JP2003172504A - Fluid blow-out nozzle and fluidized bed reactor - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a fluid blow-out nozzle which holds an appropriate pressure loss on the whole nozzle and maintains the stability of the blow without making excessive a blow-out speed when the blow-out flow rate is significantly changed, and also maintains the uniformity of the quantity of the blow from each nozzle when a plurality of nozzles are provided. <P>SOLUTION: The fluid blow-out nozzle 61 for blowing a fluid (x) into a particle layer R has a blow-out part 71 for blowing the fluid (x) to the particle layer R with a first flow resistance against the fluid and a restriction part 64 disposed on the upstream side of the blow-out part with a second flow resistance always larger than the first flow resistance. The blow-out part has a set of blow-out holes 63, and one restriction part is mounted for one set of the blow-out holes. <P>COPYRIGHT: (C)2003,JPO

Description

Detailed Description of the Invention

[0001]

TECHNICAL FIELD The present invention relates to a fluid blowing nozzle for blowing a fluid into a particle layer and a fluidized bed reactor equipped with the fluid blowing nozzle.

[0002]

2. Description of the Related Art A conventional fluid ejecting nozzle for ejecting a fluid into a particle layer has a pressure loss by narrowing a flow passage area of an ejecting portion and increasing an ejecting flow velocity in order to stabilize ejection. There is.

[0003]

In a fluid blowing nozzle for blowing a fluid, particularly a gas, into a fluidized particle bed, which is installed in a fluidized bed reactor, a component (for example, a part close to the periphery of the nozzle if the blowing velocity is too high). Other nozzles, heat transfer tubes, hearth refractories, etc.) may be damaged by the blast effect.

However, when the flow velocity of the blowout is reduced, it is impossible to provide an appropriate pressure loss, the stability of the blowout becomes insufficient, and when a plurality of nozzles are present, the uniformity of the blowout amount of each nozzle is not uniform. There is a fear that it will be sufficient.

Therefore, according to the present invention, even if the flow rate of the blowout is largely changed, the flow velocity of the blowout is not excessively increased, and an appropriate pressure loss is provided over the entire nozzle so that the stability of the blowout can be maintained and a plurality of nozzles can be maintained. In the presence of the above, the object of the present invention is to provide a fluid ejection nozzle capable of maintaining the uniformity of the ejection amount of each nozzle, and a fluidized bed reactor equipped with the ejection nozzle.

[Means for Solving the Problems]

In order to achieve the above object, a fluid ejection nozzle according to the invention according to claim 1 is a fluid ejection nozzle 61 for injecting a fluid x into a particle layer R as shown in FIG. A blow-out portion 71 that blows out to R and has a first flow resistance with respect to the fluid x; and a second flow resistance that is arranged upstream of the blow-out portion 71 and that is always larger than the first flow resistance. The blowing portion 71 has a pair of blowing holes 63 formed therein, and one narrowing portion 64 is provided for each of the pair of blowing holes 63.

With this structure, the blowing portion 71
And the throttling portion 64, the throttling portion 64 disposed upstream of the blowing portion 71 has a pressure loss that is always greater than the pressure loss of the blowing portion 71, so that the blowing flow rate is significantly changed. Also, it becomes possible to prevent the flow velocity of the fluid from the blowing portion 71 into the particle layer R from becoming excessive and to secure an appropriate pressure loss at the fluid blowing nozzle 61. Therefore, stable ejection from the fluid ejection nozzles 61 can be ensured, and when there are a plurality of fluid ejection nozzles 61, uniform ejection from each fluid ejection nozzle 61 can be ensured.

The set of blow-out holes may be a single hole, but a plurality of, for example, two, blow-out holes may be formed so that the fluid is blown out in different directions. The magnitude of the flow resistance is judged by comparing the pressure loss applied to the fluid when the fluid is arranged in a predetermined fluid flow, and the magnitude thereof. Second rather than first flow resistance
The fact that the flow resistance is always large means that the flow resistance does not become smaller than the first flow resistance even if the flow resistance of the throttle portion 64 is variable. The fluid x is typically a gas. The throttle unit 64 may be a variable orifice or a fixed orifice, but is typically the latter.

A fluid ejecting nozzle 61 according to a second aspect of the present invention is the fluid ejecting nozzle according to the first aspect, wherein the throttle portion 64 is a fixed orifice as shown in FIG.

With this structure, since the throttle portion 64 is a fixed orifice, a large flow resistance can be easily generated with a simple structure.

In order to achieve the above object, a fluidized bed reactor 1 according to a third aspect of the present invention is a fluidized bed reactor in which a reaction is carried out in a fluidized particle bed R1 as shown in FIGS. 1, the fluid ejection nozzle 61 according to claim 1 or 2; and the supply ports 83A and B for supplying the fluid x1 to the fluid ejection nozzle 61.

With this structure, the supply ports 83A, 83B
Is supplied to the fluid ejection nozzle 61 from the fluid ejection nozzle 61, and the ejection velocity into the particle layer R1 is not excessively increased even if the ejection flow rate of the fluid x1 ejected from the fluid ejection nozzle 61 is significantly changed. It is possible to secure an appropriate pressure loss in the blowing nozzle 61, and a stable fluidized bed R1 can be formed in the fluidized bed reactor 1. The fluidized bed reactor is a fluidized bed reactor,
It refers to a fluidized bed furnace (eg, fluidized bed gasification furnace).

[0013]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to FIG. FIG. 1 is a partial cross-sectional view of a dispersion nozzle device 51 including a fluid ejection nozzle 61 according to the first embodiment of this invention. Dispersion nozzle device 51
Is a plurality of fluid ejection nozzles 61 (only one fluid ejection nozzle 61 is shown in the figure), and a fluid ejection nozzle 6
A plurality of insertion holes 52 into which 1 is inserted (the insertion hole 52 in the drawing is 1
(Only one is shown in the figure). The dispersion plate 53 forms the bottom of the fluidized bed gasification furnace 1 described below, in which the dispersion nozzle device 51 is incorporated (see FIG. 2). In the figure, above the dispersion plate 53, there is a particle layer R which is a fluidized bed formed by particles of a fluidized medium by a fluidizing gas x as a fluid which is blown out from a fluid blowing nozzle 61.

The fluid blowing nozzle 61 is formed on a tubular body 62 having one end 62A closed and the fluidized gas x supplied from the other end (not shown), and an outer peripheral surface 62B near the one end 62A of the tubular body 62. Further, it is configured to include a pair of through holes 63 as blow-out holes and a plate-like body 65 that is attached in close contact with the inner peripheral surface 62C of the tubular body 62 and has a fixed orifice 64 as a narrowed portion. The shapes of the through hole 63 and the fixed orifice 64 are circular. One end 62 of the tubular body
The tip portion of the tubular body 62 including the through hole 63 including A constitutes the blowing portion 71 of the present invention. The through holes 63 of the blowing portion 71 are arranged at positions facing each other, and are symmetrically arranged so that the flow rates of the through holes 63 are equal.

The fluidizing gas x is directed from the bottom to the top in the figure, that is, in the longitudinal upper direction of the tubular body 62 (P direction in the figure).
And is supplied to the inside of the tubular body 62. Fluidized gas x
Passes through the fixed orifice 64, then through the through hole 63, and is blown toward the particle layer R outside the tubular body 62 in the direction perpendicular to the P direction (Q direction in the drawing). .
The fixed orifice 64 is arranged upstream of the through hole 63 with respect to the flow of the fluidizing gas x. Fluidized gas x
Passes through the fixed orifice 64 to generate a second flow resistance, and the fluidized gas x passes through the through hole 63 to generate a first flow resistance. The diameter of the through hole 63 and the fixed orifice 64 are set so that the second flow resistance always has a larger value than the first flow resistance (even when the fluidized gas x flow rate varies) (except when the flow rate is zero). , That is, the flow passage area of the through hole 63 and the flow passage area of the fixed orifice 64 are determined.

In the case of a conventional fluid ejection nozzle that does not include a plate-like body (and therefore a fixed orifice), the flow rates of two cases, large and small, can be determined by the operation pattern of the device incorporating the dispersion nozzle device with the fluid ejection nozzle attached. Sometimes it is necessary to supply from the same nozzle.
At this time, if the diameter of the through hole (flow passage area) is determined according to the case of a large flow rate, the pressure loss of the through hole becomes too small in the case of a small flow rate, and the blowout flow rates of the plurality of through holes become uniform. There is a case where the sex cannot be maintained. Conversely, if the diameter of the through hole (flow passage area) is determined according to the case of a small flow rate, the flow velocity from the through hole will be too high in the case of a large flow rate, and the blast effect of particles on the parts of the adjacent device May cause damage.

In the case of the fluid ejection nozzle 61 of this embodiment, the through hole 6 is formed at a location where pressure loss (pressure resistance) occurs.
In addition to 3, the pressure loss (pressure resistance) is also generated in the fixed orifice 64 so that the pressure loss in the fixed orifice 64 is always larger than the pressure loss in the through hole 63. Therefore, by determining the pressure loss of the fixed orifice 64 according to the case of the small flow rate, and by determining the flow velocity of the air blown out from the through hole 63 according to the case of the large flow rate, each through hole 6 in the case of the small flow rate is determined.
It is possible to maintain the uniformity of the flow rate in No. 3 and prevent the flow velocity of air blown out from the through hole 63 from becoming excessive in the case of a large flow rate.

Next, referring to FIG. 2 and appropriately to FIG. 1, a fluidized bed gasification furnace as a fluidized bed reactor according to the second embodiment of the present invention equipped with dispersion nozzle devices 51A and 51B. 1 will be described. FIG. 2 is a block sectional view schematically showing the basic configuration of the fluidized bed gasification furnace 1.

The fluidized bed gasification furnace 1 has a raw material supply port 2 and
Dispersion nozzle devices 51A and 51B and incombustible material discharge chute 4
And a combustible gas discharge port 5 and a fluidizing gas supply device 91. The dispersion nozzle devices 51A and 51B are shown in FIG.
The same structure as that of the dispersion nozzle device 51 shown in FIG. 1, a fluid ejection nozzle 61 (see FIG. 1), a nozzle dispersion plate 53A,
B and fluidized gas supply ports 83A and B as supply ports, and the dispersion plates 53A and B form the bottom of the fluidized bed gasification furnace 1. The dispersion nozzle device 51A is disposed in the center, and the dispersion nozzle device 51B is the dispersion nozzle device 51.
The dispersion nozzle device 51 </ b> A is arranged outside of A to surround the dispersion nozzle device 51 </ b> A. Therefore, the dispersion plate 53A is arranged in the central portion of the furnace bottom, and the dispersion plate 53B is arranged in the peripheral portion of the furnace bottom. The incombustible discharge chute 4 is arranged outside the dispersion plate 53B,
From the incombustibles discharge chute 4, incombustibles d1 and silica sand c1 which is a fluid medium are discharged.

The fluidizing gas supply ports 83A and 83B communicate with the fluid blowing nozzle 61 (see FIG. 1). A fluidizing gas supply device 91 is connected to the fluidizing gas supply ports 83A and 83B. The fluidizing gas supply device 91 includes the supply pipe 8
6A, B, header pipe 87, branch pipe 88A, B
A first fluidizing gas generator 89 that generates a first fluidizing gas x1 as a fluid, and a second fluidizing gas generator 90 that generates a second fluidizing gas y1 as a fluid. It The supply pipes 86A and B are connected to the fluidizing gas supply ports 83A and B, the supply pipes 86A and B are connected to a header pipe 87, and the header pipe 87 is branched again to branch pipes 88A and B. 88A is connected to the first fluidizing gas generator 89, and the branch pipe 88B is connected to the second fluidizing gas generator 90.

The dispersion nozzle devices 51A and 51B include a dispersion plate 53.
The flow velocity of the first fluidizing gas x1 and the second fluidizing gas y1 blown out through A and B can be changed. The superficial velocity is different in each of the dispersion plates 53A and B, and therefore the flow state of the silica sand c1 above each of the dispersion plates 53A and B is different, so that an internal swirl flow is formed inside the fluidized bed gasification furnace 1. . In the figure, a dispersion nozzle device 51A,
The size of the white arrow shown in B indicates the magnitude of the flow velocity of the first fluidized gas x1 and the second fluidized gas y1 that are blown out. The thick arrow at the location of the dispersion plate 53B on the outer periphery of the furnace bottom is
This indicates that the flow velocity is higher than that of the thin arrow at the dispersion plate 53A at the center of the furnace bottom. The fluidizing gas is water vapor, air, combustible gas, or the like.

In the normal operating condition, the first fluidizing gas generator 89, the branch pipe 88A, and the header pipe 87.
, Supply pipes 86A, B, fluidized gas supply port 83A,
The first fluidized gas x1 is supplied to the inside of the fluidized bed gasification furnace 1 from the dispersion plates 53A and 53B through B and B in this order. The inside of the fluidized bed gasification furnace 1 is maintained at a temperature of 450 to 650 ° C. The blowing speed from the dispersion plate 53B is the same as that of the dispersion plate 5
Since it is faster than the blowing speed from 3A, a fluidized bed (particle layer) R1 is formed inside the fluidized bed gasification furnace 1.

The raw material a1 is supplied to the fluidized bed gasification furnace 1 from the raw material supply port 2, and the raw material a1 is rapidly pyrolyzed and gasified by contacting the heated silica sand c1 and the first fluidized gas x1. Combustible gas b1 is generated. The generated combustible gas b1 is sent from the combustible gas outlet 5 to a combustible gas utilization device (not shown) that uses the combustible gas b1 in the subsequent stage. The silica sand c1 discharged from the incombustibles discharge chute 4 is
It is separated from the incombustible material d1 and returned to the fluidized bed gasification furnace 1. The raw material a1 and raw materials a2, a3, and a4 described later are
These include low-grade resources such as waste, RDF, and biomass, and fossil fuels such as coal.

When the fluidized bed gasification furnace 1 is started up, the branch pipe 88B, the header pipe 87, the supply pipes 86A and B, and the fluidized gas supply port 8 are connected from the second fluidized gas generator 90.
The high temperature second fluidizing gas y1 is supplied from the dispersion plates 53A and B to the inside of the fluidized bed gasification furnace 1 through 3A and B in this order.

The fluidized bed gasification furnace 1 is supplied with a large amount of the second fluidized gas y1 as much as possible to raise the temperature of the fluidized bed gasification furnace 1 as quickly as possible to a temperature at which the raw material a1 can be charged. To do. However, in the fluidized bed gasification furnace 1, in the steady gasification operation state in which the raw material a1 is gasified, the fluidization gas amount contains the oxygen amount necessary for maintaining the temperature, and is the amount necessary for an appropriate fluidization state. If there is Therefore, since the supply of the first fluidized gas x1 to the fluidized bed gasification furnace 1 more than necessary lowers the efficiency of the entire process, the supply amount of the first fluidized gas x1 in the steady gasification operation state is The flow rate is smaller than the supply amount of the second fluidizing gas y1 at the time of startup. That is,
The fluidized bed gasification furnace 1 starts up with the fluid blowing nozzle 61.
The blowing amount of the second fluidizing gas y1 from (see FIG. 1) is a large flow rate, and the flow rate of the first fluidizing gas x1 is a small flow rate in the steady gasification operation state. Therefore, since the fluidized bed gasification furnace 1 includes the dispersion nozzle devices 51A and 51B having the fluid blowing nozzles 61 (see FIG. 1), the flow rate blown out from each fluid blowing nozzle 61 is uniform in the steady gasification operation state. It is possible to maintain the property and form an appropriate fluidized bed R1 in the fluidized bed gasification furnace 1 so that the flow velocity of each fluid blowing nozzle 61 does not become excessive during the startup operation. Therefore, in the fluidized bed gasification furnace 1, the start-up time can be shortened.

Next, referring to FIG. 3 and also to FIG. 1 as needed, an integrated gasification furnace 101 of a third embodiment of the present invention in which the dispersion nozzle devices 151A to F are incorporated will be described. FIG. 3 is a block cross-sectional view schematically showing the basic configuration of the integrated gasification furnace 101 for a power generation gas turbine.

The integrated gasification furnace 101 shown in FIG. 3 is equipped with a gasification chamber 102, a char combustion chamber 103, and a heat recovery chamber 104 which are responsible for the three functions of pyrolysis or gasification, char combustion, and heat recovery, respectively. For example, the whole is housed in a furnace body having a cylindrical shape. The integrated gasification furnace 101 further includes a fluidizing gas supply device 191. Dispersion nozzle device 1
51A to 51F have the same configuration as that of the dispersion nozzle device 51 shown in FIG. 1, and include a fluid blowout 61 (see FIG. 1) and the dispersion plate 1.
53A to F and a fluidizing gas supply port 183 as a supply port
A to F are included.

The gasification chamber 102, the char combustion chamber 103, and the heat recovery chamber 104 are divided into partition walls 111, 112, 113, and 11.
It is divided by 4, 115, and a fluidized bed, which is a dense layer containing a fluidized medium, is formed at the bottom of each of them. Each room 10
In order to fluidize the fluidized bed of Nos. 2, 103 and 104, that is, the fluidized bed of the gasification chamber, the fluidized bed of the char combustion chamber, and the fluidized bed of the heat recovery chamber, the first fluidized gas x2 and the second fluidized fluid in the fluidized medium. Dispersion nozzle device 151 that blows in the gasification (hot air) y2
A to F are installed at the bottom of the furnace, which is the bottom of each chamber 102, 103, 104.

The fluidizing gas supply device 191 includes a supply pipe 1
86A-F, header piping 187, and branch piping 188
A, B, a first fluidizing gas generator 189 for generating a first fluidizing gas x2, and a second fluidizing gas generator (hot air generating furnace) 190 for generating a second fluidizing gas y2 are included. The fluidized gas supply device 91 (see FIG. 2) has the same configuration. As shown in FIG. 3, supply piping 186A-F
Are connected to the fluidizing gas supply ports 183A to 183F in which the letters at the end of the reference numerals are the same.

Dispersion plate 15 of dispersion nozzle devices 151A-F
3A to F form the furnace bottom of each chamber 102, 103, 104, and a plurality of dispersion plates 153A to F are arranged in the width direction (the heat recovery chamber 104 has one dispersion plate). 1
In order to change the superficial velocity of each part in 03 and 4, the flow velocity of the first fluidizing gas x2 and the second fluidizing gas y2 blown out through the respective dispersion plates 153A to F of the dispersion nozzle devices 151A to F is changed. I am configuring. Since the superficial velocity is relatively different in each part of the chamber, the flowing medium in each chamber 102, 103, 104 also has a different flow state in each part of the chambers 102, 103, 104, so that an internal swirl flow is formed. In the figure, the size of the white arrows shown in the dispersion nozzle devices 151A to 151F indicates the magnitude of the flow velocity of the first fluidized gas x2 and the second fluidized gas y2 that are blown out. For example, the thick arrow indicated by 103b has a larger flow velocity than the thin arrow indicated by 103a.

Dispersion nozzle devices 151A and 151B are installed below the gasification chamber 102, and the dispersion plates 153A and B form the furnace bottom of the gasification chamber 102. Dispersion nozzle devices 151C, D, E are installed below the char combustion chamber 103, and the dispersion plates 153C, D, E form the furnace bottom of the char combustion chamber 103. However, the dispersion nozzle device 151E is installed in the sedimentation char combustion chamber 105, and the dispersion plate 153E forms the furnace bottom of the sedimentation char combustion chamber 105. A dispersion nozzle device 151F is installed below the heat recovery chamber 104, and the dispersion plate 15
3F forms the furnace bottom of the heat recovery chamber 4. As shown in FIG. 3, the dispersion nozzle device and the dispersion plate correspond to each other in which the letters at the end of the reference numerals are the same.

The gasification chamber 102 and the char combustion chamber 103 are partitioned by a partition wall 111, and the char combustion chamber 103 and the heat recovery chamber 104 are partitioned by a partition wall 112.
02 and the heat recovery chamber 104 are partitioned by a partition wall 113 (note that, in this figure, a cylindrical furnace is developed in a plan view, so the partition wall 111 is separated from the gasification chamber 102 and the char. Not shown between combustion chambers 103).
That is, they are not configured as separate furnaces but are integrally configured as one furnace. Further, a sedimentation char combustion chamber 105 is provided near the surface of the char combustion chamber 103 in contact with the gasification chamber 102 so that the fluidized medium descends. That is, the char combustion chamber 103 is divided into a settling char combustion chamber 105 and a char combustion chamber main body other than the settling char combustion chamber 105. Therefore, a partition wall 114 is provided to partition the sedimentation char combustion chamber 105 from the other part of the char combustion chamber (char combustion chamber main body). The settling char combustion chamber 105 and the other part of the char combustion chamber (char combustion chamber main body) are
Under the same pressure. The settling char combustion chamber 105 and the gasification chamber 102 are separated by a partition wall 115.

Here, the fluidized bed and the interface will be described.
The fluidized bed includes a concentrated layer at a vertically lower portion thereof, which contains a fluidized medium (for example, silica sand) in a fluidized state by the first fluidized gas x2 and the second fluidized gas y2 in a concentrated state, and the concentrated layer. And a large amount of gas coexist in the vertically upper part of the splash zone where the fluid medium is vigorously bounced. 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.

The partition wall 111 between the gasification chamber 102 and the char combustion chamber 103 is almost entirely partitioned from the furnace ceiling 119 to the furnace bottom (perforated plate of the air diffuser), but the lower end is the furnace. There is no opening 121 near the bottom of the furnace without touching the bottom.
Are formed. However, the upper end of the opening 121 does not reach above the interface between the gasification chamber fluidized bed interface and the char combustion chamber fluidized bed interface. More preferably, the upper end of the opening 121 does not reach above the upper surface of the dense layer of the gasification chamber fluidized bed or the upper surface of the dense layer of the char combustion chamber fluidized bed. In other words, it is preferable that the opening 121 is always formed in the dense layer. That is, the gasification chamber 102 and the char combustion chamber 103 at least in the freeboard portion, more specifically above the interface, and more preferably above the upper surface of the dense layer, the partition wall 111 so that there is no gas flow. It will be partitioned by.

Further, the char combustion chamber 103 and the heat recovery chamber 104
The partition wall 112 between is located at the upper end near the interface, that is, above the upper surface of the rich layer, but below the upper surface of the splash zone, and the lower end of the partition wall 112 is near the furnace bottom. Like the partition wall 111, the lower end does not contact the furnace bottom, and an opening 122 is formed near the furnace bottom that does not reach above the upper surface of the rich layer.

A partition wall 113 between the gasification chamber 102 and the heat recovery chamber 104 is completely partitioned from the furnace bottom to the furnace ceiling 119. The partition wall 114 for partitioning the inside of the char combustion chamber 103 to provide the sedimentation char combustion chamber 105 has an upper end near the interface of the fluidized bed and a lower end in contact with the furnace bottom. Partition wall 11
The relationship between the upper end of 4 and the fluidized bed is the same as the relationship between the partition wall 112 and the fluidized bed. The partition wall 115 that separates the settling char combustion chamber 105 and the gasification chamber 102 is similar to the partition wall 111, and partitions almost entirely from the furnace ceiling 119 to the furnace bottom, and the lower end must be in contact with the furnace bottom. However, an opening 125 is formed near the bottom of the furnace, and the upper end of this opening is below the upper surface of the rich layer. That is, the relationship between the opening 125 and the fluidized bed is the same as the relationship between the opening 121 and the fluidized bed.

The raw material a2 charged in the gasification chamber 102 receives heat from the fluidized medium and is thermally decomposed and gasified under pressure.
Typically, the raw material a2 does not burn in the gasification chamber 102,
So-called carbonization is done. The remaining dry-distilled char flows into the char combustion chamber 103 through the opening 121 in the lower part of the partition wall 111 together with the fluidized medium. In this way, the gasification chamber 102
The char introduced from (1) is burned under pressure in the char combustion chamber 103 to heat the fluidized medium. The fluidized medium heated by the combustion heat of the char in the char combustion chamber 103 is the partition wall 11
After flowing over the upper end of 2 into the heat recovery chamber 104 under pressure, the heat is collected by the in-layer heat transfer tube 141 arranged so as to be below the interface in the heat recovery chamber 104, and after being cooled, The char combustion chamber 1 is again passed through the opening 122 at the bottom of the partition wall 112.
It flows into 03. The term “under pressure” means that the pressure is higher than the atmospheric pressure.

Here, the heat recovery chamber 104 is not essential to the integrated gasification furnace 101 of the present invention. That is, the gasification chamber 102
In the case where the amount of char mainly composed of carbon remaining after gasification of the volatile components and the amount of char required to heat the fluid medium in the char combustion chamber 103 are substantially equal to each other, heat is removed from the fluid medium. Heat recovery room 10
4 is unnecessary. If the difference in the amount of the char is small, for example, the gasification temperature in the gasification chamber 102 becomes high, and the amount of CO gas generated in the gasification chamber 102 increases, so that the balance state is maintained. Be done.

However, as shown in the figure, the heat recovery chamber 10
4 is provided, the heat recovery amount in the heat recovery chamber 104 can be adjusted to appropriately adjust the combustion temperature of the char combustion chamber 103 and appropriately maintain the temperature of the fluidized medium.

On the other hand, the fluidized medium heated in the char combustion chamber 103 exceeds the upper end of the partition wall 114 to settle the char combustion chamber 1
05, and then into the gasification chamber 102 through the opening 125 in the lower part of the partition wall 115.

Here, the flow state and movement of the fluid medium between the chambers will be described. In the vicinity of the surface of the gasification chamber 102 that contacts the partition wall 115 between the settling char combustion chamber 105 and the settling char combustion chamber 105, a strong fluidization region 102b in which a stronger fluidized state is maintained compared to the fluidization of the settling char combustion chamber 105. (Dispersion plate 15
It corresponds to 3B). As a whole, it is preferable to change the superficial velocity of the first fluidized gas x2 and the second fluidized gas y2 depending on the location so that the mixed diffusion of the charged raw material a2 and the fluidized medium is promoted. As shown in FIG. 5, a weak fluidization region 102a (corresponding to the dispersion plate 153A) is provided in addition to the strong fluidization region 102b to form a swirling flow.

The char combustion chamber 103 has a weak fluidization region 103a (corresponding to the dispersion plate 153C) in the central portion and a strong fluidization region 103b (corresponding to the dispersion plate 153D) in the peripheral portion, and the fluid medium and the char swirl inside. Forming a stream. Gasification chamber 1
02, strong fluidization region 102b in the char combustion chamber 103, 1
The fluidization speed of 03b is 5 Umf or more, weak fluidization area 102
The fluidization rate of a and 103a is preferably 5 Umf or less, but if a relatively clear difference is provided between the weak fluidization regions 102a and 103a and the strong fluidization region 103b, even if it exceeds this range. There is no particular problem. A strong fluidization region 103b is preferably arranged in a portion of the char combustion chamber 103 in contact with the heat recovery chamber 104 and the settling char combustion chamber 105. In addition, weak fluidization areas 102a, 1
It is preferable to provide a gradient so as to descend from the 03a side to the strong fluidization regions 102b and 103b side (not shown). Here, Umf is the minimum fluidization speed (speed at which fluidization is started) of 1 Umf
It is a unit. That is, 5 Umf is the minimum fluidization speed of 5
Double the speed.

As described above, the fluidization state on the side of the char combustion chamber 103 near the partition wall 112 between the char combustion chamber 103 and the heat recovery chamber 104 is relatively stronger than that on the side of the heat recovery chamber 104. By keeping the state, the fluidized medium flows from the char combustion chamber 103 side to the heat recovery chamber 104 side over the upper end of the partition wall 112 near the interface of the fluidized bed,
The inflowing fluid medium moves downward (toward the furnace bottom) due to a relatively weak fluidized state, that is, a high-density state in the heat recovery chamber 104, and the lower end (opening 1 of the partition wall 112 near the furnace bottom.
22) and the char combustion chamber 1 from the heat recovery chamber 104 side
Move to the 03 side.

Similarly, the fluidized state on the char combustion chamber main body side near the partition wall 114 between the main body of the char combustion chamber 103 and the sedimentation char combustion chamber 105 is more relative to the fluidized state on the side of the sedimentation char combustion chamber 105. By maintaining an extremely strong fluidization state, the fluidized medium moves and flows from the side of the main body of the char combustion chamber 103 to the side of the settled char combustion chamber 105 over the upper end of the partition wall 114 near the interface of the fluidized bed. The fluidized medium that has flowed into the settling char combustion chamber 105 side moves downward (toward the furnace bottom) due to the relatively weak fluidized state in the settling char combustion chamber 105, that is, the high density state, and causes the furnace of the partition wall 115 to move. It moves from the settling char combustion chamber 105 side to the gasification chamber 102 side through (the opening 125 of) the lower end near the bottom. Here, the gasification chamber 102 and the sedimentation char combustion chamber 1
The fluidized state on the gasification chamber 102 side near the partition wall 115 with 05 is kept relatively stronger than the fluidized state on the sedimentation char combustion chamber 105 side. This assists the movement of the fluidized medium from the settling char combustion chamber 105 to the gasification chamber 102 by an attractive action.

Similarly, the gasification chamber 102 and the char combustion chamber 1
The fluidized state on the char combustion chamber 103 side in the vicinity of the partition wall 111 between No. 03 and 03 is kept relatively stronger than the fluidized state on the gasification chamber 102 side. Therefore, the fluidized medium is below the interface of the fluidized bed of the partition wall 111, preferably below the upper surface of the dense layer (submerged in the dense layer).
It flows into the side of the char combustion chamber 103 through the opening 121.

The char combustion chamber 103 and the heat recovery chamber 104 are partitioned by a partition wall 112 having an upper end near the interface height and a lower end submerged in a rich layer, and the char combustion chamber 3 side near the partition wall 112. The fluidized state is maintained 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 112 from the char combustion chamber 103 side to the heat recovery chamber 104 side, and passes through the lower end of the partition wall 112 from the heat recovery chamber 104 side to the char combustion chamber 103 side. Moving.

Further, the char combustion chamber 103 and the gasification chamber 10
2 means that the lower end is partitioned by a partition wall 115 that is submerged in a thick layer, and the char combustion chamber 103 side of the partition wall 115 includes a partition wall 114 and a partition wall 115 whose upper end is near the interface height. Settling char combustion chamber 10 defined by a partition wall
5, the char combustion chamber 103 near the partition wall 114 is provided.
The fluidized state on the main body side is kept stronger than the fluidized state on the settling char combustion chamber 105 side near the partition wall 114. Therefore, the fluidized medium moves over the upper end of the partition wall 114 into the settling char combustion chamber 105 side from the main body side of the char combustion chamber 103. With such a configuration, the fluidized medium flowing into the settling char combustion chamber 105 moves from the settling char combustion chamber 105 to the gasification chamber 102 through the lower end of the partition wall 115 so as to maintain at least mass balance. At this time, the gasification chamber 10 near the partition wall 115
If the fluidized state on the second side is kept stronger than the fluidized state on the side of the settling char combustion chamber 5 near the partition wall 115, the movement of the fluidized medium is promoted by the attracting action.

Further, the gasification chamber 102 and the char combustion chamber 10
3 main body means the second partition wall 11 whose lower end is deeply hidden
It is divided by 1. The fluidized medium that has moved from the settling char combustion chamber 105 to the gasification chamber 102 passes through the lower end of the partition wall 111 and moves to the char combustion chamber 103 so as to maintain the mass balance, but at this time, in the vicinity of the partition wall 111. Of the char combustion chamber 103 side of the partition wall 11
If it is kept stronger than the fluidized state on the gasification chamber 102 side in the vicinity of 1, the fluid medium will not only keep the mass balance as before, but the fluidized medium will not be kept in the char combustion chamber 1 due to the strong fluidized state.
It is attracted to the 03 side and moves.

The heat recovery chamber 104 is fluidized uniformly 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 103 which is in contact with the heat recovery chamber 104 at maximum. Therefore, the superficial velocity of the first fluidized gas x2 in the heat recovery chamber 104 is controlled within the range of 0 to 3 Umf, and the fluidizing medium forms a sedimenting fluidized bed while gently flowing. In addition, here, 0 Umf is a state in which the first fluidizing gas x2 is stopped. With such a state, heat recovery in the heat recovery chamber 104 can be minimized. That is, the heat recovery chamber 104 can arbitrarily adjust the amount of recovered heat in the maximum to minimum range by changing the fluidized state of the fluidized medium. Further, in the heat recovery chamber 104, the fluidization may be uniformly started / stopped or the strength thereof may be adjusted throughout the chamber, but it is also possible to suspend the fluidization of a part of the area and place the other in the fluidized state. However, the strength of the fluidized state in a part of the area may be adjusted.

The most preferable example of the first fluidized gas x2 in the gasification chamber 102 is to increase the pressure of the combustible gas b2 for recycling. In this way, the gas emitted from the gasification chamber 2 is purely the gas generated from the raw material a2, 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 b2 in addition to the oxygen-free gas as necessary. You may make it burn. The first fluidizing gas x2 supplied to the char combustion chamber 103 supplies a gas containing oxygen necessary for char combustion, for example, air, or a mixed gas of oxygen and steam.
Further, the first fluidizing gas x2 supplied to the heat recovery chamber 104 is
Air, steam, combustion exhaust gas, etc. are used.

In the integrated gasification furnace 101 of this embodiment, the fluid blowing nozzle 61 of the dispersion plates 153A to 153F.
The amount of the second fluidized gas y2 blown out during the start-up operation (see FIG. 1) is significantly increased compared to the amount of the first fluidized gas x2 blown out during the normal operation. In this case, the integrated gasification furnace 101 includes the dispersion nozzle device 1
Since 51A to 51F are provided, it is possible to prevent the flow velocity of the second fluidizing gas y2 blown into the fluidized bed R2 from becoming excessive and to secure an appropriate pressure loss in the fluid blow nozzle 61. Become. Furthermore, the first fluidizing gas x
When 2 is being blown, stable blowing from the fluid blowing nozzle 61 can be secured, and uniform blowing can be secured from each of the plurality of fluid blowing nozzles 61. Therefore, a stable fluidized bed R2 is provided in each chamber 102, 1
03, 104 can be formed.

Since the flow velocity of the second fluidizing gas y2 is not excessively increased, the other fluid blowing nozzles 61,
Blast effect does not damage electric heating tubes, hearth refractories, etc. In addition, each room 102, 103, 10
4 High temperature fluid only at startup (second fluidizing gas y2)
Is sent in a larger amount than in steady operation in each room 102, 1
The integrated gasification furnace 101 of the present embodiment is useful in the case where the temperature of 03 and 104 is rapidly raised.

Combustible gas b2 generated in the gasification chamber 102
Is supplied to the topping combustor 154 through the pipe 130, and the combustion gas u2 generated in the char combustion chamber 103 is generated.
Is supplied to the topping combustor 154 via the pipe 131. In the pipe 130, a cyclone separator (dust collector) for removing the combustible gas b2, and in the pipe 131,
A cyclone separator (dust collector) for removing the combustion gas u2 may be provided.

Air or oxygen is supplied to the topping combustor 154, the supplied combustible gas b2 and the supplied combustion gas u2 are mixed, and the mixed gas is burned to generate a high temperature gas r2.
Then, the high temperature gas r2 is supplied to the gas turbine 155, and the gas turbine is driven. Since the generator 157 is connected to the gas turbine 155, the generator 157 generates electric power and the energy is recovered as electric power.

Fluid ejection nozzle 61 of the present embodiment
The integrated gasification furnace 101 equipped with the dispersion nozzle devices 151A to 151F (see FIG. 1) has a fixed orifice 64 (see FIG. 1) according to a case of a small flow rate, that is, a case of blowing out the first fluidized gas x2. ) Pressure loss,
In addition, by determining the flow velocity of the gas discharged from the through holes 63 (see FIG. 1) according to the case of large flow rate, that is, the case of blowing out the second fluidized gas y2, the flow rate in each through hole 63 is uniform in the case of small flow rate. Keeping sex, each room 10
2, 103, 104 are used to form an appropriate fluidized bed so that the flow velocity of the gas discharged from the through hole 63 does not become excessive in the case of a large flow rate, and the fluid discharge nozzle 6
It is possible to avoid damage due to the blasting effect on the parts of the device close to 1.

In the integrated gasification furnace 101, the gasification chamber 10
The raw material a2 to be gasified is charged into 2. Therefore, at the time of start-up, a large amount of hot air (second fluidized gas) y2 is supplied to the gasification chamber 102 from the external hot air generation furnace (second fluidized gas generator) 190, and first, the gasification furnace 102.
The temperature of the gasification chamber 102 as quickly as possible
It is usual to set the temperature at which the raw material a2 can be charged. However, in the gasification chamber 102, the endothermic reaction is central in the steady gasification operation state in which the raw material a2 is gasified.
The fluidization state at 02 is slow. Therefore, in the steady gasification operation state, the supply of the first fluidizing gas x2 to the gasification chamber 102 more than necessary lowers the overall process efficiency, and therefore the flow rate is smaller than the supply amount of the hot air y2 at the time of startup. is there.

That is, in the gasification chamber 102 of the integrated gasification furnace 101, the amount of hot air y2 blown out from the fluid blowing nozzle 61 is large at the time of startup, and in the steady gasification operation state, the first fluidized gas The blowing amount of x2 is a small flow rate. Therefore, in the steady gasification operation state, the uniformity of the flow rate blown out from each fluid blowing nozzle 61 (see FIG. 1) is maintained, an appropriate fluidized bed is formed in each chamber 102, 103, 104, and the startup is performed. It is possible to prevent the flow velocity of each of the fluid blowing nozzles 61 from becoming excessive during operation. Therefore, in the integrated gasification furnace 101, the start-up time can be shortened, and the gas turbine 155 that drives the generator 157 can be started in a short time to obtain electric power.

Next, referring to FIG. 4, and appropriately to FIG. 1, the fourth embodiment of the present invention including the dispersion nozzle devices 251A and 251B.
The fluidized bed catalytic reactor 201 as the fluidized bed reactor of the embodiment will be described. FIG. 4 is a block sectional view schematically showing the basic configuration of the fluidized bed catalytic reactor 201.

The fluidized bed catalytic reactor 201 has the raw material supply port 2
02, the dispersion nozzle devices 251A and 251B, and the gas discharge port 2
05 and a fluidizing gas supply device 291. The dispersion nozzle devices 251A and 251B have the same configuration as the dispersion nozzle device 51 shown in FIG. 1, and include a fluid outlet 61 (see FIG. 1), dispersion plates 253A and B, and a fluidizing gas supply port 283A as a supply port. B is included. Similarly to the dispersion nozzle devices 51A and B (see FIG. 2) forming the bottom of the fluidized bed gasification furnace 1 (see FIG. 2), the dispersion plates 253A and B are the bottoms of the fluidized bed catalytic reactor 201. Is formed. Fluidized bed catalytic reactor 2 of dispersion plates 253A, B
The arrangement in 01 is the dispersion plate 53A in the fluidized bed gasification furnace 1,
B (see FIG. 2). Fluidized bed catalytic reactor 201
The inside is filled with catalyst particles c3, and the catalyst particles c3
Also serves as a fluid medium.

The fluidizing gas supply device 291 is provided in the supply pipe 2
86A, B, header pipe 287, branch pipe 288
It is configured to include A and B, the first fluidized gas generator 289, and the second fluidized gas generator 290, and has the same configuration as the fluidized gas supply device 11 (see FIG. 2).

During a normal reaction, the first fluidizing gas x3 as a fluid from the first fluidizing gas generator 289 is
It is supplied into the fluidized bed gasification furnace 201. Dispersion plate 253
Since the blowing speed of the first fluidizing gas x3 as the fluid from B is higher than the blowing speed from the dispersion plate 253A, the fluidized bed (particle layer) R inside the fluidized bed catalytic reactor 201.
3 is formed.

The raw material supply port 2 is connected to the fluidized bed catalytic reactor 201.
The raw material a3 is supplied from 02, and the raw material a3 comes into contact with the heated catalyst particles c3 and the first fluidized gas x3 to cause a rapid reaction, thereby generating a produced gas b3. The generated gas b3 thus generated is sent from the gas outlet 205 to a generated gas utilization device (not shown) that uses the generated gas b3 in the subsequent stage.

When the catalyst in the fluidized bed catalytic reactor 201 is regenerated, the second fluidized gas y3 for regeneration is supplied from the second fluidized gas generator 290 into the fluidized bed catalytic reactor 201 to form the fluidized bed R3. Formed and regeneration of the catalyst takes place. During catalyst regeneration, an overwhelmingly large amount of the second fluidizing gas y3 for regeneration is supplied to the fluidized bed catalytic reactor 201, the catalyst regeneration is terminated as quickly as possible, and the raw material a3 can be charged. . However, the fluidized bed catalytic reactor 201 is
In the normal reaction in which the reaction is caused in 3, the supply flow rate of the first fluidizing gas x3 is set to an appropriately small value in order to obtain sufficient residence time in the bed in the fluidized bed catalytic reactor 201 and increase the reaction efficiency.

Therefore, the supply of the first fluidizing gas x3 to the fluidized bed catalytic reactor 201 more than necessary lowers the efficiency of the whole process. Therefore, during the normal reaction, the amount of the first fluidizing gas x3 supplied. Is the second fluidizing gas for regeneration (regeneration gas)
The flow rate is smaller than the supply amount of y3. That is, in the fluidized bed catalytic reactor 201, the amount of the second fluidizing gas y3 blown out from the fluid blowing nozzle 61 (see FIG. 1) during catalyst regeneration is a large flow rate, and during normal reaction, the first fluidizing nozzle The flow rate of the gas x3 is a small flow rate. Therefore, the fluidized bed catalytic reactor 201 includes the dispersion nozzle devices 251A and 251B having the fluid ejection nozzle slurries 61 (see FIG. 1).
The uniformity of the flow rate blown out of the fluidized bed is ensured so that an appropriate fluidized bed R3 is formed in the fluidized bed catalytic reactor 201, and the flow velocity of each fluid blowing nozzle 61 does not become excessive during catalyst regeneration. You can Therefore, in the fluidized bed catalytic reactor 201 of this embodiment, the catalyst regeneration time can be shortened.

Next, referring to FIG. 5 and appropriately to FIG. 1, the fifth aspect of the present invention including the dispersion nozzle devices 351A and 351B will be described.
The fluidized bed desulfurization reactor 301 as the fluidized bed reactor of the embodiment will be described. FIG. 5 is a block sectional view schematically showing the basic configuration of the fluidized bed desulfurization reactor 301.

The fluidized bed desulfurization reactor 301 comprises a raw material supply port 302, dispersion nozzle devices 351A and 351B, a combustible gas discharge port 305, and a fluidizing gas supply device 311. The dispersion nozzle devices 351A, B are configured to include a fluid dispersion nozzle 61 (see FIG. 1), dispersion plates 353A, B, and fluidizing gas supply ports 383A, B as supply ports. The fluidizing gas supply device 311 has a supply pipe 38.
6A, B, header piping 387, branch piping 388A,
B, a first fluidizing gas generator 389, and a second fluidizing gas generator 390. Hereinafter, differences from the fluidized bed catalytic reactor 201 of the fourth embodiment will be mainly described.

The raw material supply port 302 supplies the raw material a4 and the limestone e4. The first fluidizing gas x4 as the fluid supplied by the first fluidizing gas generator 389 is the reducing gas supplied during the reducing atmosphere operation which is the normal operation, and is supplied by the second fluidizing gas generator 390. The second fluidizing gas y4 as a fluid is an oxidizing atmosphere gas supplied during the operation in an oxidizing atmosphere.

During the blowing of the first fluidizing gas (reducing gas) x4, that is, during the reducing atmosphere operation, the sulfur content contained in the raw material a4 is removed from the produced gas b4 in the form of CaS, so that the reaction time is sufficient. In order to obtain
The supply flow rate is appropriately reduced in order to prolong the residence time in 01. The second fluidizing gas (oxidizing atmosphere gas) y4 is blown in, that is, the oxidizing atmosphere operation is performed, and the unstable CaS is fixed to CaSO ₄ by oxidation fixing. In this case, the second fluidizing gas (oxidizing atmosphere gas) y4 is blown in, and the fixation to CaSO ₄ is performed in the oxidizing atmosphere gas whose flow rate is overwhelmingly large with respect to the desulfurizing agent. Therefore, the flow rate of the second fluidized gas y4 is usually higher than the flow rate of the first fluidized gas x4 during the reducing atmosphere operation.

Therefore, the fluidized bed desulfurization reactor 301
Includes the dispersion nozzle devices 351A and 351B having the fluid ejection nozzles 61 (see FIG. 1), the uniformity of the flow rate blown out from each fluid ejection nozzle 61 (see FIG. 1) during the normal reducing atmosphere operation. It is possible to keep the fluidized bed type desulfurization reactor 301 to form an appropriate fluidized bed (particle layer) R4 so that the flow velocity of each fluid blowing nozzle 61 does not become excessive during the reducing atmosphere operation. Therefore, in the fluidized bed desulfurization reactor 301 of the present embodiment, it is possible to shorten the fixing time of CaS to CaSO ₄ .

[0070]

As described above, according to the present invention, since the blowing portion and the narrowing portion are provided, it is not the blowing portion in contact with the particle layer, but the narrowing portion arranged upstream of the blowing portion, Even if the flow rate of the blowout is drastically changed, the flow velocity of the blowout flow from the blowout part to the inside of the particle layer does not become excessive, and the proper pressure loss at the fluid blowout nozzle is maintained. Can be secured. Therefore, stable ejection from the fluid ejection nozzle can be ensured. Further, when there are a plurality of fluid ejection nozzles, uniform ejection from each fluid ejection nozzle can be ensured.

[Brief description of drawings]

FIG. 1 is a partial cross-sectional view of a dispersion nozzle device including a fluid ejection nozzle according to a first embodiment of the present invention.

FIG. 2 is a block sectional view schematically showing a basic configuration of a fluidized bed gasification furnace according to a second embodiment of the present invention.

FIG. 3 is a block cross-sectional view schematically showing the basic configuration of an integrated gasification furnace according to a third embodiment of the present invention.

FIG. 4 is a block cross-sectional view schematically showing the basic configuration of a fluidized bed catalytic reactor according to a fourth embodiment of the present invention.

FIG. 5 is a block sectional view schematically showing a basic configuration of a fluidized bed desulfurization reactor according to a fifth embodiment of the present invention.

[Explanation of symbols]

1 Fluidized bed gasification furnace 2 Raw material supply port 4 Incombustible discharge chute 5 Combustible gas outlet 9 First fluidized gas generator 10 Second fluidized gas generator 11 Fluidizing gas supply device 51, 51A, 51B Dispersion nozzle device 52 insertion hole 53, 53A, 53B Dispersion plate 61 Fluid ejection nozzle 62 tubular body 63 through hole 64 fixed orifice 71 Speech bubble a1 raw material b1 Combustible gas R, R1 particle bed (fluidized bed) x Fluidizing gas x1 first fluidized gas y1 Second fluidized gas

   ─────────────────────────────────────────────────── ─── 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 AA06 AE04 AE16 BA03                 4F033 AA13 BA01 BA02 BA04 CA01                       DA02 EA01 GA00 NA01

Claims (3)

[Claims] 1. A fluid blowing nozzle for blowing a fluid into a particle layer; a blowing portion for blowing the fluid to the particle layer, the blowing portion having a first flow resistance to the fluid; And a throttle portion having a second flow resistance that is always larger than the first flow resistance; and a pair of blow-out holes is formed in the blow-out portion. On the other hand, one of the throttle portions is provided; a fluid blowing nozzle. 2. The fluid ejection nozzle according to claim 1, wherein the throttle portion is a fixed orifice. 3. A fluidized bed reactor in which a reaction is carried out in a fluidized particle bed; a fluid outlet nozzle according to claim 1 or 2, and a supply port for supplying the fluid to the fluid outlet nozzle. Provide; fluidized bed reactor.