JP2011106795A - Fluidized bed gasification furnace, fluidized bed gasification system and method of separating agglomeration substance - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To take out and separate agglomeration substances to the outside of a gasification furnace when the agglomeration substances are generated during the gasification of a gasified material by using the fluidized bed gasification furnace including a flowing medium, and to efficiently perform the gasification at a high temperature by preventing a flowing trouble of the flowing medium. <P>SOLUTION: A partition member including gas supply holes supplying gas for making the flowing medium flow is provided in a gasification furnace body, and a partition face of the partition member is formed to be an inclined face. By this, the agglomeration substances are moved to a lower end of the inclined face along the inclined face by gravity action, and a takeout part capable of taking out a taken-out object is provided in a portion corresponding to the lower end of the inclined part so as to remove the agglomeration substances to the outside of the gasification furnace body. <P>COPYRIGHT: (C)2011,JPO&amp;INPIT

Description

  The present invention relates to a fluidized bed gasification furnace, a fluidized bed gasification system, and an agglomerated material separation method.

There is a fluidized bed incinerator used as an incinerator for burning incineration materials such as industrial waste and organic waste for incineration. In this fluidized bed incinerator, a fluidized bed is provided in the lower part of the incinerator body, and the fluidized bed is usually composed of granules of silica sand (main component is silicon dioxide: SiO ₂ ).

  On the other hand, incinerated materials such as industrial waste and organic waste that are incinerated include alkali metals such as sodium and potassium, alkaline earth metals such as calcium and magnesium, and so-called alkaline substances such as salts thereof. There is something that contains a lot. For example, rice straw in plant biomass and chicken manure in animal biomass contain a large amount of the alkaline substance such as potassium.

In the fluidized bed incinerator, the combustion treatment is performed at a considerably high temperature (800 ° C. or higher) in order to increase the gasification efficiency. If the incineration material containing a large amount of the alkaline substance is subjected to the combustion treatment at a considerably high temperature, Potassium glass (K ₂ O · 3SiO ₂ ), soda glass (Na ₂ O · 3SiO ₂ ), etc., which are low melting point compounds by reacting, for example, potassium or sodium with SiO _{2 in} silica sand, contained in the incinerator Generate. And its melting point is potash _{(K 2} O · 3SiO 2) is about 750 ° C., soda glass _{(Na 2} O · 3SiO 2) is about 635 ° C.. The low melting point compound melts at a high temperature of 800 ° C. or higher and adheres to the surface of the silica sand particles as a fluid medium.
As a result, when the particles come into contact with each other at the portion of the low melting point compound adhering to the particle surface in a molten state, the particles of silica sand as a fluidized medium become large particles, Causes so-called agglomeration. And since the agglomeration substance produced | generated by this enlargement phenomenon makes the silica sand which is a fluid medium hard to flow, the problem of the fluid obstacle of a fluid medium generate | occur | produces.

  Therefore, as an example of a technique for preventing the flow failure, there is a method for treating industrial waste including sludge by a fluidized bed incinerator described in JP-A-10-185154 (Patent Document 1). ). In this treatment method, instead of silica sand usually used as a fluidized medium of a fluidized bed, a fluidized bed is formed in the hearth using solid content and / or residue thereof contained in the sludge to be incinerated. Air is supplied to the fluidized bed from below to cause the fluidized bed to flow.

  However, in the method described in Patent Document 1, since the variation in the type and properties of the incinerated material (sludge) is large, the fluidized bed is stabilized using the solid content and / or the residue contained in the sludge. It was not easy and practical to form.

  Another example of the technique for preventing the flow failure is a method for preventing solidification of a fluid medium in a fluidized bed incinerator described in JP-A-11-132426 (Patent Document 2). . This solidification prevention method is a method in which an incinerated material (such as SA resin) is mixed with kaolin clay and burned when the incinerated material is an SA resin (potassium sorbate) or the like that contains a large amount of low melting point substances (for example, alkali metals). By doing so, it is intended that minerals having a high melting point are directly generated by the reaction between the alkali metal and kaolin clay in the material to be incinerated, thereby suppressing the formation of a compound having a low melting point.

  However, in the method described in Patent Document 2, it is not easy to uniformly mix kaolin clay with the material to be incinerated, and it has been difficult to stably advance the formation reaction of the high melting point compound. For this reason, a low-melting-point compound is generated, and the problem of the flow failure may occur.

In addition, since the method described in Patent Document 2 uses silica sand as a fluid medium, the production rate of low melting point compounds (K ₂ O.3SiO ₂ potash glass, etc.) can be reduced by adding kaolin clay, but still Low melting point compounds are always produced. The temperature in the incinerator main body is maintained at a high temperature of 850 to 900 ° C. (paragraph 0045) because it is a furnace intended for incineration. Therefore, the produced low melting point compound is sufficiently melted in the incinerator main body, and the grain size of the silica sand as the fluidized medium is increased from the low melting point compound in the molten state (agglomeration phenomenon). There is a problem that causes

  Therefore, with the methods described in Patent Document 1 and Patent Document 2, it is difficult to completely suppress the generation of an agglomerated substance by agglomeration.

  In the above, the flow failure due to the phenomenon of the fluidized medium becoming large is described as a problem in a fluidized bed incinerator. However, this problem is caused by incomplete combustion of a gasified raw material such as biomass and gasifying it. The same occurs in a fluidized bed gasifier that generates (a mixed gas containing carbon monoxide and hydrogen).

  In addition, although it is not a fluidized bed incinerator, the fluidized-bed separation apparatus described in Unexamined-Japanese-Patent No. 2002-21947 is a technique which separates the thermal decomposition residue at the time of processing by thermally decomposing waste. (Patent Document 3). In this fluidized bed fractionating device, an inclined perforated plate with air ejection holes is provided in the fluidized bed fractionating device, and the pyrolysis residue is fluidized by the jetted air and the fluidized medium, and the pyrolysis carbon of the pyrolysis residue is obtained. It is an apparatus for separating a powder such as a residue and a relatively heavy residue.

  However, in the technique described in Patent Document 3, the relatively heavy residue to be fractionated is rubble such as unsuitable material for pulverization, metal, etc., and is not an agglomeration substance. In the technique described in Patent Document 3, usually, waste is pyrolyzed by heating to about 450 ° C. in a pyrolysis reactor, and a pyrolysis gas and pyrolysis residue generated by the treatment are discharged. After being separated by the above, the pyrolysis residue is passed through a cooling device and then charged into the fluidized bed fractionating device. Therefore, the temperature in the fluidized bed separation apparatus is about 40 to 50 ° C., and does not reach such a high temperature that an agglomeration substance is generated. Therefore, no agglomeration substance is generated.

  In other words, the fluidized bed separation device described in Patent Document 3 is merely a separation device, and is not in an incinerator, so that it does not generate an agglomerated material, and the device itself aims to remove the agglomerated material. Not in. And since it is a separation apparatus, the structure is completely different from a fluidized bed incinerator, for example, in terms of fire resistance and parts used for operation.

JP-A-10-185154 JP-A-11-132426 JP 2002-219417 A

  The present invention has been made in view of the above circumstances, and its purpose is to use a fluidized bed gasification furnace having a fluidized medium for organic waste such as biomass or industrial waste, which is a raw material to be gasified. When the agglomerated material is produced during the gasification process, the agglomerated material is taken out of the gasification furnace and separated to prevent the flow medium from being disturbed, thereby efficiently performing the gasification process at a high temperature. There is in doing so.

  In order to achieve the above object, a fluidized bed gasification furnace according to a first aspect of the present invention includes a gasification furnace main body and a partition member having a gas supply hole for supplying a gas for flowing a fluid medium. A fluidized bed type gasification furnace, wherein a partition surface of the partition member is formed as an inclined surface, and a material to be taken out can be taken out at a position corresponding to a lower end portion of the inclined surface of the gasification furnace body. It has the part.

  According to this embodiment, a sizing phenomenon occurs in a fluidized bed gasification furnace, and the sizing phenomenon (hereinafter referred to as “agglomeration”) generates a sizing agent (hereinafter referred to as “agglomeration substance”). Even in this case, the generated agglomeration material has a particle size larger than that of the fluidized medium, so that it is less likely to float with the same fluidized gas amount, sinks in the fluidized medium, and gathers below the fluidized bed, And since the partition surface of a partition member forms the inclined surface, it moves to the lower end part of an inclined surface along an inclined surface, and is taken out from a gasifier main body from an extraction part. Therefore, the agglomerated material is less in the fluidized bed than in a normal fluidized bed gasification furnace, and has the effect of suppressing the occurrence of fluid failure in the fluidized medium. In addition, even if agglomerated material is generated, it can be automatically taken out of the gasifier body, so even if the gasifier is operated at such a high temperature that agglomerated material is generated, the gasification efficiency is reduced. There is no invitation.

  The fluidized bed type gasification system according to the second aspect of the present invention is a fluidized bed type gasification furnace according to the first aspect, and a to-be-removed material taken out from the takeout part of the gasification furnace. A first separation unit for separation, and a first return means for returning the fluid medium separated by the first separation unit into the fluidized bed gasification furnace are provided.

According to this aspect, the fluidized medium is separated by the first separation unit from the material to be retrieved that has been removed from the extraction unit of the gasification furnace, and the separated fluidized medium is returned to the fluidized bed gasification furnace efficiently. Gasification can be performed.
For example, the fluidized medium taken out from the fluidized bed gasification furnace together with the agglomeration material is separated from the agglomerated material by the first separation unit and returned to the fluidized bed gasification furnace, so that it can be used again as the fluidized medium. Therefore, since it is sufficient to add a small amount without adding the whole amount of the fluid medium that has been taken out and reduced, gasification can be performed efficiently.

  The fluidized bed gasification system according to the third aspect of the present invention is a pulverization process in the fluidized bed gasification system according to the second aspect, wherein the remainder of the fluidized medium separated from the material to be taken out is pulverized. A processing unit, a second separation unit for separating the fluidized medium from the processed product by the pulverizing unit, and a second return unit for returning the fluidized medium separated by the second separation unit into the fluidized bed gasification furnace. These are provided.

  According to this aspect, in the effect of the second aspect, the remaining part from which the fluid medium is separated from the material to be taken out, for example, the agglomeration substance is pulverized by the pulverization processing means, and the fluid medium and the low melting point substance are separated in the second separation part. Since it can be used again as a fluidized medium by separating it into a melt and returning the fluidized medium to the fluidized bed gasifier, it is added to the fluidized medium returned to the fluidized bed gasifier according to the second aspect. Therefore, gasification can be efficiently performed without newly adding a reduced amount of fluidized medium.

  The agglomeration substance separation method according to the fourth aspect of the present invention includes a first step of fluidizing a fluid medium on a partition member by setting the temperature in the fluidized bed gasifier to 635 ° C. or higher, and the partition member The agglomerated material having a large fluidized medium is guided to the lower end of the inclined surface through the inclined surface by the action of gravity, and is separated from the main body of the fluidized bed gasifier. And a second step of taking out.

  According to this aspect, by setting the temperature in the fluidized bed gasifier to 635 ° C. or higher, the gasifier is maintained in a state that does not reduce the efficiency of the gasification reaction in the fluidized bed gasifier. It can be operated. Furthermore, when the temperature is 635 ° C. or higher, the above-described low melting point compound melts and adheres to the surface of the fluidized medium to produce an agglomerated material. It becomes difficult to float with the amount of fluidized gas, and the agglomeration material collects below the fluidized bed, and since the inclined surface is formed on the partition surface of the partition member, it is guided to the lower end of the inclined surface by the action of gravity. It can be automatically removed from the fluidized bed gasifier. Therefore, it has the effect that the flow obstacle of the fluid medium in a fluid bed can be prevented.

  The agglomeration substance separation method according to the fifth aspect of the present invention is the agglomeration substance separation method according to the fourth aspect, wherein the fluidized medium is separated from the material to be taken out together with the agglomeration substance. And a third step of returning to the fluidized bed gasifier.

  According to this aspect, in addition to the effect of the fourth aspect, the effect of the third aspect is also provided.

1 is a schematic view of a fluidized bed gasifier according to the present invention. It is the enlarged view of the partition member periphery part of the fluidized bed type gasification furnace which concerns on this invention, and the partially expanded view of a partition member. It is a schematic structure figure concerning a 1st embodiment of a fluid bed type gasification system concerning the present invention. It is a schematic block diagram which concerns on 2nd Embodiment of the fluidized bed type gasification system which concerns on this invention. It is an enlarged view of an agglomeration substance.

  Hereinafter, embodiments of a fluidized bed gasification furnace, a fluidized bed gasification system, and an agglomeration substance separation method using them will be described with reference to the drawings. In addition, this invention is not limited to the following embodiment.

FIG. 1 is a schematic view of a fluidized bed gasifier according to the present invention.
The fluidized bed gasifier 1 includes a gasifier main body 15 which is a vertical type and has a space inside. The freeboard portion 2 is formed in the upper part of the gasifier main body 15, and the fluidized medium 3 'is formed in the lower part. A fluidized bed 3 is provided. Furthermore, three divided wind boxes 41, 42, 43 are provided in the lower part of the fluidized bed 3, and a valve for supplying a gas for flowing the fluid medium 3 ′ from the gas supply device 11 to each window box. Gas supply pipes 51, 52, 53 provided with b are connected.

  The fluidized bed 3 and the wind boxes 41, 42, 43 are partitioned by the partition member 6, the partition surface 61 of the partition member 6 is formed as an inclined surface, and the lower end portion X of the inclined surface is a take-out portion for taking out the medium to be taken out. Y is connected. By adopting such a structure, for example, the relatively heavy agglomeration material A that is generated in the fluidized bed, which is a medium to be taken out, is moved along the inclined surface by the action of gravity, and the lower end of the inclined surface. It can be taken out to the take-out part Y through the part X and taken out of the fluidized bed gasifier 1.

  A gas supply hole 62 is provided in the partition member 6, and the gas supplied from the gas supply pipes 51, 52, 53 into the wind box 41, 42, 43 is sent to the fluidized bed 3 through the gas supply hole 62. Has been. The gas sent to the fluidized bed 3 causes the fluidized medium 3 ′ to flow (float), and the gasified raw material M introduced into the gasification furnace main body 15 from the gasified raw material supply device 7 in the fluidized bed 3. Used for incomplete combustion to produce synthesis gas.

  As described above, the gas supplied from the gas supply pipes 51, 52, 53 plays the role of fluidizing gas for flowing the fluidized medium 3 ′ and the role for incomplete combustion of the gasified raw material M. Generally, air is used. However, the substance is not particularly limited to air as long as it has an oxidizing action, and may be, for example, water vapor, oxygen, or oxygen-enriched air.

  As shown in FIG. 2A, which is an enlarged view of the periphery of the partition member 6, the structure of the partition member 6 is a louver R having a portion R ′ whose tip is folded back so as to cover the gas supply hole 62 described above. A plurality of louver structures may be provided on the partition surface 61. By adopting such a structure, when the operation of the fluidized bed gasification furnace 1 is stopped, as shown in FIG. 2B, which is a partially enlarged view of the partition member 6, the louver R and its tip portion The portion of the portion R ′ that is folded back serves as an eaves that covers the gas supply hole 62, so that the flowing medium 3 ′ does not fall into the wind boxes 41, 42, 43. Yes.

Next, as an example of the fluidized medium 3 ′ constituting the fluidized bed 3, silica sand mainly composed of silicon dioxide can be cited, but a mixture of silica sand and other substances may be used. For example, a mixture containing alumina that reacts with an alkali substance in the gasification raw material M to form a high melting point compound may be used, and further, a mixture with silica sand, alumina, and other substances may be used.
In addition, although the average particle diameter of the silica sand of the fluid medium 3 ′ is usually about 100 to 750 microns, it is not limited to this.

  Further, the gas (oxidant) is supplied to the fluidized bed 3 to maintain the fluidized bed 3 in a fluid state, that is, the fluidized gas velocity (Uf) and the gas (oxidant) are supplied to the fluidized bed 3. Subsequently, the ratio of the speed at which the fluidized medium 3 ′ starts to flow, that is, the ratio of the fluidization start speed (Umf), is set to a predetermined value in accordance with the operation state of the gasification furnace main body 15, whereby the fluidized bed 3 The fluid medium 3 ′ can be brought into an appropriate flow (floating) state. The gas (oxidant) supply speed (fluidization gas speed Uf) to the fluidized bed 3 is measured by the flow meter F with respect to the flow rate of the gas (oxidizer) supplied to the fluidized bed 3, and the value is the gas supply device 11. It is appropriately controlled by being sent to a control unit provided inside.

  The gasified raw material M is directly supplied to the fluidized bed 3 by the gasified raw material supply device 7 provided on the side surface of the fluidized bed 3, and is incompletely combusted by the flowing fluidized medium 3 '. Since the fluidized medium 3 ′ in the fluidized bed 3 and the material to be gasified are brought into contact with each other immediately after being introduced and incompletely combusted by introducing them directly into the fluidized bed without introducing them from the top. I can do it. In addition, a raw material inlet may be provided in the upper part of the fluidized bed gasification furnace 1 as in the past, and the gasified raw material may be supplied from the upper part of the fluidized bed gasification furnace.

  It is ideal that the fluidized medium 3 ′ is not taken out from the fluidized bed gasifier 1, but the agglomeration substance A is taken out of the fluidized bed gasifier 1 by using the action of gravity. Therefore, it is taken out of the fluidized bed gasifier 1 together with the agglomeration substance A. Therefore, in the fluidized bed gasification furnace 1, the amount of both the amount of the fluid medium that constitutes the agglomeration substance A (described later) and at least the part that is removed from the fluidized bed type gasification furnace 1 together with the agglomeration substance A. Since 3 ′ decreases, the decreased amount can be appropriately replenished from the replenishment fluid medium supply device 8.

  The temperature of the fluidized bed 3 is preferably set to 635 to 900 ° C. A more preferable range is 650 to 750 ° C. When the temperature of the fluidized bed is lower than 635 ° C., the gasification reaction in the fluidized bed gasification furnace is lowered and the gasification efficiency is deteriorated.

  On the other hand, if it is 635 degreeC or more, the low melting-point compound mentioned above will melt | dissolve and an agglomeration substance will be produced | generated by this. However, in the fluidized bed gasification furnace according to the present invention, the agglomeration material is formed on the partition surface 61 of the partition member 6, so that the inclined surface is formed to the lower end X of the inclined surface by the action of gravity. It can be taken out from the fluidized bed gasifier at the lead-out part Y. As a result, it is possible to prevent the flow failure of the flow medium 3 '. That is, the fluidized bed gasification furnace 1 according to the present invention can be operated without lowering the gasification efficiency, that is, with the temperature of the gasification furnace main body 15 being high, and the flow obstacle of the fluidized medium 3 ′. Can be prevented.

  The temperature in the fluidized bed 3 is measured by a thermocouple 32 provided in the fluidized bed 3 and transmitted to the temperature control unit 71. The temperature control unit 71 refers to the measurement value measured by the thermocouple 31 and sends an electric signal to the gasification raw material supply device 7 to adjust the supply of the gasification raw material M to the fluidized bed 3. The temperature of the fluidized bed 3 is controlled so that the temperature of the fluidized bed 3 in the embodiment of the present invention is maintained at a set temperature (650 to 750 ° C.) with high gasification efficiency.

Next, temperature control of the fluidized bed 3 will be described in detail.
First, when the operation of the fluidized bed gasifier 1 is started, an oxidant (for example, air) as a fluidizing gas is supplied from the gas supply device 11 through the gas supply pipes 51, 52, 53 to the wind boxes 41, 42, The fluidized medium 3 ′ is supplied to the fluidized bed 3 through the gas supply holes 62, and the fluidized medium 3 ′ is heated (floated) while the fluidized medium 3 ′ is heated (floating), and the fluidized medium 3 ′ is heated (air ratio is about 1).

  Next, when the temperature in the fluidized bed 3 measured by the thermocouple 31 reaches a predetermined temperature, an electric signal is sent from the temperature control unit 71 to the gasified raw material device 7 to send the gasified raw material M to the fluidized bed 3. (Air ratio is adjusted to about 0.3 to 0.6). Then, the gasified raw material M is incompletely combusted by the fluidized medium 3 ′, and the temperature of the fluidized medium 3 ′ itself, that is, the temperature in the fluidized bed 3 by the heat of partial oxidation (carbon monoxide generation) generated at that time. Is maintained. In addition, when the temperature in the fluidized bed 3 measured by the thermocouple 31 is higher than a predetermined temperature and is likely to be overheated, an electric signal is sent from the temperature control unit 71 to the gasification raw material device 7. By reducing the input amount of the gasified raw material M into the fluidized bed 3, it is possible to suppress overheating.

  Finally, when the operation of the fluidized bed gasification furnace 1 is stopped, the supply of the gasified raw material M is stopped. However, the supply of the oxidizing agent that is the fluidizing gas is continued for a while. As a result, the temperature in the fluidized bed 3 is lowered and the agglomerated substance A remaining in the fluidized bed 3 is moved to the lower end X of the inclined surface along the inclined surface formed on the partition surface 61 of the partition member 6. And take it out of the fluidized bed gasifier from the connected take-out part Y.

  In addition, when there are many gasification raw materials M thrown in in the fluidized bed 3, gas (oxidant) is supplied using the gas secondary blowing inlet 12 provided in the upper part of the temperature rising burner 10. FIG. To do. If a large amount of oxidant as fluidizing gas is supplied from the gas supply device 11 when there are many gasified raw materials M, that is, if the flow rate of the oxidant is increased, the fluidized medium 3 ′ will float too much upward, and the efficiency The state that cannot be gasified well occurs. Therefore, in order not to cause such a state, the flow rate of the oxidant supplied from the gas supply device 11 is suppressed to some extent, and the reduced amount of gas (oxidant) is supplied using the gas secondary blowing port 12. It is supposed to be.

  The gasification raw material M used in the present invention is a so-called industrial waste or organic waste. Examples of industrial waste include metals and plastics. Organic waste includes biomass such as rice straw, wheat straw, rice husk, bamboo, straw, palm palm empty fruit bunch, palm palm trunk, herbaceous biomass such as sugarcane-derived waste material such as bagasse, and the remainder of sawmill , Thinned wood (cedar, pine, firewood, lawan, beech, rubber, figs, etc.), roadside tree pruning wood, building waste, waste power poles, bark, dam driftwood, etc. And other biomass derived from livestock, and fermentation residue, food residue, black liquor, seaweed and the like.

Next, the fluidized bed gasification system and the agglomerated material separation method according to the present invention will be described with reference to FIGS.
FIG. 3 shows a first embodiment of a fluidized bed gasification system according to the present invention.
In this embodiment, the material to be taken out (fluid medium 3 ′, agglomeration substance A) taken out from the fluidized bed gasification furnace 1 according to the present invention is agglomerated with the fluid medium 3 ′ by the first separation unit 100. The material A is separated, the fluidized medium 3 ′ is returned to the fluidized bed gasification furnace 1 through the first return means 110, and the agglomerated material A is discarded.

  The to-be-removed thing which moved to the extraction part Y, in this aspect, the fluidized medium 3 ′ and the agglomeration substance A are extracted from the fluidized bed gasification furnace 1 by the fluidized medium extraction device 9 provided downstream of the extraction part Y. Then, it is sent to the first separation unit 100 where it is separated into the fluid medium 3 ′ and the agglomeration substance A.

The separated fluid medium 3 ′ is sent to the storage portion 81 constituting a part thereof via the return line 120 of the first return means 110, from which it also constitutes a part of the first return means 110. It is sent to the supplementary fluid medium supply device 8 and returned to the fluidized bed gasifier 1. Thus, once again using the fluidized medium 3 ′ taken out from the fluidized bed gasification furnace 1, the amount of the fluidized medium 3 ′ to be newly used can be saved. The separated fluid medium 3 ′ may be sent directly to the supplementary fluid medium supply device 8 without going through the storage unit 81. A conveyor or the like can be used as a device for feeding the separated fluid medium 3 ′ to the storage unit 81 or the supplementary fluid medium supply device 8.
On the other hand, the agglomerated substance A separated from the fluid medium 3 ′ is discarded.

  Here, as the first separation unit, a known device or the like can be used as long as it can separate the fluid medium 3 ′ from the agglomeration substance. For example, a vibration sieve, a trommel (rotary sieve), an inclined screen, etc. are mentioned. The agglomeration substance A has an average particle diameter of 5 to 20 mm (some of which are larger), and is considerably larger than the average particle diameter of the silica sand used as one embodiment of the fluid medium 3 ′. When the silica sand is used, the fluidized medium 3 ′ and the agglomerated material A can be separated almost completely in the first separation unit 100, and the fluidized medium 3 ′ returned to the fluidized bed gasification furnace 1 is used as the fluidized medium 3 ′. Can be used as it is without impurities.

FIG. 4 shows a second embodiment of the fluidized bed gasification system according to the present invention.
In the description of this aspect, the description of the same part as the first embodiment is omitted, and the characteristic part of this aspect will be described.
Here, the agglomeration substance A will be described with reference to FIG. As described above, since the fluidized bed gasification furnace 1 according to the present invention is operated at a high temperature (about 635 ° C. or higher, preferably 650 ° C. or higher), a melt B in which a low melting point compound is dissolved is generated.

FIG. 5 shows an enlarged view of the agglomeration substance A. The agglomeration substance A is composed of the fluid medium 3 ′ and the melt B, and the fluid medium is formed by the melt B adhering to the surface of the fluid medium 3 ′. 3 ′ are bonded together to produce a large particle size product, that is, an agglomerated material.
In this aspect, the agglomerated material separated by the first separation unit in the first embodiment is pulverized by the pulverization processing means 230, and the pulverized product is separated into the moving medium 3 ′ and the melt B by the second separation unit 200. The separated fluid medium 3 ′ is returned to the fluidized bed gasifier 1 through the return line 210 of the second return means 210.

  In the pulverizing means 230, pulverization is performed such that the melt B adhering to the fluid medium 3 ′ is removed from the agglomerated material, and the pulverized material is separated by the second separation unit 200 into the fluid medium 3 ′, the melt B, and the like. To separate. Then, the separated fluid medium 3 ′ is sent to the storage portion 81 (common to the first return means) that constitutes a part thereof through the second return means 210, and forms a part of the second return means 210 therefrom. To the replenishing fluid medium supply device 8 (common with the first return means) and returned to the fluidized bed gasifier 1.

  In this way, the fluidized medium 3 ′ separated from the agglomerated material A from the agglomerated material A by the second separation unit 200 is returned to the fluidized bed gasification furnace 1, and separated from the agglomerated material A by the first separation unit 100. By combining with the fluidized medium 3 ′ returned to the fluidized bed gasifier 1 by the first return means 110, it is possible to reduce the loss of the fluidized medium 3 ′ as much as possible. As a result, the amount of the fluidized medium 3 ′ at the initial stage of the operation of the fluidized bed gasifier 1 can be secured, and the amount of the fluidized medium 3 ′ to be newly added can be reduced as much as possible. Can improve the operating efficiency.

The separated fluid medium 3 ′ may be sent directly to the supplementary fluid medium supply device 8 without going through the storage unit 81. The apparatus that feeds the separated fluid medium 3 ′ to the storage unit 81 or the replenishment fluid medium supply device 8 is the same as the first aspect in that a conveyor, an air current transporter, or the like can be used.
On the other hand, the melt B separated from the fluid medium 3 ′ is discarded.

  The synthesis gas produced by using the present invention is collected by the production gas collector 14 through the production gas outlet 13 and then purified and used for synthesis of useful substances such as ethanol, methanol, mixed alcohol and the like. It is done.

  As described above, according to the present invention, when the agglomerated material is generated when the gasified raw material is gasified using a fluidized bed gasification furnace having a fluidized medium, the agglomerated material is By taking it out of the gasification furnace and separating it to prevent the flow medium from being obstructed, gasification can be efficiently performed at a high temperature.

DESCRIPTION OF SYMBOLS 1 Fluidized bed type gasification furnace 2 Free board 3 Fluidized bed 3 'Fluidized medium 41, 42, 43 Wind box 51, 52, 53 Gas supply pipe 6 Partition member 61 Partition surface 62 Gas supply hole 7 Gasification raw material supply apparatus 8 Fluid supply device for replenishment 81 Reservoir 9 Extraction device for agglomerates 10 Temperature rising burner 11 Gas supply device 12 Gas secondary inlet 13 Generated gas outlet 14 Generated gas collector 15 Gasification furnace main body 100 First separation unit DESCRIPTION OF SYMBOLS 110 1st return means 120 Return line of 1st return means 200 2nd separation part 210 2nd return means 220 Return line of 2nd return means 230 Crushing process means A Agglomerated substance B Melt X Lower end of inclined surface Y Extraction partValve

Claims (6)

A gasifier body,
A fluidized bed type gasification furnace provided with a partition member having a gas supply hole for supplying a gas for flowing a fluid medium,
The partition surface of the partition member is formed as an inclined surface,
A fluidized bed type gasification furnace comprising a takeout part capable of taking out an object to be taken out at a position corresponding to a lower end part of the inclined surface of the gasification furnace main body. A fluidized bed gasifier as claimed in claim 1;
A first separation unit for separating a fluid medium from an object to be taken out from the take-out part of the gasification furnace;
A fluidized bed type gasification system comprising: a first return means for returning the fluidized medium separated by the first separation unit into the fluidized bed type gasification furnace. In the fluidized bed gasification system according to claim 2, pulverization processing means for pulverizing the remaining portion from which the fluidized medium is separated from the material to be taken out;
A second separation unit for separating the fluid medium from the processed product by the pulverization means;
A fluidized bed type gasification system comprising: a second return means for returning the fluidized medium separated by the second separation unit into the fluidized bed type gasification furnace. A first step of fluidizing the fluid medium on the partition member by setting the temperature in the fluidized bed gasification furnace to 635 ° C. or higher;
A partition surface of the partition member is formed into an inclined surface, and the agglomerated material in which the fluidized medium is agglomerated is guided to the lower end portion of the inclined surface through the inclined surface by the action of gravity, and the fluidized bed gasifier And a second step of taking the substance out of the main body.   5. The agglomeration material separation method according to claim 4, wherein the fluidized medium is separated from a material to be taken out that is taken out together with the agglomeration material, and is returned to the fluidized bed gasification furnace. A method for separating an agglomeration substance, comprising: In the agglomeration substance separation method according to claim 5, a fourth step of pulverizing the remaining portion from which the fluid medium is separated from the material to be taken out;
A fifth step of separating the fluid medium from the processed product of the fourth step;
And a sixth step of returning the fluid medium separated in the fifth step into the fluidized bed gasification furnace.

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