam spout.
Activated carbon production apparatus according to item 7. (24) The activated carbon manufacturing apparatus according to claim 17, wherein a preheated oxygen or oxygen-containing gas supply line passing through an air preheater is connected to the oxygen or oxygen-containing gas inlet. (25) The activated carbon production apparatus according to claim 17, wherein the combustion radiation chamber is provided with a starting burner. (26) The activated carbon production apparatus according to claim 17, wherein the secondary combustion chamber is provided with a starting burner. (27) The activated carbon manufacturing apparatus according to claim 17, wherein the volume V_2 of the combustion radiation chamber is approximately 3 to 10 times the volume V_1 of the fluidization activation chamber. (28) The activated carbon production apparatus according to claim 17, wherein the cross-sectional area S_2 at the upper end surface of the fluidization activation chamber is about 1.2 to 2 times the lower end cross-sectional area S_1. (29) The activated carbon manufacturing apparatus according to claim 17, wherein the cross-sectional area S_3 of the combustion radiation chamber is approximately 1.2 to 3 times the cross-sectional area S_1 at the upper end surface of the fluid activation chamber. (30) The activated carbon production apparatus according to claim 17, wherein the height H of the fluidization activation chamber is about 2 m or less.