JP2003172501A - Reactor with particle/gas separating device - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a reactor hardly causing trouble in treating particles in separating them from a reaction gas, preventing lowering of the reaction efficiency in the total system, and hardly depositing liquid material. <P>SOLUTION: The reactor 1 has a first chamber 2 in which the flow of gas (b) carrying particles (c) is formed, a second chamber 2 integrally formed with the first chamber adjacently, and a particles/gas separating device 31 set inside the first chamber for separating the gas and the particles carried in the gas. The separated particles are guided into the second chamber and the gas is the object of reaction in the reactor 1. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a reactor equipped with a particle / gas separator for the reaction of gas, and in particular to low-grade resources such as waste, RDF and biomass, and raw materials such as fossil fuels such as coal. The present invention relates to a reactor equipped with a particle / gas separation device that gasifies and separates the gasified gas and particles.

[0002]

2. Description of the Related Art As shown in FIG. 10, a conventional fluidized bed gasification furnace 601 has a charging port 602 into which a raw material a is charged, an air diffusing slope 603 into which a fluidizing gas g is supplied, and a generated combustible material. And a discharge port 604 for discharging the gas b. The combustible gas b discharged from the discharge port 604 of the fluidized bed gasification furnace 601 is supplied to the cyclone separator 60 via a pipe 606.
5, the particles c were separated by the cyclone separator 605, and the separated particles c were returned to the fluidized bed gasification furnace 601 via the pipe 607. The combustible gas b from which the particles c have been separated was sent to a combustible gas utilization device (not shown) in the subsequent stage that utilizes the combustible gas b.

[0003]

In the fluidized bed gasification furnace 601, the particles c are separated by the cyclone separator 605 from the gas flow once discharged outside the furnace, and the separated particles c are separated from the gasification furnace 601. It's back inside. For this purpose, pipes 606 and 607 outside the furnace for transferring the particles c are required, and special measures are required to avoid troubles in handling the particles c. Further, since the particle c is at a high temperature and is a process that utilizes the heat, the heat is released from the cyclone separator 605 and the external pipes 606 and 607 once the heat is discharged to the outside of the furnace, and the heat dissipation loss of the particle c is reduced. And the reaction efficiency of the entire system decreases. When there is a liquid substance such as tar that precipitates when the temperature decreases, the influence thereof further increases the trouble factor in handling.

The present invention has been made in view of the above circumstances. When separating particles from a reaction gas, troubles in handling the particles hardly occur, the reaction efficiency of the entire system does not decrease, and the liquid state It is an object of the present invention to provide a reactor in which a substance does not easily deposit.

[0005]

In order to achieve the above object, the reaction apparatus 1 according to the invention according to claim 1 has a flow of a gas b entrained with particles c inside as shown in FIG. 1, for example. A first chamber 2 formed; a second chamber 3 integrally formed adjacent to the first chamber 2; particles entrained in the gas b, which are installed inside the first chamber 2 a particle / gas separator 31 for separating c and gas b; separated particles c
Are introduced into the second chamber 3; the gas is the target of the reaction.

According to this structure, the particle / gas separation device 31 installed inside the first chamber 2 is provided, and the particles c entrained in the gas b and the gas b are separated, and the separated particles c are separated. Can be introduced into the second chamber 3 integrally formed adjacent to the first chamber 2, so that the particles c and the gas b are separated inside the furnace, and the separated particles are separated inside the furnace. It is not necessary to convey the inside of an external pipe routed outside the furnace, and it is not necessary to separate the particles c and the gas b outside the furnace. Therefore, handling problems of the separated particles c are unlikely to occur, and the temperature does not drop, so that liquid substances such as tar are less likely to deposit, and the reaction efficiency of the entire system is lowered due to the temperature drop, and the occurrence of troubles is avoided. be able to. Further, the particles c can be continuously retained in the system, and the retention time in the system can be lengthened.

The particle / gas separation device 31 may be either a single unit or a plurality. The target of the reaction may be, for example, one that causes a certain chemical reaction (including gasification and combustion), or the result of these reactions including the case where gas is produced from the solid fuel by the gasification reaction. It means that it may have occurred. The reaction device typically means a device that causes a gasification reaction and a combustion reaction. Further, it may be one that causes partial oxidation or catalytic reaction. The pressure within the device may be the same as or below atmospheric pressure, or it may be above atmospheric pressure. Introducing particles means, for example, a particle discharge pipe for discharging particles, which is the second chamber 3
Not only when it is opened inside and is introduced into the second chamber 3,
Even if the first chamber 2 is open, the first chamber 2 to the second chamber 3
Including the case of being introduced into the second chamber 3 with almost no retention in the first chamber 2 while being carried on the flow of the fluidized medium to the second chamber 3.

The reaction apparatus 1 according to the second aspect of the invention is
For example, as shown in FIG. 1, in the reactor according to claim 1, the first chamber 2 fluidizes a fluidized medium inside to form a fluidized bed having an interface, and the particle / gas separation device 31 includes It is installed so that it is located vertically above the interface.

According to this structure, the particle / gas separation device 31 is installed vertically above the interface, so that the particle / gas separation device 31 is installed on the freeboard portion containing no fluid medium and carries the gas c accompanied by the particles c. The particles c can be efficiently separated from b.

A reactor 301 according to the invention of claim 3
For example, as shown in FIG. 6, a first chamber 302 in which a fluidized medium is made to flow to form a fluidized bed having an interface, and a flow of gas b accompanied by particles c is formed therein.
And; a second chamber 303 provided separately from the first chamber 302
And a particle / gas separation device 331 installed inside the first chamber 302 for separating the particles c entrained in the gas b from the gas b; the separated particles c to the second chamber. 303
Gas b is targeted for the reaction.

According to this structure, the particle / gas separation device 331 installed inside the first chamber 302 is provided, the particles c entrained in the gas b and the gas b are separated, and the separated particles c are separated. Can be introduced into the second chamber 303 provided separately from the first chamber 302, so that the separated particles c
3 for transporting the air from the first chamber 302 to the second chamber 303
It is possible to shorten the external pipe that passes through the outside of the chambers 302 and 303 of 33, and minimize the routing of the external pipe. Therefore, the trouble in handling the separated particles c is less likely to occur, the temperature decrease of the separated particles c is less likely to occur, and the reaction efficiency of the entire system is reduced due to the temperature decrease of the separated particles c. Occurrence can be avoided. It should be noted that being provided separately from the first chamber means that there is no adjacent method of partitioning with a wall in one container, and they may be connected by piping or the like.

A reactor 301 according to the invention of claim 4
Is, for example, as shown in FIG.
In the reactor described in paragraph 1, the fluidized medium is configured to circulate between the first chamber 302 and the second chamber 303.

According to this structure, the fluidized medium is
Since it is configured to circulate between the first chamber 302 and the second chamber 303, for example, the combustible gas b is generated in one chamber 302, and the char that is generated in association with the generation of the combustible gas b is generated. And the fluid medium can be sent to the other chamber 303 to burn the combustible components in the char, and the fluid medium can be returned to the one chamber 302.

The reaction apparatus 1 according to the invention of claim 5 is
For example, as shown in FIG. 1, in the reactor according to any one of claims 1 to 4, the particle / gas separator 31 is a cyclone separator 31. Since the particle / gas separator 31 is a cyclone separator 31,
The particles can be separated from the gas in a wide temperature range.
Further, the structure of the particle / gas separation device can be simplified, and a separation device that is less likely to cause clogging can be obtained.

The reaction apparatus 1 according to the invention of claim 6 is
For example, as shown in FIG. 1, in the reaction device according to any one of claims 1 to 5, the reaction is at least one of combustion, partial oxidation and gasification. Therefore, the reactor 1 can be applied to a reactor in which various reactions such as combustion, partial oxidation and gasification are performed. Further, the first chamber 2 and the second chamber 3 may have the same function or may have different functions.

The reactor 1 according to the invention of claim 7 is
For example, as shown in FIG. 1, in the reactor according to any one of claims 1 to 6, the first chamber 2 and the second chamber
The chamber 3 has a different function. Therefore, the separated particles c can be introduced from a chamber having a certain function to a chamber having a different function, and different functions can be added.

For example, when each chamber has a different function such as an oxidizing atmosphere and a reducing atmosphere, particles containing unburned components, which are scattered with the gas flow from the reducing atmosphere, are separated from the gas. However, it is possible to add a function of burning unburned components by transferring the unburned components into the oxidizing atmosphere.

The reaction apparatus 1 according to the invention of claim 8 is
For example, as shown in FIG. 4, in the reaction apparatus according to any one of claims 1 to 7, a flow of gas b is formed inside the second chamber 203, and inside the first chamber 202. The flow velocity of the gas b formed in the second chamber 203 and the flow velocity of the gas u1 formed in the second chamber 203 are different.

If a particle / gas separation device is installed in one of the chambers where the flow velocity is high and particles are easily scattered, the particles c are captured and the captured particles c are introduced into the other chamber where the flow velocity is low, the particles c are scattered. It can be made difficult and the reaction can be carried out. Typically, the flow velocity of the gas b formed inside the first chamber 202 is lower than the flow velocity of the gas b formed inside the second chamber 203. In this case, the particle / gas separation device 23 is placed in the second chamber 203 having a high flow velocity in which the particles c are easily scattered.
1 is provided, the particles c are captured, and the particles c are introduced into the first chamber 202 having a low flow rate, so that the particles c are less likely to be scattered and the reaction can be performed.

When the gas flow velocity in each chamber is different, the residence time of the particles in the system can be further increased by transferring the particles from the chamber having a high gas flow velocity to the chamber having a low gas flow velocity. This is because, for example, in a fluidized bed furnace, the normal combustion zone (oxidizing atmosphere) becomes vigorous fluidization, and the gasification / pyrolysis zone becomes slow fluidization, so reaction particles scattered from the combustion zone are slowly fluidized (gas By returning to the gasification / pyrolysis zone where the flow rate is low and particles are less likely to scatter, the residence time of the particles in the system is increased, and the reaction efficiency (eg desulfurization efficiency) of the particles can be improved.

[0021]

BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, an integrated gasification furnace 1 as a reactor according to a first embodiment of the present invention will be described with reference to FIG. In each drawing, the same or corresponding members are designated by the same reference numerals or similar reference numerals, and redundant description will be omitted.

FIG. 1 is a schematic representation of the basic structure of the gasification furnace portion of the present invention. The integrated gasification furnace 1 shown in the figure has a gasification chamber 2 as a first chamber and a char combustion chamber as a second chamber which are respectively in charge of three functions of pyrolysis, that is, gasification, char combustion, and heat recovery. 3, a heat recovery chamber 4 is provided, and the whole is housed in a cylindrical or rectangular furnace body. The char combustion chamber 3 is integrally formed adjacent to the gasification chamber 2.

Gasification chamber 2, char combustion chamber 3, heat recovery chamber 4
Is divided by partition walls 11, 12, 13, 14, and 15, and a fluidized bed, which is a dense layer containing a fluidized medium, is formed at the bottom of each of them. Furnace at the bottom of each chamber 2, 3, 4 for fluidizing the fluidized bed of each chamber 2, 3, 4 ie, gasification chamber fluidized bed, char combustion chamber fluidized bed, heat recovery chamber fluidized bed An air diffuser for injecting a fluidizing gas into a fluidized medium is provided at the bottom. The air diffuser is configured to include, for example, a perforated plate laid on the bottom of the furnace, and the perforated plate is divided into a plurality of rooms by dividing the perforated plate in the width direction to change the superficial velocity of each part in each room. In addition, the flow velocity of the fluidizing gas blown out from each room of the air diffuser through the perforated plate is changed. Since the superficial velocity is relatively different in each part of the chambers, the fluidized medium in each chamber 2, 3, 4 also has a different flow state in each part of the chambers 2, 3, 4 so that an internal swirl flow is formed. In the figure,
The size of the white arrow shown in the air diffuser indicates the flow velocity of the fluidizing gas blown out. For example, the thick arrow at the location indicated by 3b has a higher flow velocity than the thin arrow at the location indicated by 3a.

The gasification chamber 2 and the char combustion chamber 3 are partitioned by a partition wall 11, the char combustion chamber 3 and the heat recovery chamber 4 are partitioned by a partition wall 12, and the gasification chamber 2 and the heat recovery chamber 4 are separated. The space between them is partitioned by a partition wall 13 (this drawing shows a cylindrical furnace developed in a plan view, so that the partition wall 11 is located between the gasification chamber 2 and the char combustion chamber 3). Not shown). That is, they are not configured as separate furnaces but are integrally configured as one furnace. Further, a sedimentation char combustion chamber 5 is provided near the surface of the char combustion chamber 3 in contact with the gasification chamber 2 so that the fluidized medium descends. That is, the char combustion chamber 3 includes the sedimentation char combustion chamber 5 and the sedimentation char combustion chamber 5
Other than the char combustion chamber body part. Therefore, a partition wall 14 is provided for partitioning the settled char combustion chamber 5 from the other part of the char combustion chamber (char combustion chamber main body). Further, the settling char combustion chamber 5 and the gasification chamber 2 are separated by the partition wall 1.
It is divided by 5.

Here, the fluidized bed and the interface will be described.
The fluidized bed consists of a concentrated layer in the vertically lower part, which contains a fluidized medium (for example, silica sand) in a fluidized state by the fluidizing gas, and a fluidized medium in the vertically upper part of the concentrated layer. It consists of a splash zone where a large amount of gas coexists and the fluid medium is vigorously splashing. Above the fluidized bed, that is, above the splash zone, there is a freeboard section containing almost no fluidized medium and mainly gas.
The interface in the present invention refers to the splash zone having a certain thickness, but it may be regarded as a virtual surface intermediate between the upper surface and the lower surface (the upper surface of the dense layer) of the splash zone.

Further, "partitioned by a partition wall so that gas does not flow above the interface of the fluidized bed in the vertical direction."
In that case, it is preferable that the gas does not flow above the upper surface of the dense layer below the interface.

The partition wall 11 between the gasification chamber 2 and the char combustion chamber 3 is almost entirely partitioned from the furnace ceiling 19 to the furnace bottom (perforated plate of the air diffuser), but the lower end is the furnace. An opening 21 is formed near the bottom of the furnace without contacting the bottom. However, the upper end of the opening 21 does not reach above any of the gasification chamber fluidized bed interface and the char combustion chamber fluidized bed interface. More preferably, the opening 2
The upper end of 1 does not reach above the upper surface of the dense layer of the fluidized bed of the gasification chamber or the upper surface of the dense layer of the fluidized bed of the char combustion chamber. In other words, the opening 21
Is preferably constructed so that it always dives in the dense layer. That is, the gasification chamber 2 and the char combustion chamber 3 are separated from each other by a partition wall 11 so that there is no gas flow at least in the freeboard portion, that is, above the interface, and more preferably above the upper surface of the rich layer. It will be partitioned by.

The partition wall 12 between the char combustion chamber 3 and the heat recovery chamber 4 has its upper end near the interface, that is, above the upper surface of the rich layer, but below the upper surface of the splash zone. The lower end of the partition wall 12 is up to the vicinity of the furnace bottom, and like the partition wall 11, the lower end does not contact the furnace bottom, and an opening 22 is formed near the furnace bottom that does not reach above the upper surface of the dense layer. Has been done.

Partition wall 13 between the gasification chamber 2 and the heat recovery chamber 4
Completely partitions from the bottom of the furnace to the ceiling 19 of the furnace. The partition wall 14 for partitioning the inside of the char combustion chamber 3 to provide the sedimentation char combustion chamber 5 has an upper end near the interface of the fluidized bed and a lower end in contact with the furnace bottom. The relationship between the upper end of the partition wall 14 and the fluidized bed is similar to the relationship between the partition wall 12 and the fluidized bed. The partition wall 15 for partitioning the settling char combustion chamber 5 and the gasification chamber 2 is similar to the partition wall 11, and is partitioned almost entirely from the ceiling 19 of the furnace to the furnace bottom, and the lower end must contact the furnace bottom. However, an opening 25 is formed near the furnace bottom, and the upper end of this opening is below the upper surface of the rich 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.

A raw material a such as coal or dust that has been put into the gasification chamber 2 receives heat from the fluidized medium and is pyrolyzed and gasified.
Typically, the raw material a does not burn in the gasification chamber 2 and is so-called carbonized. The remaining dry-distilled char flows into the char combustion chamber 3 together with the fluidized medium through the opening 21 at the bottom of the partition wall 11. In this way, the char introduced from the gasification chamber 2 burns in the char combustion chamber 3 to heat the fluidized medium. The fluidized medium heated by the combustion heat of the char in the char combustion chamber 3 flows into the heat recovery chamber 4 over the upper end of the partition wall 12,
After the heat is collected by the in-layer heat transfer tube 41 arranged below the interface in the heat recovery chamber 4 and cooled, the char combustion chamber 3 passes through the opening 22 at the lower part of the partition wall 12 again. Flow into. As the raw material a, lower resources such as waste, RDF and biomass, fossil fuels such as coal and the like can be used.

Here, the heat recovery chamber 4 is not essential in the gasification system of the raw material a of the present invention. That is, if the amount of char mainly consisting of carbon remaining after gasification of the volatile components in the gasification chamber 2 and the amount of char required to heat the fluidizing medium in the char combustion chamber 3 are substantially equal, the flow The heat recovery chamber 4 which takes heat from the medium is unnecessary. If the difference in the amount of the char is small, for example, the gasification temperature in the gasification chamber 2 becomes high, and the amount of CO gas generated in the gasification chamber 2 increases, so that the balance state is maintained. Be done.

However, when the heat recovery chamber 4 is provided as shown in the figure, it is possible to cope with a wide variety of raw materials a, from coal with a large amount of char generation to municipal waste that hardly generates char. That is, for any material a, the combustion temperature of the char combustion chamber 3 can be appropriately adjusted and the temperature of the fluidized medium can be appropriately maintained by adjusting the heat recovery amount in the heat recovery chamber 4. .

On the other hand, the fluidized medium heated in the char combustion chamber 3 flows into the settling char combustion chamber 5 over the upper end of the partition wall 14, and then into the gasification chamber 2 through the opening 25 at the bottom of the partition wall 15. To do.

Here, the flow state and movement of the flowing medium between the chambers will be described. In the vicinity of the surface in contact with the partition wall 15 between the settling char combustion chamber 5 and the inside of the gasification chamber 2, a strong fluidization region 2b in which a stronger fluidized state is maintained as compared with the fluidization of the settling char combustion chamber 5. It has become. As a whole, in order to promote mixing and diffusion of the charged raw material a and the fluidized medium,
It is preferable to change the superficial velocity of the fluidizing gas depending on the place, and as an example, as shown in the figure, a weak fluidizing region 2a is provided in addition to the strong fluidizing region 2b to form a swirling flow.

The char combustion chamber 3 has a weak fluidization region 3 at the center.
a, a strong fluidization region 3b is provided in the peripheral portion, and the fluidizing medium and the char form an internal swirling flow. The fluidization speed of the strong fluidization regions 2b and 3b in the gasification chamber 2 and the char combustion chamber 3 is 5 Um.
It is preferable that the fluidization rate of the weak fluidization regions 2a and 3a be f or more and 5 Umf or less, but if a relatively clear difference is provided between the weak fluidization regions 2a and 3a and the strong fluidization region 3b. , There is no particular problem even if it exceeds this range. A strong fluidization region 3b is preferably arranged in a portion of the char combustion chamber 3 which is in contact with the heat recovery chamber 4 and the settling char combustion chamber 5. Further, if necessary, it is preferable to provide a gradient on the bottom of the furnace so as to descend from the weak fluidization regions 2a, 3a side to the strong fluidization regions 2b, 3b side (not shown). Here, Umf is a unit in which the minimum fluidization speed (speed at which fluidization is started) is 1 Umf. That is, 5 Umf is 5 times the minimum fluidization rate.

In this way, the char combustion chamber 3 and the heat recovery chamber 4
By keeping the fluidized state of the char combustion chamber 3 side near the partition wall 12 relatively stronger than the fluidized state of the heat recovery chamber 4 side, the fluidized medium of the fluidized bed of the partition wall 12 becomes The fluid medium that has flowed from the char combustion chamber 3 side to the heat recovery chamber 4 side beyond the upper end near the interface and the flowing-in medium flows into the heat recovery chamber 4 side.
Due to the relatively weak fluidized state in the inside, that is, a high-density state, it moves downward (toward the bottom of the furnace) and passes through (the opening 22 of) the lower end of the partition wall 12 near the bottom of the heat recovery chamber 4 side. To the char combustion chamber 3 side.

Similarly, the fluidization state on the char combustion chamber body side near the partition wall 14 between the body of the char combustion chamber 3 and the sedimentation char combustion chamber 5 is more relative to that on the sedimentation char combustion chamber 5 side. By maintaining a strong fluidization state, the fluid medium moves and flows from the char combustion chamber 3 main body side to the sedimentation char combustion chamber 5 side over the upper end of the partition wall 14 near the interface of the fluidized bed. The fluidized medium flowing into the settling char combustion chamber 5 moves downward (toward the bottom of the furnace) due to the relatively weak fluidized state in the settling char combustion chamber 5, that is, the high-density state, and the furnace of the partition wall 15 is moved. Lower end (opening 25) near the bottom
Through the settling char combustion chamber 5 side to the gasification chamber 2 side. In addition, here, the gasification chamber 2 and the sedimentation char combustion chamber 5
The fluidized state on the gasification chamber 2 side near the partition wall 15 is kept relatively stronger than the fluidized state on the sedimentation char combustion chamber 5 side. This assists the movement of the fluidized medium from the settling char combustion chamber 5 to the gasification chamber 2 by an attractive action.

Similarly, the fluidized state on the char combustion chamber 3 side near the partition wall 11 between the gasification chamber 2 and the char combustion chamber 3 is relatively stronger than the fluidized state on the gasification chamber 2 side. It has been kept in an activated state. Therefore, the fluidized medium is the partition wall 11
Flows into the char combustion chamber 3 side through an opening 21 below the interface of the fluidized bed, preferably below the upper surface of the rich layer (submerged in the rich layer).

The char combustion chamber 3 and the heat recovery chamber 4 have a partition wall 12 having an upper end near the interface height and a lower end submerged in a rich layer.
, The fluidized state on the char combustion chamber 3 side near the partition wall 12 is kept stronger than the fluidized state on the heat recovery chamber 4 side near the partition wall 12. Therefore, the fluidized medium flows over the upper end of the partition wall 12 into the heat recovery chamber 4 side from the char combustion chamber 3 side, and passes through the lower end of the partition wall 12 from the heat recovery chamber 4 side to the char combustion chamber 3 side. Moving.

Further, the char combustion chamber 3 and the gasification chamber 2 are
The lower end is partitioned by a partition wall 15 that is submerged in a dense layer, and the partition wall 15 has a partition wall 15 on the side of the char combustion chamber 3 which has an upper end near the height of the interface. The formed sedimentation char combustion chamber 5 is provided, and the partition wall 14
The fluidized state on the side of the main body of the char combustion chamber 3 near the partition wall 14 is kept stronger than the fluidized state on the side of the settling char combustion chamber 5 near the partition wall 14. Therefore, the fluidized medium flows over the upper end of the partition wall 14 into the settling char combustion chamber 5 side from the main body side of the char combustion chamber 3. With this configuration, the fluidized medium that has flowed into the settling char combustion chamber 5 passes through the lower end (opening 25) of the partition wall 15 from the settling char combustion chamber 5 so as to maintain at least mass balance.
Move to. At this time, the fluidized state on the gasification chamber 2 side in the vicinity of the partition wall 15 is changed to the settling char combustion chamber 5 in the vicinity of the partition wall 15.
If it is kept stronger than the fluidized state on the side, the attracting action promotes the movement of the fluidized medium.

Further, the gasification chamber 2 and the main body of the char combustion chamber 3 are separated from each other by a second partition wall 11 having a lower end submerged in a rich layer. The fluidized medium that has moved from the settling char combustion chamber 5 to the gasification chamber 2 passes through the lower end of the partition wall 11 and moves to the char combustion chamber 3 so as to maintain the mass balance, but at this time, in the vicinity of the partition wall 11 If the fluidized state on the side of the char combustion chamber 3 is kept stronger than the fluidized state on the side of the gasification chamber 2 in the vicinity of the partition wall 11, not only to maintain the previous mass balance, but also the strong fluidization. Depending on the state, the fluidized medium is attracted and moves to the char combustion chamber 3 side.

The heat recovery chamber 4 is uniformly fluidized as a whole, and is usually maintained so as to be in a fluidized state weaker than the fluidized state of the char combustion chamber 3 which is in contact with the heat recovery chamber 4 at maximum. Therefore, the superficial velocity of the fluidizing gas in the heat recovery chamber 4 is 0 to 3
Controlled during Umf, the fluidizing medium forms a settling fluidized bed while slowly flowing. Here, 0 Umf is a state in which the fluidizing gas is stopped. With this kind of state,
The heat recovery in the heat recovery chamber 4 can be minimized. That is, the heat recovery chamber 4 can arbitrarily adjust the amount of recovered heat in the range of maximum to minimum by changing the fluidization state of the fluidized medium. Further, in the heat recovery chamber 4, the fluidization may be uniformly started / stopped or the strength may be adjusted throughout the chamber.
It is also possible to stop the fluidization of part of the area and put the other in the fluidized state, or adjust the strength of the fluidized state of the part of the area.

The most preferable fluidized gas in the gasification chamber 2 is to pressurize the combustible gas b for recycling. In this way, the gas emitted from the gasification chamber 2 is purely the gas generated from the raw material a, and a very high quality gas can be obtained. If that is not possible, it is preferable to use a gas containing as little oxygen as possible (oxygen-free gas) such as water vapor. When the bed temperature of the fluidized medium decreases due to the endothermic reaction during gasification, oxygen or a gas containing oxygen, for example, air is supplied to remove a part of the combustible gas b in addition to the oxygen-free gas as necessary. You may make it burn.
The fluidizing gas supplied to the char combustion chamber 3 is a gas containing oxygen necessary for char combustion, such as air, or a mixed gas of oxygen and steam. As the fluidizing gas supplied to the heat recovery chamber 4, air, steam, combustion exhaust gas, or the like is used.

The upper portion of the fluidized bed of the gasification chamber 2 and the char combustion chamber 3 (the upper surface of the splash zone), that is, the freeboard portion, is completely partitioned by the partition walls 11 and 15. Furthermore, since the upper portion of the dense bed of the fluidized bed, that is, the splash zone and the freeboard portion are completely partitioned by the partition walls 11 and 15, the pressures of the char combustion chamber 3 and the gasification chamber 2 are reduced. Even if the balance of P1 and P2 is slightly disturbed, the difference in the position of the interface between the two fluidized beds,
Alternatively, the turbulence can be absorbed only by a slight difference in the position difference of the upper surface of the dense layer, that is, the layer height difference. That is, since the gasification chamber 2 and the char combustion chamber 3 are partitioned by the partition walls 11 and 15, even if the pressures P1 and P2 of the respective chambers fluctuate, this pressure difference can be absorbed by the bed height difference. , It is possible to absorb until either of the layers descends to the upper ends of the openings 21 and 25.
Therefore, the upper limit of the pressure difference between the freeboard of the char combustion chamber 3 and the gasification chamber 2 that can be absorbed by the height difference is the gasification chamber from the upper ends of the openings 21 and 25 in the lower part of the partition wall 15 that separates each other. It is almost equal to the head difference between the head of the fluidized bed and the head of the char combustion chamber fluidized bed.

In the integrated gasification furnace 1 of the above-described embodiment, the gasification chamber 2, the char combustion chamber 3 and the heat recovery chamber 4 are provided inside one fluidized bed furnace through partition walls. Further, the char combustion chamber 3 and the gasification chamber 2, and the char combustion chamber 3 and the heat recovery chamber 4 are provided adjacent to each other. Unlike the two-column circulation type furnace, this integrated gasification furnace 1 enables a large amount of fluidized medium circulation between the char combustion chamber 3 and the gasification chamber 2, so that gasification is achieved only by the sensible heat of the fluidized medium. It is possible to supply a sufficient amount of heat for the purpose of gasification, and it is the easiest to realize the principle of gasification furnace, "to obtain as little combustible gas as possible with high calorific value".

Further, in the embodiment of the present invention, since the seal between the char combustion gas u1 and the combustible gas b is completely sealed, the pressure balance between the gasification chamber 2 and the char combustion chamber 3 is well controlled, and the combustion gas u1 and the combustible gas b are not mixed, and the property of the combustible gas b is not deteriorated.

Further, the fluidizing medium serving as the heat medium and the char flow from the gasification chamber 2 side to the char combustion chamber 3 side, and the same amount of the fluidizing medium is introduced from the char combustion chamber 3 side to the gasification chamber. Since it is configured to return to the 2 side, it is necessary to mechanically convey the fluid medium from the char combustion chamber 3 side to the gasification chamber 2 side by using a conveyor or the like so that the fluid medium is naturally balanced. In addition, there are no problems such as difficulty in handling high-temperature particles and large loss of sensible heat.

As described above, in the embodiment of the present invention, as shown in FIG. 1, the raw material a is placed in one fluidized bed furnace.
Pyrolysis / gasification of charcoal, char combustion, and in-bed heat recovery coexist in the gasification chamber 2 as a heat medium for the pyrolysis / gasification heat source supply. In the integrated gasification furnace 1 to be supplied, the gasification chamber 2 and the heat recovery chamber 4 are arranged so as not to be in contact with each other, or are completely partitioned by the partition wall 13 from the furnace bottom to the ceiling 19 and gasification The chamber 2 and the char combustion chamber 3 are completely partitioned by the partition wall 15 above the interface of the fluidized bed, and the fluidization strength of the gasification chamber 2 side near the partition wall 15 and the char combustion chamber 3 side fluidization By maintaining a relative relationship with the strength of the state in a predetermined relationship, the partition wall 15
The fluidized medium is moved from the char combustion chamber 3 side to the gasification chamber 2 side through the opening 25 provided in the vicinity of the furnace bottom. Also, from the gasification chamber 2 side to the char combustion chamber 3
The flowing medium containing char is moved to the side through the opening 21.

According to this embodiment, the gasification chamber 2 and the char combustion chamber 3 are completely partitioned by the partition wall 15 above the interface of the fluidized bed, so the gas pressure in each chamber fluctuates. However, the problem that the pressure balance is lost and the combustion gas u1 and the combustible gas b are mixed does not occur. For this reason,
No special pressure balance control is required between the gasification chamber 2 and the char combustion chamber 3. Then, by keeping the strength of the fluidized state on the gasification chamber 2 side near the partition wall 15 and the fluidized state on the char combustion chamber 3 side at a predetermined state, the partition wall 1 concerned.
Through the opening 25 provided in the vicinity of the furnace bottom of No. 5, a large amount of fluid medium can be stably moved from the char combustion chamber 3 side to the gasification chamber 2 side. Therefore, no mechanical means for handling high-temperature particles is required to move the fluidized medium from the char combustion chamber 3 side to the gasification chamber 2 side. Although oxygen-free gas is used as the fluidizing gas in the gasification chamber 2, a gas containing no oxygen such as water vapor may be used as the so-called oxygen-free gas.

Inside the gasification chamber 2 in which the flow of the combustible gas b is formed, a cyclone separator 31 as a particle / gas separator or a cyclone separator is arranged. Cyclone separator 31
Is an inlet 32 for introducing the combustible gas b generated in the gasification chamber 2, a particle discharge pipe 33 that is entrained in the combustible gas b and guides the particles c separated by the cyclone separator 31, and a tip of the particle discharge pipe 33. And a gas outlet 35 for discharging the combustible gas b from which the particles c have been separated.

As shown in FIG. 2, the combustible gas b entering the cyclone separator 31 from the inlet 32 forms a swirling flow, and the particles c are centrifugally generated by the cyclone separator 31.
Toward the inner wall 31A of the cyclone separator 31 while falling along the inner wall 31A while rotating, and discharged from the particle discharge pipe 33 attached to the lower portion of the cyclone separator 31 in FIG. 2B. The combustible gas b from which the particles c have been separated is discharged from the gas discharge port 35 formed in the upper portion of the cyclone separator 31 in FIG. The cyclone separator 13 described later
1, 231, 331, 431, and 531 also have the same structure as the cyclone separator 31.

Returning to FIG. 1, the description will be continued. The gas outlet 35 of the cyclone separator 31 is connected to the gas outlet 36 of the gasification chamber 2 by a pipe 37. The particle discharge pipe 33 is configured to exit the gasification chamber 2 and enter the char combustion chamber 3, and the particle discharge port 34 is provided for the char combustion chamber 3
Is located above the fluidized bed interface. The separated particles c are directly introduced from the gasification chamber 2 into the char combustion chamber 3 via the particle discharge pipe 33.

Therefore, the combustible gas b from which the particles c such as char have been removed is discharged from the gas discharge port 36 of the gasification chamber 2. The particles c separated from the combustible gas b generated in the gasification chamber 2 by the cyclone separator 31 are sent to the char combustion chamber 3 and the char portion and the like are combusted.

In the present embodiment, since the cyclone separator 31 is arranged in the gasification chamber 2, there is no heat radiation from the cyclone separator to the outside air, which occurs when the cyclone separator is arranged outside the furnace, and the cyclone separator is discharged to the cyclone separator. Since the external pipe for guiding the combustible gas b and the external pipe for guiding the particles c separated from the cyclone separator to the char combustion chamber 3 are unnecessary, the heat radiation loss can be reduced.
Further, since the temperature decrease can be reduced, the trouble factor due to the temperature decrease can be eliminated when there is a liquid substance such as a tar component which is precipitated when the temperature is decreased.

FIG. 3 shows an integrated gasification furnace 101 according to another embodiment. The integrated gasification furnace 101 shown in FIG.
The integrated gasification furnace 1 shown in FIG. 2 has the same configuration as the integrated gasification furnace 1 except for the arrangement of a cyclone separator 131 described later. As shown in the figure, the gasification chamber 102 of the integrated gasification furnace 101
Cyclone separator 131 is arranged inside, and particle discharge pipe 133A is further arranged inside gasification chamber 102, and particle discharge port 134A is divided into partition wall 111 between gasification chamber 102 and char combustion chamber 103. It may be arranged near the opening 121, and the particles c emitted from the particle discharge port 134 may be carried to the char combustion chamber 103 by the flow of the char and the fluid medium. The particles c are introduced from the gasification chamber 102 into the char combustion chamber 103. In this case, the particles c separated by the cyclone separator 131 are sent to the char combustion chamber 103, and the char portion and the like are combusted. In addition, the gas outlet 13 of the gasification chamber 102
Combustible gas b from which particles c such as char have been removed is discharged from 6. Therefore, the same effect as that of the integrated gasification furnace 101 of FIG. 1 can be obtained.

3, a cyclone separator 131 is arranged inside the gasification chamber 102, a particle discharge pipe 133B is arranged inside the gasification chamber 102, and a particle discharge port 134B. May be located above the interface of the gasification chamber fluidized bed of the gasification chamber 102. In this way, the residence time of the particles c inside the gasification chamber 102 can be lengthened.

In the present embodiment, since the cyclone separator 131 is arranged in the gasification chamber 102, there is no heat radiation from the cyclone separator 131 to the outside air, which occurs when the cyclone separator is arranged outside the furnace, and the cyclone separator 131 is eliminated. Since an external pipe for guiding the combustible gas b to the gas, and an external pipe for guiding the particles c separated from the cyclone separator to the gasification chamber 102 are not necessary, heat dissipation loss can be reduced. Further, since the temperature decrease can be reduced, the trouble factor due to the temperature decrease can be eliminated when there is a liquid substance such as a tar component which is precipitated when the temperature is decreased.

FIG. 4 shows an integrated gasification furnace 201 according to another embodiment. The integrated gasification furnace 201 shown in FIG.
The integrated gasification furnace 1 shown in FIG. 4 and the integrated gasification furnace 1 shown in FIG. As shown in the figure, the cyclone separator 231 may be installed in the char combustion chamber 203 of the integrated gasification furnace 201.
As indicated by the solid line in the figure, the cyclone separator 231
Extending the particle discharge pipe 233A to the gasification chamber 202,
The particle outlet 234A may be located in the gasification chamber fluidized bed of the gasification chamber 202. In this case, the separated particles c are directly introduced into the gasification chamber 202 from the char combustion chamber 203.

Further, as shown by the two-dot chain line in the figure,
The particle discharge pipe 233B is extended to above the partition wall 214 that partitions the char combustion chamber main body part and the settling char combustion chamber 215 so that the particle discharge port 234B is located above the partition wall 214. The particles c discharged from the fuel cell may flow from the char combustion chamber 203 into the sedimentation char combustion chamber 205 along with the flow toward the sedimentation char combustion chamber 205 over the partition wall 214, and further into the gasification chamber 202. . In this way, the separated particles c are returned to the gasification chamber 202, so that the gasification chamber 20 for the particles c is
The residence time at 2 can be extended. Further, as indicated by a partly broken line in the figure, the particle discharge port 234C of the particle discharge pipe 233C may be located above the interface of the char combustion fluidized bed. In this way, the separated particles c are returned to the char combustion chamber 203, so that the residence time of the particles c in the char combustion chamber 203 can be lengthened.

In this embodiment, since the cyclone separator 231 is arranged inside the char combustion chamber 203, there is no heat radiation from the cyclone separator 231 to the outside air, which occurs when the cyclone separator is arranged outside the furnace. Since the external pipe for guiding the combustible gas b to the gasification chamber 202 from the cyclone separator or the external pipe for guiding the separated particles c to the char combustion chamber 203 is not required, the heat radiation loss can be reduced. Further, since the temperature decrease can be reduced, the trouble factor due to the temperature decrease can be eliminated when there is a liquid substance such as a tar component which is precipitated when the temperature is decreased. By transferring the particles from the char combustion chamber 203 having a high gas velocity to the gasification chamber 202 having a low gas velocity, the residence time of the particles c in the furnace can be increased.

FIG. 5 shows a case where the integrated gasification furnace 1 according to the first embodiment of the present invention is used in a combined cycle power generation system.

The integrated gasification furnace 1 of the present invention comprises a pressure vessel 50.
And is operated under pressure. Integrated gasifier 1
The outer wall may have an integral structure that doubles as a pressure vessel. After the combustible gas b generated in the gasification chamber 2 is separated into particles c by the cyclone separator 31 in the gasification chamber 2,
Together with the combustion gas u1 from which the ash has been separated by the dust collector 51, it is guided to the topping combustor 53 as an auxiliary combustion chamber and burned to become a high temperature gas r. The dust collector 51 may have the same structure as the cyclone separator 31, or may use a ceramic filter, a metal filter using a heat-resistant alloy, or the like as the dust collector. The hot gas r is supplied to the gas turbine unit 55 as an energy recovery device. The gas turbine section 55 is a device similar to the output turbine section of a normal combustion gas turbine, and is also called a power recovery turbine.

A heat transfer tube 42 may be installed above the char combustion chamber 3 if necessary. Even if the raw material a contains chlorine, the chlorine is combustible gas generated in the gasification chamber 2 b.
The char combustion gas u1 in the present embodiment contains almost no chlorine because it is mostly contained in the side. Therefore, the heat transfer tube 42 can be used as a steam superheater for steam superheating at 500 ° C. or higher. Since the in-layer heat transfer tube 41 arranged in the heat recovery chamber 4 is not in a more corrosive environment than the heat transfer tube 42, the steam superheater can handle temperatures higher than the heat transfer tube 42.

In the power generation system using the pressurized fluidized bed furnace shown in the figure, first, the raw material a is gasified in the pressurized gasification chamber 2 and the unburned carbon (so-called char) generated is burned in the pressurized char combustion chamber 3. The ash is separated from the combustion gas u1 discharged from the char combustion chamber 3 by the dust collector 51, and the combustible gas b generated in the gasification chamber 2 is removed by the cyclone separator 31 in the gasification chamber 2 to remove the particles c. After, topping combustor 5
The mixed combustion is performed in 3 to obtain the high temperature gas r, and the gas turbine unit 55 is driven. The particles c removed by the cyclone separator 31 are guided from the gasification chamber 2 to above the fluidized bed interface of the char combustion chamber 3, and the char component is burned.

What is important in the power generation system using the pressurized fluidized bed furnace is how to raise the temperature of the gas flowing into the gas turbine section 55 to the maximum allowable temperature determined by the gas turbine side. The largest condition to be met is cleaning of the combustible gas b generated in the gasification chamber 2. Here, the cleaning is, for example, desulfurization. Desulfurization is necessary, for example, to protect the turbine blades of the gas turbine section 55.

In order to clean the combustible gas b, it is usually necessary to cool it to about 450 ° C. because of the optimum temperature of the desulfurization reaction in the reducing atmosphere. On the other hand, the gas turbine unit 5
The higher the inlet gas temperature of 5, the higher the reaction efficiency.
It should be as hot as possible. At present, it is general to raise the temperature to a little less than 1200 ° C. due to heat resistance and corrosion resistance of gas turbine constituent materials. That is, the gas cleaning temperature of 450 ° C. to the gas turbine inlet temperature of 120
The combustible gas b is required to have a calorific value sufficient to raise the temperature of the gas up to 0 ° C.

Although not shown in FIG. 5, a combustible gas cooler is provided in the gas path between the gasification chamber 2 and the cyclone separator to cool the combustible gas b to, for example, about 450 ° C. Desulfurization equipment may also typically be provided. This is done to protect the blades of the gas turbine. A gas cooler and a desulfurizer are usually unnecessary in the gas passage from the char combustion chamber 3. This is because limestone is introduced into the furnace, limestone is circulated together with the fluid medium, and the char combustion chamber 3 is also in an oxidizing atmosphere in which oxygen exists, so that the sulfur content is removed as CaSO ₄ .

Therefore, in the power generation system using the improved pressurized fluidized bed furnace, it is necessary to develop the system so as to obtain the combustible gas b having a high unit calorific value in a small amount as much as possible. Because, if the amount of the combustible gas b to be cleaned at 450 ° C. is reduced, the sensible heat loss due to cooling is reduced and the minimum required calorific value required for the combustible gas b is also low. Further, if the calorific value of the combustible gas b is equal to or higher than the calorific value necessary to raise the gas temperature at the inlet of the gas turbine, the combustion air ratio is increased to increase the gas turbine section 55.
This is because it is possible to increase the amount of the combustible gas b flowing into the fuel cell, and it is possible to expect further improvement in power generation efficiency.

In the system of FIG. 5, after the combustion gas u1 from the char combustion chamber 3 is collected and dedusted by the dust collector 51,
The power is guided to the turbine unit 55 and the power is recovered. At this time,
The combustion gas u1 may be directly guided to the turbine section 55,
Since the temperature of this combustion gas u1 is not so high, the efficiency of power recovery is not necessarily high. Therefore, the combustible gas b generated in the gasification chamber 2 is collected and dedusted by the cyclone separator 31 in the gasification chamber 2, and then guided to the topping combustor 53 where it is burned. This combustion is an auxiliary combustion for the combustion gas u1 from the char combustion chamber 3 described above. Due to this combustion heat, the combustion gas u1 from the char combustion chamber 3 becomes a high temperature gas r of about 1200 ° C. (1500 ° C. is possible depending on the heat resistant temperature of the output turbine section). The high temperature gas r is supplied to the output turbine unit (power recovery device) 55. In such an apparatus, the combination of the char combustion chamber 3 and the topping combustor 53 corresponds to a normal gas turbine combustor.

A reduction gear is attached to the rotary shaft of the output turbine section.
Drive a generator 57 directly or via
Generate electricity. In the embodiment of FIG. 5, the output type
A compressor (typically an axial flow air) is installed on the rotary shaft of the bin portion 55.
A compressor 56 is directly connected to generate compressed air.
This compressed air is mainly used with the combustion air in the char combustion chamber 3.
Then, it is supplied to the char combustion chamber 3. Some are toppins
It is supplied to the gucon buster 53. Most toppings
In the blaster 53, the exhaust gas from the char combustion chamber 3 is usually
The combustible gas b can be burned by the oxygen remaining in the gas.
It In addition, in this embodiment, the inside of the pressure vessel 50 is 5 to
10 kg / cm^Two  Pressurized to the extent. Inside the pressure vessel 50
Is, for example, 30 according to the specifications of the output turbine section 55.
kg / cm ^TwoYou may pressurize to some extent.

In the embodiment of FIG. 5, in order to guide the exhaust gas u1 from the char combustion chamber 3 and the combustible gas b from the gasification chamber 2 to the output gas turbine section 55, the premixing chamber for mixing them once is provided. Also, the topping combustor 53 is required, but when only the combustible gas b from the gasification chamber 2 is guided to the output gas turbine section 55, the combustible gas b is directly supplied to a combustor (not shown) attached to the gas turbine. May be introduced. If only the combustible gas b from the gasification chamber 2 is introduced,
The gas turbine can be operated by using the gas having a high heat amount as fuel.

Further, the exhaust gas h discharged from the output turbine section 55 is guided to the waste heat boiler 58 through the route 125, and then, through the exhaust gas route 128, desulfurization (not shown),
It is emitted from a chimney (not shown) via a denitration device or the like.

On the other hand, in the waste heat boiler 58, the heat of the exhaust gas h is recovered and the steam s is generated. The steam s is supplied to the steam turbine 162 through the steam pipe 127, and drives the generator 163 that is directly connected to the rotating shaft of the steam turbine 162 via a speed reducer or to generate electric power. The steam s supplied to the steam turbine 162 may include the steam s from the heat transfer tubes 41 and 42.

Since the combined cycle power generation system shown in the figure uses the integrated gasification furnace 1 according to the first embodiment of the present invention, heat dissipation from the cyclone separator 31 is prevented and the surrounding pipes are prevented. The heat radiation loss can be greatly reduced, and the temperature drop of the high temperature gas r can be reduced. Therefore, a decrease in power generation efficiency due to heat radiation loss can be suppressed.

Next, referring to FIG. 6, a two-column circulation type gasification furnace 30 as a reactor according to the second embodiment of the present invention.
1 will be described. The two-tower circulation type gasification furnace 301 is composed of two separate gasification furnaces 302 and a char combustion furnace 303, and a fluidized medium having chars generated when the raw material a is gasified in the gasification furnace 302 is attached to the char combustion furnace. Char conveying pipe 305 to be sent to 303 and the attached tar are char combustion furnace 303
It is configured to include a fluidized medium transport pipe 304 that sends the fluidized medium that has been burned and removed in the above to the gasification furnace 302.

The gasification furnace 302 and the char combustion furnace 303 are provided with diffuser slopes 306 and 307, respectively, and fluidized gas is introduced from the diffuser slopes 306 and 307 to the upper part of the furnace,
Fluidization of the fluidized medium takes place to form a fluidized bed. The gasification furnace 302 is supplied with vapor s or combustible gas b as a fluidizing gas, and the char combustion furnace 303 is supplied with air k as a fluidizing gas.

The attachment portion of the char transport pipe 305 to the gasification furnace 302 is located above the fluidized bed of the gasification furnace 302, and the attachment portion of the char transport pipe 305 to the char combustion furnace 303 is located slightly above the aeration slope 307. To be located. The attachment portion of the fluid combustion medium conveying pipe 304 to the char combustion furnace 303 is attached to the upper part of the fluidized bed of the char combustion furnace 303 at the fluid medium conveyance pipe 30.
The mounting portion of the gasification furnace 302 of No. 4 is located slightly above the diffuser slope 306.

The raw material a is put into the gasification furnace 302,
The raw material a is gasified by the sensible heat of the fluidized medium and combustible gas b
Is generated. The char and the fluidized medium generated by the gasification of the raw material a are sent from the gasification furnace 302 to the char combustion furnace 303 through the char transport pipe 305, and the char is combusted in the char combustion furnace 303 to generate the combustion gas u1. At this time, the combustion heat generated by the combustion of char is given to the fluidized medium as sensible heat.

The fluidized medium from which the char has been removed and which has been given sensible heat passes through the fluidized medium conveying pipe 304 and the char combustion furnace 3
03 is sent to the gasification furnace 302, and the raw material a is gasified. A cyclone separator 331 is installed on the freeboard part of the gasification furnace 302. Dust of the combustible gas b generated in the gasification furnace 302 is removed by the cyclone separator 331, and the combustible gas b after the dust removal is removed by the gasification furnace 30.
Emitted from 2.

As shown in the plan view of FIG. 7, the particle discharge pipe 333 of the cyclone separator 331 (FIG. 6) for discharging the separated particles c exits the gasification furnace 302 and enters the char combustion furnace 303. It is configured. Particle discharge pipe 3
In the figure, 33 is the center of the gasification furnace 302 and the char combustion furnace 3
It is arranged so as to pass on the line connecting the center of 03,
A predetermined gradient is provided. The predetermined gradient is a gradient in which particles are gradually lowered so as to smoothly move from the gasification furnace 302 to the char combustion furnace 303. The route of the particle discharge pipe 333 shown in the figure is the shortest route from the gasification furnace 302 to the char combustion furnace 303 with a predetermined gradient.

The particle discharge port 334 at the tip of the particle discharge pipe 333 is located above the interface of the fluidized bed of the char combustion furnace 303. Therefore, the char component in the particles sent to the char combustion furnace 303 is combusted, and the combustion gas u1 is generated.

Therefore, in the two-column circulation type gasification furnace 301 of this embodiment, the cyclone separator 331 for removing the particles c in the combustible gas b generated in the gasification furnace 302 is installed in the freeboard section inside the gasification furnace 302. Therefore, there is no heat radiation from the cyclone separator to the outside air that occurs when the cyclone separator is placed outside the furnace, and there is no heat radiation from the external pipe that guides the combustible gas to the cyclone separator. Furthermore, the particle discharge pipe 333 that conveys and discharges the removed particles c to the char combustion furnace 303 can be arranged in a straight line through the shortest route, and the particle discharge pipe 333 can be arranged.
The length of the external pipe passing through the outside of the furnace can be shortened, and the routing of the external pipe can be minimized.
Therefore, the trouble in handling the separated particles c is unlikely to occur, the temperature decrease of the separated particles c can be minimized, and the decrease of the reaction efficiency of the entire system can be minimized.

FIG. 8 shows a two-column circulation type gasification furnace 401 according to another embodiment. Two tower circulation type gasification furnace 401 shown in the figure
Has the same configuration as that of the two-column circulation type gasification furnace 301 shown in FIG. 6 and the arrangement of a cyclone separator 431 described later. As shown in the figure, the cyclone separator 431 is installed in the freeboard section inside the gasification furnace 402 of the two-column circulation gasification furnace 401, the particle discharge pipe 433A is arranged inside the gasification furnace 402, and the particle discharge port 434A is installed. The inlet 405A of the char transport pipe 405 of the gasification furnace 402
The particle c discharged from the particle discharge port 434 may be placed in the vicinity of the above, and sent to the char combustion furnace 403 along with the flow of the particles c discharged into the char transport pipe 405.
In addition, as indicated by a partly broken line in the figure, the particle outlet 434
B may be positioned above the fluidized bed interface of the gasification furnace 402, and the particles c discharged from the particle discharge port 434B may circulate inside the gasification furnace fluidized bed.

In the present embodiment, since the cyclone separator 431 is arranged in the gasification furnace 402, there is no heat radiation from the cyclone separator to the outside air, which occurs when the cyclone separator is arranged outside the furnace, and the cyclone separator 431 is discharged to the cyclone separator. Since an external pipe for guiding the combustible gas b and an external pipe for guiding the particles c separated from the cyclone separator to the gasification furnace 402 are not required, heat dissipation loss can be reduced. Further, when there is a liquid substance such as tar that precipitates when the temperature decreases, the trouble factor due to the temperature decrease can be eliminated.

FIG. 9 shows a two-column circulation type gasification furnace 501 according to another embodiment. Two tower circulation type gasification furnace 501 shown in the figure
Has the same configuration as that of the two-column circulation type gasification furnace 301 shown in FIG. 6 and the arrangement of a cyclone separator 531 described later. As shown in the figure, the cyclone separator 531 is installed on the freeboard part inside the char combustion furnace 503, the particle discharge pipe 533A is arranged inside the gasification furnace 503, and the particle discharge port 534A is arranged on the fluidized bed interface of the gasification furnace 503. May be located above. Further, as shown by a partly broken line in the figure, the particle discharge pipe 533B is connected to the char combustion furnace 50.
3 inside, the particle discharge port 534B is arranged in the vicinity of the inlet 504A of the fluidized medium transport pipe 504, the particles c discharged from the particle discharged port 534B ride on the flow entering the fluidized medium transport pipe 504, and the gas is discharged. It may be sent to the chemical conversion furnace 502. In addition, as indicated by the chain double-dashed line in the figure, the particle discharge pipe 533C and the particle discharge port 534C are positioned above the fluidized bed interface of the char combustion furnace 503, and the particle c discharged from the particle discharge port 534C. May circulate inside the char combustion furnace fluidized bed. The two-column circulation gasification furnace 501 of the present embodiment does not release heat from the cyclone separator 531 and does not release heat from the particle discharge pipe 533 when returning the particles c to the char combustion furnace 503. When returning to the gasification furnace 502, since the particle discharge pipe 533 can be made linear, heat radiation from the particle discharge pipe 533 can be minimized.

[0086]

As described above, according to the present invention, the particle / gas separation device provided inside the first chamber is provided, and the particles entrained in the gas are separated from the gas. To
Since it can be introduced into the second chamber integrally formed adjacent to the first chamber, the separated particles can be conveyed through the inside of the furnace, and inside the external pipe routed outside the furnace. Need not be transported. Therefore, a trouble in handling the separated particles is unlikely to occur, the temperature does not decrease, and the decrease in reaction efficiency of the entire system and the occurrence of trouble due to the temperature decrease can be avoided. Further, the particles can be continuously retained in the system, and the retention time in the system can be lengthened.

[Brief description of drawings]

FIG. 1 is a configuration diagram showing a basic concept of an integrated gasification furnace according to a first embodiment of the present invention.

FIG. 2A is a plan view of a cyclone separator,
(B) is a front view.

FIG. 3 is a configuration diagram showing the basic concept of an integrated gasification furnace when the form of a particle discharge pipe of a cyclone separator is changed.

FIG. 4 is a configuration diagram showing the basic concept of the integrated gasification furnace when the installation position of the cyclone separator is changed.

5 is an explanatory diagram of an embodiment of a combined cycle power generation system using the integrated gasification furnace of FIG.

FIG. 6 is an explanatory diagram showing a basic configuration of a two-column circulation type gasification furnace according to a second embodiment of the present invention.

7 is a plan view of the two-column circulation type gasification furnace of FIG.

FIG. 8 is an explanatory diagram showing a basic configuration of a two-column circulation type gasification furnace when the form of the particle discharge pipe of the cyclone separator is changed.

FIG. 9 is an explanatory diagram showing a basic configuration of a two-column circulation type gasification furnace when the installation position of the cyclone separator is changed.

FIG. 10 is an explanatory view of a conventional fluidized bed gasification furnace provided with a cyclone separator outside.

[Explanation of symbols]

1,301 Integrated gasification furnace 2,302 gasification chamber 3,303 Char combustion chamber 4 Heat recovery room 5 Settling char combustion chamber 10 Integrated gasifier 11, 12, 13, 14, 15 Partition wall 19 ceiling 21, 22, 25 openings 31, 331 cyclone separator 32 entrance 33, 333 Particle discharge pipe 34,334 Particle outlet 35 gas outlet 36 Gas outlet 50 pressure vessel 53 Topping combustor 55 Power recovery turbine (output turbine section) 56 air compressor 104 Combustible gas compressor 105 Combustor 106 Output turbine section 107 air compressor 109 gas turbine 141 Power recovery turbine (output turbine section) a raw material b Combustible gas c particles u1, u2 Combustion gas k air s steam

   ─────────────────────────────────────────────────── ─── Continued front page    (72) Inventor Shugo Hosoda             11-1 Haneda Asahi-cho, Ota-ku, Tokyo Edo Co., Ltd.             In the original factory (72) Inventor Tatsuo Tokudome             11-1 Haneda Asahi-cho, Ota-ku, Tokyo Edo Co., Ltd.             In the original factory F term (reference) 3K064 AA10 AA17 AB03 AD05 AD08                       AE04 AE15 BA03 BA05 BA07                       BA13 BA18

Claims (8)

[Claims] 1. A first chamber in which a gas flow entrained by particles is formed; a second chamber integrally formed adjacent to the first chamber; and the first chamber. A particle / gas separator for separating the gas entrained in the gas from the gas, the particle / gas separating device being installed inside;
A reactor configured to be introduced into the second chamber; targeting the gas for reaction; 2. The first chamber internally flows a fluidized medium to form a fluidized bed having an interface, and the particle / gas separation device is installed so as to be vertically above the interface. The reactor according to claim 1. 3. A first chamber in which a fluidized medium is fluidized to form a fluidized bed having an interface, and a gas flow entrained with particles is further formed therein; and the first chamber. A second chamber separately provided; a particle / gas separation device installed inside the first chamber for separating the particles entrained in the gas from the gas; the separated particles To
A reactor configured to be introduced into the second chamber; targeting the gas for reaction; 4. The reactor according to claim 2 or 3, wherein the fluidized medium is configured to circulate between the first chamber and the second chamber. 5. The reactor according to any one of claims 1 to 4, wherein the particle / gas separator is a cyclone separator. 6. The reaction is at least one of combustion, partial oxidation and gasification;
The reaction apparatus according to any one of 1. 7. The reactor according to claim 1, wherein the first chamber and the second chamber have different functions. 8. A gas flow is formed inside the second chamber, the flow velocity of the gas flow formed inside the first chamber and the gas flow formed inside the second chamber. The reactor according to any one of claims 1 to 7, which has a different flow velocity.