JP6834387B2 - Fluidized bed system - Google Patents

Description

The present disclosure relates to a fluidized bed system for burning or gasifying raw materials.

As a technique for gasifying raw materials such as coal and biomass, fluidized gas is introduced from the bottom of a storage tank containing a fluidized medium at about 700 ° C. to 900 ° C. to form a fluidized bed of the fluidized medium, and the raw materials are further stored. A gasification furnace has been developed in which the raw material is gasified in the fluidized bed by putting it in a tank.

The fluid medium is generally composed of silica sand. Therefore, when the raw material contains an alkali metal, the silica (SiO ₂ ) contained in the silica sand reacts with the alkali metal to form a composite oxide. Since this composite oxide melts at about 800 ° C., the fluidized medium agglomerates (aggregates) due to the melted composite oxide in the gasification furnace. Then, the fluidized medium may cause a fluidized bed, the fluidized bed may not be formed, or the gasifier itself or the equipment connected to the gasifier may be blocked by the aggregated fluidized medium.

Therefore, a technique has been developed in which an additive that raises the melting temperature of the composite oxide itself by reacting with the composite oxide is introduced into the gasification furnace to suppress aggregation of the flow medium in the gasification furnace (). For example, Patent Document 1).

Japanese Unexamined Patent Publication No. 2011-219505

Conventionally, the presence or absence of agglomeration of a fluid medium has been visually detected or detected by a change in temperature distribution or pressure loss. In other words, it was not possible to take measures against aggregation until the fluid medium aggregated. Therefore, even if the additive is added after the agglutination of the flow medium, it may take time to eliminate the agglutination, or the additive may not be distributed and some parts may not be agglutinated. Therefore, there is a need for the development of a technique capable of predicting agglutination of a fluid medium in advance.

In view of such problems, the present disclosure aims to provide a fluidized bed system capable of predicting agglomeration of fluidized media in advance.

In order to solve the above problems, the fluidized bed system according to one aspect of the present disclosure includes a combustion furnace, a cyclone connected to the downstream side of the combustion furnace, and a first seal pot connected to the downstream side of the cyclone. The viscosities of the gasification furnace connected to the downstream side of the first seal pot, the second seal pot connected to the downstream side of the gasification furnace, and the fluidized bed formed in the first seal pot. A viscosity measuring unit to be measured and a viscosity control unit that performs a process of not increasing the viscosity of the fluidized bed formed in the gasification furnace when the viscosity measured by the viscosity measuring unit exceeds a predetermined threshold value. Be prepared.

In order to solve the above problems, the fluidized bed system according to another aspect of the present disclosure includes a combustion furnace, a cyclone connected to the downstream side of the combustion furnace, and a first connected to the downstream side of the cyclone. The seal pot, the gasifier connected to the downstream side of the first seal pot, the second seal pot connected to the downstream side of the gasifier, the cyclone, and the first seal pot are connected. A medium extraction unit for extracting a fluidized medium from a pipe, a fluidized bed chamber for forming a fluidized bed with the extracted fluidized bed, and a viscosity measuring unit for measuring the viscosity of the fluidized bed formed in the fluidized bed chamber. A viscosity control unit is provided which performs a process of not increasing the viscosity of the fluidized bed formed in the gasification furnace when the viscosity measured by the viscosity measuring unit becomes equal to or higher than a predetermined threshold value.

It is possible to predict the agglutination of the flow medium in advance.

It is a figure explaining the fluidized bed system which concerns on 1st Embodiment. It is a figure explaining the 1st seal pot. It is a figure explaining the viscosity measuring part. It is a figure explaining the relationship between the viscosity of a fluidized bed, and the gas ray velocity at the start of fluidization. The fluidized bed system according to the second embodiment.

An embodiment of the present disclosure will be described in detail below with reference to the accompanying drawings. The dimensions, materials, other specific numerical values, etc. shown in such an embodiment are merely examples for facilitating understanding, and do not limit the present disclosure unless otherwise specified. In the present specification and drawings, elements having substantially the same function and configuration are designated by the same reference numerals to omit duplicate description, and elements not directly related to the present disclosure are omitted from the illustration. To do.

(First Embodiment: Fluidized Bed System 100)
FIG. 1 is a diagram illustrating a fluidized bed system 100 according to the first embodiment. As shown in FIG. 1, the fluidized bed system 100 includes a fluidized bed reactor 110, a viscosity measuring unit 120, and a viscosity control unit 130. In FIG. 1, the flow of substances such as raw materials, fluid media, water vapor, gasified gas, and flue gas is indicated by solid arrows, and the signal flow is indicated by dashed arrows.

As shown in FIG. 1, the fluidized bed reactor 110 includes a combustion furnace 210, a first pipe 212, a cyclone 220, a second pipe 222, a first seal pot 230, a third pipe 232, and gasification. It includes a furnace 240, a fourth pipe 242, a second seal pot 250, a fifth pipe 252, a heat exchanger 260, and a dust removal device 262.

In the present embodiment, the fluidized bed reactor 110 is a circulating fluidized bed gasification system, and has a combustion furnace 210, a first pipe 212, a cyclone 220, a second pipe 222, a first seal pot 230, and a third pipe 232. A fluidized bed is circulated as a heat medium in the gasification furnace 240, the fourth pipe 242, the second seal pot 250, and the fifth pipe 252. The fluid medium is composed of silica sand having a particle size of about 300 μm.

The combustion furnace 210 has a tubular shape, and the first pipe 212 is connected to the upper part and the fifth pipe 252 is connected to the lower part. Fuel and a fluid medium are introduced into the combustion furnace 210 through the fifth pipe 252. In the combustion furnace 210, the fuel is burned and the flow medium is heated to about 900 ° C. to 1000 ° C. The heated fluid medium and combustion exhaust gas are sent to the cyclone 220 through the first pipe 212.

The cyclone 220 solid-gas separates the mixture of the flow medium introduced from the combustion furnace 210 and the combustion exhaust gas through the first pipe 212. The high-temperature fluid medium separated by the cyclone 220 is introduced into the first seal pot 230 through the second pipe 222 connecting the bottom of the cyclone 220 and the first seal pot 230.

The first seal pot 230 (loop seal) fluidizes the fluidized medium introduced from the cyclone 220 through the second pipe 222 to form a fluidized bed.

FIG. 2 is a diagram illustrating the first seal pot 230. The first seal pot 230 includes a storage tank 230a for accommodating a flow medium and a wind box 230b provided below the storage tank 230a.

An inlet 230c is formed on the ceiling of the storage tank 230a. A second pipe 222 is connected to the inlet 230c. An outlet 230d is formed on the side surface of the storage tank 230a. A third pipe 232 is connected to the outlet 230d. A partition plate 230e extending vertically downward from the ceiling is provided in the storage tank 230a. The partition plate 230e divides the inside of the storage tank 230a into a region 230f where the inlet 230c is formed and a region 230g where the outlet 230d is formed. Further, the tip of the partition plate 230e extends vertically downward from the lower end of the outlet 230d. The configuration including the partition plate 230e can prevent the inflow of the combustion exhaust gas from the cyclone 220 to the gasification furnace 240 and the inflow of the gasification gas from the gasification furnace 240 to the cyclone 220.

The upper part of the air box 230b is composed of a breathable dispersion plate, and also functions as the bottom surface of the storage tank 230a. Water vapor is supplied to the air box 230b from a water vapor supply unit (not shown). The water vapor supplied to the air box 230b is introduced into the storage tank 230a from the bottom surface (dispersion plate) of the storage tank 230a. Therefore, the fluidized medium introduced from the cyclone 220 through the second pipe 222 is fluidized by water vapor, and a bubble fluidized bed is formed in the storage tank 230a.

Then, when the vertical position of the fluidized bed becomes higher with the introduction of the further fluidized medium from the cyclone 220, the fluidized medium overflows the lower end of the outlet 230d and is introduced into the gasifier 240 through the third pipe 232. The Rukoto.

The flow medium introduced from the first seal pot 230 (third pipe 232) is fluidized by the fluidized gas (for example, steam) in the gasification furnace 240. More specifically, the gasification furnace 240 includes a storage tank 240a for accommodating a flow medium and a wind box 240b provided below the storage tank 240a. The upper part of the air box 240b is composed of a breathable dispersion plate, and also functions as the bottom surface of the storage tank 240a. Water vapor is supplied to the air box 240b from a water vapor supply unit (not shown). The water vapor supplied to the air box 240b is introduced into the storage tank 240a from the bottom surface (dispersion plate) of the storage tank 240a. Therefore, the high-temperature fluidized medium introduced from the first seal pot 230 is fluidized by water vapor, and a bubble fluidized bed is formed in the storage tank 240a.

Further, raw materials such as coal and biomass are put into the gasification furnace 240 (containment tank 240a). The charged raw material is gasified by the heat of the flow medium at about 700 ° C. to 900 ° C., whereby gasification gas (synthetic gas) is generated. The generated gasification gas is sent to the subsequent equipment.

Then, the fluidized medium in the gasification furnace 240 is introduced into the second seal pot 250 through the fourth pipe 242 connecting the gasification furnace 240 and the second seal pot 250.

The second seal pot 250 (loop seal) fluidizes the fluidized medium introduced from the gasifier 240 through the fourth pipe 242 to form a fluidized bed. The second seal pot 250 prevents the inflow of gasified gas from the gasification furnace 240 to the combustion furnace 210 and the inflow of combustion exhaust gas from the combustion furnace 210 to the gasification furnace 240. Since the configuration of the second seal pot 250 is substantially the same as that of the first seal pot 230, detailed description thereof will be omitted here. The flow medium overflowing from the second seal pot 250 is returned to the combustion furnace 210 through the fifth pipe 252.

As described above, in the fluidized bed reactor 110 according to the present embodiment, the fluidized medium is the combustion furnace 210, the first pipe 212, the cyclone 220, the second pipe 222, the first seal pot 230, the third pipe 232, and gasification. The reactor 240, the fourth pipe 242, the second seal pot 250, and the fifth pipe 252 are moved in this order and introduced into the combustion furnace 210 again to circulate them.

The combustion exhaust gas separated by the cyclone 220 is heat exchanged (cooled) by the heat exchanger 260 (boiler), dedusted by the dust removal device 262, and then sent to the outside.

Further, the residue of the raw material remaining after the raw material is gasified in the gasification furnace 240 is introduced into the combustion furnace 210 through the fifth pipe 252. Therefore, the residue of the raw material introduced from the gasification furnace 240 into the combustion furnace 210 is used as fuel in the combustion furnace 210.

As described above, the fluidized medium is heated to about 900 ° C. to 1000 ° C. in the combustion furnace 210, and a fluidized bed of the fluidized medium of about 700 ° C. to 900 ° C. is formed in the gasification furnace 240. Then, the raw material is put into the gasification furnace 240 to generate gasification gas.

Here, when the raw material contains an alkali metal (for example, sodium or potassium), the silica contained in the silica sand constituting the flow medium reacts with the alkali metal in the combustion furnace 210 and the gasification furnace 240, and the alkali metal reacts with each other. A composite oxide is produced. This composite oxide melts at about 800 ° C. Therefore, in the gasification furnace 240, the fluidized medium is aggregated by the molten composite oxide. In the combustion furnace 210, since the fluidized bed forms a dilute fluidized bed, the moving speed of the fluidized medium is higher than that of the gasification furnace 240 in which the bubble fluidized bed of the fluidized medium is formed. Therefore, in the combustion furnace 210, although the composite oxide melts, the fluid medium hardly aggregates.

If the fluidized medium is agglomerated, the fluidized medium causes poor flow, and the fluidized bed is not formed in the first seal pot 230, the gasifier 240, and the second seal pot 250, or the second pipe 222 and the first seal are formed. The pot 230, the third pipe 232, the gasifier 240, the fourth pipe 242, the second seal pot 250, and the fifth pipe 252 may be blocked by the agglomerated fluid medium.

Therefore, the viscosity of the fluidized bed is measured by the viscosity measuring unit 120, and the aggregation of the fluidized medium is predicted in advance.

Returning to FIG. 1, the viscosity measuring unit 120 measures the viscosity of the fluidized bed formed in the first seal pot 230. The raw material charged into the gasification furnace 240 will be consumed in the combustion furnace 210. Therefore, the viscosity of the fluidized layer of the fluidized medium itself can be measured by the configuration in which the viscosity measuring unit 120 measures the viscosity of the first seal pot 230.

FIG. 3 is a diagram illustrating the viscosity measuring unit 120. FIG. 3A is a diagram illustrating a usage pattern of the viscosity measuring unit 120. FIG. 3B is a diagram illustrating the shape of the cup 122.

As shown in FIG. 3A, the viscosity measuring unit 120 includes a cup 122, a rotating shaft 124, a motor 126, and a viscosity conversion unit 128. Since the viscosity measuring unit 120 can apply the existing technology of the rotational viscometer other than the shape of the cup 122, detailed description thereof will be omitted here.

The cup 122 is arranged in the fluidized bed formed in the region 230 g in the first seal pot 230. The cup 122 includes a disk 122a and a cylindrical main body 122b erected from the outer periphery of the disk 122a. The cup 122 is installed in the flow tank so that the disk 122a is located vertically above.

The rotating shaft 124 is connected to the center of the disk 122a of the cup 122. The motor 126 rotates the cup 122 by rotating the rotation shaft 124. The viscosity conversion unit 128 measures the torque applied to the rotating shaft 124 and converts the torque into viscosity. Information indicating the viscosity obtained by the viscosity conversion unit 128 is transmitted to the viscosity control unit 130.

As shown in FIG. 3B, in the present embodiment, a plurality of holes 122c are formed in the disk 122a of the cup 122. By having the holes 122c, it is possible to avoid a situation in which the water vapor supplied from the air box 240b stays in the cup 122 and hinders the introduction of the flow medium into the cup 122. Therefore, it is possible to stably measure the viscosity of the fluidized bed.

Returning to FIG. 1, the viscosity control unit 130 is composed of a semiconductor integrated circuit including a CPU (Central Processing Unit). The viscosity control unit 130 reads a program, parameters, and the like for operating the CPU itself from the ROM, and manages and controls the fluidized bed system 100 in cooperation with the RAM as a work area and other electronic circuits. In the present embodiment, the viscosity control unit 130 determines whether or not the viscosity measured by the viscosity measurement unit 120 is equal to or higher than a predetermined threshold value. Here, the threshold value is a value determined by the design value of the fluidized bed reactor 110 and is held in a memory (not shown).

Specifically explaining the determination of the threshold value, when the viscosity of the fluidized bed is high, the fluidization start gas ray velocity (minimum fluidization velocity) Umf becomes large. FIG. 4 is a diagram for explaining the relationship between the viscosity of the fluidized bed and the fluidization start gas linear velocity Umf.

Potassium hydroxide is added to the fluidized medium as an alkali metal to form a fluidized bed with the superficial gas linear velocity U0 / fluidized start gas linear velocity Umf constant (2.0), and the viscosity of the fluidized bed and the fluidized gas. The flow rate of (water vapor) and the pressure loss of the fluidized bed were measured. The addition rates of potassium hydroxide were 0.0% (indicated by white circles in FIG. 4), 0.6% (indicated by white triangles in FIG. 4), and 1.1% (indicated by white squares in FIG. 4). The viscosity and flow rate were measured at 1.7% (indicated by black circles in FIG. 4) and 2.2% (indicated by black triangles in FIG. 4). In addition, the pressure loss and the flow rate were measured when the addition rate of potassium hydroxide was 0.0%, 0.6%, and 1.1%.

The relationship between the viscosity of the fluidized bed and the flow rate of the fluidized gas obtained as a result is shown in FIG. 4 (a). The relationship between the pressure loss in the fluidized bed and the flow rate of the fluidized gas is shown in FIG. 4 (b).

As shown in FIG. 4A, the viscosity decreases as the flow rate of the fluidized gas increases, regardless of the addition rate of potassium hydroxide. Then, when the predetermined flow rate is reached, the viscosity becomes constant. If the flow rate of the fluidized gas is small, the fluidized medium does not fluidize, so the viscosity is high. However, when the flow rate of the fluidized gas reaches a predetermined flow rate, the fluidized medium fluidizes and begins to form a fluidized bed, so that the viscosity decreases. That is, the flow rate of the fluidized gas when the viscosity becomes constant is the fluidization start gas linear velocity Umf.

Further, as shown in FIG. 4B, the pressure loss increases as the flow rate of the fluidized gas increases regardless of the addition rate of potassium hydroxide. Then, when the predetermined flow rate is reached, the pressure loss becomes constant. When the flow rate of the fluidized gas is small, the pressure loss is small because the fluidized gas passes through the fluidized medium without floating (fluidizing the fluidized medium). However, when the flow rate of the fluidized gas reaches a predetermined flow rate, the fluidized medium is floated to be fluidized to start forming a fluidized bed, so that the pressure loss increases. That is, the flow rate of the fluidized gas when the pressure loss becomes constant is the fluidization start gas linear velocity Umf.

Examining the fluidization start gas linear velocity Umf, as shown in FIGS. 4 (a) and 4 (b), the fluidization start gas linear velocity Umf increases as the addition rate of potassium hydroxide increases. Was confirmed.

On the other hand, the maximum permissible value of the flow rate of steam supplied by the air box 240b in the gasifier 240 is determined by the design. Therefore, the threshold value is set to the viscosity of the fluidized bed in which the fluidization start gas linear velocity Umf is a predetermined value equal to or less than the maximum allowable value.

By determining whether or not the viscosity of the fluidized bed exceeds the threshold value by the viscosity control unit 130, it is possible to predict the aggregation of the fluidized medium in advance.

Then, when the viscosity measured by the viscosity measuring unit 120 becomes equal to or higher than the threshold value, the viscosity control unit 130 performs a process of not increasing the viscosity of the fluidized bed. The viscosity control unit 130, for example, extracts a part of the fluidized medium from the fluidized bed reactor 110, cleans it, and returns the washed fluidized bed to the fluidized bed reactor 110. Further, the viscosity control unit 130 may partially extract the fluidized medium from the fluidized bed reactor 110 and introduce a new fluidized medium (not containing the composite oxide). Further, the viscosity control unit 130 may introduce an additive for raising the melting point of the composite oxide into the fluidized bed reactor 110. Further, the viscosity control unit 130 may stop the operation of the fluidized bed reactor 110.

As described above, according to the fluidized bed system 100 according to the present embodiment, the aggregation of the fluidized medium can be predicted in advance by measuring the viscosity of the fluidized bed. As a result, it is possible to avoid a situation in which the fluidized bed system 100 malfunctions due to aggregation. Therefore, the fluidized bed reactor 110 can be operated stably.

The frequency of determination by the viscosity control unit 130 (or the frequency of measurement of viscosity by the viscosity measurement unit 120) is determined by the concentration of the alkali metal contained in the raw material, the amount of the raw material input per unit time, and the addition rate of the alkali metal. It is determined based on the corresponding fluidization start gas ray velocity Umf and the threshold value. The relationship between the addition rate of the alkali metal and the fluidization start gas linear velocity Umf differs depending on the type of the alkali metal. Therefore, for example, a map in which the addition rate of the alkali metal and the fluidization start gas ray velocity Umf are associated with each alkali metal is stored in a memory (not shown). Then, the viscosity control unit 130 refers to the map and derives the time until the viscosity reaches the threshold value based on the type and concentration of the alkali metal contained in the raw material and the input amount of the raw material per unit time. To do. Then, the viscosity control unit 130 performs the above determination process at the time interval from the previous process of not increasing the viscosity of the fluidized bed to the derived time.

(Second Embodiment: Fluidized Bed System 300)
FIG. 5 is a diagram illustrating the fluidized bed system 300 according to the second embodiment. As shown in FIG. 5, the fluidized bed system 300 includes a fluidized bed reactor 110, a medium extraction unit 310, a fluidized bed chamber 320, a viscosity measuring unit 120, and a viscosity control unit 130. .. In FIG. 5, the flow of substances such as raw materials, fluid media, water vapor, gasified gas, and flue gas is indicated by solid arrows, and the signal flow is indicated by dashed arrows. Further, the components substantially the same as those of the fluidized bed system 100 are designated by the same reference numerals and the description thereof will be omitted.

The medium extraction unit 310 includes a discharge pipe 312 and a valve 314. One end of the discharge pipe 312 is connected to the second pipe 222 (specifically, a portion of the second pipe 222 that is inclined from vertically upward to vertically downward), and the other end is a fluidized bed chamber 320 (accommodation tank). ) Is a pipe connected to. The valve 314 is composed of, for example, a butterfly valve and is provided in the discharge pipe 312. When the valve 314 is opened, the fluidized medium temporarily retained in the second pipe 222 is discharged to the fluidized bed chamber 320 through the discharge pipe 312 under its own weight. That is, when the valve 314 is opened, the flow medium is pulled out from the second pipe 222.

The fluidized bed chamber 320 is configured to include a storage tank for accommodating the fluidized medium and a wind box provided below the storage tank. The upper part of the air box is composed of a breathable dispersion plate, which also functions as the bottom surface of the storage tank. Water vapor is supplied to the air box. The water vapor supplied to the air box is introduced into the storage tank from the bottom surface (dispersion plate) of the storage tank. Therefore, the fluidized medium introduced from the medium extraction unit 310 is fluidized by water vapor, and a bubble fluidized bed is formed in the storage tank.

Further, in the present embodiment, the viscosity measuring unit 120 measures the viscosity of the fluidized bed formed in the fluidized bed chamber 320.

Also in the fluidized bed system 300 according to the present embodiment, the aggregation of the fluidized medium can be predicted in advance by measuring the viscosity of the fluidized bed. Further, since the fluidized bed is extracted from the fluidized bed reactor 110 and the viscosity of the fluidized bed is measured, the aggregation of the fluidized bed is predicted in advance even when the viscometer cannot be installed in the fluidized bed reactor 110. Is possible.

Further, the raw material charged into the gasification furnace 240 will be consumed in the combustion furnace 210. Therefore, the viscosity of the fluidized bed of the fluidized medium itself can be measured by the configuration in which the fluidized medium is extracted from the second pipe 222. In addition, it is possible to avoid a situation in which the raw material (residue of the raw material) is discharged to the outside.

Although the embodiments have been described above with reference to the accompanying drawings, it goes without saying that the present disclosure is not limited to such embodiments. It is clear that a person skilled in the art can come up with various modifications or modifications within the scope of the claims, and it is understood that they also naturally belong to the technical scope.

For example, in the above-described first embodiment, the configuration in which the viscosity measuring unit 120 measures the viscosity of the first seal pot 230 has been described as an example. However, the viscosity measuring unit 120 is formed in the viscosity of the portion where the fluidized bed is formed in the fluidized bed reactor 110, specifically, the bubble fluidized bed formed in the lower part of the combustion furnace 210, the first seal pot 230. The viscosity of any one or more of the fluidized bed formed in the bubble fluidized bed, the bubble fluidized bed formed in the gasification reactor 240, and the bubble fluidized bed formed in the second seal pot 250 may be measured.

Further, in the above embodiment, the case where the fluidized bed reactor 110 is a circulating fluidized bed type gasification system has been described as an example. However, the structure of the fluidized bed reactor 110 is not limited as long as it can form a fluidized bed of a fluidized medium and burn or gasify a raw material containing an alkali metal by the fluidized bed.

Further, in the second embodiment, the configuration in which the medium extraction unit 310 extracts the flow medium from the second pipe 222 has been described as an example. However, the medium extraction unit 310 is not limited in the extraction position as long as the fluidized medium can be extracted from the fluidized bed reactor 110. For example, the combustion furnace 210, the first pipe 212, the cyclone 220, the second pipe 222, and the first The fluidized medium may be extracted from any one or more of the 1 seal pot 230, the 3rd pipe 232, the gasifier 240, the 4th pipe 242, the 2nd seal pot 250, and the 5th pipe 252.

The present disclosure can be used in fluidized bed systems that burn or gasify raw materials.

100 Fluidized bed system 110 Fluidized bed reactor 120 Viscosity measuring unit 130 Viscosity control unit 210 Combustion furnace 220 Cyclone 230 First seal pot 240 Gasifier 250 Second sealed pot 300 Fluidized bed system 310 Medium extraction unit 320 Fluidized bed chamber

Claims (2)

Combustion furnace and
With the cyclone connected to the downstream side of the combustion furnace,
The first seal pot connected to the downstream side of the cyclone and
A gasifier connected to the downstream side of the first seal pot and
A second seal pot connected to the downstream side of the gasifier and
A viscometer measuring unit for measuring the viscosity of the fluidized bed formed in the first seal pot,
When the viscosity measured by the viscosity measuring unit exceeds a predetermined threshold value, a viscosity control unit that performs a treatment that does not increase the viscosity of the fluidized bed formed in the gasification furnace.
Fluidized bed system with. Combustion furnace and
With the cyclone connected to the downstream side of the combustion furnace,
The first seal pot connected to the downstream side of the cyclone and
A gasifier connected to the downstream side of the first seal pot and
A second seal pot connected to the downstream side of the gasifier and
A medium extraction portion for extracting a flow medium from a pipe connecting the cyclone and the first seal pot,
A fluidized bed chamber that forms a fluidized bed with the extracted fluidized medium,
A viscometer measuring unit for measuring the viscosity of the fluidized bed formed in the fluidized bed chamber,
When the viscosity measured by the viscosity measuring unit exceeds a predetermined threshold value, a viscosity control unit that performs a treatment that does not increase the viscosity of the fluidized bed formed in the gasification furnace.
Fluidized bed system with.

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