JP2014019834A - Carbonization apparatus and carbonization method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a carbonization apparatus and a carbonization method in which improvement of heat efficiency or the like can be performed.SOLUTION: A carbonization apparatus 100 includes: a carbonization furnace 110 that includes a fluid bed in which a heat exchanger tube 150a that passes a heating medium is installed, and in which a raw material of an organic material is fluidized by fluidization gas and is performed by direct heating by heat of the gas, and is performed by indirect heating by heat of the heating medium through the heat exchanger tube 150, thereby the raw material is performed by carbonization to generate a carbonization product material of carbonization gas and solid; a raw material input port 160 that is disposed at one side face of the carbonization furnace 110, and in which the raw material is input to the carbonization furnace; and a carbonization product material discharge port 170 that is disposed at a part countering the fluid bed in the other side face of the carbonization furnace 110, and in which the raw material performed by carbonization is discharged.

Description

  The present invention relates to an organic matter carbonization apparatus and a carbonization method.

  Conventionally, techniques for carbonizing organic matter (for example, coal, sewage sludge, biomass, and garbage) have been proposed.

  For example, Patent Document 1 discloses a carbonization device that collects carbonization gas generated by carbonizing garbage. In this dry distillation apparatus, the raw material waste is made into a fluidized bed using fluidized gas. Furthermore, this carbonization apparatus flows the gas for indirect heating into the heat transfer pipe which penetrates a fluidized bed. That is, this carbonization apparatus carbonizes garbage by using a fluidized bed and indirect heating in combination. Heating using a fluidized bed is an embodiment of direct heating.

  Moreover, as a carbonization apparatus for carbonizing coal, for example, a coke oven is known. This coke oven has a combustion chamber for burning combustible gas and a carbonization chamber for carbonizing coal. Combustion gas generated in the combustion chamber (gas generated by burning combustible gas) transfers heat to the carbonization chamber through the furnace wall, and dry-coalizes the coal in the carbonization chamber. That is, a coke oven dry-distills coal by indirect heating. Since the coke oven performs dry distillation of coal by indirect heating, the dry distillation gas generated by dry distillation of coal can be recovered with high purity. The recovered carbonization gas is used in steelworks.

  A shaft furnace is also known as another carbonization apparatus for carbonizing coal. In dry distillation using a shaft furnace, coal is first charged into the shaft furnace. Then, a high temperature gas is supplied into the shaft furnace from below the shaft furnace. Thereby, coal is carbonized. That is, the shaft furnace dry-distills coal by direct heating.

JP 2005-330370 A

  However, the carbonization apparatus disclosed in Patent Document 1 throws in garbage from above the fluidized bed, performs carbonization in the fluidized bed, and discharges carbonization gas and accompanying fly ash and carbon residues from above, such as metal Since the incombustible material is discharged from below, it is considered that the fluidized bed has a substantially uniform mixed layer, and there is a problem that the temperature distribution tends to be uniform and the thermal efficiency is low. For the same reason, this carbonization apparatus has a problem that the residence time in the fluidized bed, that is, the carbonization time becomes shorter as the particle size of the raw material is larger. For this reason, the raw material with a large particle size may be discharged | emitted from the downward direction with dry distillation inadequate (namely, as an undried product).

  In the carbonization apparatus disclosed in Patent Document 1, the object to be treated is garbage, and the main discharge from the bottom is a non-combustible material such as metal. Therefore, the discharge from the bottom contains a small amount of undistilled material. There is no big problem. However, when this carbonization apparatus is applied to coal carbonization, the carbonization product becomes a useful coal char. For this reason, when the dry distillation apparatus disclosed in Patent Document 1 is applied to the dry distillation of coal as it is, the quality of the coal char may be deteriorated. This is because coal having a large particle size may be mixed into the coal char as an undistilled product.

  In addition, since the carbonization apparatus disclosed by patent document 1 diverts a part of carbonization gas to fluidization gas, it can collect | recover carbonization gas with high purity. However, for example, when combustion gas is used as the fluidizing gas, there arises a problem that the calorific value of the dry distillation gas is reduced. This is because the dry distillation gas is diluted by the combustion gas.

  Furthermore, when raw materials having no caking property (for example, coal having no caking property or organic matter other than coal) are dry-distilled in a coke oven, clogging may occur. For this reason, dry distillation using a coke oven has a problem that the raw material is limited to coal having caking properties. In addition, the dry distillation by indirect heating has a problem that the thermal efficiency is lower than the dry distillation by direct heating. For this reason, the dry distillation apparatus which performs indirect heating like a coke oven had the problem that it became enormous and complicated compared with the dry distillation apparatus which performed direct heating, and installation cost was required. On the other hand, when carbonization using a shaft furnace is performed, it is necessary to form coal in advance to ensure air permeability.

  Therefore, the present invention has been made in view of the above problems, and the object of the present invention is to improve the quality of the dry distillation product, to suppress the decrease in the calorific value of the dry distillation gas, to dry distillation of various raw materials, and equipment It is an object of the present invention to provide a dry distillation apparatus and a dry distillation method that can reduce the size of the raw material and that does not require forming of a raw material.

  In order to solve the above-described problems, according to an aspect of the present invention, a fluidized bed in which a heat transfer tube through which a heat medium passes is installed, and an organic material is fluidized with a fluidizing gas and the heat of the gas is used. Is provided on one side of the carbonization furnace and the carbonization furnace for producing carbonization gas and solid carbonization product by dry distillation of the raw material by direct heating through the heat transfer tube by the heat of the heat medium. A raw material input port for supplying raw material to the carbonization furnace, and a dry distillation product discharge port provided at a portion facing the fluidized bed on the other side surface of the carbonization furnace and for discharging the carbonized raw material. A carbonization device is provided.

  Here, in the fluidized bed, at least one partition wall provided to suppress the progress of the raw material in the direction connecting the one side surface and the other side surface, and an opening formed below the partition wall and through which the raw material can pass. May be provided.

  Further, in the fluidized bed, the progress of the raw material in the direction connecting the one side surface and the other side surface is suppressed, and the one side surface of the dry distillation gas generated by dry distillation of the raw material is connected in the direction connecting the other side surface. At least one partition wall provided so as to block the movement of the carbonization gas, and a dry distillation gas discharge port provided in each dry distillation space in the dry distillation furnace partitioned by the partition wall for discharging the dry distillation gas generated in each dry distillation space. May be.

  According to another aspect of the present invention, a step of introducing an organic raw material from one side of a dry distillation furnace having a fluidized bed in which a heat transfer tube through which a heat medium passes is provided, and the raw material is fluidized with a fluidizing gas. And the step of dry distillation of the raw material by direct heating by the heat of the gas and indirect heating through the heat transfer tube by the heat of the heat medium, and the fluidized bed of the other side of the dry distillation furnace, And a step of discharging from a carbonization product discharge port provided in a portion facing the water. A carbonization method is provided.

  Here, the step of moving the raw material toward the dry distillation product discharge port, the step of suppressing the progress of the raw material in the direction connecting the one side surface and the other side surface by the partition wall, and the raw material are formed below the partition wall. Introducing into the opening.

  In addition, the step of carbonizing the raw material in each of the carbonization spaces in the carbonization furnace partitioned by a partition provided so as to block movement of the carbonization gas generated by the carbonization of the raw material in a direction connecting one side surface and the other side surface And a step of discharging a carbonization gas generated in each carbonization space from a carbonization gas discharge port provided in each carbonization space.

  As described above, according to the present invention, the dry distillation apparatus performs dry distillation using both direct heating by a fluidized bed and indirect heating by a heat transfer tube, so that a large amount of heat necessary for dry distillation can be provided by indirect heating. Therefore, the dry distillation apparatus can reduce the flow rate of the fluidized gas, and thus can suppress the decrease in the calorific value of the dry distillation gas.

  Further, in the dry distillation apparatus, a dry distillation product discharge port is provided on the side surface of the fluidized bed. Furthermore, the raw material is directly heated by being fluidized by a fluidizing gas and indirectly heated by a heat transfer tube. For this reason, the raw material has a temperature difference in the direction connecting the one side surface and the other side surface. Therefore, the thermal efficiency of the carbonization apparatus is higher than that in a substantially uniform mixed state (for example, in the case of the cited document 1). Moreover, since the average residence time in the furnace differs depending on the particle size, the raw material is heated for different times. Specifically, the larger the particle size, the longer the residence time. On the other hand, the raw material having a larger particle size takes longer to dry distillation. Therefore, the carbonization apparatus can sufficiently carbonize a raw material having a large particle size, so that the quality of the carbonization product can be improved.

  Furthermore, since the carbonization apparatus uses carbonization using a fluidized bed, carbonization can be performed even when the raw material does not have caking properties. That is, the carbonization apparatus can also carbonize coal that has been difficult to carbonize in a coke oven. Furthermore, since the carbonization apparatus uses carbonization using a fluidized bed, the equipment becomes small and simple. Furthermore, the carbonization apparatus does not need to form a raw material.

It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the 1st Embodiment of this invention. It is a top view which shows arrangement | positioning of the heat exchanger tube concerning the embodiment. It is a top view which shows the modification of a heat exchanger tube. It is a top view which shows the modification of a heat exchanger tube. It is a top view which shows the modification of a heat exchanger tube. It is a top view which shows the modification of a heat exchanger tube. It is a block diagram which shows the example of the process flow using a dry distillation apparatus. It is a block diagram which shows the example of the process flow using a dry distillation apparatus. It is a block diagram which shows the example of the process flow using a dry distillation apparatus. It is a block diagram which shows the example of the process flow using a dry distillation apparatus. It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the 2nd Embodiment of this invention. It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the 3rd Embodiment of this invention. It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the modification of 3rd Embodiment. It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the modification of 3rd Embodiment. It is a sectional side view which shows the structure of the dry distillation apparatus which concerns on the modification of 3rd Embodiment. It is a sectional side view which shows the structure of a comparative example.

  Exemplary embodiments of the present invention will be described below in detail with reference to the accompanying drawings. In addition, in this specification and drawing, about the component which has the substantially same function structure, duplication description is abbreviate | omitted by attaching | subjecting the same code | symbol.

  The present inventors examined a carbonization apparatus capable of carbonizing a variety of raw materials containing organic substances, and as a result, focused on a carbonization apparatus using a fluidized bed. This is because a carbonization apparatus using a fluidized bed has advantages such as high thermal efficiency and small and simple equipment. However, as described above, the dry distillation apparatus using a fluidized bed has a problem that the amount of heat generated by the dry distillation gas is reduced by the combustion gas when the combustion gas is used as the fluidizing gas. Therefore, the present inventors examined a technique for suppressing a decrease in the calorific value of the dry distillation gas. Furthermore, the present inventors also examined the outlet for the dry distillation product. This is because the same problem as in Patent Document 1 occurs when the outlet of the dry distillation product exists below the fluidized bed. As a result of the above studies, the present inventors have developed a dry distillation apparatus 100 (see FIG. 1 and the like) described in the following embodiments. These carbonization apparatuses 100 perform carbonization of raw materials by using a fluidized bed and indirect heating in combination. Further, in the carbonization apparatus 100, an inlet and an outlet are provided on both sides of the carbonization furnace, respectively.

  Since the carbonization apparatus 100 performs carbonization using both a fluidized bed and indirect heating, most of the amount of heat required for carbonization can be covered by indirect heating. Therefore, since the dry distillation apparatus 100 can reduce the flow rate of the fluidized gas, it is possible to suppress a decrease in the calorific value of the dry distillation gas.

  Furthermore, in the carbonization apparatus 100, a discharge port (dry distillation product discharge port) is provided on a side surface of the carbonization furnace. Furthermore, the raw material is directly heated by being fluidized by a fluidizing gas and indirectly heated by a heat transfer tube. For this reason, the raw material has a temperature difference in the length direction of the carbonization furnace main body 120 (the direction connecting the rear end surface 120a and the front end surface 120b). Specifically, the temperature of the raw material in the carbonization furnace becomes the minimum immediately after being put into the carbonization furnace, rises as the raw material moves, and becomes the highest when the raw material reaches the carbonization product discharge port. . That is, the temperature of the fluidized bed increases substantially in proportion to the distance from the raw material inlet. In other words, the temperature gradient of the fluidized bed shows a positive value. In Patent Document 1, it is considered that the fluidized bed is in a substantially uniform mixed state, and the temperature distribution in the fluidized bed is substantially uniform, so the temperature gradient is almost zero. Therefore, the thermal distillation apparatus 100 has high thermal efficiency. Moreover, since the average residence time in the furnace differs depending on the particle size, the raw material is heated for different times. Specifically, the larger the particle size, the longer the residence time. On the other hand, the raw material having a larger particle size takes longer to dry distillation. Therefore, since the carbonization apparatus 100 can sufficiently carbonize a raw material having a large particle size, the quality of the carbonization product can be improved.

  Furthermore, since the carbonization apparatus 100 uses carbonization using a fluidized bed, carbonization can be performed even when the raw material does not have caking properties. That is, the carbonization apparatus 100 can also carbonize coal that has been difficult to carbonize in a coke oven. Furthermore, since the carbonization apparatus 100 uses carbonization using a fluidized bed, the equipment becomes small and simple. Furthermore, the carbonization apparatus 100 does not need to form a raw material. Hereinafter, the carbonization apparatus 100 according to each embodiment will be described in detail.

<1. First Embodiment>
First, the first embodiment will be described. FIG. 1 is a side sectional view showing a configuration of a dry distillation apparatus 100 according to the first embodiment. The dry distillation apparatus 100 includes a dry distillation furnace 110, a raw material input port 160, a dry distillation product discharge port 170, and a dry distillation gas discharge port 180.

  The dry distillation furnace 110 has a fluidized bed X2 in which a heat transfer tube 150 through which a heat medium 151 for indirect heating passes is installed. The fluidized bed X2 here refers to a region and a state in which the raw material X1 is fluidized, and the region is also referred to as a fluidizing unit. The dry distillation furnace 110 fluidizes the raw material X1 with the fluidizing gas 130a and directly heats the raw material X1 with the heat of the gas 130a, and indirectly heats the raw material X1 through the heat transfer tube 150 with the heat of the indirect heating heat medium 151. The raw material X1 is carbonized to produce a carbonization gas and a solid carbonization product. That is, the dry distillation furnace 110 is a furnace that performs dry distillation using both direct heating by a fluidized bed and indirect heating by a heat transfer tube, and includes a dry distillation furnace main body 120, a plenum chamber 130, a dispersion plate 140, and a heat transfer tube 150. The dry distillation furnace main body 120 is a portion into which the raw material X1 is charged, and the dispersion plate 140 is the bottom surface of the dry distillation furnace main body 120. The dry distillation furnace main body 120 has a substantially rectangular shape in plan view. Hereinafter, one of the side surfaces in the length direction of the carbonization furnace body 120 is also referred to as a rear end surface 120a, and the other side surface is also referred to as a front end surface 120b. The rear end face 120a is provided with a raw material inlet 160, and the front end face 120b is provided with a dry distillation product outlet 170.

  The raw material X1 is a raw material containing organic substances, such as coal, sewage sludge, biomass, and garbage, for example. The raw material X1 is directly heated by being fluidized by a fluidizing gas 130a described later and indirectly heated by the heat transfer tube 150. For this reason, the raw material X1 has a temperature difference in the length direction of the dry distillation furnace main body 120. Specifically, the temperature of the raw material X1 becomes the lowest immediately after being put into the dry distillation furnace main body 120, rises as the raw material X1 moves, and becomes the highest when the raw material X1 reaches the dry distillation product discharge port 170. It becomes. That is, the temperature of the fluidized bed X2 increases in proportion to the distance from the raw material inlet 160. In other words, the temperature gradient of the fluidized bed shows a positive value.

  The average particle diameter of the raw material X1 is preferably about 3 mm or less. This is because if the particle size of the raw material X1 is too large, it is necessary to increase the flow rate (flow velocity) of the fluidizing gas 130a in order to fluidize the raw material X1, and as a result, the heating value of the dry distillation gas 180a decreases. Moreover, the raw material X1 is thrown into the carbonization furnace main body 120, for example at normal temperature, when prior drying is not performed. On the other hand, the raw material X1 is charged into the dry distillation furnace main body 120 at about 200 ° C., for example, when pre-drying is performed.

  The average particle diameter is measured as follows, for example. First, a plurality of sieves having different openings are prepared, and the raw material is divided into each of a plurality of particle size categories using these sieves. Then, based on the median value of each particle size category and the ratio of the raw materials belonging to each particle size category (% by mass with respect to the total mass of the material), the arithmetic average value of the particle size (mm) is measured as the average particle size. .

  The plenum chamber 130 is a portion into which the fluidized gas 130a is introduced from the outside. The fluidizing gas 130a is supplied from, for example, a combustion apparatus 200 (see FIG. 7) described later. The fluidizing gas 130 a is introduced into the dry distillation furnace main body 120 through the dispersion plate 140. The fluidizing gas 130a fluidizes the raw material X1 in the dry distillation furnace main body 120, thereby forming a fluidized bed X2 of the raw material X1. Thereafter, the fluidized gas 130a is mixed with a gas generated by dry distillation, and is discharged from the dry distillation gas outlet 180 as a dry distillation gas 180a.

  In the first embodiment, most of the heat necessary for dry distillation of the raw material X1 is covered by the heat from the heat transfer tube 150, that is, indirect heating, so the flow rate of the fluidized gas 130a is reduced. For example, when the raw material X1 is coal, the dry distillation start temperature is about 300 ° C. and the dry distillation completion temperature is about 1000 ° C. Therefore, the temperature of the fluidized gas 130a is preferably about 400 ° C. to 1200 ° C.

  The dispersion plate 140 is a plate that partitions the carbonization furnace main body 120 and the plenum chamber 130. A large number of through holes are formed in the dispersion plate 140 for the fluidized gas 130a to flow therethrough. Above the dispersion plate 140, the inside of the dry distillation furnace in which the fluidized bed X2 is formed is also referred to as a fluidizing chamber. Further, the raw material flowing in the fluidizing chamber and the produced dry distillation product are not accompanied by the dry distillation gas 180a and discharged from the dry distillation gas outlet 180, or the raw material larger than a predetermined particle size and the produced dry distillation are produced. In the dry distillation furnace above the fluidization chamber, the cross sectional area is increased (enlarged in the width direction) so that the product is not discharged from the dry distillation gas outlet 180 with the dry distillation gas 180a. It is preferable to provide a free board part which drops the

  The heat transfer tube 150 is a portion that performs indirect heating. FIG. 2 is a plan view showing the arrangement of the heat transfer tubes 150. In FIG. 2, an arrow A indicates the flow of the raw material X1. The same applies to FIGS. 3 to 6 described later. As shown in FIGS. 1 and 2, the heat transfer tube 150 is a straight tube and penetrates the front end surface 120 b and the rear end surface 120 a of the dry distillation furnace main body 120. Further, the heat transfer tube 150 passes through the lower end of the dry distillation furnace main body 120. Therefore, the heat transfer tube 150 penetrates the fluidized bed X2 when the fluidized bed X2 is formed.

  The indirect heating heat medium 151 passes through the heat transfer tube 150. The indirect heating heat medium 151 is not particularly limited as long as it has a necessary sensible heat, such as a high-temperature liquid such as a molten salt or a high-temperature gas such as exhaust gas. In consideration of ease and cost reduction, it is preferable to use an indirect heating gas which is a gas such as exhaust gas. Hereinafter, an example using the indirect heating gas 151 as the indirect heating heat medium 151 will be described.

  Specifically, the indirect heating gas 151 is introduced into the dry distillation furnace main body 120 from the front end surface 120b and discharged from the rear end surface 120a. The amount of heat of the indirect heating gas 151 is supplied to the fluidized bed X <b> 2 through the heat transfer tube 150. That is, the indirect heating gas 151 supplies heat to the fluidized bed X2 while moving. Thereby, the fluidized bed X2 is indirectly heated. Since the indirect heating gas 151 is introduced into the dry distillation furnace main body 120 from the front end surface 120b, the temperature is highest at the front end surface 120b and lowest at the rear end surface 120a. Therefore, the temperature of the indirect heating gas 151, that is, the temperature of the heat transfer tube 150 increases in proportion to the distance from the raw material inlet 160. That is, the temperature gradient of the heat transfer tube 150 also shows a positive value. Therefore, the temperature gradient of the fluidized bed X2 becomes steeper (the temperature gradient becomes larger) than when the indirect heating is not performed. The indirect heating gas 151 is supplied from, for example, a combustion device 200 described later. The temperature of the indirect heating gas 151 is preferably about 400 ° C. to 1200 ° C., similar to the fluidizing gas 130a. Therefore, the raw material X1 is dry-distilled by the fluidizing gas 130a and the indirect heating gas 151. The temperature of the carbonization product X3 (the carbonized raw material X1, also referred to as char) is about 400 ° C to 1000 ° C.

  From the viewpoint of increasing the heat transfer area, the heat transfer tube 150 preferably has a smaller diameter (outer diameter). However, the number of heat transfer tubes 150 increases as the diameter of the heat transfer tubes 150 decreases. This is because the total amount of heat needs to be secured. Therefore, the diameter of the heat transfer tube 150 is preferably about 2 to 10 cm, for example. The number of heat transfer tubes 150 depends on the processing amount per unit time of the raw material X1. Similarly, the size of the carbonization furnace 110 also depends on the throughput per unit time of the raw material X1.

  1 and 2, the heat transfer tube 150 is a straight tube, but the shape of the heat transfer tube 150 is not limited to this, and may be a bent shape. 3-6 is a top view which shows the modification of the heat exchanger tube 150. As shown in FIG.

  In the modification shown in FIG. 3, heat transfer tubes 150 a and 150 b penetrate the dry distillation furnace main body 120 instead of the heat transfer tube 150. The heat transfer tube 150a is introduced into the dry distillation furnace main body 120 from the front end surface 120b of the dry distillation furnace main body 120, is bent 90 ° near the center of the dry distillation furnace main body 120, and comes out upward. The indirect heating gas 151 a flowing through the heat transfer tube 150 a is introduced into the dry distillation furnace main body 120 from the front end surface 120 b of the dry distillation furnace main body 120.

  On the other hand, the heat transfer tube 150 b is introduced into the dry distillation furnace main body 120 from the rear end surface 120 a of the dry distillation furnace main body 120, is bent 90 ° near the center of the dry distillation furnace main body 120, and comes out upward. The indirect heating gas 151b flowing through the heat transfer tube 150b is introduced from above the vicinity of the center of the dry distillation furnace main body 120. The indirect heating gas 151b may be introduced into the dry distillation furnace main body 120 from the rear end surface 120a of the dry distillation furnace main body 120 as shown in FIG. The indirect heating gases 151a and 151b are supplied from, for example, a combustion apparatus 200 described later.

  The modification shown in FIGS. 3 and 4 is preferably used when increasing the total amount of heat given to the fluidized bed X2. That is, in the example shown in FIG. 2, since the heat transfer tube 150 extends from the front end surface 120b to the rear end surface 120a, the heat transfer tube 150 supplies heat to the entire region in the length direction of the fluidized bed X2. For this reason, when there is much processing amount of the raw material X1, the heat amount of the heat exchanger tube 150 may run short. In the arrangement method of the heat transfer tubes 150 shown in FIG. 2, the number of the heat transfer tubes 150 is determined by the thickness × width of the fluidized bed X2. Therefore, in order to change the number of heat transfer tubes 150, it is only necessary to change at least one of the thickness and width of the fluidized bed X2. However, since the thickness is determined by the relationship between the particle size of the raw material and the fluidized gas, it is not easy to change the thickness. Therefore, as a method of increasing the number of heat transfer tubes 150 in order to increase the amount of heat, it is possible to increase the width of the fluidized bed X2. When the width of the fluidized bed X2 is increased, the length of the fluidized bed X2 is shortened if the processing amount is the same. However, since the piston flow is increased as the length is long, the thermal efficiency is deteriorated when the length of the fluidized bed X2 is short.

  On the other hand, in the example shown in FIGS. 3 and 4, the heat transfer tube 150a supplies heat to the region on the front end surface 120b side in each region of the fluidized bed X2, and the heat transfer tube 150b is a region on the rear end surface 120a side. The amount of heat can be supplied. For this reason, in the example shown in FIGS. 3 and 4, even when the amount of the raw material X1 is large, a larger amount of heat can be supplied to the entire region in the length direction of the fluidized bed X2. In addition, from the viewpoint of generating a temperature gradient in the fluidized bed X2, the temperature of the heat transfer tube 150a is preferably higher than the temperature of the heat transfer tube 150b.

  In the modification shown in FIG. 5, a heat transfer tube 150 c penetrates the dry distillation furnace main body 120 instead of the heat transfer tube 150. The heat transfer tube 150 c extends in the direction orthogonal to the arrow A, that is, in the width direction of the dry distillation furnace 110. In addition, a plurality of heat transfer tubes 150 c are arranged at predetermined intervals in the length direction of the dry distillation furnace main body 120. In addition, the direction in which the indirect heating gas 151c flows in a certain heat transfer tube 150c and the direction in which the indirect heating gas 151c flows in the adjacent heat transfer tube 150c are opposite to each other. Thereby, the temperature distribution in the width direction of the fluidized bed X2 becomes more uniform. The indirect heating gas 151c is supplied from, for example, a combustion device 200 described later.

  The modification shown in FIG. 5 is also preferably used when the amount of raw material X1 is large. This is because each heat transfer tube 150c can supply heat to different regions among the regions in the length direction of the fluidized bed X2. Note that, from the viewpoint of generating a temperature gradient in the fluidized bed X2, it is preferable to increase the temperature of the heat transfer tube 150c as the distance from the heat transfer tube 150c to the tip surface 120b is shorter.

  Further, the adjacent heat transfer tubes 150c are connected to each other, and the indirect heating gas 151c is introduced from the heat transfer tube 150c closest to the front end surface 120b and discharged from the heat transfer tube 150c closest to the rear end surface 120a. It is also possible.

  In the modification shown in FIG. 6, a heat transfer tube 150 d penetrates the dry distillation furnace main body 120 instead of the heat transfer tube 150. The heat transfer tube 150d extends in a direction that obliquely intersects the arrow A. A plurality of heat transfer tubes 150d are arranged at predetermined intervals in the length direction of the dry distillation furnace main body 120. Indirect heating gas 151d is circulated in the same direction. Of course, as shown in FIG. 5, each indirect heating gas 151 d may flow in alternate directions. The indirectly heating gas 151d is supplied from, for example, a combustion device 200 described later. The modification shown in FIG. 6 is also preferably used when the amount of raw material X1 is large. From the viewpoint of generating a temperature gradient in the fluidized bed X2, it is preferable to increase the temperature of the heat transfer tube 150d as the distance from the heat transfer tube 150d to the tip surface 120b is shorter.

  The raw material charging port 160 shown in FIG. 1 is a portion where the raw material X1 is charged into the dry distillation furnace main body 120, and is provided on the rear end surface 120a of the dry distillation furnace main body 120. A raw material supply hopper 165 is connected to the raw material charging port 160, and the raw material X 1 is supplied from the raw material supply hopper 165 into the dry distillation furnace main body 120. The dry distillation product discharge port 170 is a portion where the dry-distilled raw material X1, that is, the dry distillation product X3, is discharged. The dry distillation product discharge port 170 is provided at a lower end portion of the front end surface 120b, that is, a portion of the front end surface 120b facing the fluidized bed X2. In other words, the dry distillation product discharge port 170 is provided on the side surface of the fluidized bed X2.

  The dry distillation gas outlet 180 is a portion from which the dry distillation gas 180 a is discharged, and is provided on the upper end surface of the dry distillation furnace main body 120. The dry distillation gas 180a has a different composition depending on the temperature of the raw material X1. For example, the dry distillation gas 180a obtained from 300 ° C. to 600 ° C. coal contains a gas containing a large amount of methane and carbon monoxide and tar. The dry distillation gas 180a obtained from the raw material X1 at 600 ° C. to 1000 ° C. contains a lot of hydrogen. In the first embodiment, a dry distillation gas 180a in which all of these components are mixed is obtained. However, in the third embodiment to be described later, dry distillation gases 180a having different compositions can be recovered.

  Next, a dry distillation method using the dry distillation apparatus 100 will be described. First, the raw material X1 is input from the raw material input port 160. The raw material X1 is continuously charged. Next, the fluidizing gas 130 a is supplied to the dry distillation furnace main body 120 from below the dispersion plate 140. Thereby, the raw material X1 in the dry distillation furnace main body 120 is fluidized. That is, the raw material X1 is a fluidized bed X2. On the other hand, an indirect heating gas 151 flows through the heat transfer tube 150. The raw material X1 in the fluidized bed X2 moves toward the dry distillation product discharge port 170 by being pushed by the subsequent raw material X1. The raw material X1 is dry-distilled by being heated by the fluidizing gas 130a and the heat transfer tube 150. That is, the dry distillation apparatus 100 performs dry distillation using both the fluidized bed X2 and indirect heating. The raw material X1 is carbonized by the time it reaches the carbonization product discharge port 170 to obtain a carbonization product X3. The dry distillation product X3 is discharged from the dry distillation product discharge port 170 to the outside. On the other hand, the gas generated by dry distillation of the raw material X1, that is, the dry distillation gas 180a, is discharged to the outside through the dry distillation gas outlet 180 together with the fluidizing gas 130a.

  Next, a process flow using the dry distillation apparatus 100 will be described. 7-10 shows an example of the process flow using the carbonization apparatus 100. FIG. 7 and 8 show a process flow for a raw material X1 that has been pre-dried or a raw material X1 that does not require pre-drying. In the process flow shown in FIG. 7, the raw material X1 is carbonized by the carbonization apparatus 100 to be a carbonized product X3 (in the figure, the carbonized product X3 is an example of char X3. The same applies to FIGS. 8 to 10). The The dried product X3 is cooled by the cooler 300 and then used in another device. On the other hand, the dry distillation gas 180 a generated by dry distillation of the raw material X <b> 1 is introduced into the combustion apparatus 200. The combustion apparatus 200 generates combustion gas by burning the dry distillation gas 180a, and supplies the combustion gas to the dry distillation apparatus 100. The dry distillation apparatus 100 uses the combustion gas as the indirect heating gas 151 and the fluidizing gas 130a.

  The cooler 300 is not particularly limited, and may be, for example, an external heat type rotary cooler or a cooler using a fluidized bed. In the dry distillation apparatus 100, the dry distillation gas 180a may be classified. By this classification, a fine powder carbonization product X3 (or raw material X1) is recovered from the carbonization gas 180a. The recovered fine powder may be used as the raw material X1 after being molded, or may be used as a heat source for the combustion apparatus 200. In addition, when the cooler 300 uses a fluidized bed, classification may be performed by the cooler 300. In this case, fine powder is classified from the recovered cooling gas.

  Also in the process flow shown in FIG. 8, the raw material X1 is dry-distilled by the dry distillation apparatus 100, and is made into the dry distillation product X3. The dry distillation product X3 is cooled in the cooler 300 and then used in another device. On the other hand, the dry distillation gas 180 a generated by the dry distillation of the raw material X 1 is introduced into the separator 500. Separator 500 separates dry distillation gas 180a into combustible gas and tar. Combustible gas and tar are used in other equipment. The dry distillation apparatus 100 is supplied with a high-temperature gas 220 from an external heat source. The dry distillation apparatus 100 uses the hot gas 220 as the indirect heating gas 151 and the fluidizing gas 130a. The hot gas 220 is, for example, combustion gas or preheated dry distillation gas 180a. When the high temperature gas 220 becomes the dry distillation gas 180a, the dry distillation gas 180a can be recovered from the dry distillation apparatus 100 at a high concentration.

  The process flow shown in FIG. 9 is obtained by adding a drying step to the process flow shown in FIG. That is, in the process flow shown in FIG. 9, the raw material X <b> 1 is first introduced into the drying device 400 and dried by the drying device 400. The drying device 400 is not particularly limited, and may be either a drying device using indirect heating or a drying device using direct heating. Examples of the drying device using indirect heating include a drying device using, for example, a call-in tube, a steam tube dryer, WTA, or the like. Examples of the drying apparatus using direct heating include a drying apparatus using a pressure dehydration method (such as a mechanical thermal compression method (MTE)) or a fluidized bed. The dried raw material X1 is introduced into the carbonization apparatus 100. The subsequent processing is the same as in FIG. On the other hand, the combustion gas 210 generated from the combustion apparatus 200 is introduced into the dry distillation apparatus 100 and the drying apparatus 400. The drying apparatus 400 dries the raw material X1 using the combustion gas 210.

  The process flow shown in FIG. 10 is obtained by adding a drying step to the process flow shown in FIG. However, the drying apparatus 400 dries the raw material X1 using the high temperature gas 230 supplied from an external heat source.

  By the above, since the carbonization apparatus 100 which concerns on 1st Embodiment performs the carbonization which used the fluidized bed X2 and indirect heating together, much heat amount required for carbonization can be covered by indirect heating. Therefore, since the dry distillation apparatus 100 can reduce the flow rate of the fluidized gas 130a, the heat generation amount of the dry distillation gas 180a can be kept low.

  Further, in the carbonization apparatus 100, a carbonization product discharge port 170 is provided on the side surface of the fluidized bed X2. Furthermore, the raw material X1 is directly heated by being fluidized by the fluidizing gas 130 a and indirectly heated by the heat transfer tube 150. For this reason, the raw material X1 has a temperature difference in the length direction of the dry distillation furnace main body 120. Therefore, the thermal distillation apparatus 100 has higher thermal efficiency than that in a substantially uniform mixed state (for example, in the case of the cited document 1). Moreover, since the average residence time in the furnace differs depending on the particle size, the raw material X1 is heated for different times. Specifically, the residence time of the raw material X1 having a larger particle size becomes longer. On the other hand, the raw material X1 having a larger particle size takes longer to dry distillation. Therefore, since the carbonization apparatus 100 can sufficiently carbonize a raw material having a large particle size, the quality of the carbonization product X3 can be improved.

  Furthermore, since the carbonization apparatus 100 uses carbonization using the fluidized bed X2, carbonization can be performed even when the raw material X1 does not have caking properties. That is, the carbonization apparatus 100 can also carbonize coal that has been difficult to carbonize in a coke oven. Furthermore, since the carbonization apparatus 100 uses carbonization using the fluidized bed X2, the facilities are small and simple. Furthermore, the carbonization apparatus 100 does not need to form a raw material.

<2. Second Embodiment>
Next, a second embodiment will be described. FIG. 11 is a side sectional view showing a configuration of the dry distillation apparatus 100 according to the second embodiment. The carbonization apparatus 100 according to the second embodiment is obtained by adding a partition wall 190 to the first embodiment.

  The partition wall 190 suppresses the progress of the raw material X1 in the length direction (that is, the direction connecting the rear end surface 120a and the front end surface 120b) of the raw material X1 in the fluidized bed X2. Specifically, three partition walls 190 are provided inside the dry distillation furnace main body 120. The number of the partition walls 190 is not particularly limited, but the flow of the raw material X1 approaches the piston flow as the number of the partition walls 190 increases. Therefore, it is preferable that the number of the partition walls 190 is large. The interval between the partition walls 190 is not particularly limited. The partition wall 190 is orthogonal to the length direction of the dry distillation furnace main body 120 (that is, the direction in which the raw material X1 travels in the fluidized bed X2). In addition, the partition wall 190 should just be provided in the direction which cross | intersects the length direction of the carbonization furnace main body 120. FIG. The partition 190 divides the space inside the dry distillation furnace main body 120 into four dry distillation spaces 121 to 124.

An opening (gap) 191 is formed between the lower end of the partition wall 190 and the dispersion plate 140. Similarly, an opening 192 is also formed between the upper end portion of the partition wall 190 and the upper end surface of the dry distillation furnace main body 120. Therefore, in the second embodiment, the carbonization spaces 121 to 124 are connected by the openings 191 and 192. The height of the opening 191 may be about a fraction of the static bed thickness of the fluidized bed X2 (thickness when the fluidized bed X2 is not flowing). The opening 191 may be formed over the entire region in the width direction of the dry distillation furnace main body 120 or may be formed in a part in the width direction. When the opening 191 is formed in a part in the width direction, the height of the opening 191 may be higher than the stationary layer thickness of the fluidized bed X2.

  The partition wall 190 plays the following role by the above configuration. That is, since the partition wall 190 suppresses the progress of the raw material X1 in the length direction of the dry distillation furnace main body 120 in the fluidized bed X2, the movement of the raw material X1 between the respective carbonization spaces is limited to the opening portion 191. Mixing of X1 in the furnace can be suppressed. Accordingly, the flow of the raw material X1 is closer to the piston flow by the partition wall 190. Further, as the number of partition walls 190 increases, the mixing of the raw materials X1 (that is, the mixing of the raw materials X1 having different temperatures) is more reliably suppressed, so that the flow of the raw materials X1 becomes closer to the piston flow. And as the flow of the raw material X1 approaches the piston flow, the thermal efficiency of the dry distillation apparatus 100 improves (the temperature gradient becomes steeper), so the flow rate of the fluidized gas 130a is reduced. Thereby, the carbonization apparatus 100 can collect the carbonization gas 180a with higher purity. Furthermore, since the thermal efficiency of the carbonization apparatus 100 is improved, the total length of the carbonization apparatus 100 can be shortened.

<3. Third Embodiment>
Next, a third embodiment will be described. FIG. 12 is a side sectional view showing the configuration of the dry distillation apparatus 100 according to the third embodiment. The carbonization apparatus 100 according to the third embodiment is different from the second embodiment in the following points.

  The upper end portion of the partition wall 190 is connected to the upper end surface of the dry distillation furnace main body 120. Therefore, the partition wall 190 blocks the movement of the carbonization gas in the length direction of the carbonization furnace main body 120 (that is, the direction connecting the rear end surface 120a and the front end surface 120b). That is, the dry distillation spaces 121 to 124 are separated from each other when the fluidized bed X2 is formed. In addition, dry distillation gas discharge ports 181 to 184 are provided in the dry distillation spaces 121 to 124, respectively. The dry distillation gas discharge ports 181 to 184 are portions through which the dry distillation gases 181a to 184a in the dry distillation spaces 121 to 124 are discharged.

  As described above, the composition of the dry distillation gas varies depending on the temperature of the raw material X1. And since the raw material X1 in each carbonization space 121-124 mutually differs in temperature, the carbonization gas 181a-184a in the carbonization space 121-124 also differs in a composition mutually. Therefore, the dry distillation gases 181a to 184a having different compositions are discharged from the dry distillation gas discharge ports 181 to 184. That is, the dry distillation apparatus 100 can collect the dry distillation gases 181a to 184a having different compositions.

[First Modification]
Next, a first modification of the third embodiment will be described. FIG. 13 is a side sectional view showing a configuration of the dry distillation apparatus 100 according to the first modification. In the first modification, the carbonization temperature range (from the carbonization start temperature to the carbonization completion temperature) is divided into three at substantially equal intervals, and the carbonization gas is recovered from the raw material X1 in each temperature division.

  Specifically, two partition walls 190 are provided in the dry distillation furnace main body 120. Thereby, the space inside the dry distillation furnace main body 120 is partitioned into three dry distillation spaces 121 to 123. Further, dry distillation gas discharge ports 181 to 183 are provided in the respective carbonization spaces 121 to 123. The dry distillation gases 181a to 183a having different compositions are discharged from the dry distillation gas discharge ports 181 to 183.

  Moreover, in the 1st modification, the length of the dry distillation spaces 121-123 is so large that the distance from the dry distillation spaces 121-123 to the front end surface 120b is short. Therefore, the length of the dry distillation space 123 is the largest. Thereby, the raw material X1 in the dry distillation space 121 has a temperature of about room temperature to 300 degrees. The raw material X1 in the dry distillation space 122 has a temperature of about 300 to 600 degrees. Moreover, the raw material X1 in the dry distillation space 123 has a temperature of about 600 to 1000 degrees.

  In addition, it is based on the following reasons that each carbonization space 121-123 is arrange | positioned as mentioned above. That is, the larger the temperature difference between the fluidized gas 130a and the raw material X1, the better the heat transfer efficiency. Therefore, the higher the temperature of the raw material X1, the longer it takes to raise the temperature of the raw material X1. For example, the time taken to raise the temperature of the raw material X1 from 300 degrees to 600 degrees is longer than the time taken to raise the temperature of the raw material X1 from room temperature to 300 degrees. Therefore, when it is desired to recover the dry distillation gas from the raw material X1 in a certain temperature range, it is necessary to set the dry distillation space according to the temperature range. Specifically, it is necessary to lengthen the carbonization space as the temperature range is wider and the lower limit of the temperature range is higher. Therefore, in the first modification, the lengths of the dry distillation spaces 121 to 123 are set as described above. The lengths of the dry distillation spaces 121 to 123 are, for example, about 1.4 m, 2.4 m, and 2.6 m, respectively. Further, the number and arrangement of the partition walls 190 are not limited to the above example. The number and arrangement of the partition walls 190 can be changed according to the composition of the dry distillation gas to be recovered.

[Second Modification]
Next, a second modification of the third embodiment will be described. FIG. 14 is a side cross-sectional view showing the configuration of the dry distillation apparatus 100 according to the second modification. The second modification is obtained by adding a partition wall 135 to the third embodiment.

  The partition wall 135 is provided in a portion of the plenum chamber 130 immediately below the partition wall 190. For example, in the example shown in FIG. 14, three partition walls 135 are provided in the plenum chamber 130. Thereby, the space in the plenum chamber 130 is divided into gas supply spaces 131 to 134. And fluidization gas 131a-134a is introduced into dry distillation space 121-124 from each gas supply space 131-134. The temperature and flow rate of the fluidizing gases 131a to 134a may be different from each other. For example, the temperature and flow rate of the fluidized gases 131a to 134a may be increased as the distance from the gas supply spaces 131 to 134 to the tip surface 120b is shorter. In this case, the temperature and flow rate of the fluidizing gas 134a are the largest. This is to increase the temperature difference between the temperature of the raw material X1 in the dry distillation space 124 and the fluidized gas 134a. According to the 2nd modification, fluidization gas 131a-134a of the flow according to the temperature of dry distillation spaces 121-124 and temperature can be supplied to dry distillation spaces 121-124. Note that the number of the partition walls 135 is not limited to that in FIG. 14, and it is needless to say that only one of the temperature and flow rate of the fluidizing gases 131 a to 134 a may be adjusted.

  In the second modification, the dry distillation space 124 may be a cooling space. In this case, the raw material X1 is carbonized at least before leaving the carbonization space 123. Further, the heat transfer tube 150 does not pass through the cooling space. Further, a cooling gas (for example, a non-flammable gas at room temperature to about 100 degrees) is introduced into the gas supply space 134.

[Third Modification]
Next, a third modification of the third embodiment will be described. FIG. 15 is a side sectional view showing the configuration of the dry distillation apparatus 100 according to the third modification. In the third modification, auxiliary partition walls 190 a are provided in the dry distillation spaces 121 to 124. The auxiliary partition wall 190 a has the same configuration as the partition wall 190, but a space is formed between the upper end portion and the upper end surface of the dry distillation furnace main body 120. That is, the auxiliary partition wall 190a plays a role of bringing the flow of the raw material X1 closer to the piston flow. According to the third modification, the dry distillation apparatus 100 can recover the dry distillation gases 181a to 184a having a desired composition, and can bring the flow of the raw material X1 closer to the piston flow.

  In each of the above-described embodiments, coal has been described as an example of coal to be distilled. However, the present invention is not limited to this, and the present invention is not limited to this and can be applied to organic materials in which carbonization gas and a carbonization product are generated by carbonization. Obviously, this is possible and can be applied to, for example, sewage sludge, biomass, or general waste, or a mixture thereof.

<Example 1>
Next, Example 1 will be described. Example 1 corresponds to the first embodiment. The first embodiment will be described with reference to FIG. In Example 1, coal was used as the raw material X1. Coal was dried in advance, and was put into the carbonization furnace main body 120 at room temperature. Moreover, the average particle diameter of coal was about 2 mm. When this coal is carbonized at 800 ° C., theoretically, about 3700 kcal / Nm ³ of gas and about 7900 kcal / kg of tar are generated at a mass ratio of about 34% and 7%, respectively, with respect to the total mass of the coal. Coal was charged into the dry distillation furnace main body 120 at a rate of 25 t / h.

  The carbonization furnace main body 120 has a width of 1.0 m and a length of about 6.7 m, and does not include the partition wall 190. The static layer thickness was 0.3 m. Further, a part of the dry distillation gas generated by the dry distillation of the raw material X1 was combusted, and a gas having a low temperature was mixed with the combustion gas to generate a gas of 1000 ° C., which was used as the fluidizing gas 130a. The superficial velocity (corresponding to the flow rate) of the fluidizing gas 130a was 1 Nm / s. In addition, 200 straight tubes having a diameter of 5 cm were used as the heat transfer tubes 150. As the indirect heating gas 151, the same 1000 ° C. gas as the fluidizing gas 130a was used, and the flow rate was set to 6 Nm / s.

The raw material X1 was heated to about 800 ° C. by the above treatment. The calorific value of the dry distillation gas 180a was 1290 kcal / Nm ^{3 in} total of the gas and tar.

<Example 2>
Next, Example 2 will be described. Example 2 corresponds to a first modification of the third embodiment. Note that Example 2 also serves as an example of the second embodiment. This is because the second embodiment and the third embodiment are common in that a partition wall 190 is provided in the dry distillation furnace main body 120.

  A second embodiment will be described with reference to FIG. Example 2 is the same as Example 1 except for the following points. That is, the lengths of the carbonization spaces 121 to 123 were set to about 1.4 m, 2.4 m, and 2.6 m, respectively. Therefore, the total length of the carbonization furnace main body 120 was 6.4 m, which was shorter than that of Example 1.

  In Example 2, the temperature of the opening 191a (the opening 191 disposed between the dry distillation spaces 121 and 122) was about 300 ° C. The temperature of the opening 191b (opening 191 disposed between the dry distillation spaces 122 and 123) was about 600 ° C. The temperature of the dry distillation product outlet 170 was about 800 ° C. The combustible dry distillation gas 181a was hardly recovered from the dry distillation gas outlet 181.

However, combustible dry distillation gas 182a was recovered from the dry distillation gas outlet 182. The dry distillation gas 182a contained a combustible gas containing a large amount of methane and carbon monoxide, tar, and fluidized gas. The calorific value of the dry distillation gas (that is, the calorific value when the combustible gas is mixed with tar, product water, and fluidizing gas) was about 2260 kcal / Nm ³ .

The combustible gas contained methane, carbon monoxide, and hydrogen in a volume ratio with respect to the total volume of the combustible gas of 18%, 32%, and 9%, respectively. Therefore, the calculated lower heating value of only the combustible gas was about 3600 kcal / Nm ³ .

  Further, dry distillation gas containing hydrogen and fluidizing gas was recovered from the dry distillation gas outlet 183. The dry distillation gas 183a contained 15% of hydrogen by volume ratio with respect to the total volume of the dry distillation gas 183a. Note that the dry distillation gas 183a includes 68% of hydrogen in a volume ratio with respect to the total volume of the dry distillation gas 183a in the calculation in a state where the fluidizing gas 130a is excluded. Therefore, in the second embodiment, it is possible to selectively use the dry distillation gas such that the dry distillation gas 182a is used as the heat source of the combustion apparatus 200 and the dry distillation gas 183a having a high hydrogen ratio is used as the chemical raw material.

<Comparative example>
Next, a comparative example will be described. FIG. 16 shows a dry distillation apparatus 1000 according to a comparative example. As shown in FIG. 16, the carbonization apparatus 1000 is obtained by removing the heat transfer tube 150 from the first embodiment. The carbonization furnace main body 120 has a width of 1.0 m and a length of about 6.7 m, and does not include the partition wall 190. The static layer thickness was 0.3 m. In addition, a gas having a low temperature was mixed with the dry distillation gas generated by the dry distillation of the raw material X1, thereby generating a gas of 1000 ° C., which was used as the fluidizing gas 130a. The superficial velocity (corresponding to the flow rate) of the fluidizing gas 130a was set to 2 Nm / s in order to raise the coal temperature to 800 ° C. as in the example.

By the above treatment, the raw material X1 was heated to about 800 ° C., but the calorific value of the dry distillation gas 180a was only 750 kcal / Nm ³ in total of the gas and tar.

<Evaluation>
Comparing Examples 1 and 2 and the comparative example, in Examples 1 and 2, the raw material X1 could be heated by the fluidizing gas 130a having a smaller flow rate. Further, in Examples 1 and 2, the calorific value of the dry distillation gas 180a was greatly improved as compared with the comparative example. Moreover, in Example 2, the full length of the dry distillation furnace main body 120 was able to be shortened rather than the comparative example. When the flow rate of the fluidized gas 130a in the first and second embodiments is the same as that in the comparative example, in the first and second embodiments, the length of the dry distillation furnace main body 120 is significantly shorter than that in the comparative example. Can do. As a result, in Examples 1 and 2, the floor area of the carbonization furnace main body 120 can be significantly reduced.

  The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings, but the present invention is not limited to such examples. It is obvious that a person having ordinary knowledge in the technical field to which the present invention pertains can come up with various changes or modifications within the scope of the technical idea described in the claims. Of course, it is understood that these also belong to the technical scope of the present invention.

DESCRIPTION OF SYMBOLS 100 Carbonization apparatus 110 Carbonization furnace 120 Carbonization furnace main body 130 Plenum chamber 130a Fluidization gas 140 Dispersion plate 150 Heat transfer tube 151 Heat medium for indirect heating (gas for indirect heating)
160 Raw material inlet 170 Drying product outlet 180 Drying gas outlet 190 Bulkhead 191 Opening

Claims (6)

It has a fluidized bed in which a heat transfer tube for passing a heat medium is installed, and the organic raw material is fluidized by a fluidizing gas and directly heated by the heat of the gas, and indirectly through the heat transfer tube by the heat of the heat medium. A carbonization furnace for carbonizing the raw material to produce a carbonization gas and a solid carbonization product by heating;
A raw material charging port provided on one side surface of the carbonization furnace, and the raw material is charged into the carbonization furnace;
A dry distillation apparatus comprising: a dry distillation product discharge port provided at a portion facing the fluidized bed on the other side surface of the dry distillation furnace, and discharging the raw material subjected to dry distillation. In the fluidized bed, at least one partition wall provided so as to suppress the progress of the raw material in a direction connecting the one side surface and the other side surface;
The dry distillation apparatus according to claim 1, further comprising: an opening formed below the partition wall through which the raw material can pass. In the fluidized bed, the one side surface and the other side surface of the dry distillation gas generated by dry distillation of the raw material are suppressed while the progress of the raw material in the direction connecting the one side surface and the other side surface is suppressed. At least one partition wall provided to block movement in the direction connecting
The carbonization apparatus according to claim 1, further comprising: a carbonization gas discharge port that is provided in each carbonization space in the carbonization furnace partitioned by the partition wall and exhausts carbonization gas generated in the carbonization space. Introducing an organic material from one side of a dry distillation furnace having a fluidized bed in which a heat transfer tube for passing a heat medium is installed;
The raw material is fluidized by a fluidizing gas and directly heated by the heat of the gas, and indirectly heated through a heat transfer tube by the heat of the heat medium, thereby dry-distilling the raw material;
A step of discharging the carbonized raw material from a carbonization product discharge port provided in a portion of the other side surface of the carbonization furnace facing the fluidized bed. Advancing the raw material toward the dry distillation product outlet;
Suppressing the progress of the raw material in a direction connecting the one side surface and the other side surface by a partition;
And introducing the raw material into an opening formed below the partition wall. The raw material in each dry distillation space in the dry distillation furnace partitioned by the partition provided so as to block movement of the dry distillation gas generated by the dry distillation of the raw material in a direction connecting the one side surface and the other side surface A step of carbonizing,
6. The carbonization method according to claim 5, further comprising a step of discharging a carbonization gas generated in each carbonization space from a carbonization gas outlet provided in each carbonization space.

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