WO2004016716A1

WO2004016716A1 - Gasification furnace

Info

Publication number: WO2004016716A1
Application number: PCT/JP2003/010267
Authority: WO
Inventors: Kei Matsuoka; Tatsuo Tokudome; Shugo Hosoda; Seiichiro Toyoda
Original assignee: Ebara Corporation
Priority date: 2002-08-15
Filing date: 2003-08-12
Publication date: 2004-02-26
Also published as: AU2003255009A1; JPWO2004016716A1; JP4283222B2

Abstract

A gasification furnace (101) having increased control characteristics, comprising a gasification chamber (1) for flowing hot flow medium (c), forming a fluidized bed, and gasifying treated matter (a), a char combustion chamber (2) for flowing the flow medium (c), forming the fluidized bed, and burning char (h) generated by the gasification of the treated matter in the chamber (1) to heat the flow medium and a control device (6) for controlling the temperature of the gasification chamber or the char combustion chamber by controlling the intensity of flow in a weak flow state to control the amount of the flow medium circulating between the chambers, wherein the chambers (1) and (2) are separated from each other through partition walls (11) and (15) to prevent gas from flowing therebetween over the boundary surface of the fluidized bed, communication ports (21) and (25) allowing the chamber (1) to communicate with the chamber (2) and having upper end heights of below the boundary surface are formed in the lower parts of the partition walls, the flow state of the flow medium (c) near the communication port of one chamber of the chambers (1) and (2) on both sides of the communication ports is set stronger than the flow state of the flow medium near the communication port of the other chamber to move the flow medium (c) from a weak flow state to a strong flow state through the communication ports.

Description

Description Gasification furnace Technical field

The present invention, _t background art various waste and solid fuel such as a gas furnace for gasifying by pyrolysis

In a fluidized-bed gasifier that pyrolyzes various wastes and solid fuels to gasify it. Among the factors related to the reaction, for example, to change the bed temperature of the fluidized bed of the gasifier, gasification The flow rate of oxygen supplied into the furnace or the flow rate of gas containing oxygen (for example, air) was changed.

However, when the supply of oxygen is increased, the amount of combustion gas contained in the product gas increases, and the calorific value of the product gas decreases. On the other hand, if the supply of oxygen is reduced, the amount of gasification residues such as char and tar increases, and the gasification efficiency decreases.

To cope with this, a gasification zone is provided for gasification of various wastes and solid fuels, and a combustion zone is provided for burning gasification residues such as char and tar generated by gasification. The heat of combustion is used for heat of gasification reaction in the gasification zone, and each of the gasification zone and the combustion zone is used as a fluidized bed apparatus, and the above-mentioned transfer of the gasification residue and heat is transferred via a fluidized medium. There is a method that employs an internal circulating fluidized bed gasifier.

In an internal circulating fluidized bed gasifier, the amount of fluidized medium particles to move smoothly from the gasification zone to the combustion zone and to the heat from the combustion zone to the gasification zone It is important to control precisely. However, in this conventional internal-circulating fluidized-bed gasifier, the amount of fluidizing gas supplied to the fluidized bed device needs to be greatly changed in order to control the movement amount of the fluidized medium particles. There was a problem that the operating conditions of the device changed significantly. In addition, there were situations in which it was desired to improve control easiness, control freedom, operation stability characteristics, control accuracy, control width, and control speed. SUMMARY OF THE INVENTION The present invention has been made in view of the above-mentioned problems of the related art, and has as its object to provide an internal circulating fluidized bed gasifier having significantly improved control characteristics. Disclosure of the invention

In the present invention, for example, as shown in FIG. 1, a high temperature fluid medium c is caused to flow inside to form a gasification chamber fluidized bed having a first interface. And a gasification chamber 1 for gasifying the gas; a high-temperature fluidized medium c is caused to flow therein to form a fluidized bed of a combustion chamber having a second interface, and a gas generated by gasification in the gasification chamber 1 A combustion chamber for burning 1 h in the fluidized bed of the combustion chamber and heating a fluid medium c; and a gasification chamber 1 and a combustion chamber 2 of the combustion chamber are located at an interface between the respective fluidized beds. The upper part in the vertical direction is partitioned by partition walls 11 and 15 so that gas does not flow, and the gasification chamber 1 and the char combustion chamber 2 are located below the partition walls 11 and 15. The communication ports 21 and 25 communicate with each other, and the height of the upper end of each of the communication ports 21 and 25 is equal to or lower than the first interface and the second interface. A certain communication port 21, 25 is formed, and the flow in the vicinity of the communication port 21, 25 of one of the gasification chamber 1 and the char combustion chamber 2 sandwiching the communication port 21, 25. The fluidized state of the medium c is stronger than the fluidized state of the fluidized medium c near the communication ports 21 and 25 of the other chamber, and the weak fluidized state is provided through the communication ports 21 and 25. The fluidized medium c is configured to move from the fluidized state to the strong fluidized state; and by adjusting the flow strength of the weak fluidized state, the gasification chamber 1 and the char- A control device 6 is provided for controlling the temperature of the gasification chamber 1 or the combustion chamber 2 by controlling the amount of the fluid medium c flowing between the gasification chamber 1 and the gasification furnace 101. With the goal.

With this configuration, the gasification chamber 1, the combustion chamber 2, and the control device 6 are provided. By adjusting the strength of the flow in the weak fluidized state, the gasification chamber 1 and the gas chamber 1 are controlled. By controlling the amount of the fluid medium c flowing between the first combustion chamber 2 and the first combustion chamber 2, the temperature of the gasification chamber 1 or the first combustion chamber 2 can be controlled. The control device 6 may also adjust the strength of the strong fluidized state. The temperature of the gasification chamber 1 is typically the temperature of the gasification fluidized bed, and the temperature of the char combustion chamber 2 is typically the temperature of the fluidized bed. Also, since the strength of the flow in the weak fluidized state is adjusted, the amount of the fluid medium c The flow rate of fluidizing gas g1, g2, and g4 is small, and the temperature of gasification chamber 1 or combustion chamber 2 is controlled without significantly affecting other operating conditions. can do.

The fluidized bed is typically fluidized by a fluidizing gas g blown from the furnace bottom. The fluidization state can be adjusted by the blowing speed and the amount of the fluidizing gas g. Furnace bottom diffuser air device in 3: Place 1-3 5, a plurality of compartments _{la, lb, 2 a s 2} b, 4 may it divided into a. Control valves 61 to 65 for controlling the flow rates of the fluidizing gas g1, g2, g4 may be provided for each section where the amount of the fluidizing gas g1, g2, g4 is to be controlled. Control unit that controls the opening of control valves 6 1 to 65 of compartments 1 a, lb, 2 a, 2 b, and 4 a of gasification chamber 1 and channel combustion chamber 2 sandwiching communication ports 2 1 and 25 By adjusting with 6, the fluidization state can be adjusted by adjusting the blowing speed and the blowing amount of the fluidizing gas gl, g2, and g4.

For example, as shown in FIG. 1, the gasification furnace 101 includes a gasification chamber 1 for thermally decomposing an object a with a high-temperature fluidized medium c to generate a gas b and a charge h; A combustion chamber for heating the fluid medium c by burning the fuel h generated in 1; the fluid medium c is configured to circulate between the gasification chamber 1 and the combustion chamber 2 Further, a control device 6 for controlling the composition of the gas b generated in the gasification chamber 1 by adjusting the circulation amount of the fluid medium c may be provided.

With this configuration, the gasification chamber 1, the combustion chamber 2, and the control device 6 are provided. By adjusting the circulation amount of the fluid medium c, the gas generated in the gasification chamber 1 is adjusted. The composition of b can be controlled. The control device 6 may control the concentration of one type of gas, or may control the concentration ratio of a plurality of gases to a predetermined set value.

In the gasification furnace 101, for example, as shown in FIG. 1, a high-temperature fluidized medium c is caused to flow locally, thereby forming a gasification chamber fluidized bed having a first interface. A gasification chamber 1 for gasifying the object to be treated a; a high-temperature fluidized medium c is caused to flow therein to form a fluidized bed in a combustion chamber having a second interface, and the gasification in the gasification chamber 1 is performed. And a combustion chamber 2 for heating the fluid medium c by burning the generated h in the fluidized bed of the combustion chamber; and the gasification chamber 1 and the combustion chamber 2 floor The partition walls 11 and 15 prevent the flow of gas vertically above the interface between the gasification chamber 1 and the combustion chamber 2 at the bottom of the partition walls 11 and 15. Communication ports 21, 25 for communicating with the communication ports 21, 25, wherein the height of the upper ends of the communication ports 21, 25 is less than or equal to the first interface and the second interface. The fluidized state of the fluid medium c in the vicinity of the communication ports 21 and 25 of one of the gasification chamber 1 and the combustion chamber 2 sandwiching the communication port 21. The fluid medium c is stronger than the fluidized state of the fluid medium c near the communication ports 21 and 25 through the communication ports 21 and 25 and moves from the weak fluidized state to the fluidized state toward the strong fluidized state. c is configured to move; and further, by controlling the strength of the flow in the weak fluidized state, the flow flowing between the gasification chamber 1 and the char combustion chamber 2 is controlled. A control device 6 may be provided which controls the amount of the moving medium c to control the composition of the gas b generated by the gasification.

With this configuration, the gasification chamber 1, the combustion chamber 2, and the control device 6 are provided. By adjusting the strength of the flow in the weak fluidized state, the gasification chamber 1 and the gas chamber 1 are controlled. The composition of the gas b generated by gasification can be controlled by controlling the amount of the fluid medium c flowing between the combustion chambers 2. In addition, since the strength of the flow in the weak fluidized state is adjusted, the change in the flow rate of the fluidized gas g1, g2, and g4 generated to control the amount of the fluidized medium c is small, and the flow rate of the fluidized gas g1, g2, and g4 is small. The composition of the gas b generated from the gasification chamber 1 can be controlled without significant influence.

The gasifier 101 is, for example, as shown in FIG. 1, a heat recovery chamber 3 for introducing a fluid medium c from the char combustion chamber 2 and a fluid recovery medium c from the char combustion chamber 2. A heat recovery chamber 3 having a heat recovery device 41 for recovering heat; and a control device 6 for controlling the amount of heat recovery in the heat recovery device 41 by adjusting the strength of the flow in the heat recovery chamber 3. It may be provided.

With such a configuration, since the heat recovery chamber 3 having the heat recovery device 41 and the control device 6 are provided, the control device 6 controls the strength of the flow in the heat recovery chamber 3 so that the heat recovery device 3 is controlled. The amount of heat recovery in 4 1 can be controlled. The heat recovery chamber 3 is typically a heat recovery chamber 3 provided adjacent to the char combustion chamber 2. The heat recovery apparatus 41 typically includes an in-layer heat transfer tube 41. The heat recovery unit 41 typically heats the steam s 1 with the recovered heat. Control device 6 is steam s 1 The amount may be controlled.

When the gasifier 101 has a heat recovery chamber 3 provided in contact with the char combustion chamber 2, the flow of the char combustion chamber is between the char combustion chamber 2 and the heat recovery chamber 3. A partition wall 12 is provided to partition the fluidized bed of the bed, and an opening 22 is formed at the lower part of the partition wall 12. The fluid medium c of the chamber 1 is recovered from the upper part of the partition wall 12. Preferably, a circulating flow into chamber 3 and back through opening 22 to char combustion chamber 2 is formed: gasifier 101 is further equipped, for example, as shown in FIG. The control device 6 for controlling the heat recovery amount may control the heat recovery amount in the heat recovery device 41 and control the temperature of the first combustion chamber 2.

For example, as shown in FIG. 1, the gasification furnace 101 further includes a first pressure above the first interface of the gasification chamber 1 and a second pressure of the second combustion chamber 2. Pressure measuring devices 8 1, 8 2 for measuring the upper second pressure and the gas; the first discharge linear velocity of the gas b generated from the gasification chamber 1 discharged from the gasification chamber 1; Adjusting devices 78, 79 for adjusting the second discharge linear velocity of the combustion gas e generated from the chamber 2 and discharged from the combustion chamber 2; the first pressure and the second pressure with urchin configuration this it may also be _c be one and a control device 6 for controlling the urchin adjusting device 7 8, 7 9 I to a predetermined value the pressure difference between the pressure measuring device 81, 82 and Since the control device 6 is provided with the control devices 7 8 and 7 9 and the control device 6, the first pressure and the second pressure are measured by the pressure measurement devices 8 1 and 8 2, and the control device 7 8 , 79 adjust the first discharge linear velocity and the second discharge linear velocity, and the controller 6 controls the pressure difference between the first pressure and the second pressure to a predetermined value. The adjusting devices 78, 79 can be controlled.

Since the pressure difference between the first pressure and the second pressure can be set to a predetermined value, the effect of the pressure on the moving amount of the fluid medium particles between the gasification chamber 1 and the chamber 1 Can be suppressed to a constant value, and it becomes easy to precisely control the moving amount of the fluid medium particles. The predetermined value may be substantially equal to zero, or the control device 6 may control the adjusting devices 78 and 79 so that the first pressure and the second pressure become substantially equal. . This application was filed in Japanese Patent Application No. 200-23, filed on August 15, 2002 in Japan. No. 6997, the contents of which form a part of the present application.

The invention will be more fully understood from the detailed description below. Further areas of applicability of the present invention will become apparent from the detailed description provided hereinafter. However, the detailed description and specific examples are preferred embodiments of the invention and are described for illustrative purposes only. From this detailed description, various changes and modifications will be apparent to those skilled in the art without departing from the spirit of the invention.

Applicant does not intend to publish any of the described embodiments to the public, and discloses any of the disclosed modifications and alternatives that may not be literally included within the scope of the claims. It shall be part of the invention under the doctrine of equivalents. BRIEF DESCRIPTION OF THE FIGURES

Figure 1 is a block diagram conceptually showing the configuration of the integrated gasifier.

FIG. 2 is a schematic side sectional view of two chambers separated by a partition wall. It is classified into (a), (b) and (c) according to the form of the partition wall.

FIG. 3 is a diagram showing the relationship between the fluidizing gas velocity and the apparent bed viscosity.

FIG. 4 is a diagram showing the relationship between the fluidizing gas velocity and the moving amount of the fluidized medium.

FIG. 5 is a block diagram in a case where a predetermined weak fluidized region and a strong fluidized region are separated into a region near a predetermined opening and a remote region.

FIG. 6 is a diagram for explaining the definition of the circulation amount of the fluid medium circulating between the gasification chamber and the settling chamber.

FIG. 7 is a diagram for explaining the diffusion of the flowing medium between the gasification chamber and the settling chamber.

FIG. 8 is a diagram showing the relationship between the superficial velocity of the fluidized gas in the settling channel combustion chamber, the amount of heat transfer from the settling channel combustion chamber to the gasification chamber, and the amount of circulation (convection).

Fig. 9 is a graph showing the relationship between the superficial velocity of the fluidized gas in the settling channel combustion chamber and the amount of fluidized medium transferred from the settling channel combustion chamber to the gasification chamber (convection + diffusion).

FIG. 10 is a diagram for explaining the relationship between the fluidized bed height and the circulation amount. FIG. 11 is a diagram showing the relationship between the circulation ratio and the gasification chamber layer temperature in case 1. FIG. 12 is a diagram showing the relationship between the circulation ratio and the gasification chamber layer temperature in case 2. FIG. 13 is a diagram showing the relationship between the circulation ratio and the product gas composition.

FIG. 14 is a diagram showing the relationship between the circulation ratio and the H ₂ / CO ratio of the produced gas.

FIG. 15 is a diagram showing the relationship between the circulation ratio and the calorific value of the produced gas.

FIG. 16 is a diagram showing the relationship between the gasification chamber bed temperature and the gasification chamber outlet calorific value ratio. FIG. 17 is a diagram showing the relationship between the gasification chamber layer temperature and the cold gas efficiency.

FIG. 18 is a diagram showing the relationship between the circulation ratio and the calorific value of the generated gas.

FIG. 19 is a graph showing the relationship between the gasification chamber bed temperature and the rate at which carbon in the raw material transfers to tar.

FIG. 20 is a diagram showing the relationship between the amount of circulation and the rate at which carbon in the raw material transfers to the combustion chamber.

FIG. 21 is a graph showing the relationship between the gasification chamber bed temperature and the rate at which carbon in the raw material transfers to the combustion chamber.

FIG. 22 is a block diagram showing the configuration of the fluid medium supply device. BEST MODE FOR CARRYING OUT THE INVENTION

Hereinafter, embodiments of the present invention will be described with reference to the drawings.

FIG. 1 is a block diagram conceptually showing the configuration of an integrated gasifier 101 as a gasifier.

The integrated gasifier 101 has a gasification chamber 1 for pyrolysis and gasification of waste or solid fuel a as an object to be treated, and a chamber for burning one minute h generated in the gasification chamber 1. And a combustible gas generated in the gasification chamber 1 and a combustion gas e generated in the first combustion chamber 2 as an integrated gas. It is characterized in that it is supplied separately to a gas utilization device (not shown) at the subsequent stage of the gasification furnace 101. The char combustion chamber 2 is composed of the char combustion chamber body 5 and the sedimentation char combustion chamber.

(Flow medium settling chamber) 4. The integrated gasifier 101 is connected to a gasification chamber 1 and supplies a generated gas b generated in the gasification chamber 1 for supplying a generated gas b. Combustion gas generated in the combustion chamber body 5 And a combustion gas supply pipe 27 for supplying e. The integrated gasifier 101 further includes a gas composition measuring device 46 installed on the generated gas supply pipe 26 and measuring the gas composition of the generated gas b.

The integrated gasifier 101 is installed in the generated gas supply pipe 26 and controls the discharge linear velocity (first discharge linear velocity) of the generated gas b discharged from the generated gas supply pipe 26. A control valve 78 (for example, a damper) as a regulating device, and a discharge line speed (second discharge line) of the combustion gas e discharged from the combustion gas supply pipe 27 installed in the combustion gas supply pipe 27 And a control valve 79 (for example, a damper) as an adjusting device for adjusting the speed. The integrated gasifier 101 has a gasification chamber 1 and a char combustion chamber 2 that are responsible for the pyrolysis gasification and char combustion functions described above, respectively. A recovery chamber 3 is provided, and the gasification chamber 1, the char combustion chamber 2, and the heat recovery chamber 3 are housed in, for example, a cylindrical or rectangular furnace. The integrated gasifier 101 has a control device 6 that controls the control valves 61, 62, 63, 64, 65, 66, and 67 (61 to 67) described below, respectively. Is provided. The control device 6 also controls the control valves 78 and 79 described above. The gasification chamber 1, the combustion chamber 2, and the heat recovery chamber 3 are divided by partition walls 11 to 15.A fluidized bed that is a dense layer containing a high-temperature fluidized medium c is formed at the bottom of each. .

In the gasification chamber 1 and the combustion chamber main body 5, temperature measuring devices 42 and 43 for measuring the layer temperature of each dense layer are installed. In the present embodiment, the layer temperature of the rich layer in the gasification chamber 1 is the temperature of the gasification chamber 1, and the layer temperature of the rich layer in the main section 5 of the combustion chamber is the temperature of the combustion chamber 2. And The temperature measuring devices 42 and 43 send a temperature signal i 3 (partially indicated by a broken line in the figure) based on the measured temperature to the control device 6. The controller 6 controls the control valves 6 1 to 67 so that the temperature of the gasification chamber 1 and the temperature of the combustion chamber 2 become the set value based on the temperature signal i 3 as described later. In this case, the control device 6 is the temperature control device of the present invention. Further, the above-mentioned gas composition measuring device 46 sends a gas composition signal i 4 based on the measured gas composition to the control device 6. The control device 6 can be configured to control the control valves 61 to 67 so that the gas composition of the generated gas b becomes a set value based on the gas composition signal i4, as described later. In this case, the control device 6 This is a control device for controlling the composition of the steel. The thermometers 42 and 43 use thermocouples.

In the gasification chamber 1 and the combustion chamber main body 5, pressure measuring devices 81 and 82 are installed to measure the pressure in the freeboard sections. The pressure at the freeboard portion of the gasification chamber 1 is the first pressure of the present invention, and the pressure at the freeboard portion of the chamber 1 for the combustion chamber is the second pressure of the present invention. The freeboard section will be described later. The pressure measuring devices 8 1 and 8 2 send a pressure signal i 5 (partially indicated by broken lines in the figure) to the control device 6 based on the measured pressure. The control device 6 is configured to control the control valves 61 to 67 so that the pressure in the gasification chamber 1 and the pressure in the combustion chamber 2 are set to predetermined values based on the pressure signal i5. can do.

Gas composition signal i 4 is yo When _{_{H 2, CO, C 0 2}} , CH 4, H 2 mole ^_0/0, such as 0 les. The control device 6 obtains the gas composition signal i 4, calculates the H ₂ / CO ratio, etc., and further calculates the gas composition signal i 4 and the temperature signal i 3 of the product gas b measured by the temperature measuring device 42. It is preferable that the calorific value of the gas of the generated gas b be calculated based on the pressure signal i 5 of the generated gas b measured by the pressure measuring device 81.

The fluidized bed of each of the chambers 1 to 3, namely the fluidized bed of the gasification chamber, the fluidized bed of the combustion chamber and the fluidized bed of the fluidized bed of the heat recovery chamber, the furnace bottom which is the bottom of each of the chambers 1 to 3 In the fluid medium c, the fluidizing gas gl, g2, g3, g4 (the distinction between the fluidizing gas gl, g2, g3, and g4 will be described later. Is provided with a symbol g). That is, the gasification chamber 1 is provided with an air diffuser 31.32, the chamber 1 is provided with an air diffuser 33, 34, 35, and the heat recovery unit 3 is provided with an air diffuser 36. Is provided. Each of the diffusers 31 to 36 includes, for example, a perforated plate laid on the furnace bottom where the diffusers 3:! To 36 are installed, and the perforated plates are divided in the width direction. Is divided into several rooms.

The integrated gasifier 1 0 1 has a supply pipe 5 1 connected to the diffuser 3 1, a supply pipe 5 connected to the diffuser 3 2, a supply pipe 5 connected to the diffuser 3 3 5 3, a supply pipe 54 connected to the diffuser 34, a supply pipe 55 connected to the diffuser 35, and a supply pipe 56 connected to the diffuser 36. Each of the supply pipes 51 to 56 includes a control valve 61 to 66 as a control device and a flow measuring device 71 to 76, respectively. The mobilizing gas g is supplied to each of the air diffusers 31 to 36. The control valves 61 to 66 adjust the supply amount of the fluidizing gas g to each of the air diffusers 31 to 36. Therefore, each air diffuser 31 to 36 is in each room! In order to change the superficial velocity of each part in ~ 3 (in the figure, the location indicated by la and lb in room 1, the location indicated by 2a, 2b, 4a in room 2 and the location indicated by 3a in room 3) In addition, it is configured to change the flow velocity of the fluidizing gas g blown out from the chambers of the air diffusers 31 to 36 through the perforated plate. The flow measuring devices 71 to 76 are installed downstream of the control valves 61 to 66 of the supply pipes 5 :! to 56, respectively, and measure the flow rate of the fluidized gas g. Each of the control valves 61 to 66 receives a separate control signal i1 (partially indicated by a broken line in the figure) sent from the control device 6, and operates to change the opening. Flowmeter 7 :! To 76 send a flow signal i 2 (partially indicated by a broken line in the figure) based on the measured flow rate to the controller 6.

In addition, since the superficial velocity is relatively different in each part of the chambers 1 to 3, the fluidized state of the fluid medium _c in each of the chambers 1 to 3 is also different in each part of the chambers 1 to 3, so that an internal swirling flow is formed. You. In addition, the internal swirling flow circulates through the chambers 1 to 3 in the furnace because the fluidization state is different in each part of the chambers 1 to 3. In the figure, the size of the white arrows indicated by the air diffusers 3:! To 36 indicates the flow velocity of the fluidized gas g to be blown out. For example, the thick arrow at the point indicated by 2b has a larger flow velocity than the thin arrow at the point indicated by 2a. The flow velocity at the location indicated by the white arrow is uniform throughout the location.

A partition wall 11 and a partition wall 15 separate the gasification chamber 1 from the combustion chamber main body 5, and a partition wall 12 separates the combustion chamber main body 5 from the heat recovery chamber 3. The gasification chamber 1 and the heat recovery chamber 3 are separated by a partition wall 13 (note that in this drawing, the furnace is developed in a plan view, so that the partition wall 11 is a gasification chamber). It is shown as if it was not between 1 and the main part 5 of the combustion chamber, and the partition 13 was not between the gasification chamber 1 and the heat recovery chamber 3). That is, in the integrated gasification furnace 101, each of the first to third chambers is not configured as a separate furnace, but is integrally configured as one furnace. Further, a sedimentation chamber 1 is provided near the surface of the main body 5 of the chamber 1 in contact with the gasification chamber 1 so that the fluid medium c descends. That is, as described above, the first combustion chamber 2 is divided into the sedimentation combustion chamber 4 and the main body 5 of the combustion chamber other than the sedimentation combustion chamber _4c. Other parts of combustion chamber 2 A partition wall 14 for partitioning from the part 5) is provided. In addition, the sedimentation chamber combustion chamber 4 and the gasification chamber 1 are separated by a partition wall 15 as shown in FIG.

Here, the fluidized bed and the interface will be described. The fluidized bed consists of a dense layer at the lower part in the vertical direction, which contains the fluidized medium c (for example, silica sand), which is placed in a fluidized state by the fluidizing gas g, and a vertically upper part of the dense layer. A large amount of gas coexists with the fluid medium c in the part, and the fluid medium c consists of a splash zone that is vigorously splashing. Above the fluidized bed, that is, above the splash zone, there is a freeboard portion mainly containing gas and containing almost no fluid medium c. The interface may be considered as a force that refers to the splash zone having a certain thickness, or as a virtual surface intermediate the upper surface and the lower surface (the upper surface of the dense layer) of the splash zone.

In addition, the phrase "partitioned by a partition wall so that gas does not flow vertically above the interface of the fluidized bed" means that it is vertically above the upper surface of the dense layer further below the interface. It is preferable that there is no gas flow in the area.

The partition wall 11 between the gasification chamber 1 and the chamber 1 of the combustion chamber is almost entirely partitioned from the ceiling 19 of the furnace to the bottom of the furnace (perforated plate of the diffuser 31). However, the lower end does not contact the furnace bottom, and there is an opening 21 near the furnace bottom as a communication port. However, the upper end of the opening 21 is located above any of the interface of the fluidized bed of the gasification chamber as the first interface and the interface of the fluidized bed of the combustion chamber as the second interface. More preferably, the upper end of the opening 21 reaches the upper part of the upper surface of the dense bed of the fluidized bed of the gasification chamber or the upper surface of the dense bed of the fluidized bed of the combustion chamber. Not to be. In other words, it is preferable that the opening 21 is configured so as to always dive into the dense layer. That is, the gasification chamber 1 and the char combustion chamber 2 are separated from each other at least at the free board part, more specifically, above the interface, and more preferably, above the upper surface of the dense layer. In other words, it is divided by a partition wall so that there is no distribution.

The upper end of the partition wall 12 between the combustion chamber 2 and the heat recovery chamber 3 is near the interface, that is, above the upper surface of the dense layer, but below the upper surface of the splash zone. The lower end of the partition wall 12 is close to the bottom of the furnace, and the lower end does not contact the bottom of the furnace like the partition wall 11 and does not reach above the upper surface of the dense layer near the bottom of the furnace. There are two openings 22. In other words, only the fluidized bed portion is partitioned by the partition wall 12 between the first combustion chamber 2 and the heat recovery chamber 3, and the partition wall 12 has an opening 22 near the hearth surface. The fluid medium c in the first combustion chamber 2 flows into the heat recovery chamber 3 from above the partition wall 1 2, and returns to the first combustion chamber 2 again through the opening 22 near the hearth surface of the partition wall 12. It is configured to have flow.

The partition wall 13 between the gasification chamber 1 and the heat recovery chamber 3 completely separates from the furnace bottom to the furnace ceiling. The upper end of the partition wall 14 that partitions the inside of the first combustion chamber 2 in order to provide the first settling combustion chamber 4 is near the interface of the fluidized bed, and the lower end is in contact with the furnace bottom. The relationship between the upper end of the partition wall 14 and the fluidized bed is the same as the relationship between the partition wall 12 and the fluidized bed. Sedimentation chamber The partition wall 15 that separates the combustion chamber 4 and the gasification chamber 1 is similar to the partition wall 11 and almost entirely partitions from the furnace ceiling to the furnace bottom, and the lower end is located at the furnace bottom. There is no contact, and there is an opening 25 as a communication port near the furnace bottom, and the upper end of this opening is below the upper surface of the dense layer. That is, the relationship between the opening 25 and the fluidized bed is the same as the relationship between the opening 21 and the fluidized bed.

The waste or solid fuel a charged into the gasification chamber 1 receives heat from the fluidized medium c, and is pyrolyzed and gasified to generate product gas b. Typically, waste or fuel a does not burn in gasification chamber 1 but is so-called carbonized. The remaining dry distillation channel h flows together with the fluid medium c from the opening 21 at the lower part of the partition wall 11 into the main chamber 5 of the combustion chamber. In this way, the channel h introduced from the gasification chamber 1 is burned in the main chamber 5 of the channel combustion chamber to heat the fluid medium c. The fluid medium c heated by the combustion heat of the channel h in the channel chamber main body 5 flows into the heat recovery chamber 3 beyond the upper end of the partition wall 12 and below the interface in the heat recovery chamber 3. After the heat is collected and cooled by the in-layer heat transfer tube 41 as a heat recovery device arranged as shown in Fig. 2, it passes through the lower opening 22 of the partition wall 1 2 again and the combustion chamber It flows into the main unit 5.

The in-layer heat transfer tube 4 1 includes an in-layer heat transfer tube main body 4 1 A disposed in the heat recovery chamber 3, an introduction portion 4 1 B for guiding the steam s 1 to the in-layer heat transfer tube main body 4 1 A, It consists of a discharge section 41 C that discharges superheated steam s 2 from the heat transfer tube body 41 A. The steam s1 introduced into the bed heat transfer tube body 41A is superheated and becomes superheated steam s2.

The integrated gasifier 101 has temperature measuring devices 44, 45, a control valve 67, and flow measurement Vessel 7 7. The temperature measuring device 44 is installed in the introduction section 41B and measures the temperature of the steam s1. The control valve 67 is installed in the introduction section 41B and controls the flow rate of the steam s1. The flow rate measuring device 77 is installed in the introduction section 41B to measure the flow rate of the steam s1. The temperature measuring instrument 45 is installed in the discharge section 41C to measure the temperature of the superheated steam s2. The control valve 67 operates in response to a control signal i 1 (partially indicated by a broken line in the figure) sent from the control device 6 to change the opening. The flow measuring device 7 7 sends a flow signal i 2 based on the measured flow rate (partially indicated by a broken line in the figure) to the control device 6, and the temperature measuring devices 4 4 and 4 5 A temperature signal i 3 (partially indicated by a broken line in the figure) is sent to the control device 6. The control device 6 is a control device for controlling the heat recovery amount of the present invention.

Here, the heat recovery chamber 3 is not essential in the integrated gasification furnace 101 according to the embodiment of the present invention. That is, it is necessary to heat the fluid medium c in the gas combustion chamber 2 and the amount of the carbon mainly composed of mainly carbon remaining after gasification of volatile components in the gasification chamber 1. If the amount of the charged particles is almost the same, the heat recovery chamber 3 for removing heat from the fluid medium c is unnecessary. If the difference in the amount of the h is small, for example, the gasification temperature in the gasification chamber 1 becomes higher, and the amount of co-gas generated in the gasification chamber 1 increases. Is kept.

However, when the heat recovery chamber 3 is provided as shown in Fig. 1, it can handle a wide variety of wastes or fuels a, from coal that generates a large amount of char-h to municipal waste that generates almost no char-a-h. be able to. That is, no matter what kind of waste or fuel a, by adjusting the amount of heat recovery in the heat recovery chamber 3, the combustion temperature of the combustion chamber main body 5 can be appropriately adjusted, and the fluid medium The temperature of c can be maintained properly. Further, the supply amount of the fluidizing gas g3 to the air diffuser 36 is adjusted by the control valve 66, and the heat recovery chamber 3 having the weak fluidization region 3a maintained in the weak fluidization state is provided. The amount of heat recovery in the heat recovery chamber 3 can be controlled by adjusting the strength of the fluidized state. Therefore, the control device 6 that controls the heat recovery amount controls the heat recovery amount in the in-layer heat transfer tube 41, and controls the temperature of the combustion chamber 2.

On the other hand, the fluid medium c heated in the main part 5 of the combustion chamber of the chamber flows over the upper end of the partition wall 14 and flows into the combustion chamber 4 of the sedimentation chamber, and then from the opening 25 at the lower part of the partition wall 15. Flow into gasification chamber 1.

Here, referring to the schematic side sectional views of FIGS. 2 (a), (b), and (c), two chambers separated by a partition X, a partition Y, or a partition Z formed in the furnace F. The fluidization state and movement of the fluid medium c between R a R b will be described. In FIG. 2 (a), the two chambers R a R b are separated by a partition wall X having an opening PX only in the upper part. In FIG. 2 (b), the two chambers R a R b are separated by a partition wall Y having an opening Q y only at the lower part. In FIG. 2 (c), the two chambers R a R b are partitioned by a partition wall Z having an opening P z at the top and an opening Q z at the bottom. In FIGS. 2 (a), (b) and (c), a diffuser D a D b for injecting fluidized gas gagb is provided at the bottom of each of the chambers R a R b for accommodating the fluidized medium c. Has been. It is assumed that the upper end of the partition wall XZ is near the height of the interface, and the opening QyQz is located at a position below the dense layer. Fig. 2 (a)

(b) In (c), the fluidized state in the chamber Ra is uniform in the chamber Ra, and the fluidized state in the chamber Rb is uniform in the chamber Rb.

The movement of the fluid medium c between the two chambers R a and R b separated by the partition wall X, the partition wall Y or the partition wall Z is the difference in the fluidization state between the chamber Ra side and the chamber R b side. By changing the fluidity difference between the chambers Ra and Rb arbitrarily in practice, the opening P x between the chambers Ra and Rb The moving amount and moving direction (from the chamber Ra to the chamber Rb or from the chamber Rb to the chamber Ra) of the fluid medium c via QyPzQz can be adjusted. The following specifically describes how the amount of movement of the fluid medium c between the chambers Ra and Rb can be adjusted when the fluidization state of the chambers Ra and Rb is changed. I do.

The movement of the fluid medium c between the chamber R a and the chamber R b via the opening Q y Q z generally takes place in the fluidized state near the opening Q y Q z on the chamber Ra side. As a result, the fluid medium c moves from the weakly fluidized chamber to the strongly fluidized chamber, affected by the difference in the fluidized state near the opening <3 Qz on the chamber 1 side. In FIGS. 2 (a), (b) and (c), the fluidization state in the chamber R a is uniform in the chamber R a, and the fluidization state in the chamber R b is uniform in the chamber R b Therefore, the difference in the gas velocity of the fluidized gas gagb in the chamber R a and the chamber R b can be discussed. The fluid medium c moves to the faster chamber.

First, a case where the two chambers R a and R b are partitioned by a partition wall X whose upper end is near the height of the interface will be described with reference to FIG. When the fluidized state of the two chambers R a and R b is equal, the amount of the fluid medium c splashed from the chamber Ra side moves across the partition wall X to the chamber R b side, and from the chamber R b side The amount of the fluid medium c that has jumped over the partition wall X and moves toward the chamber Ra becomes equal on average. Therefore, the movement of the fluid medium c between the two chambers R a and R b occurs locally, but the movement of the fluid medium c as a whole (the entire chamber R a and the chamber R b, the same applies hereinafter). Is 0.

For example, when the fluidized state of the chamber R a is made stronger than the fluidized state of the chamber R b while the fluidized state of the chamber R b is kept constant, that is, the fluidized gas velocity of the chamber R b is kept constant When the velocity of the fluidizing gas in chamber R a is set to be higher than the velocity of the fluidizing gas in chamber R b, the fluid medium c splashed from chamber R a crosses partition X to chamber R b. Since the amount of the fluid medium c that has splashed from the chamber R b side moves beyond the partition wall X to the chamber Ra side than the amount of movement, the overall amount from the chamber Ra side to the chamber R b side increases. The moving amount of the fluid medium c does not become 0, and the fluid medium c moves from the chamber Ra side to the chamber Rb side (this state is indicated by a white arrow in the figure).

Here, we considered a case where the fluidizing gas velocity in the chamber R a was increased while keeping the fluidizing gas velocity in the chamber R b constant. The same effect can be obtained by changing the fluidizing gas velocity in the chamber Rb so as to decrease it while keeping the degree constant.

Now, assuming that the fluid medium c is not externally replenished or extracted outside in the chambers Ra and Rb, the fluid medium c moves from the chamber Ra side to the chamber Rb side. As a result, the height of the fluidized bed in the chamber Ra decreases gradually, and the height of the fluidized bed in the chamber Rb gradually increases.

The amount of the fluid medium c moving from the chamber Ra side to the chamber Rb side beyond the partition wall X decreases as the fluidized bed interface on the chamber Ra side becomes lower. Due to the decrease in bed height, the moving amount of the fluid medium c from the chamber Ra side to the chamber Rb side decreases. Similarly, the amount of the fluid medium c from which the splashing from the chamber Rb moves over the partition X to the chamber Ra side increases as the fluidized bed interface on the chamber Rb side increases. Of room R As the height of the fluidized bed increases, the amount of movement of the fluid medium c from the chamber Rb to the chamber Ra increases.

For this reason, the case where the gas velocities of the fluidizing gases ga and gb in the chamber R a and the chamber R b are the same as the initial state, and the fluidizing gas velocity in the chamber Ra is If a certain amount of difference is set so as to be larger, initially the entire fluid medium c moves from the chamber Ra side to the chamber Rb side, but the fluidized bed height of the chamber Ra is somewhat increased. At the stage where the height of the fluidized bed in chamber Rb rises, the amount of local movement of fluid medium c from chamber Ra side to chamber Rb side again and from chamber Rb side to chamber Ra side Since the movement amount of the local fluid medium c is balanced as a whole, the overall movement amount of the fluid medium c between the two chambers Ra and Rb becomes zero again.

Therefore, when a certain amount of difference is made so that the fluidizing gas velocity in the chamber Ra is higher than the fluidizing gas velocity in the chamber Rb, the movement of the fluid medium c from the chamber Ra to the chamber Rb is performed. In order to perform the process continuously, the fluid medium c is supplied from the outside to the chamber Ra so that the amount of the fluid medium c filled in both chambers Ra and Rb, that is, the fluidized bed height is constant. In addition, the configuration may be such that the fluid medium c is extracted from the chamber Rb to the outside.

In this case, the larger the difference between the fluidizing gas velocities of the chambers R a and R b, the larger the movement amount of the fluid medium c from the chamber R a to the chamber R b can be. In a state where the fluidization is stopped or close to the minimum fluidization, that is, preferably, the fluidization speed is 2 Umf or less, and more preferably, 1 Umf or less. When the fluidization speed is maintained at a sufficiently high level, preferably at a fluidization velocity force of at least Umf, and more preferably at 5 Umf or more, the maximum movement amount of the fluid medium c can be ensured. Here, Umf is a unit where the minimum fluidization speed (speed of fluidized gas at which fluidization starts) is defined as lUmf. That is, 5Umf is 5 times the minimum fluidization rate.

Next, as shown in FIG. 2 (b), let us consider a case where the two chambers R a and R b are partitioned by a partition wall Y having an opening Q y buried in the dense layer. When the fluidized state of the two chambers Ra and Rb is equal (when the fluidized gas velocity of the chamber Ra is equal to the fluidized gas velocity of the chamber Rb), the chamber Ra through the opening Qy From side to room R b side, or Since the diffusion amount of the fluid medium c from the chamber Ra side to the chamber Rb side is balanced, the movement of the fluid medium c between the two chambers R a and R b occurs locally, but the overall flow The moving amount of the medium c is 0.

When the fluidized state of the chamber Rb is made stronger than that of the chamber Rb while the fluidized state of the chamber Rb is kept the same, that is, while the fluidized gas velocity in the chamber Rb is kept constant When the fluidizing gas velocity in the chamber R a is set higher than the fluidizing gas velocity in the chamber R b, more bubbles are generated in the dense layer of the chamber R a than in the dense layer 室 of the chamber R b. The apparent layer density of the chamber R a is lower than the apparent layer density of the chamber R b. For this reason, if the heights of the fluidized beds of the chambers Ra and Rb are equal, the pressure near the opening Qy near the lower part of the chamber Ra is equal to the pressure near the opening Qy near the lower part of the chamber Rb. Lower than pressure. Due to the attraction effect using this pressure difference as a driving force, the movement of the fluid medium c occurs from the chamber Rb side to the chamber Ra side over the entire opening Qy. This is indicated by the arrow).

Conversely, when the fluidizing gas velocity in the chamber Rb is reduced while the velocity of the fluidizing gas in the chamber Ra is kept constant, the situation is slightly different. The movement of the fluid medium c considered here occurs through the opening Qy of the partition wall Y provided in the dense layer, and the vicinity of the opening Qy at the lower part of the layer of the chambers Ra and Rb. Is the driving force. In other words, the pressure difference near the opening Qy in the lower part of the layer between the chambers R a and R b balances the resistance required for the fluid medium c to move through the opening Q y. However, this resistance is closely related to the apparent layer viscosity of the particle layer.

Next, a description will be given with reference to FIGS. 2 (b), 3 and 4.

Figure 3 shows the relationship between the fluidized state of the fluid medium c and the apparent layer viscosity of the particle layer. This shows a case where the gas velocity of the fluidizing gas gb in the chamber R b is changed in the range shown in FIG. 3, while the gas velocity of the fluidizing gas ga in the chamber R a is kept constant. In the case of a simple publishing fluidized bed (no sedimentation flow), the viscosity of the fluidized bed in a fixed bed with a fluidizing gas velocity of 1 Umf or less is almost equal to infinity. When the fluidizing gas velocity exceeds 1 Umf, the viscosity of the fluidized bed decreases rapidly. In the case of the chamber R b (sedimentation chamber), the relative velocity between the settling fluid medium and the rising fluidizing gas occurs, so that even if the fluidizing gas velocity is 1 Umf or less, the relative velocity of the fluidizing gas is 1 Umf or more. As it becomes a fluidized bed, the viscosity changes and the amount of movement (Circulation amount) can be controlled. Therefore, the amount of change in the amount of fluidizing gas for controlling the amount of movement (circulation) of the fluid medium c can be minimized. In other words, the effect of changes in the process factor for controlling the circulation amount (here, the amount of fluidized gas) on other process factors can be minimized.

Therefore, if the velocity of the fluidizing gas in the chamber R b is reduced while keeping the velocity of the fluidizing gas in the chamber R a constant, the amount of movement of the fluid medium c according to the absolute value of the velocity of the fluidizing gas in the chamber R b Change behavior is different. In the initial state, it is assumed that both the chamber Ra and the chamber Rb have sufficiently fluidized, that is, the fluidized gas velocity exceeds 5 Umf. From this state, if the velocity of the fluidizing gas in the chamber R b is reduced, the relative velocity of the fluidizing gas in the chamber R b (the relative velocity between the settling velocity of the fluid medium and the rising velocity of the fluidizing gas) becomes about 2 Umf. In the range above, as the fluidizing gas velocity in the chamber Rb decreases, the pressure difference near the opening Py at the lower part of the layer between the chamber Rb and the chamber Rb increases, so that the pressure from the chamber Rb to the chamber Ra increases. The moving amount of the fluid medium c increases. However, when the relative velocity of the fluidizing gas in chamber R b (the relative velocity between the settling velocity of the fluidized medium and the rising velocity of the fluidizing gas) is smaller than about 2 Umf, the lower the velocity of the fluidizing gas in chamber R b, Since the bed viscosity increases sharply and the resistance of the fluid medium c to pass through the opening Qy of the partition wall Y increases, the amount of movement of the fluid medium c from the chamber Rb to the chamber Ra is increased. Becomes smaller on the contrary. Figure 4 shows that the relative velocity of the fluidized gas ga in the chamber Ra (the relative velocity between the settling velocity of the fluidized medium and the rising velocity of the fluidized gas) is kept constant (4 Umf, 5 Umf, 6 Umf). The three cases are shown below) .However, when the gas velocity of the fluidizing gas gb in the chamber Rb is changed, how does the movement amount of the flowing medium c from the chamber Ra to the chamber Rb change? Indicates As shown in Fig. 4, when the relative velocity of the fluidizing gas in the chamber Rb (the relative velocity between the sedimentation velocity of the fluidizing medium and the fluidizing gas) is less than about 2 Umf, the relative velocity of the fluidizing gas (the sedimentation of the fluidizing medium) It can be seen that the moving amount of the fluid medium c changes almost linearly with respect to the velocity (the relative speed between the velocity and the rising velocity of the fluidizing gas). In other words, by actively using this range, a small change in the amount of fluidized gas can cause a large change in the amount of movement of the fluidized medium c under a small amount of fluidized gas. . Fig. 4 shows the case where the fluidization state of the chamber Ra is kept constant, but as shown in this figure, the fluidization state of the chamber Ra is maintained at a sufficiently strong fluidization state. Is particularly preferred.

According to the findings of the inventors, the relative velocity of the fluidizing gas gb (the sedimentation velocity of the fluidizing medium and the fluidizing velocity of the fluidizing gas gb) that gives the maximum amount of movement of the fluidizing medium c from the chamber Ra to the chamber Rb in FIG. The relative velocity with the gas is about 1.7 Umf. From the above viewpoint, the relative velocity of the fluidizing gas in the chamber Rb (the relative velocity between the settling velocity of the fluidizing medium and the fluidizing gas) is preferably in the range of lUmf to 2Umf, more preferably in the range of lUmf to 1.7Umf. The flow rate of the fluidizing gas in the chamber Ra is preferably adjusted to 4 Umf or more, more preferably 5 Umf or more.

Even if the gas velocity of the fluidizing gas ga in the chamber R a is increased while the gas velocity of the fluidizing gas gb in the chamber R b is kept constant, or the gas velocity of the fluidizing gas ga in the chamber R a is kept constant. Even if the gas velocity of the fluidizing gas gb in the chamber R b is reduced while maintaining the pressure in the chamber R b, if the fluid medium c is not replenished or extracted from the outside, Due to the movement of the fluid medium c to the chamber Ra side, the height of the fluidized bed in the chamber Rb decreases and the height of the fluidized bed in the chamber Ra increases.

That is, when the fluidized gas velocity in the chambers R a and R b is the same as the initial state, the fluidized gas velocity in the chamber Ra is higher than the fluidized gas velocity in the chamber R b. Thus, when a certain amount of difference is made, the fluid medium c moves from the chamber Rb to the chamber Ra immediately after the difference is made, but the fluidized bed height of the chamber Ra rises to some extent, When the height of the fluidized bed of Rb decreases, the pressure near the opening Qy at the bottom of the chamber Ra increases, and the pressure near the opening Qy at the bottom of the chamber Rb decreases. The pressure difference in the vicinity of the opening Qy at the bottom of the layer between the chambers Ra and Rb, which was the driving force for the movement of the air, becomes smaller. When the pressure difference becomes zero, the overall movement amount of the fluid medium c between the two chambers Ra and Rb becomes zero again.

Therefore, a certain amount of difference is set so that the velocity of the fluidizing gas in the chamber R a becomes larger than the relative velocity of the fluidizing gas in the chamber R b (the relative velocity between the settling velocity of the fluid medium and the rising velocity of the fluidizing gas). In this case, in order to continuously move the fluid medium c from the chamber Rb to the chamber Ra, the amount of the fluid medium c filled in both chambers Ra and Rb, that is, the height of the fluidized bed, In this case, the fluid medium c may be supplied from the outside to the chamber Rb, and the fluid medium c may be withdrawn from the chamber Ra to the outside so that the pressure is constant. Next, description will be made with reference to FIG. In FIG. 2 (c), the opening Pz is provided at the upper part and the opening Qz is provided at the lower part. Therefore, at the upper opening Pz, the phenomenon described above with reference to FIG. At z, the phenomenon described above with reference to Fig. 2 (b) occurs.

Therefore, for example, if the fluidized state of the chamber R a is made stronger than the fluidized state of the chamber R b while keeping the fluidized state of the chamber R b constant, the fluidized gas velocity of the chamber R a If the relative velocity of the fluidizing gas in the chamber R b (the relative velocity between the settling velocity of the fluid medium and the relative velocity of the fluidizing gas) is changed to be small while maintaining the same, the opening Pz will start from the chamber Ra side. Movement of the fluid medium c to the chamber R b side occurs, and at the opening Q z, movement of the fluid medium c from the chamber Ra side to the chamber R b side occurs. Therefore, circulation of the fluid medium c occurs between the chamber Ra and the chamber Rb.

In this case, the amount of movement of the fluid medium c through the opening Q z and the amount of movement of the fluid medium c through the opening P z are such that the fluidized state of the chamber Ra is stronger than the fluidized state of the chamber Rb. In the initial state, they are not always equal. However, after a certain transient state, the moving amount of the fluid medium c through each opening Q z P z becomes equal due to the change in the fluidized bed height caused by the difference in the moving amount of the fluid medium c. A certain steady state of the circulation of the fluid medium c is obtained.

For example, the amount of movement of the fluid medium c from the chamber Rb to the chamber Ra via the opening Qz is greater than the amount of movement of the fluid medium c from the chamber Ra to the chamber Rb via the opening Pz. Think about the bigger case. In this case, the height of the fluidized bed in the chamber Rb gradually decreases, and at the same time, the height of the fluidized bed in the chamber Ra gradually increases. A decrease in the fluidized bed height of the chamber Rb decreases the pressure near the hearth of the chamber Rb, while an increase in the fluidized bed height of the chamber Ra increases the pressure near the hearth of the chamber Ra. As a result, the pressure difference between the chamber R a and the chamber R b sandwiching the opening Q z is reduced, that is, the amount of movement of the fluid medium c from the chamber R b to the chamber Ra via the opening Q z is reduced. You. In addition, as the height of the fluidized bed in the chamber Ra increases, the fluid medium c easily jumps from the chamber Ra to the chamber Rb beyond the upper end of the partition Z. That is, the amount of movement of the fluid medium c from the chamber Ra to the chamber Rb via the opening Pz increases. Due to the above effects, the amount of movement of the fluid medium c from the chamber Rb to the chamber Ra through the opening Qz decreases, and the fluid medium c from the chamber Ra to the chamber Rb through the opening Pz. Room R a and room R The height of the fluidized bed of R b further changes and balances where the amount of movement of the fluid medium c from chamber R b to chamber R a and the amount of movement of chamber R a to chamber R b are equal.

In the above, the movement amount (circulation amount) of the fluid medium c finally obtained by balancing is determined by the width, height, area and shape of the opening Q z and the furnace F such as the height of the partition wall Z. It depends on the shape conditions and the amount of fluidizing gas supplied to each chamber. Therefore, in order to obtain a desired circulation amount, the width, height, area and shape of the opening Q z and the height of the partition wall Z are taken into consideration in consideration of the supply amount of the fluidizing gas amount. The shape of the furnace F should be determined.

Here, with reference to FIG. 6, the definition of the amount of circulation of the fluid medium c circulating through the opening 25 between the gasification chamber 1 and the settling chamber 1 combustion chamber 4 will be described below. In the figure, the gasification furnace 101 has the same configuration as that shown in Fig. 1, but for simplicity of explanation, the strong fluidization zone 1 b of the gasification chamber 1 and the weak fluidization It is described as being constituted by the sedimentation chamber 1 which is the area 4a, the combustion chamber 4, and the partition wall 15 in which the opening 25 is formed, and other components are omitted.

The superficial velocity of the fluidized gas g1 (Fig. 1) in the strong fluidized zone 1b of the gasification chamber 1 is V1b, and the fluidized gas in the sedimentation chamber 1 combustion chamber 4, which is the weak fluidized zone 4a. Let the superficial velocity of g 4 (Figure 1) be V 4 a. Since the superficial velocity V lb is higher than the superficial velocity V 4 a (V 1 b> V 4 a), the fluidization state of the gasification chamber 1 is stronger than that of the sedimentation chamber and combustion chamber 4. There is a pressure difference between the bottom B 4 a of the sedimentation chamber 1 combustion chamber 4 and the bottom B 1 b of the strong fluidization zone 1 b of the gasification chamber 1, and there is a partition wall between the two fluidization zones. The fluid medium c circulates and moves through the opening 25 at the bottom of 15. The furnace bottom pressure (fluid bed pressure at the furnace bottom) is P m [Pa], the bulk density of the fluid bed is D f [kg / m ³ ], the gravitational acceleration is ga [kg / s ² ], and the height of the fluid bed is If (floor height) is H f [m],

P m = D f X g a X H f. (1)

The sedimentation chamber 4 has a weak fluidized zone 4a and a small amount of air bubbles, so the fluidized bed bulk density Df4a is large (there are few voids and the particle concentration is high). On the other hand, in the strong fluidization zone 1 b of the gasification chamber 1, the bulk density D f 1 b of the fluidized bed is small because there are many bubbles (there are many voids and the particle density is low). Therefore, the fluidized bed bulk density D f 4 a of the sedimentation chamber 1 combustion chamber 4 (weak fluidized zone 4 a) is the fluidized bed bulk density D f 1 of the strong fluidized zone 1 b of the gasification chamber 1. b (D f 4 a> D flb), and a pressure difference is generated from the char combustion chamber 4 (weak fluidization zone 4 a) to the strong fluidization zone 1 b of the gasification chamber 1 The fluid medium c moves. On the other hand, as shown in FIG. 7, when the superficial velocity V 1 b of the strong fluidization zone 1 b of the gasification chamber 1 is equal to the superficial velocity V 4 a of the sedimentation chamber 1 combustion chamber 4 (VI b = V 4 a) is the furnace bottom pressure P m 1 b at the bottom B 1 b of the strong fluidization zone 1 b of the gasification chamber 1, and the furnace pressure at the bottom B 4 a of the settling chamber 1 Since the bottom pressure is equal to P m 4 a (P m 1 b = P m 4 a), the lower opening 25 of the partition wall 15 gasifies from the sedimentation chamber 1 combustion chamber 4 from a macro perspective. Neither the movement of the fluid medium c to the strong fluidization zone 1 b of the chamber 1 nor the movement of the fluid medium c from the gasification chamber 1 to the sedimentation chamber 1 combustion chamber 4 occurs.

However, in a fluidized bed with the same superficial velocity in all fluidized areas in the fluidized bed, focusing on microscopic particles one by one, the particles are constantly moving in an arbitrary direction, so gasification At the lower opening 25 of the partition wall 15 between the chamber 1 and the sedimentation-chamber combustion chamber 4, the bidirectional flow of the fluid medium particles c flows between the gasification chamber 1 and the sedimentation-chamber combustion chamber 4. And the exchange of the fluid medium particles c has occurred.

The macroscopic one-way movement of the fluid medium c between the gasification chamber 1 and the settling chamber 1 as shown in Fig. 6 is called convection. The two-way movement of particles between the gasification chamber 1 of the fluid medium c and the settling chamber 1 as shown in Fig. 7 is called diffusion. Even in the region where convection occurs in Fig. 6, if attention is paid to each particle in the micro region, diffusion as shown in Fig. 7 occurs.

On the other hand, the mass flow rate [kg / s] of the macro one-way flow shown in Fig. 6 is defined as the circulation amount. The amount of circulation is determined by the pressure difference at the bottom of the fluidized bed, the viscosity of the upstream fluidized bed and the viscosity of the downstream fluidized bed (especially, the viscosity of the upstream fluidized bed is dominant). . In FIG. 6, as the difference between the furnace bottom pressure P m 4 a of the bottom B 4 a of the sedimentation chamber 1 and the bottom B 1 a of the gasification chamber 1 and the bottom pressure P m 1 b of the bottom B 1 b of the gasification chamber 1 increases, The amount of movement (circulation) of the fluid medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 increases through the lower opening 25 of the partition wall 15. The lower opening 25 of the partition wall 15 acts as a throttle resistance against the flow of the flowing medium c. Therefore, the smaller the apparent viscosity of the fluidized bed of the settling chamber 1 combustion chamber 4 is, the easier the fluid medium c flows through the throttle resistance at the opening 25 and the amount of circulation increases. The apparent viscosity of the fluidized bed is It depends on the mobilization state, that is, the superficial velocity V 1 b and V 4 a of the fluidizing gas. Therefore, the fluidized gas velocity V 1 b in the strong fluidization zone 1 b of the gasification chamber 1 is changed, or the superficial velocity V 4 a of the fluidized gas in the sedimentation chamber 1 combustion chamber 4 is changed. The amount of circulation can be controlled by changing the apparent viscosity.

For example, if the fluidized state of the entire area of the gasification chamber 1 and the fluidized state of the entire area of the sedimentation chamber and the combustion chamber 4 are made the same, the circulation amount becomes zero. However, in this way, even if the circulation amount is set to 0, the fluid medium c between the two chambers 1 and 4 is exchanged by diffusion at the opening 25 at the lower part of the partition wall 15. Along with the exchange of c, the pyrolysis residue (excluding large non-fluidized residue) in the strong fluidization zone 1 b of the gasification chamber 1 moves to the sedimentation char combustion chamber 4 and burns.

Therefore, the fluidized bed temperature is higher in the sedimentation-chamber combustion chamber 4 where the residue is burned than in the gasification chamber 1 where the pyrolysis of the raw material as the endothermic reaction is performed. In the lower opening 25 of the partition wall 15, the fluid medium c is exchanged between the two chambers 1 and 4 by diffusion, so that the exchange of the fluid medium c also causes the sensible heat of the fluid medium c to change. , Exchanged between rooms 1 and 4. Therefore, the sensible heat of the fluidized medium c is transferred from the high-temperature settling chamber combustion chamber 4 to the low-temperature gasification chamber 1.

From the above, there is a relationship as shown in Fig. 8 between the fluidizing gas velocity (superficial velocity of fluidizing gas) in the sedimentation chamber 1 and the amount of circulation (convection) and heat transfer. That is, when the superficial velocity of the fluidized medium c in the settling chamber 1 becomes zero, the circulation amount (convection) becomes zero, but the heat transfer amount does not become zero. This is due to the diffusion medium between the gasification chamber 1 and the combustion chamber main body 5 due to the diffusion between the gasification chamber 1 and the combustion chamber main body 5 at the lower opening 21 of the partition wall 11 of the gasification chamber 1 and the combustion chamber main body 5. This is due to the exchange of residue and the corresponding transfer of residue and heat.

Figure 9 shows that the superficial velocity (assumed to be Umf) of the fluidized gas in the sedimentation chamber 1 that is the weak fluidization zone 4a where the fluid medium c settles is from 0 Umf to about 1.7 Umf. The figure shows the change in the amount of fluid medium transferred from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 (convection + diffusion) (unit: _kg / s) when changed. As shown in the figure, the moving amount of the fluid medium increases almost linearly with an increase in the superficial velocity. Even below lUmf, the moving amount of the fluid medium changes and is within the control range. Here, Umf is the minimum fluidization speed (the flow at which fluidization starts The superficial velocity of activated gas) is defined as l Umf. In addition, in the figure, when the fluidization speed of the settling channel combustion chamber 4 is set to 0, the moving amount of the moving medium from the settling channel combustion chamber 4 to the gasification chamber 1 is not 0. This is because the fluid medium moves due to diffusion between the openings 25 formed in the partition wall 15 between the gasification chamber 1 and the settling chamber 1 combustion chamber 4. Therefore, the fluidized state of the settling channel combustion chamber 4 is stopped, the amount of heat transfer by convection is set to 0, and the fluidization around the opening 25 of the gasification chamber 1 and the settling channel combustion chamber 4 is performed. By changing the state (changing the amount of fluidizing gas), the amount of heat transfer by diffusion around the gasification chamber 1 and the sedimentation chamber 1 and the opening 25 of the combustion chamber 4 is changed to reduce the amount of heat transfer. It is possible to control in a smaller range.

Therefore, fluidized gas supplied to the region near the opening 21 in the weak fluidization region 1a of the gasification chamber 1 and the region near the opening 21 in the strong fluidization region 2b of the combustion chamber body 5 By installing flow rate measuring devices 71 1 and 7 4 for measuring the quantities gl and g 2 and flow rate control devices (for example, flow control valves 61 and 64) to change the flow rates, the gasification chamber 1 and the channel It is possible to control the amount of heat transfer due to diffusion around the opening of the combustion chamber body 5.

For example, when it is desired to control the heat transfer amount to a small value, the control device 6 as the heat transfer amount control device is connected to the fluidized gas flow control device (for example, the flow control valve 65) of the sedimentation chamber and the combustion chamber 4. Send a signal to reduce the flow rate to zero. As a result, fluidization of the sedimentation-chamber combustion chamber 4 stops, and the movement of the fluid medium due to convection between the gasification chamber 1 and the combustion chamber 1 does not occur. In addition, the control device 6 as a heat transfer amount control device controls the fluidization gas g1 to be supplied to the region near the opening 21 in the weak fluidization region 1a of the gasification chamber 1. And a fluidizing gas for controlling the fluidizing gas g2 to be supplied to the region near the opening 21 in the strong fluidizing region 2b of the combustion chamber body 5. Send a signal to reduce the flow rate to the quantity control device (eg flow rate control valve 63). As a result, the amount of fluidized gas in the region near the opening 21 in the weak fluidization region 1a of the gasification chamber 1 and in the region near the opening 21 in the strong fluidization region 2b of the main body 5 of the combustion chamber 5 And the diffusion around the opening 21 is weakened, and the amount of heat transfer is reduced.

The relationship between the fluidized bed height and the circulation amount will be described with reference to FIG. In the figure, furnace 10 2 includes two chambers R p and R q partitioned by a partition wall W. The chambers R p and R q contain the fluid medium c. The partition wall W has an opening Pw at the top and an opening Qw at the bottom. A diffuser D pa and a diffuser D pb for blowing fluidized gas are provided at the furnace bottom of the chamber R p, and a diffuser D qa for blowing a fluidized gas is provided at the furnace bottom of the chamber R q. I have. It is assumed that the upper end of the partition wall W is near the height of the interface, and the opening Qw is located at a position below the dense layer. The chamber R p has two compartments: a weak fluidization zone pa just above the diffuser D pa where the fluidization state is weak, and a strong fluidization zone pb just above the diffuser D pb and the fluidization state. It is divided into The chamber R q is a weakly fluidized zone qa with a weak fluidized state. Further, it is assumed that the fluidized state is uniform in the weakly fluidized region pa of the room Rp, in the strong fluidized region pb of the room Rp, and in the room Rq. It is assumed that the strong fluidization zone pb of the chamber R p has a furnace bottom B pb, and the chamber R q has a furnace bottom B qa.

For the following two reasons, the higher the fluidized bed height, the greater the circulation volume. As described above, the pressure between the furnace bottom pressure P mqa at the furnace bottom B qa of the chamber R q, which is the weak fluidization region qa, and the furnace bottom pressure P mpb at the furnace bottom B pb of the strong fluidization region pb of the room R p. Due to the difference in force, the flowing medium moves from the opening Qw below the partition W between the two regions. As described above, the pressure at the furnace bottom is obtained from Pm = DfXgaXHf (1). Here, P m [Pa] is the pressure at the bottom of the furnace, and D f [kg / m ³ ] is the volume of the fluidized bed. In the chamber R q, which is the weak fluidized zone qa, there are few bubbles, so the fluidized bed bulk density D fqa is Large (small voids and high particle concentration). In the strong fluidization zone pb of the chamber R p, there are many bubbles, and the bulk density D fpb of the fluidized bed is small (there are many voids and the particle density is low). Therefore, the flow of the chamber R q in the weak fluidization zone qa The bed bulk density D fqa is larger than the fluidized bed bulk density D fpb in the strong fluidization zone pb of the chamber R p (D fqa> D fpb), and therefore the furnace bottom pressure P mqa of the furnace bottom B qa of the chamber R q Is larger than the pressure P mpb at the bottom B pb of the strong fluidization zone pb of the chamber R p (Pm qa> P mpb), and a pressure difference occurs, and the chamber R at the weak fluidization zone qa The fluid medium moves c from q through the strong fluidization zone pb opening Qw of the chamber R p.

According to Eq. (1), the higher the fluidized bed height, the more proportionally the pressure P mqa at the bottom B qa of the weak fluidization zone qa of the chamber R q and the strong fluidization zone pb of the chamber R p Since the pressure difference from the pressure Pm pb at the bottom B pb of the furnace increases, the higher the height of the fluidized bed, the greater the amount of movement. It becomes bad. The circulation amount increases as the moving amount of the fluid medium c moving from the chamber Rq to the chamber Rp increases (the first reason that the circulation amount increases as the height of the fluidized bed increases).

As shown in FIG. 10, the bubble rupture occurs in the upper part of the strong fluidization region pb of the chamber Rp, and the rupture of the bubble causes the fluid medium c to scatter around, opening from the chamber Rp to the chamber Rq. Movement of the fluid medium c occurs through section P w. The higher the height of the fluidized bed, the greater the distance (Δ の in the figure) from the upper end of the partition wall W between the chamber Rq and the chamber Rp to the upper surface of the fluidized bed. Due to the accompanying movement of the particles of the fluid medium c, the amount of the fluid medium c moving to the chamber R q increases, so that the circulation amount increases (the higher the bed height, the greater the circulation amount). Reason) . The phenomenon that the fluid medium c moves to the chamber Rq due to the burst of the bubble at the upper part of the chamber Rp occurs in a limited range near the upper part of the fluidized bed where the bubble is ruptured. Even if the height is increased, the movement of the fluid medium c does not increase.

Therefore, the circulation amount can be increased by increasing the height of the fluidized bed within a certain range. During operation, when it is desired to adjust the circulation amount, the fluid medium c is supplied into the chambers Rq and Rp to increase the height of the fluidized bed to increase the circulation amount, or to move the fluid medium c to the room R. q, It is possible to take out from the chamber R p and lower the fluidized bed height to reduce the circulation amount.

Next, a method of measuring the height of the fluidized bed will be described with reference to FIG. As shown in the figure, two pressure measuring devices 91 and 92 are installed in the settling channel combustion chamber 4 at two upper and lower points (preferably the same horizontal position) in the fluidized bed of the settling channel combustion chamber 4. It is set up to measure fluidized bed pressure. By measuring the pressure with the pressure measuring devices 91 and 92, it is possible to calculate the fluidized bed height and control the circulation amount. However, the pressure measurement point for calculating the fluidized bed height may be the gasification chamber 1 instead of the sedimentation chamber combustion chamber 4. First, the relationship between fluidized bed pressure and fluidized bed height is described. Fluidized bed pressure P f and fluidized bed height H f have the relationship described below.

P f = D f X g a X H f x + P O---(2)

Where P f is the fluidized bed pressure [Pa], D f is the fluidized bed bulk density [kg / m ³ ], ga is the gravitational acceleration [kg / s ² ], and H f X is the height of the fluidized bed above [ m] and PO are the pressure [Pa] on the freeboard. From equation (2), if the fluidized bed pressure at the measurement point near the furnace bottom B4a is Pf1 and the fluidized bed height above is HfX1,

P f l = D f 4 a X g a X H f x l + P 0-

If the fluidized bed pressure at the measurement point far from the furnace bottom B 4 a is P f 2 and the fluidized bed height above is H f X 2,

P f 2 = D f 4 a X g a X H f x 2 + P 0-(2) "

It becomes. Here, assuming that the distance between the measurement points is ΔH f (known), ΔH f = H f X 1 — H f X 2. Taking the difference between the two equations (2) 'and (2) "representing the fluidized bed pressure, Pfl-Pf2 = Df4aXgaXAHf'. '(3).

The fluidized bed height can be calculated by the following steps. First, the fluidized bed pressures P f 1 and P f 2 at the upper and lower two points (preferably at the same horizontal position) in the fluidized bed are measured, and the pressure difference ΔP (= P f 1 -Calculate P f 2). next,

Calculate the fluidized bed bulk density D f 4 a from equation (3) (the height ΔH f between the upper and lower points is known). The value of the fluidized bed pressure at one of the measurement points (the height of the measured bed is known and it is desirable to select the one closer to the furnace bottom B4a) and the pressure at free board is almost 0. From P 0 = 0, the height H f X 1 from the fluidized bed pressure measurement point to the fluidized bed upper surface is calculated using the equation (2) ′. Assuming that the height of the fluidized bed is H f and the height of the measurement point near the furnace bottom B 4 a is H f 1 (known), then H f = H fl + H fxl. Is calculated.

A pressure measuring device 91, 92 is installed to measure the fluidized bed pressures Pf1, Pf2, and a control device is used as a computing unit that receives a pressure signal based on the measured value from the pressure measuring device 91, 92. The fluidized bed height H f can be calculated by the controller 6. By controlling the fluidized bed height H f calculated in this way by the control device 6, the circulation amount can be controlled. The control device 6 may output a fluidized bed height signal indicating the calculated fluidized bed height Hf.

The pressure measuring devices 9 1 and 9 2 have slow fluidization and small pressure fluctuations, and have weak sedimentation chamber 1 and weak gasification chamber 1a of gasification chamber 1 and weak flow of chamber 1 Although it is desirable to install it in the gasification zone 2a, it may be installed in the strong fluidization zone 1b of the gasification chamber 1 and the strong fluidization zone 2b of the main body 5 of the combustion chamber. By changing the fluidized bed height, The amount of ring can be controlled. To change the height of the fluidized bed, supply the fluidized medium when increasing the height of the fluidized bed, and extract the fluidized medium when decreasing the height of the fluidized bed. Therefore, in order to change the height of the fluidized bed, a fluidized medium supply device for supplying the fluidized medium may be provided, a fluidized medium may be supplied, and a fluidized medium extracting device for extracting the fluidized medium may be provided to extract the fluidized medium.

As shown in FIG. 22, the fluid medium supply device 1 1 1 supplies the fluid medium c from the fluid medium storage device 1 1 2 that stores the fluid medium c and the fluid medium c from the fluid medium storage device 1 1 2 that stores the fluid medium c. The fluid medium supply amount measuring device 1 13 that measures the amount and outputs the fluid medium supply amount signal i 21 representing the supply amount, and the fluid medium storage tank in the fluid medium storage device 1 1 2 for the fluid medium c And a fluid medium supply amount control device 114 for controlling the supply amount of the fluid.

The fluid medium supply amount control device 114 is installed, for example, on a line 115 for free-falling the fluid medium from the fluid medium storage device 112 and transporting it to the gasification chamber 1, for example. This is a control valve for controlling the supply amount. The fluid medium supply amount measuring device 113 measures, for example, the change over time of the weight of the fluid medium storage tank in the fluid medium storage device 112 and obtains the fluid medium supply amount from the measured change over time.

The fluid medium supply amount control device 1 14 (for example, the control valve described above) is connected to the fluid medium supply amount signal i 21 from the fluid medium supply amount measurement device 113 and the control device 6 (FIG. 1) described later. To control the fluid medium supply amount.

For example, the fluid medium extraction device 1 16 includes a fluid medium extraction pipe 1 17 provided at the furnace bottom of the gasification chamber 1 and a fluid medium transfer device 1 18 (a screw conveyor, an apron conveyor, etc.). It is comprised including. The fluid medium c extracted and transported by the fluidized-bed medium extracting device 1 16 is supplied to and stored in the above-mentioned “fluid medium storage device 1 12”. The fluid medium discharge amount control device 1 19 (for example, a screw conveyor on / off switch or a screw speed controller) is used to extract the fluid medium from the fluid medium discharge amount measurement device 120. In response to the signal i 22 and the circulating amount signal described below from the control device 6 (Fig. 1), the fluid medium extracting device drive signal i 23 is sent to the fluid medium extracting device 1 16 to control the fluid medium extracting amount. I do. Here, in the present embodiment, the fluid medium The supply amount measuring device 1 1 3 and the fluid medium withdrawal amount measuring device 1 2 0 are the same, for example, by measuring the change over time of the weight of the fluid medium storage tank in the fluid medium storage device 1 12 and measuring. The amount of withdrawal of the fluid medium is determined from the change with time. The fluid medium withdrawal amount measuring device 120 is different from the fluid medium supply amount measuring device 113, and the transport amount of the fluid medium c transported by the fluid medium transport device 118 is defined as the withdrawal amount. It can be measured directly.

Next, a method of measuring the circulation amount will be described with reference to FIG.

The pressure loss of the fluidizing gas in a fluidized bed with a settling flow of the fluidized medium c, such as the settling channel combustion chamber 4, is greater than the pressure loss of the fluidizing gas in a fluidized bed without a settling flow. The reason for this is that the fluidizing gas has an upward flow, and therefore runs counter to the sedimentation flow of the fluidizing medium, thus increasing the resistance of the fluidizing gas. Consider the pressure loss of the fluidized gas between the upper and lower two points with different heights in the fluidized bed (the horizontal position is preferably the same). Assuming that the resistance of the fluidizing gas when there is no sedimentation flow of the fluid medium is Pn and the resistance of the fluidizing gas when there is the sedimentation flow of the fluid medium is Pd, the difference Pd_Pn between them is The faster the settling flow of the flowing medium, the greater. By utilizing this phenomenon, the velocity of the settling flow of the flowing medium can be measured, and from the result, the circulation amount of the flowing medium c can be measured.

That is, the circulation amount can be measured using the following phenomena. (1) The velocity of the settling flow of the fluid medium increases as the circulation volume increases. (2) The higher the velocity of the settling flow of the fluidized medium, the greater the pressure loss of the fluidized gas. (3) The higher the fluidizing gas velocity Vg, the greater the pressure loss of the fluidizing gas.

For example, in the sedimentation chamber 1 combustion chamber 4, the circulation amount can be measured using the following equation.

(Circulation rate) [ _kg / s] = (Body density of fluidized bed) [kg / m ³ ] X (Sedimentation velocity of fluidized medium) [m / s]) X (Cross section of sedimentation chamber) [m ² ] , · '①

(Flowing medium settling velocity) = a XF l (Pd-Pn) XF2 (Vg) · · · Fl which is a function of (Pd-Pn) and F2 which is a function of Vg Can be represented, for example, as follows:

F 1 (Pd-Pn) = a0 + a1X (Pd-Pn) + a2X (Pd-Pn) ² + a 3 X (P d-P n) ³ + · · '③

One reed

F 1 (P d— Ρ η) = β (P d— P n) ^γ · · '④

F 2 (V g) = b O + bl XV g + b 2 XV g ² + b 3 XV g ³ +-

F 2 (V g) = Vg ^f

Here, α, β, γ,, ", 0, 31, 32, 33,"., 130, 131, 2, 63, '' are constants determined by the shape of the gasifier 101. is there. Equations (3) and (4) are of the third-order approximation, but may be first-order and second-order approximations, respectively.

Here, the pressure difference P f 1 — P f 2 between the upper and lower points when there is no sedimentation flow is P fl — P f 2 = P n, and the pressure difference P f between the upper and lower points when there is a sedimentation flow 1 — P f 2 is P f 1 −P f 2 = P d. For example, a state where there is no sedimentation flow is generated under various conditions during the test operation stage, the pressure between the upper and lower points is measured, and the measured data is sent to the control device 6 (Fig. 1). The control unit 6 calculates and stores the pressure difference Pn between the two. Measure the pressure between the upper and lower points when there is a sedimentation flow during the actual production gas production operation of the gasifier 101, and send the measured data to the control device 6 to control the upper and lower points when there is a sedimentation flow. The control device 6 calculates the pressure difference Pd between them, and further causes the control device 6 to calculate (Pd-Pn).

The flow rate of the fluidizing gas g4 (Fig. 1) supplied to the sedimentation-chamber combustion chamber 4 (Fig. 1) is determined by the flow meter 75 (Fig. 1), and the flow signal i2 (Fig. 1) is obtained. Since it is sent to the controller 6, the controller 6 can calculate the fluidized gas velocity V g (V g 4) of the sedimentation chamber 1 and the combustion chamber 4.

Therefore, in the control device 6, V g is substituted into equation (or equation (1)) to obtain F2, and (Pd-Pn) is substituted into equation (3) (or equation (2)) to obtain F1, and equation (2) is obtained. Substituting F 1 and F 2 into, the flow medium settling velocity is determined. Substituting the settling velocity of the fluidized medium thus obtained and the bulk density of the fluidized bed obtained from the above equation (3) into equation (1), α is known (it can be empirically obtained at the time of test operation etc.) Therefore, the circulation amount can be obtained. The amount of circulation can be controlled using the amount of circulation obtained in this way. That is, the flow rate of the sedimentation channel and combustion chamber 4 is set so that the obtained circulation amount becomes an appropriate value. The gasification chamber layer temperature and the gasification chamber outlet gas composition can be controlled by controlling the amount of mobilized gas. The control device 6 may output a fluid medium circulation amount signal indicating the amount of circulation of the fluid medium.

As described above, the pressure measuring devices 91 and 9 2 for measuring the fluidized bed pressure at the upper and lower points in the fluidized bed of the settling channel combustion chamber 4 and the fluidizing gas of the settling channel combustion chamber 4 g 4 Flow rate measuring device (flow rate measuring device) 7 5 (Fig. 1) and control device as an arithmetic device for calculating the circulation amount from the difference between the fluidized bed pressure at the upper and lower points and the amount of fluidized gas 6 , The amount of circulation can be measured.

According to the principle described above, the amount of fluidized gas in the sedimentation-chamber combustion chamber 4 is an operating factor of the circulation amount control. Therefore, in order to control the amount of circulation, a flow control valve (control valve) 65 (Fig. 1) for changing the flow rate of the fluidized gas in the sedimentation chamber 1 combustion chamber 4 is provided. It can be carried out.

The circulating volume can be controlled by combining the measurement of the fluidized bed height and the circulating volume described above.

The circulation amount is controlled as follows. First, the height of the fluidized bed is measured (step 1). In order to measure the fluidized bed height, the fluidized bed pressure at each point is measured by each pressure measuring device 91, 92 installed between two points in the fluidized bed. The measured value of the fluidized bed pressure is input to the control device 6 as an arithmetic unit for calculating the fluidized bed height, where the fluidized bed height is calculated. The calculated fluidized bed height is input to the control unit 6 for controlling the circulation amount (data is exchanged in the control unit 6).

Next, the circulation amount is measured (step 2).

Measured values by the pressure measuring devices 91 and 92 installed between two points in the fluidized bed of the settling channel combustion chamber 4 and the flow rate installed for measuring the fluidized gas flow rate of the settling channel combustion chamber 4 The measured value of the measuring device 75 is input to the control device 6 as an arithmetic device for calculating the amount of circulation, and the amount of circulation is calculated by the control device 6. The calculated circulation amount is input to the control device 6 for controlling the circulation amount (data is exchanged in the control device 6).

Next, the circulation amount is controlled (step 3).

For example, at some point, if the amount of circulation of Wp is controlled to the amount of circulation of Ws, The signal corresponding to the measurement value Wp of the circulation amount calculated in Step 2 and the signal corresponding to the circulation amount Ws to be set are sent to the control device 6. If Ws <Wp, the controller 6 sends a signal to increase the height of the fluidized bed to the fluid medium supply controller 114 (FIG. 22) .If Ws> WP, the controller 6 increases the fluidized bed height. The lowering signal is sent to the fluid extraction device 118 (FIG. 22).

When the fluid medium supply control device 114 (FIG. 22) receives a signal to increase the fluidized bed height. The fluid medium supply control device 114 increases the fluid medium supply amount by, for example, opening the control valve. To the control valve. As a result, when the opening of the control valve is opened, the fluidized medium is supplied into the furnace, the height of the fluidized bed is increased, and the circulation amount is increased. The fluid medium supply amount control device 114 also receives a signal from the fluid medium supply amount measurement device 113 (FIG. 22), and performs an operation for determining the fluid medium supply amount so that the fluid medium is not suddenly supplied into the furnace. Perform (Because the fluid medium stored in the fluid medium storage layer of the fluid medium storage device 112 (Fig. 22) is lower than the furnace temperature, make sure that the furnace temperature does not fall too low due to the rapid supply of the fluid medium. .

When the fluid medium withdrawal control device 119 (Fig. 22) receives a signal to lower the fluidized bed height, a switch to reduce the fluidized media supply, for example, a screw conveyer 118 for fluidized media withdrawal (Fig. 22) Send an ON signal or a signal to increase the speed of the screw conveyor. As a result, the screw conveyer is activated or the number of revolutions of the screw conveyer increases, and as a result, the flow medium is discharged from the furnace through the flow medium discharge pipe 117 (Fig. 22). As a result, the height of the fluidized bed is reduced and the circulation amount is reduced. With the above configuration, it is possible to control the circulation amount by changing the fluidized bed height. Next, a description will be given with reference to FIG. In the integrated gasifier 101 according to the present invention, the combustion chamber main body 5 and the sedimentation combustion chamber 4 (which have an opening PX at the top) are separated by a partition wall 14 having an opening at the top. The fluid medium c moves between the chambers A and B separated by the partition wall X (see Fig. 2 (a)), and the partition wall 11 has an opening 21 at the bottom. Fluid medium c between gasification chamber 1 and chamber 5 of the combustion chamber (corresponding to chambers A and B separated by a partition wall Y having an opening Qy at the bottom (see Fig. 2 (b))) Movement by a partition wall 15 with an opening 25 at the bottom Separated sedimentation channel 1 Fluid medium between combustion chamber 4 and gasification chamber 1 (corresponding to chambers A and B separated by a partition wall Y having an opening Qy at the bottom (see Fig. 2 (b))) Movement of c, heat recovery chamber 3 and char combustion chamber body 5 separated by a partition wall 12 having an upper opening and a lower opening 22 (an upper opening P z and a lower opening Corresponds to chambers A and B separated by a partition wall Z having a section Q z (see Fig. 2 (c)). By appropriately combining the movement of the fluid medium between It is configured so that c can be moved continuously and the amount of movement can be adjusted. In the gasification chamber 1, near the surface in contact with the partition wall 15 between the sedimentation chamber and the combustion chamber 4, there is a weak fluidization zone 4 a where the weak fluidization state of the sedimentation chamber and the combustion chamber 4 is maintained. There is a strong fluidized area 1b as a section where the fluidized state is maintained stronger than the fluidized state. As a whole, the superficial velocity of the fluidizing gas should be varied depending on the location so that the mixed diffusion of the injected fuel and the fluidized medium c is promoted.As an example, as shown in FIG. In addition to the strong fluidization zone 1b, a weak fluidization zone 1a is provided as a section where a weak fluidization state is maintained so that a swirling flow is formed. In the strong fluidization zone 1 b and the weak fluidization zone la, the fluidizing gas g 1 has a uniform fluidization rate over the entire area.

The main combustion chamber main part 5 is a weak fluidized area 2a in the center where a weak fluidized state is maintained, and a strong fluidized area in the periphery where a strong fluidized state is maintained. It has a zone 2b, in which the fluid medium c and the channel h form an internal swirling flow. In the strong fluidization zone 2b and the weak fluidization zone 2a, the fluidizing gas g2 has a uniform fluidization rate over the entire area. It is preferable that the fluidization speed in the strong fluidization zone 2 b in the gasification chamber 1 and the chamber 1 of the combustion chamber main body 5 be 5 Umf or more, and that in the weak fluidization zone 2 a be 5 Umf or less. However, if there is a clear difference in the fluidization rate between the weak fluidization zone 2a and the strong fluidization zone 2b, there is no particular problem if the difference is exceeded. It is preferable to provide a strong fluidization zone 2b in the part that contacts the heat recovery chamber 3 in the main chamber 5 and the settling chamber 4. In the heat recovery chamber 3, a weak fluidized area 3a is provided, and in the settling channel combustion chamber 4, a weak fluidized area 4a is provided. In the weak fluidization zone 3a and the weak fluidization zone 4a, the fluidizing gas g3 and g4 each have a uniform fluidization rate over the entire area. If necessary, the bottom of the furnace should be located from the weak fluidization zone to the strong fluidization zone. It is better to provide a gradient that goes down (not shown).

As described above, the fluidized state of the main combustion chamber main body 5 near the partition wall 12 between the main combustion chamber main body 5 and the heat recovery chamber 3 is relative to the fluidized state of the heat recovery chamber 3 side. By maintaining the fluidized state, the fluid medium c flows into the heat recovery chamber 3 from the combustion chamber main body 5 side over the upper end of the partition wall 12 near the fluidized bed interface, and flows in The fluid medium c moves downward (toward the bottom of the furnace) due to the relatively weak fluidized state, ie, high density state, in the heat recovery chamber 3, and the lower end of the partition wall 12 near the bottom of the furnace (opening of the bottom). 2 2), and move from the heat recovery chamber 3 side to the char combustion chamber main body 5 side. The fluid medium c moves through the opening 22 from the heat recovery chamber 3 to the combustion chamber main body 5 side through the opening 2 2 in the strong fluidization zone 2 b of the combustion chamber main body 5. Comparing the fluidized state of the fluid medium c near 2 and the fluidized state of the fluid medium c near 2 2 near the opening of the weak fluidized area 3 a of the heat recovery chamber 3, the former is better than the latter. Is also strong.

Similarly, the fluidization state on the side of the combustion chamber main body 5 near the partition wall 14 between the main chamber 5 of the combustion chamber and the combustion chamber 4 on the sedimentation is referred to as the fluidization state on the side of the combustion chamber 4 By maintaining a relatively strong fluidization state, the fluid medium c is settled from the side of the combustion chamber main body 5 over the upper end of the partition wall 14 near the interface of the fluidized bed and the sedimentation chamber 4 Move in to the side. The fluid medium c that has flowed into the settling chamber 4 moves downward (toward the furnace bottom) due to the relatively weak fluidized state in the settling chamber 4, that is, the high-density state. Through the lower end (opening 25) near the bottom of the furnace of No. 15, the sedimentation chamber moves from the combustion chamber 4 side to the gasification chamber 1 side. Here, the fluidized state of the fluid medium c near the opening 25 of the strong fluidization zone 1 b of the gasification chamber 1 and the vicinity of the opening 25 of the weak fluidization zone 4 a of the sedimentation combustion chamber 4 Comparing with the fluidized state of the fluid medium c, the former is stronger than the latter. Thereby, the movement of the fluid medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 is assisted by the attracting action.

Similarly, the fluidization state on the side of the combustion chamber body 5 near the partition wall 11 between the gasification chamber 1 and the combustion chamber body 5 is higher than the fluidization state on the gasification chamber 1 side. Relatively strong liquidity is maintained. Therefore, the fluid medium c passes through the opening 21 below the fluidized bed interface of the partition wall 11, preferably below the upper surface of the dense layer (submerged in the dense layer), and through the opening portion 21, the main body of the combustion chamber of the chamber is discharged. Flow into the 5 side. Fluid medium c has opening 2 1 Moving from the gasification chamber 1 side to the combustion chamber main body 5 side through the chamber is the fluidization of the fluid medium c near the opening 21 of the strong fluidization zone 2 b of the combustion chamber main body 5 When the state is compared with the state of fluidization of the fluid medium c near the opening 21 of the weak fluidization zone 1a of the gasification chamber 1, the former is stronger than the latter.

As described above, the entire heat recovery chamber 3 is uniformly fluidized, and the fluidized state is generally weaker than the fluidized state of the main combustion chamber main body 5 in contact with the heat recovery chamber 3 at most. Will be maintained. Therefore, the superficial velocity of the fluidizing gas g3 in the heat recovery chamber 3 is controlled between 0 and 3 Umf, and the fluidized medium c forms a settling fluidized bed while flowing slowly. Here, 0 Umf means that the fluidizing gas g 3 has stopped. In such a state, the heat recovery in the heat recovery chamber 3 can be minimized. That is, the heat recovery chamber 3 can arbitrarily adjust the amount of recovered heat from the maximum to the minimum by changing the fluidized state of the fluid medium c. In the heat recovery chamber 3, the fluidization may be uniformly started and stopped or controlled in intensity throughout the entire chamber.However, it is also possible to stop the fluidization in a part of the area and place the others in the fluidized state. However, the flow strength of the fluidized state in a part of the area may be adjusted.

Further, with reference to FIG. 1, a method of adjusting the amount of circulation of the fluid medium c between the gasification chamber 1 and the combustion chamber main body 5 will be specifically described below.

Fluidized gas velocity in the weak fluidization zone 1a located on the gasification chamber 1 side of the opening 21 provided in the lower end of the partition wall 1 1 that separates the gasification chamber 1 from the chamber 1 of the combustion chamber Let us consider a case in which the amount of movement of the fluid medium c from the gasification chamber 1 through the opening 21 to the main chamber 5 of the combustion chamber is increased by changing the pressure. In this case, the movement amount of the fluid medium c from the gasification chamber 1 to the combustion chamber main body 5 through the opening 21 first increases, so that the height of the fluidized bed of the combustion chamber main body 5 increases. Then, the height of the fluidized bed in the gasification chamber 1 decreases temporarily.

As described above, due to such a change in the fluidized bed height, the movement of the fluidized medium c through the opening 21 acts in a direction that can be suppressed, and the fluid medium c is balanced in a certain state. The rise in the fluidized bed height in the main chamber 5 of the combustion chamber increases the amount of the fluid medium c that jumps from the main body 5 of the combustion chamber into the sedimentation chamber 4 through the partition wall 14. Bring increase. As a result, the pressure at the bottom of the sedimentation chamber 1 combustion chamber 4 increases, On the other hand, the pressure at the bottom of the gasification chamber 1 decreases due to the decrease in the height of the fluidized bed in the gasification chamber 1.

For this reason, paying attention to the opening 25 provided at the lower end of the partition wall 15 that separates the gasification chamber 1 and the sedimentation-chamber combustion chamber 4, the pressure on the sedimentation-chamber combustion chamber 4 side increases, Since the pressure on the gasification chamber 1 side decreases, the amount of movement of the fluid medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 via the opening 25 increases using the pressure difference as the driving force. I do. As described above, the height of the fluidized bed changes due to the increase in the amount of movement of the fluidized medium c from the gasification chamber 1 given to the chamber 1 to the combustion chamber main body 5. The increase in the amount of fluidized medium c transferred to the combustion chamber body 5 is slightly negated, and the amount of fluidized medium c transferred from the cylinder to the gasification chamber 1 via the sedimentation chamber 1 and the combustion chamber 4 Is brought about. By this mechanism, the flow of gas between the gasification chamber 1 and the main part of the combustion chamber 5 is finally balanced so that the amount of particles of the fluid medium c between the gasification chamber 1 and the main part of the combustion chamber 5 is balanced. The bed height changes and stabilizes, but the amount of particle movement in a stable state is kept higher than the initial state.

That is, in order to adjust the circulation amount of the fluid medium c between the gasification chamber 1 and the char combustion chamber main body 5, the movement amount of the fluid medium c from the gasification chamber 1 to the char combustion chamber main body 5 is adjusted. May be changed. Also, the amount of movement of the fluid medium c from the chamber 1 to the gasification chamber 1 may be changed, or both may be changed. By changing the height of the fluidized bed, only one of the two operations is performed, and the amount of movement of the fluid medium c from the gasification chamber 1 to the chamber 1 of the combustion chamber and the It is possible to stabilize the state in which the amount of movement of the fluid medium c from one combustion chamber body 5 to the gasification chamber 1 is balanced.

Therefore, in order to adjust the amount of movement of the fluid medium c between the gasification chamber 1 and the main chamber 5 of the combustion chamber, as described above, the combustion chamber 1 is moved from the gasification chamber 1 through the opening 21 as described above. The amount of movement of the fluid medium c to the firing chamber body 5 may be adjusted, or the fluid medium from the combustion chamber body 5 to the sedimentation chamber 4 beyond the upper end of the partition wall 14 The moving amount of c may be adjusted, or the moving amount of the fluid medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 through the opening 25 may be adjusted. Here, in either case, the amount of movement of the fluidized medium c is adjusted by changing the amount of fluidized gas g supplied from the furnace bottom. In order to ensure the function, the supply amount of the fluidizing gas g was changed to change the fuel gasification reaction performed in the gasification chamber 1 and the fuel gasification reaction performed in the combustion chamber body 5. It is desirable that the combustion reaction is not affected. That is, it is desirable that the total amount of the fluidizing gas g 1 supplied to the gasification chamber 1 or the total amount of the fluidizing gas g 2 supplied to the chamber 1 for the combustion chamber does not change.

For example, near the opening 21 of the gasification chamber 1, the supply of the fluidized gas g 1 in the weak fluidization zone 1 a is reduced, and the strong flow near the opening 21 of the combustion chamber body 5 is reduced. By increasing the supply of the fluidizing gas g2 in the gasification zone 2b, it is possible to increase the amount of movement of the fluidizing medium c from the gasification chamber 1 to the char combustion chamber main body 5 through the opening 21. When adjusting the flow rate, the supply amount of the fluidizing gas g1 to the strong fluidization area 1b of the opening 21 of the gasification chamber 1 is increased, and the opening 21 of the main body 5 of the combustion chamber is reduced. By reducing the supply of the fluidized gas g2 in the weak fluidized zone 2a, each fluidized gas g1, g2 supplied to each of the gasification chamber 1 and the combustion chamber main body 5 is reduced. It is desirable to perform an operation that does not change the total amount including the supply amount.

In addition, the supply amount of the fluidizing gas g2 in the strong fluidization zone 2b near the partition wall 14 of the chamber 1 of the combustion chamber was increased, and the sedimentation chamber 1 By increasing the amount of the fluid medium c that jumps across the partition wall 14 to the partition wall 4, the amount of the fluid medium c that moves from the main combustion chamber body 5 to the sedimentation chamber 4 increases. When the amount of fluidized gas g2 supplied to the weak fluidization zone 2a away from the partition wall 14 of the combustion chamber main body 5 is reduced, the supply volume of the combustion chamber main body 5 is reduced. It is desirable to perform an operation so that the total amount of the supplied fluidized gas g2 does not change. On the other hand, when adjusting the movement amount of the fluidized medium c from the sedimentation chamber 1 to the gasification chamber 1 through the opening 25, the gasification chamber 1 or the chamber 5 The amount of fluidized gas g4 supplied to the sedimentation chamber 1 combustion chamber 4 only by changing the amount of fluidized gas g4 supplied to the sedimentation chamber 1 without changing the supply of fluidized gas gl and g2 This is particularly suitable because

In this case, the strong flow area 1 b is located near the opening 25 on the gasification chamber 1 side, The submerged sedimentation chamber 4 side is maintained in a weakly fluidized state because it is a weak fluidized area 4a as a section, so the strong fluidized area on the gasification chamber 1 side is maintained. By changing the strength of the weak fluidization state on the settling channel combustion chamber 4 side while maintaining the strong fluidized state of 1 b constant, the sedimentation channel combustion chamber 4 is effectively moved from the sedimentation channel combustion chamber 4 to the gasification chamber 1. The moving amount of the fluid medium c can be adjusted.

As described above, the strong fluidization region 1b near the gasification chamber 1 side of the opening 25 is desirably maintained in a strong fluidization state, and the fluidizing gas velocity is preferably 4 Umf or more. However, more preferably, it should be kept at 5 Umf or more. In this case, the velocity of the fluidizing gas in the sedimentation chamber 1 is set to a range of 4 Umf or less (when the flow rate of the fluidizing gas in the strong fluidization region lb is 4 Umf or more) or a range of 5 Umf or less (the strong fluidization region lb The flow rate of the fluidized medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 is adjusted in accordance with the characteristics shown in Fig. 4 by changing the flow rate of the fluidizing gas to 5 Umf or more. can do.

According to FIG. 4, especially when the velocity of the fluidizing gas on the settling chamber 1 combustion chamber 4 side is changed in the range of lUmf to 2Umf, more preferably in the range of lUmf to 1.7Umf, It can be seen that the movement amount of c changes largely linearly. In this case, the amount of the fluidizing gas g4 supplied to the sedimentation-chamber combustion chamber 4 can be reduced, and the moving amount of the fluidizing medium _c can be finely adjusted.

Of course, conversely, the weak fluidization state of the settling channel combustion chamber 4 is kept constant, and the strong fluidization state of the gasification chamber 1 is changed. It is also possible to change the moving amount of the fluid medium c to 1. However, in that case, the change in the flow rate of the fluidizing gas g1 for changing the moving amount of the fluidizing medium c increases, and the conditions of the gasification reaction in the gasification chamber 1 also change, which is not preferable. In other words, as described later, in practice, changing the bed temperature of the gasification chamber 1 is very important in controlling the properties of the generated gas b. When the state is changed, the reaction conditions of the gasification chamber 1 are also changed with the change of the bed temperature, and it becomes difficult to independently control only the bed temperature of the gasification chamber 1. On the other hand, in the case of controlling the amount of movement of the fluidized medium c by changing the state of weak fluidization of the settling channel combustion chamber 4 described above, the change in the flow rate of the fluidized gas g4 Very little Since a large change in the moving amount of the fluid medium c can be realized without this (see Fig. 4), the gasification chamber has the advantages of good controllability and little effect on the efficiency of the entire process. There is a great advantage in that the bed temperature of the gasification chamber 1 can be controlled without changing the flow rate of the fluidizing gas g1 supplied to 1.

Next, control of the gas velocity of the fluidizing gas g will be described with reference to FIG. First, control of the gas velocity of the fluidizing gas g1 supplied to the gasification chamber 1 will be described. As described above, the control valve 61 installed in the supply pipe 51 connected to the air diffuser 31 arranged at the bottom of the furnace corresponding to the weak fluidization zone 1a of the gasification chamber 1 is controlled by the control valve 61. The valve opening is set in response to the control signal i 1 from the device 6. Fluidizing gas g 1 having a flow rate corresponding to the valve opening is supplied to the air diffuser 31 via the control valve 61. The fluidized gas g 1 is supplied to the weak fluidized zone 1 a at the fluidized gas velocity determined by the flow rate of the supplied fluidized gas _{c The} fluidized gas g 1 is supplied to the fluidized area 1 a The control valve 6 on the supply pipe 5 1 The flow rate is measured by a flow rate measuring device 71 installed on the downstream side of 1 and the measured flow rate is sent from the flow rate measuring device 71 to the control device 6 as a flow rate signal i 2. The control device 6 compares the measured flow signal i 2 with the target flow rate in the weak fluidization zone 1 a stored inside, and controls the control valve 61 so that the flow signal i 2 approaches the target value. The value of the control signal i 1 is changed, and the changed control signal i 1 is sent from the control device 6 to the control valve 61.

The control of the gas velocity of the fluidized gas g1 in the weak fluidization zone 1a of the gasification chamber 1 has been described above.The weak flow in the strong fluidization zone 1b of the gasification chamber 1 and the weak combustion chamber 2 The same applies to the fluidized zone 2a, the strong fluidized zone 2b, the weak fluidized zone 4a, and the weakly fluidized zone 3a of the heat recovery chamber 3.

The target value of the flow rate of the fluidized gas g1 supplied to the weak fluidization zone 1a of the gasification chamber 1 and the target value of the flow rate of the fluidized gas g1 supplied to the strong fluidization zone 1b are the target The strength of the fluidized state inside the gasification chamber 1 that moves from the weakly fluidized area 1a of the gasification chamber 1 to the weakly fluidized area 1a of the main body 5 of the combustion chamber via the opening 21. Of the fluidized medium c moving from the settling chamber 1 to the strong fluidized area 1 b of the gasification chamber 1, the amount of the fluidized medium c moved to the gasification chamber 1 measured by the temperature measuring device 4 2 Bed temperature and gas composition of the gas b measured by the gas composition measuring device 46 are taken into consideration, and the bed temperature of the gasification chamber 1 is set to a predetermined value (for example, 600 to 800 ° C). Or the gas composition is When it is determined that the content is constant (for example, the H ₂ / CO molar ratio is 2.6 to 5.8),

The target value of the flow rate of the fluidizing gas g2 supplied to the weak fluidization zone 2a of the first combustion chamber 2. The target value of the flow rate of the fluidizing gas g2 supplied to the strong fluidization zone 2b is settling. The target value of the flow rate of the fluidizing gas g4 supplied to the chamber 1 is determined by the strength of the fluidized state inside the main body 5 of the combustion chamber and the target sedimentation chamber by the target. The strength of the fluidized state at 4, the amount of movement of the fluid medium c that moves from the strong fluidized area 2b of the chamber 1 to the sedimentation chamber 4 over the upper end of the partition wall 14. The amount of the fluid medium c moving from the sedimentation chamber combustion chamber 4 to the strong fluidization zone 2 b of the gasification chamber 1 via the opening 25, and from the heat recovery chamber 3 via the opening 22. The amount of movement of the fluid medium c moving to the strong fluidization zone 2 b of the combustion chamber body 5, the heat recovery chamber from the strong fluidization zone 2 b of the combustion chamber body 5 to the upper end of the partition wall 1 2 Move to 3 Considering the total amount of movement of the flowing medium c and the layer temperature of the chamber 1 of the combustion chamber measured by the temperature measuring device 4 3, the layer temperature of the chamber 5 of the combustion chamber becomes a predetermined value (for example, 850-950 ° C), and the gasification residue (char, tar, etc.) supplied from the gasification chamber 1 is determined to be completely burned.

When the heat recovery chamber 3 is provided, the layer temperature of the main chamber 5 is affected by the amount of heat recovered in the heat recovery chamber 3, and if the amount of heat recovery increases, the layer temperature of the main body 5 of the combustion chamber 5 increases. The bed temperature decreases, and if the heat recovery amount decreases, the bed temperature of the main chamber 5 of the combustion chamber increases.

Next, a control method for increasing or decreasing the heat recovery amount in the heat recovery chamber 3 will be described. The amount of heat recovery in the heat recovery chamber 3 is determined by the heat transfer coefficient between the fluid medium c and the in-bed heat transfer tube 41A. This heat transfer coefficient is closely related to the degree of fluidization in the heat recovery chamber 3, and the stronger the fluidization, the larger the heat transfer coefficient, and the more the in-bed heat transfer tubes take away heat from the fluid medium. . Therefore, in order to keep the bed temperature of the main chamber 5 of the combustion chamber constant, the flow rate of the fluidizing gas g3 supplied to the fluidized bed of the heat recovery chamber 3 is controlled to control the heat recovery chamber 3 In this case, the level of fluidization may be changed.

The control valve 6 6 installed in the supply pipe 56 for introducing the fluidized gas g 3 supplied to the heat recovery chamber 3 receives the control signal i 1 from the control device 6 and sets the valve opening. Fluidizing gas g3 at a flow rate corresponding to the valve opening is supplied to the fluidized bed of the heat recovery chamber 3 via the control valve 66. Supplied. The flow rate of the fluidizing gas g3 is measured by a flow rate measuring device 76 installed downstream of the control valve 66, and the measured flow rate is sent to the control device 6 as a control signal i2. As described above, the greater the flow rate of the fluidizing gas g3, the stronger the fluidization of the heat recovery chamber 3 and the greater the amount of heat recovery, so that the bed temperature of the main chamber 5 of the combustion chamber is higher than the target value. In this case, the control device 6 changes the value of the control signal i 1 to the control valve 66 so that the bed temperature of the main portion 5 of the combustion chamber approaches the target value, and adjusts the flow rate of the fluidizing gas g 3. What is necessary is just to configure so that it may increase. If the bed temperature of the main chamber 5 is lower than the target value, the controller 6 controls the control valves 6 6 so that the bed temperature of the main chamber 5 approaches the target value. What is necessary is just to change the value of the signal i 1 and reduce the flow rate of the fluidizing gas g 3.

On the other hand, for steam, a control valve 67 installed in the introduction section 41B of the in-layer heat transfer tube 41 receives the control signal i1 from the control device 6 and sets the valve opening. Steam s 1 having a flow rate corresponding to the valve opening is supplied to the in-layer heat transfer tube main body 41 A via the control valve 67. The steam s 1 introduced into the bed heat transfer tube body 4 1 A receives heat from the fluid medium c according to the heat transfer coefficient determined by the fluidized state of the heat recovery chamber 3 and is heated to become superheated steam s 2, which is discharged. Emitted from part 41 C. The flow rate of the steam s 1 is measured by a flow rate measuring device 77 installed downstream of the control valve 67 on the inlet 41 B, and the measured flow rate is a flow rate signal i 2, 7 Sent to controller 6 from 7 The temperature of the steam s 1 before overheating is measured by a temperature measuring device 44 installed in the introduction section 41B, and the measured temperature is sent to the control device 6 as a temperature signal i 3. The temperature of the steam s 2 after the overheating is measured by a temperature measuring device 45 installed in the discharge part 41 C, and the measured temperature is sent to the control device 6 as a temperature signal i 3.

For example, if the fluidization of the heat recovery chamber 3 is strengthened to increase the amount of heat recovery, if the flow rate of the steam si supplied to the in-bed heat transfer tubes 41 is kept constant, the obtained superheated steam The temperature of s2 rises. If the use of superheated steam s2 makes it unfavorable to increase the temperature, the flow rate of superheated steam s2 is recovered by increasing the flow rate of steam s1 supplied to recover the increase in heat recovery. Can be reflected in the increase. In this case, the controller 6 changes the value of the control signal i 1 to the control valve 67 when the temperature signal i 3 of the steam s 2 after overheating is higher than the target temperature of the steam s 2. Stream of steam s 1 It may be configured to increase the amount. Conversely, if the temperature signal i 3 of the steam s 2 after overheating is lower than the target temperature of the steam s 2, the value of the control signal i 1 to the control valve 67 is changed to decrease the flow rate of the steam s 1 It may be configured as follows.

Relatively large incombustibles contained in waste or fuel a are discharged from the incombustible outlet (not shown) provided at the bottom of the gasification chamber 1. In addition, the bottom of the furnace in each chamber may be horizontal. In order not to form a stagnant portion for the flow of the fluidized medium c, the furnace bottom may be inclined according to the flow of the fluidized medium c near the furnace bottom. In addition, the noncombustible material discharge port (not shown) may be provided not only in the furnace bottom of the gasification chamber 1 but also in the furnace bottom of the combustion chamber main body 5, the sedimentation combustion chamber 4, or the heat recovery chamber 3. .

The most preferable fluidized gas g1 in the gasification chamber 1 is to use the product gas b at a high pressure for recycle. In this way, the generated gas b from the gasification chamber 1 is only the generated gas b purely generated from the fuel, and a very high quality generated gas b can be obtained. If this is not possible, a gas containing as little oxygen as possible (oxygen-free gas), such as steam, carbon dioxide (C02) or flue gas from the combustion chamber 2, is used as the fluidizing gas g1. Is good. If the bed temperature of the fluidized medium c decreases due to the endothermic reaction during gasification, supply combustion exhaust gas with a temperature higher than the thermal decomposition temperature as necessary, or add oxygen to the oxygen-free gas. Alternatively, a gas containing oxygen, for example, air may be supplied to burn a part of the product gas b. The fluidizing gas g2, g4 supplied to the char combustion chamber 2 supplies a gas containing oxygen necessary for char combustion, for example, a mixed gas of air, oxygen and steam. When the calorific value of fuel a is low, it is preferable to increase the amount of oxygen, and oxygen is supplied as it is. Air, steam, combustion exhaust gas, and the like are used as the fluidizing gas g3 to be supplied to the heat recovery chamber 3.

The portion above the upper surface of the fluidized bed (the upper surface of the splash zone) of the gasification chamber 1 and the combustion chamber 2, that is, the freeboard portion, is completely separated by partition walls 11, 15. Furthermore, since the upper part of the fluidized bed above the dense layer, that is, the splash zone and the freeboard part, are completely separated by partition walls, the freebore of each of the combustion chamber 2 and the gasification chamber 1 is used. Even if the pressure balance at the tip part is slightly disturbed, the difference in the position of the interface between both fluidized beds or the difference in the position of the upper surface of the dense bed, that is, the difference in the height of the fluidized bed is large Disturbance can be absorbed with only a small change. That is, since the gasification chamber 1 and the char combustion chamber 2 are separated by the partition walls 11 and 15, even if the pressure in each chamber fluctuates, this pressure difference is absorbed by the fluidized bed height difference. It can be absorbed until either layer falls to the top of the openings 21, 25. Therefore, the upper limit of the pressure difference between the freeboard of the char combustion chamber 2 and the freeboard of the gasification chamber 1 that can be absorbed by the height difference of the fluidized bed is the lower opening 21, 25 of the partition walls 11, 15. The head difference between the head of the gasification chamber fluidized bed and the head of the fluidized bed of the combustion chamber from the upper end of the chamber is approximately equal.

However, in the case described above, when a slight disturbance in the pressure balance is absorbed by the difference in the height of the fluidized bed, the amount of movement of the fluidized medium c between the chambers changes according to the change in the height of the fluidized bed. Therefore, in order to keep the moving amount of the fluid medium c between the respective chambers, it is important to add a control mechanism for minimizing the disturbance of the pressure balance.

With reference to FIG. 1, a control method for suppressing the disturbance of the pressure balance will be described below. The generated gas b discharged from the gasification chamber 1 and the combustion gas e discharged from the char combustion chamber 2 pass through a control valve 78 or 799 for pressure control installed at the subsequent stage, respectively. It is discharged and used.

Here, in FIG. 1, it is illustrated that the control valves 78 and 79 are installed immediately after the gas is discharged from the gasification chamber 1 or the char combustion chamber 2. Even if the control valve 78 or control valve 79 is installed after passing through other equipment, the corresponding gasification chamber 1 or control valve can be controlled by adjusting the opening of the control valve 78 or control valve Ί9. It suffices if the resistance of gas discharge from the first combustion chamber 2 can be changed and the pressure of the gasification chamber 1 or the first combustion chamber 2 can be changed. The freeboard section of the gasification chamber 1 and the freeboard section of the char combustion chamber 2 are equipped with pressure measuring devices 81 and 82 as pressure measuring devices, respectively. , 2 are detected and sent to the controller 6 as a pressure signal i 5. The controller 6 compares the pressure signal i5 of the freeboard section of the gasification chamber 1 with the pressure signal i5 of the freeboard section of the combustion chamber 2 and finds the difference between the chambers of the fluid medium c. Within a certain range that does not affect the amount of movement, preferably the pressure difference between the two chambers 1 and 2 is less than ± 10% of the pressure loss of the fluidized bed in the gasification chamber 1 or the char-combustion chamber 2, and The control signal i 1 is adjusted so that the pressure is preferably ± 5% or less, and more preferably the pressures in both chambers 1 and 2 are equal. Alternatively, it is sent to the control valve 79 to change the opening of the control valve 78 or the control valve 79 _; in the integrated gasifier 101 described above, the inside of one fluidized bed furnace is provided with a gasification chamber. 1.Character combustion chamber 2 and heat recovery chamber are respectively provided via partition walls.Charger combustion chamber 2 and gasification chamber 1, and char combustion chamber 2 and heat recovery chamber 3 are adjacent to each other. It is set up. The integrated gasifier 101 enables circulation of a large amount of the fluid medium c between the combustion chamber 2 and the gasification chamber 1, so that only the sensible heat of the fluid medium c can be used for gasification. A sufficient amount of heat can be supplied.

Furthermore, in the integrated gasifier 101 described above, the seal between the combustion gas e and the generated gas b is completely completed, so that the pressure balance between the gasification chamber 1 and the combustion chamber 2 can be controlled. Successful, the combustion gas e and the product gas b do not mix, and the properties of the product gas b do not deteriorate.

In addition, the fluid medium c as a heat medium and the channel h flow from the gasification chamber 1 to the channel combustion chamber 2 side. Since it is configured to return from the chamber 2 side to the gasification chamber 1 side, a natural balance is achieved, and a conveyer etc. is used to return the fluid medium c from the first combustion chamber 2 side to the gasification chamber 1 side. There is no need to transport them mechanically, and there are no problems such as difficulty in handling high-temperature particles and large sensible heat loss.

Next, the control of the gas composition of the generated gas b of the integrated gasifier 101 will be described with reference to FIG.

In the present invention, as described above, by adjusting the moving amount of the fluid medium c between the gasification chamber 1 and the char combustion chamber 2, that is, the internal circulation amount, the gasification chamber 1 and the char combustion chamber are adjusted. The purpose of this method is to control the fluidized bed temperature arbitrarily in practical use, or to change the composition of the generated gas b generated from the gasification chamber 1. For this reason, integrated gasifier

In the operation of 101, the controller 6 is instructed to change the fluidized gas amount. That is, a control signal i for controlling the flow rate from the control device 6 to the control valves 61 to 67.

1 is sent and control valve 6:! ~ 67 adjusts the fluidizing gas flow rate. Adjusting the fluidizing gas flow rate means adjusting the fluidizing gas velocity. When the velocity of the fluidizing gas is adjusted, how the internal circulation rate is adjusted, whereby the temperature of the fluidized bed of the gasification chamber 1 and the combustion chamber 2 of the gasification chamber, and also the product gas b generated from the gasification chamber 1 Composition It is preferable to configure the control device 6 with a control logic that measures whether or not it changes as described above and adjusts the fluidized gas amount based on the result.

For example, the case where the internal circulation amount is adjusted for the purpose of changing the fluidized bed temperature of the gasification chamber 1 will be described below.

More specifically, the fluidizing gas velocity in the settling chamber 1 combustion chamber 4 is in a weak fluidization state in the range of about lUmf to 2Umf, and the temperature of the fluidized bed temperature in the gasification chamber 1 is measured by the temperature measuring device 42. Consider the case where the temperature is lower than the target fluidized bed temperature of gasification chamber 1. In this case, as described above, the viscosity of the fluidized bed of the sedimentation-chamber combustion chamber 4 is reduced by increasing the amount of fluidizing gas in the sedimentation-chamber combustion chamber 4 within the range of lUmf to 2Umf ( The amount of movement of the fluid medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 can be reduced (see Fig. 3) (see Fig. 4).

As described above, at this time, if the moving amount of the fluidized medium c from the sedimentation chamber 1 combustion chamber 4 to the gasification chamber 1 increases, the gas height of the gasification chamber 1 temporarily increases, and the gas The moving amount of the fluid medium c from the gasification chamber 1 to the first combustion chamber 2 increases, and the bed height of the first combustion chamber 2 slightly increases. Then, the amount of the flowing medium c from the chamber 1 to the combustion chamber 4 also increases, and as a result, the combustion chamber 2 from the gasification chamber 1 and the combustion chamber 2 from the combustion chamber 2 settle. Combustion chamber 4, sedimentation channel 1 The amount of movement of fluid medium c from combustion chamber 4 to gasification chamber 1 is stabilized with the amount of movement increased from the initial state _(at this time, gasification chamber 1 and The temperature difference between the gasification chamber 1 and the combustion chamber 2 becomes smaller due to the increase in the amount of movement of the fluid medium c between the combustion chambers 2. That is, the fluidized bed temperature of the gasification chamber 1 rises. Therefore, the fluidized bed temperature of the first combustion chamber 2 will decrease.The following is the case where the first combustion chamber 2 from the gasification chamber 1, the second combustion chamber 4 from the first combustion chamber 2, and the first combustion chamber of the sedimentation. When the amount of movement of all the fluid medium c from chamber 4 to gasification chamber 1 is stable at the same value, The amount of movement of the fluid medium c between the combustion chambers 2 is called "internal circulation amount".

After a certain period of time, at the stage where the fluidized bed temperature of the gasification chamber 1 is stabilized, if the stabilized temperature is still lower than the target fluidized bed temperature, the amount of fluidized gas in the sedimentation chamber 1 combustion chamber 4 May be further increased. If the stable temperature is higher than the target fluidized bed temperature, the amount of fluidized gas in the settling chamber 1 Or decrease it.

The above operation is performed by inputting the measured value and the target value of the fluidized bed temperature of the gasification chamber 1 to the control device 6 including the arithmetic unit by the configuration as shown in Fig. 1. The control signal i1 to the control valve 65 changes to change the supply amount of the fluidizing gas g4 to the settling chamber 1 combustion chamber 4 based on the magnitude of the difference, and the opening of the control valve 65 is changed. It can be easily realized by changing the configuration.

In the above description, the weak fluidization zones la, 2a, 3a, 4a and the strong fluidization zones lb, 2b are air diffusers 3 1 to 3 6 each connected to one control valve 61 to 66. It was explained that it had.

However, as shown in Fig. 5 (a part of the integrated gasifier 101 is omitted), for example, the weak fluidized zone 1a and the strong fluidized zone 2b sandwiching the opening 21 are respectively 2 1 is separated into neighboring areas 1 aX and 2 bX immediately adjacent to 1 and remote areas 1 ay and 2 by other than the neighboring areas 1 aX and 2 bx. Even if it is configured to be separated into the neighboring parts 31 x and 34 x corresponding to the neighboring areas 1 ax and 2 bx and the remote parts 31 y and 34 y corresponding to the remote areas lay and 2 by respectively. Good.

Connect the above-mentioned supply pipes 51 and 54 to the remote parts 3 1 y and 34 y of the diffusers 31 and 34, respectively, and connect the parts 31 and 34 near the diffusers 31 and 34. , 34X may be connected to supply pipes 51X, 54x provided with flow rate measuring devices 71x, 74x and control valves 61x, 64X. The speed of the fluidizing gas g1, g2 supplied to control the amount of movement of the fluid medium c through the opening 21 is reduced to the weak fluidized area 1a and the strong fluidized area 2b, respectively. Instead of controlling over the range, the gas velocities of the fluidizing gases g1 and g2 supplied from the neighborhoods 1aX and 2bX may be controlled respectively. This control is performed by controlling the control valves 6 lx and 64 x by the control device 6 (see FIG. 1) as described above.

Similarly, the openings 25, 22 of the weak fluidization zone 4a and the strong fluidization zone 1b sandwiching the opening 25, and the weak fluidization zone 3a and the strong fluidization zone 2b sandwiching the opening 22 Is separated into a nearby area (not shown) directly adjacent to and a remote area (not shown) other than the nearby area, and flows supplied to control the amount of movement of the medium c through the openings 25 and 22. Instead of controlling the velocity of the gasification over the weak fluidization zone 4a, 3a and the strong fluidization zone lb, 2b, respectively, The gas flow velocity of the fluidizing gas supplied from the vicinity may be controlled individually.

The phenomena that occur when the amount of internal circulation is changed from one stable operating state of the integrated gasifier 101 and the effects obtained are described below. First, a change in the temperature of the gasification chamber 1 or the temperature of the two-chamber combustion chamber occurs according to the change in the internal circulation volume. When the internal circulation volume is increased, the bed temperature in the gasification chamber 1 rises and the bed temperature in the combustion chamber 2 decreases. Conversely, when the amount of internal circulation is reduced, the bed temperature in the gasification chamber 1 decreases and the bed temperature in the combustion chamber 2 increases.

In addition, the residence time of the fluid medium c in the chambers 1 and 2 changes in both the gasification chamber 1 and the combustion chamber 2. For example, when the internal circulation amount is reduced to 1/2, the residence time of the fluid medium c in each of the chambers 1 and 2 is doubled. Conversely, when the internal circulation amount is doubled, the residence time of the fluid medium c in each of the chambers 1 and 2 becomes 1/2.

In addition, the amount of char h generated in the gasification chamber 1 changes. For example, when the amount of internal circulation is reduced, the amount of generated gas per hour in the gasification chamber 1 increases, reflecting the decrease in the bed temperature in the gasification chamber 1. In general, the amount of char h increases as the bed temperature decreases. When the amount of internal circulation is increased, the amount of generated gas per hour decreases, reflecting the rise in the bed temperature of the gasification chamber 1. In general, the amount of char h decreases as the bed temperature of the gasification chamber 1 increases. The gas composition of the product gas b generated in the gasification chamber 1 changes, reflecting the change in the amount of generated gas and the change in the bed temperature in the gasification chamber 1. This is due to the element balance (molar ratio (%) of carbon, hydrogen, oxygen, etc.) due to the change in the amount of char h generated (the amount of combustibles moving from gasification chamber 1 to char combustion chamber 2). And the change in the equilibrium state of the gas components with temperature.

The H ₂ / CO ratio and gas calorific value of the generated gas b change due to the change in the generated gas composition.The H 2 ZCO ratio is an important factor related to the production efficiency of hydrogen, liquid fuel, etc. from the generated gas b. It is. The gas calorific value is an important factor when using the generated gas b for combustion.

From the above, by changing the internal circulation amount, the bed temperature of the gasification chamber 1 is arbitrarily controlled in practical use, and thereby the composition of the generated gas b (H ₂ , CO, C 0 ₂ , CH ₄ , in addition to the mole percent of such H ₂ 0, H ₂ / CO ratio, such as a gas heating value, and concept including factor determined by the product gas composition.) can be changed. In this case, for example, when the bed temperature of the gasification chamber 1 is controlled to be lowered, the bed temperature of the first combustion chamber 2 is correspondingly increased. Conversely, if the bed temperature of the gasification chamber 1 is controlled to increase, the bed temperature of the combustion chamber 2 will decrease correspondingly. The operating temperature of the char combustion chamber should be maintained within the optimal temperature range for complete combustion of the char and tar transferred from the gasification chamber 1, preferably 850-950 ° C. Therefore, if the bed temperature of the gasification chamber 1 is changed by changing the internal circulation amount, another method is used so that the temperature of the combustion chamber 2 does not deviate from the above optimum range. Need to adjust.

To this end, when the heat recovery chamber 3 is provided as described above, by controlling the amount of heat recovery in the heat recovery chamber 3, the layer temperature of the main chamber 5 of the combustion chamber is kept constant. Control can be performed. In addition, by directly supplying a part of the raw materials used to the char combustion chamber, or by changing the supply amount, control is performed so as to directly change the combustion amount of the combustible component in the char combustion chamber. May be. When the temperature of the combustion chamber 2 becomes extremely high, the temperature of the fluidized bed is directly cooled by supplying water to the fluidized bed or changing the supply amount. You can perform such control.

The following is an example of the results of a trial calculation assuming an integrated gasifier 1 ◦ 1 (Figure 1) (Figure 11, Figure 13 to Figure 15). Raw material a was woody biomass, gasification chamber 1 was gasified by steam in 200, and char combustion chamber 2 was to burn char h by air. The bed temperature of the combustion chamber 2 is kept constant at 900 ° C by controlling the amount of heat recovered in the heat recovery chamber 3, and when the internal circulation rate is changed, the layer temperature of the gasification chamber 1 changes. We calculated the changing power and how the composition and calorific value of the generated gas b change accordingly. The internal circulation volume is organized by the dimensionless number (hereinafter referred to as “circulation ratio”) obtained by dividing the circulation volume of media particles (kg / h) by the input volume of raw material a (kg / h).

Figure 11 shows the relationship between the internal circulation volume (circulation ratio) in Case 1 and the gasification chamber layer temperature (unit ° C). Figure 12 shows the internal circulation volume (circulation ratio) in Case 2 and the gasification chamber layer. Shows the relationship between temperature (in units). Figures 11 and 12 show the calculation results. Although the absolute value of the gasification chamber temperature that decreases depends on the scale of the gasifier 1, the raw material a, and the process conditions (fluidized steam, air, etc.), it is shown in Figs. 11 and 12. As the internal circulation amount (circulation ratio) decreases, the bed temperature of the gasification chamber 1 decreases and the internal circulation amount (circulation ratio) increases. However, the temperature of the gasification chamber 1 rises. For example, in Fig. 11 (Case 1), based on the internal circulation amount for maintaining the bed temperature of gasification chamber 1 at 800 ° C, the internal circulation amount for maintaining 700 ° C is Approximately 44% (20/45), the amount of circulation to maintain at 600 ° C is approximately 22% (10/45). From the above, in order to be able to control the bed temperature of the gasification chamber 1 in the range of 600 to 800 ° C, the internal circulation amount of the fluid medium c should be within the range of the maximum value to about 20% of the maximum value. It is preferable to configure so that it can be changed arbitrarily in practice. Typically, the internal circulation amount is controlled so that the bed temperature of the gasification chamber 1 becomes constant.

Figure 13 shows the relationship between the amount of internal circulation (circulation ratio) and the composition of the product gas. This figure shows the calculation results when the gas residence time in the gasification chamber 1 is assumed to be sufficiently long, or when the reaction proceeds to a state close to the equilibrium composition by a catalyst or the like.

As shown in the figure, as the internal circulation amount (circulation ratio) decreases, the bed temperature of the gasification chamber 1 decreases, so the composition of the generated gas b decreases in H ₂ and CO and increases in CO H ₂₀ . In particular, when the amount of internal circulation (circulation ratio) is small and the bed temperature of the gasification chamber 1 is low, the amount of CH ₄ increases remarkably, and H ₂ and CO decrease correspondingly. By changing the internal circulation amount (circulation ratio), it is possible to control so as to obtain a gas composition shown in a desired diagram.

Figure 14 shows the relationship between the internal circulation amount (circulation ratio) and the HzZCO ratio of the produced gas. This figure shows the calculation results when the gas residence time in the gasification chamber 1 is assumed to be sufficiently long, or when the reaction has progressed to a state close to the equilibrium composition by a catalyst or the like.

As shown in the figure, the HsZCO ratio increases as the internal circulation amount (circulation ratio) decreases in response to changes in the product gas composition. Therefore, it is possible to control H ₂ and CO to a desired value between 2.6 and 5.7 by controlling the internal circulation amount (circulation ratio).

Figure 15 shows the relationship between the amount of internal circulation (circulation ratio) and the calorific value of the generated gas. This figure shows the calculation results when it is assumed that the gas residence time in gasification chamber 1 (Fig. 1) is sufficiently long, or when the reaction has progressed to a state close to the equilibrium composition by a catalyst or the like.

As shown in the figure, as a whole, as the internal circulation amount (circulation ratio) decreases in response to changes in the product gas composition, the CO concentration decreases, and the calorific value of the product gas decreases. Tend to be. In particular, when the internal circulation amount (circulation ratio) is small and the bed temperature of the gasification chamber 1 is low, the calorific value increases because the CH ₄ concentration increases. The Rukoto changing the internal circulation rate (recycle ratio), about 1 0, 6 0 0 Power et al. About 1 0, 9 0 0 k J / m 3 (HHVD B..) - controlled to a desired value between the NTP can do.

When the gas residence time in the gasification chamber 1 is short and the gas composition is different from the equilibrium composition, the following phenomenon occurs.

The first control of the gas property of the gasifier 101 (FIG. 1) will be described. Figure 16 shows the gasification chamber bed temperature (in units) and gasification chamber (GC) outlet gas calorific value ratio (counting tar to calorific value) (unit%) when gasification raw material a is biomass. If _t gasification chamber layer temperature showing a relationship is low, since Atamanetsu loss is small, the gasification chamber outlet gas heating value is high, if the gasification chamber layer temperature is hot, since the sensible heat loss is large However, the calorific value at the outlet of the gasification chamber is reduced. Since there is a dependence between the gasification chamber layer temperature and the circulation amount, the calorific value at the gasification chamber outlet gas can be increased by reducing the circulation amount. The gasification chamber outlet calorific value ratio is the ratio of the calorific value of the gas (including tar) generated from the unit weight of the gasification raw material at the gasification chamber outlet divided by the heat generation amount due to the combustion of the unit weight of the gasification raw material. One center.

Figure 17 shows the gasification chamber bed temperature (unit) and cold gas efficiency (unit%) when gasification raw material a is biomass (based on the calorific value of combustible gas excluding tar at the gasification chamber outlet). )). When the gasification chamber layer temperature is low, the amount of tar generated increases, and the cold gas efficiency decreases. When the gasification chamber layer temperature is high, tar generation decreases, and the cold gas efficiency increases. Cold gas efficiency is the percentage of the calorific value of the gas (excluding tar) generated from a unit weight of gasification raw material at the gasification chamber outlet divided by the calorific value of the unit weight gasification raw material combustion. Say.

Figure 18 shows the internal circulation amount (circulation ratio) and the calorific value of the generated gas at the gasification chamber outlet (excluding tar) when the gasification raw material a is biomass (excluding tar) (HHV D.B) (unit: KJ / m ³ -NPT). If the internal circulation volume (circulation ratio) is small, the gasification chamber bed temperature will be low and tar will increase, so the heat generation will decrease. If the internal circulation volume (circulation ratio) is large, the gasification chamber bed temperature will be high. The amount of generated heat increases because tar generation is reduced. Figure 19 shows the gasification chamber bed temperature when the gasification raw material a is biomass (unit: C). And the ratio (unit%) of carbon (C) in raw material a transferred to tar. The figure shows that the lower the gasification chamber layer temperature, the higher the amount of tar generated, and the higher the gasification chamber layer temperature, the lower the amount of tar generation.

Therefore, in order to increase the cold gas efficiency of raw material a, which generates a large amount of tar such as biomass and generates a small amount of heat, it is necessary to (1) reduce the sensible heat loss by setting the gasification chamber layer temperature to a low temperature. There is a method of lowering and reducing the amount of tar generated by decomposing (lower molecular weight) tar generated at that time. (2) Increasing the amount of circulation and raising the temperature of the gasification chamber layer. Next, the second control of the gas property of the gasifier 101 (FIG. 1) will be described.

By controlling the circulation amount, it is possible to control the amount of volatile matter released from the gasification raw material a, and to control the amount of carbon in the raw material a to be transferred to the first combustion chamber 2. Figure 20 shows the amount of circulation (unit: kg h) when gasification raw material a is biomass, and the transfer ratio of carbon in raw material a supplied to gasification chamber 1 to char combustion chamber 2 (unit). %). The figure shows that as the circulation amount increases, the ratio of carbon that has not been released as volatile matter to the char-chamber 2 increases, and as the circulation amount decreases, the unreleased carbon is released as volatile matter. This indicates that the rate at which carbon transfers to the first combustion chamber 2 decreases.

Figure 21 shows the gasification chamber bed temperature (unit: C) when gasification raw material a is biomass, and the carbon gas in the gasification raw material a supplied to gasification chamber 1 to combustion chamber 2. This shows the relationship with the rate of transfer (unit%). When the bed temperature is high, the amount of volatile matter released is large (the amount of remaining volatile matter is small) and the volatile matter release rate is also high, so that the ratio of carbon in the raw material a to the combustion chamber 2 is small. Although it is thought to be the case, it is the opposite phenomenon in the figure. That is, when the gasification chamber layer temperature is high, the ratio of carbon in the raw material a to the char combustion chamber 2 increases, and when the gasification chamber layer temperature is low, the carbon in the raw material a is char combustion. The rate of transition to room 2 is small. This means that the gasification chamber layer temperature is high, which means that the amount of circulation is large, so that the gasification raw material a (here, biomass) that has not released volatile components accompanies the flowing medium. It is shown that the transition to one combustion chamber 2 is dominant.

From the above, it is possible to control the amount of combustion in the first combustion chamber 2 by controlling the amount of circulation. —The amount of combustion in the combustion chamber 2 can be controlled optimally.

The illustrated embodiments are merely examples, and do not limit the technical scope of the present invention. Industrial applicability

Since the gasification furnace according to the present invention includes the gasification chamber, the combustion chamber, and the control device, the gasification chamber and the combustion chamber are controlled by adjusting the strength of the flow in the weak fluidized state. By controlling the amount of the fluid medium flowing between the firing chambers, the composition of the gas generated from the gasification chamber can be controlled, and the control characteristics can be further improved.

Claims

The scope of the claims

1. a gasification chamber in which a high-temperature fluidized medium is flown to form a gasification chamber fluidized bed having a first interface; and a gasification object is gasified in the gasification chamber fluidized bed;

A high-temperature fluidized medium is caused to flow in a part, thereby forming a fluidized bed in the combustion chamber having a second interface, and the fluid generated by gasification in the gasification chamber is fluidized in the fluidized bed in the combustion chamber. A combustion chamber for burning and heating the fluid medium;

The gasification chamber and the first combustion chamber are separated by a partition wall so that gas does not flow vertically above an interface between the respective fluidized beds, and the gasification chamber is formed at a lower portion of the partition wall. A communication port for communicating between the chamber and the first combustion chamber, the communication port having a height at an upper end that is equal to or lower than the first interface and the second interface. The fluidized state of the fluid medium in the vicinity of the communication port of one of the gasification chamber and the char combustion chamber sandwiching the fluidized medium is the fluidized state of the fluid medium in the vicinity of the communication port of the other chamber. The fluid medium is configured to move from the weak fluidized state to the strong fluidized state through the communication port;

Further, by controlling the strength of the flow in the weak fluidized state, the amount of the fluidized medium flowing between the gasification chamber and the combustion chamber is controlled, and the gasification chamber or A control device for controlling the temperature of the combustion chamber;

Gasifier.

2. a gasification chamber for pyrolyzing the object to be processed with a high-temperature fluidized medium to produce gas and char;

A char combustion chamber for heating the fluid medium by burning the char generated in the gasification chamber;

The fluid medium is configured to circulate between the gasification chamber and the char combustion chamber;

Further, a control device is provided for controlling a composition of gas generated in the gasification chamber by adjusting a circulation amount of the fluidized medium;

Gasifier.

3. A gasification chamber fluidized bed having a first interface with a hot fluidized medium flowing therethrough And a gasification chamber for gasifying an object to be processed in the fluidized bed of the gasification chamber; and flowing a high-temperature fluidized medium therein to form a fluidized bed of a combustion chamber having a second interface. A char combustion chamber for heating the fluid medium by burning the char generated with gasification in the gasification chamber in the fluidized bed of the char combustion chamber;

The gasification chamber and the char combustion chamber are separated by a partition wall so that gas does not flow vertically above the interface between the respective fluidized beds, and the gas is provided below the partition wall. A communication port for communicating the gasification chamber with the first combustion chamber, the communication port having a height at an upper end that is equal to or lower than the first interface and the second interface. The fluidized state of the fluid medium in the vicinity of the communication port of one of the gasification chamber and the char combustion chamber sandwiching the port is the fluidization state of the fluid medium in the vicinity of the communication port of the other chamber. A fluid medium that is stronger than the fluid state and moves from the weak fluidized state to the strong fluidized state through the communication port;

Further, by controlling the strength of the flow in the weak fluidized state, the amount of the fluidized medium flowing between the gasification chamber and the first combustion chamber is controlled, and Equipped with a control device for controlling the composition of the generated gas;

Gasifier.

4. A heat recovery chamber for introducing a fluid medium from the first combustion chamber, the heat recovery chamber having a heat recovery device for recovering heat from the fluid medium from the chamber; and a flow in the heat recovery chamber. A control device for controlling the amount of heat recovery in the heat recovery device by adjusting the strength of the heat recovery device;

The gasifier according to any one of claims 1 to 3.

5. The control device for controlling the heat recovery amount controls the heat recovery amount in the heat recovery device, and controls the temperature of the first combustion chamber;

The gasifier according to claim 4.

6. a pressure measuring device for measuring a first pressure above a first interface of the gasification chamber and a second pressure above a second interface of the gas combustion chamber;

A first discharge linear velocity of the gas generated from the gasification chamber, a second discharge linear velocity discharged from the gasification chamber, and a second discharge rate of the combustion gas generated from the charge combustion chamber from the charge combustion chamber. An adjusting device for adjusting the discharge linear velocity; A control device that controls the adjusting device so that a pressure difference between the first pressure and the second pressure is a predetermined value;

The gasifier according to any one of claims 1 to 5.