JP2007507555A - Gasification method and apparatus - Google Patents

Abstract

The gasification method is used for gasifying raw materials such as biomass to generate combustible gas with high efficiency and low cost. In the gasification method, the raw material is pretreated in a pretreatment step, and the pretreated raw material is gasified in a gasification chamber to generate a combustible gas and a residue. The pyrolysis residue generated in the gasification chamber (4-1) is combusted in the combustion chamber (4-2) to generate combustion gas (107). The generated combustion gas is supplied to the pretreatment process and volatilized. A part of the components is separated from the raw material.

Description

  The present invention relates to a gasification method and apparatus for generating a combustible gas with high efficiency and low cost by gasifying a raw material such as biomass.

  There is a demand for gasification of raw materials such as biomass to generate combustible gas with high utility value at high efficiency and low cost. In order to recover energy from a low calorific value raw material such as biomass with high efficiency, it is important to provide a drying step and lower the water content of the low calorific value raw material through the drying step to increase the low calorific value. A material dryer used in such a drying process requires a large amount of heat, and conventionally, a fossil fuel such as heavy oil or kerosene is burned, and the moisture contained in the low heating value raw material is evaporated by the combustion heat. It was mainstream.

The method of burning low-calorific value raw materials by burning fossil fuel as described above is not only expensive to run, but also emits carbon dioxide (CO ₂ ) by burning fossil fuels such as heavy oil and kerosene. There are also problems such as global warming caused by

  This invention is made | formed in view of the above-mentioned point, and it aims at providing the gasification method and apparatus which produce | generate a combustible gas from raw materials, such as biomass, with high efficiency and low cost.

  In order to achieve the above object, according to the first aspect of the present invention, a raw material pretreatment step and a gasification step in which a pretreated raw material is gasified to produce a combustible gas and a residue in a gasification chamber. And a combustion step of burning residue in the combustion chamber to generate combustion gas, and a supply step of supplying the combustion gas to the pretreatment step and separating a part of volatile matter from the raw material. Provide a method

  By supplying the raw material such as biomass to the gasification step after pretreatment, the raw material is gasified by increasing the calorific value of the raw material, so that a combustible gas (generated gas) can be obtained efficiently. Further, by removing harmful volatile elements in the raw material by pretreatment of the raw material and then sending the raw material to the gasification step, it is possible to avoid mixing harmful substances in the product gas (combustible gas). For example, arsenic can be cited as a harmful substance that is removed in the pretreatment process.

  In a preferred embodiment of the present invention, the gasification method includes a cooling step of cooling the gaseous substance discharged from the pretreatment step and recovering an arsenic compound and / or a wood vinegar component.

  In order to achieve the above object, according to the second aspect of the present invention, the raw material is dried by a drying device, the dried raw material is gasified in a gasification chamber to produce a combustible gas and a residue, and the residue in the combustion chamber The gasification method is characterized in that combustion gas is generated to generate combustion gas, and the combustion gas is supplied to the drying device to dry the raw material.

  By supplying the low calorific value raw material dried by the raw material dryer to the gasification chamber, the water contained in the low calorific value raw material is evaporated, and most of the hydrogen component is generated as a volatile component. Since it is discharged from the gasification chamber, the combustion gas discharged from the combustion chamber has a drying capacity equivalent to a drying gas obtained by diluting a gas obtained by burning high-grade hydrogen-containing fuel with a large amount of air. . Therefore, by supplying the combustion gas discharged from the combustion chamber to the raw material dryer as a drying gas, a low calorific value raw material such as biomass, municipal solid waste, or organic sludge can be efficiently dried.

  Further, when a raw material having a high water content is gasified in a gasification furnace, a fluidized bed gasification furnace (for example, an internal circulation type fluidized bed gasification furnace) having a combustion chamber that generates a combustible gas with high thermal efficiency. However, cold gas efficiency is reduced. That is, since the rate of burning the raw material increases, the amount of combustion gas per unit raw material discharged from the combustion chamber increases, and the drying capacity in the raw material dryer also increases. As a result, the moisture content of the raw material before being supplied to the gasification chamber can always be stabilized, and the amount of generated gas per unit raw material can be stabilized.

  Also, by using the sensible heat of combustion gas to dry raw materials with low calorific value, not only can the efficiency of cold gas be improved and the energy recovery efficiency can be improved, but it is also necessary to recover heat and recover power using a boiler. This eliminates the need to reduce equipment costs and recover energy with high efficiency and low cost.

  In a preferred embodiment of the present invention, the gasification method is further characterized in that the gaseous substance discharged from the drying apparatus is cooled to recover an essential oil component and / or a wood vinegar component.

  Since the biomass material contains essential oil components and wood vinegar components, when introducing the combustion gas into the material dryer to dry the biomass material, the combustion gas is adjusted to an appropriate temperature, and the essential oil component in the biomass material And wood vinegar components can be selectively extracted into the combustion gas. The extracted essential oil component and wood vinegar component can be easily condensed and recovered by cooling the combustion gas obtained by drying the raw material.

  In a preferred aspect of the present invention, the gasification method is further characterized in that after recovering heat from the combustion gas discharged from the combustion chamber, the combustion gas is supplied to the drying device.

  In a preferred embodiment of the present invention, the gasification chamber and the combustion chamber are provided in a fluidized bed gasification furnace so that a fluidized medium can circulate between the gasification chamber and the combustion chamber. It is characterized by being.

  In a preferred aspect of the present invention, the gasification method includes at least one fluidized medium settling chamber that sinks the fluidized medium and sends the fluidized medium to at least one of the gasified chamber and the combustion chamber. .

  In order to achieve the above object, according to the third aspect of the present invention, a pretreatment chamber for pretreating the raw material, a gasification chamber for gasifying the pretreated raw material to generate a combustible gas and a residue, And a combustion chamber that burns the residue and generates combustion gas, and a part of the volatile matter is separated from the raw material by supplying the combustion gas from the combustion chamber to the pretreatment chamber. A device is provided.

  As described above, with such a configuration, the low calorific value raw material is dried and pretreated and supplied to the pyrolysis gasification step, so that the product gas can be obtained with high efficiency, and harmful substances are produced by the product gas. Is not mixed in. Furthermore, the heat generated by the combustion of the pyrolysis residue is supplied by the fluid medium moving from the combustion chamber to the pretreatment chamber and the combustible gas supplied to the pretreatment chamber, so that the combustion heat is efficient for drying and pretreatment. Can be used.

  In order to achieve the above object, according to a fourth aspect of the present invention, a drying apparatus for drying a raw material, a gasification chamber for gasifying the dried raw material to generate a combustible gas and a residue, and burning the residue And a combustion chamber for generating combustion gas, wherein the raw material is dried in the drying device by supplying combustion gas from the combustion chamber to the drying device.

  As described above, the combustion gas burned in the combustion chamber of the internal circulation fluidized bed gasifier is obtained by diluting a gas obtained by burning high-grade hydrogen-containing fuel such as kerosene with a large amount of air. Has the same drying capacity as gas. Therefore, by recovering heat from the combustion gas and supplying this combustion gas as a drying gas to the raw material dryer, the low heating value raw material can be efficiently dried.

  Further, in the case of the internal circulation type fluidized bed gasification furnace, as described above, since the ratio of burning the raw material increases, the amount of combustion gas discharged from the combustion chamber increases and the drying capacity in the raw material dryer also increases. . As a result, the moisture content of the raw material before being supplied to the gasification chamber can always be stabilized, and the amount of generated gas per unit raw material can be stabilized.

  Also, by using the sensible heat of combustion gas to dry raw materials with low calorific value, not only can the efficiency of cold gas be improved and the energy recovery efficiency can be improved, but it is also necessary to recover heat and recover power using a boiler. This eliminates the need to reduce equipment costs and recover energy with high efficiency and low cost.

  In a preferred aspect of the present invention, the gasification method further includes a cooling device for cooling the gaseous substance discharged from the drying chamber and recovering the essential oil component and / or the wood vinegar component.

  Biomass raw material, which is one of low calorific value raw materials, contains an essential oil component and a wood vinegar component. The essential oil component and the wood vinegar component in the biomass raw material are extracted into the gas for drying in the drying process, and the extracted essential oil component and the wood vinegar component are easily condensed and recovered by cooling the combustion gas that dried the raw material. Can do.

  Since the recovered essential oil component and wood vinegar component are relatively expensive and can be sold, significant improvements are expected in the profitability of the product gas from biomass resources and energy recovery business.

  The basic concept and embodiment of the present invention will be described below with reference to FIGS. The same or corresponding parts are denoted by the same or corresponding reference numerals in all drawings, and redundant description is omitted.

  FIG. 1 is a block diagram showing the basic concept of the gasification method and apparatus of the present invention. As shown in FIG. 1, the raw material 100 is pre-dried in an apparatus for the drying / pre-treatment process DP. In the present invention, the pretreatment means that the raw material is heat-treated at a low temperature in order to remove harmful compounds such as an arsenic compound before the raw material is supplied to the gasification chamber. The dried / pretreated raw material is supplied to an apparatus for the pyrolysis / gasification step GP, and is pyrolyzed / gasified in the pyrolysis / gasification step GP, thereby generating a product gas (combustible gas) 101. The pyrolysis residue (mainly containing carbon) generated in the pyrolysis and gasification step GP is supplied to an apparatus for the pyrolysis residue combustion step CP and burned in the pyrolysis residue combustion step CP. Is obtained. By drying and pretreating the low calorific value raw material 100 such as biomass, municipal solid waste, or organic sludge and supplying it to the pyrolysis / gasification process GP, the raw material 100 is heated by increasing the calorific value of the raw material. Since it is decomposed and gasified, a combustible gas (product gas) can be obtained efficiently. In addition, after removing harmful volatile elements such as arsenic, mercury, or halogen in the raw material by pre-treatment of the raw material, the raw material is sent to an apparatus for the pyrolysis / gasification process GP to produce a product gas (product gas) ) It can be avoided that harmful substances such as arsenic compounds are mixed in. For example, arsenic is mentioned as a harmful substance removed by pretreatment, that is, heat treatment by introducing high-temperature combustion gas. When wood such as construction waste is coated with arsenic compounds such as CCA (copper chromium arsenic) for the purpose of preserving and preventing ants, arsenic volatilizes in the pyrolysis and gasification process GP and the product gas (product) Gas), arsenic is mixed into the product gas. Since arsenic compounds, particularly arsenous acid, are extremely toxic, it is necessary to prevent arsenic compounds from being mixed into the product gas regardless of the use of the product gas. This is because changing the mixed product gas to a harmless product gas is relatively more difficult due to technical difficulties and cost disadvantages. In the present invention, by using the sensible heat of the combustion gas generated in the pyrolysis residue combustion process CP as the heat required in the drying / pretreatment process DP, the calorific value of the raw material without using external fossil fuel such as heavy oil or coal Since a part of is used for drying the raw material, the energy efficiency in product gas production can be increased. The gas 115 generated in the drying / pretreatment process DP is cooled in the cooling process 15 to recover the essential oil component and / or the vinegar component and / or arsenic and other harmful substances 111, and the combustion gas is discharged outside the system as the exhaust gas 112. Is done.

In FIG. 1, the drying process and the pretreatment process are collectively described as one drying / pretreatment process, but the drying process and the pretreatment process may be separated as described later.
The raw material is dried at a temperature of 100 to 280 ° C, preferably 120 to 150 ° C. This is because a temperature of 100 ° C. or higher is required to evaporate the water in the raw material, and the drying time becomes shorter as the drying temperature is higher. However, if the temperature exceeds 280 ° C., thermal decomposition of the raw material starts. The drying temperature should be lower than 280 ° C. In addition, although the essential oil component and the wood vinegar component are volatilized in the drying step, the drying step is preferably performed at a temperature of about 150 ° C. or lower in order to selectively extract these components.

  In order to recover arsenic from CCA-treated construction waste and the like, the pretreatment step is performed at 135 to 280 ° C, preferably 150 to 200 ° C. The volatilization temperature of arsenic is 135 ° C. or higher, and if it exceeds 280 ° C., thermal decomposition of the raw material starts, so the pretreatment step is preferably performed at a temperature between 135 ° C. and 280 ° C. Since arsenic release occurs remarkably at a temperature of 150 to 200 ° C., it is more preferable to use this temperature range.

  Although the drying process and the pretreatment process may be performed in the same raw material dryer, the drying process and the pretreatment process can be performed independently by adjusting the operation temperature as described above. By carrying out the drying process and the pretreatment process independently, it is possible to avoid harmful volatile components from being mixed into the essential oil component and the wood vinegar component, especially when the construction waste material subjected to CCA treatment is used as a raw material. It is also possible to recover the pyroligneous acid solution at a low temperature drying step of 120 to 150 ° C. and volatilize arsenic at a high temperature of 150 to 200 ° C. to recover arsenic.

  The raw material dried and pretreated in the drying / pretreatment process DP is sent to the pyrolysis gasification process GP, where it is pyrolyzed and gasified. The pyrolysis / gasification step GP is preferably performed at a temperature of 350 to 900 ° C. The raw material is hydrocarbon gas having up to 3 carbon atoms such as hydrogen, carbon monoxide, methane, etc., a product gas containing a tar content consisting of hydrocarbons having 4 or more carbon atoms, and a pyrolysis residue mainly composed of fixed carbon of the raw material It is broken down into ash (also called char). The product gas 101 is discharged from the furnace outlet and sent to the apparatus for the gas reforming process 6. In the gas reforming step 6, the product gas 101 is heated at a high temperature by partial combustion, reaction with water vapor (reforming reaction), catalyst (zeolite, silica-alumina, limestone, or metal (Rh, Ru, Ni, Pd, Pt). , Co, Mo, Ir, Re, Fe, Na, K) or a catalyst using a catalyst made of an oxide of these metals such as Ni / Al203). Hydrogen generation occurs due to the reduction of molecular compounds and the reaction with water vapor. The reformed gas is supplied to the heat recovery process 7 and reduced in temperature, and then supplied to the gas cleaning / dust removal process 8 to be cleaned / dedusted. Thereafter, the cleaned reformed gas is removed from the system as a product gas 106 after chlorine compounds and / or sulfur compounds are removed in an apparatus for the gas purification step 9, and is then discharged to a predetermined position (facility, facility, Container).

  The pyrolysis residue generated in the pyrolysis process GP is sent to an apparatus for the pyrolysis residue combustion process CP and burned by reaction with oxygen-containing gas such as air (including preheated air and air containing combustion exhaust gas). The The high-temperature combustion gas 107 generated by the combustion of the pyrolysis residue is sent to the apparatus for the heat recovery step 11 and is reduced in temperature from the range of 400-1000 ° C. to the range of 150-500 ° C. in the heat recovery step 11, It is sent to the dust removal process 12. After removing ash and dust contained in the combustion gas 107 in the dedusting step 12, the combustion gas 107 passes through the desalting step 13 and the denitration step 14 to remove hydrogen chloride and nitrogen oxides from the combustion gas 107. At least a part of the clean combustion gas 107 obtained in this way is supplied to the drying / pretreatment step DP and used as a heat source necessary for drying and pretreatment of the raw material.

Next, an embodiment of the present invention that further embodies the basic concept of the present invention shown in FIG. 1 will be described with reference to FIGS.
FIG. 2 is a block diagram showing the gasifier according to the first embodiment of the present invention. As shown in FIG. 2, the gasifier includes a raw material dryer 1, a raw material hopper 2 disposed at the lower end of the raw material dryer 1, a raw material feeder 3 disposed at the lower end of the raw material hopper 2, and an internal circulation fluidized bed gas. It consists of a chemical reactor 4. The internal circulation type fluidized bed gasification furnace includes a gasification chamber 4-1 and a combustion chamber 4-2 provided in one furnace. The low calorific value raw material 100 such as biomass charged into the raw material dryer 1 is dried by the combustion gas discharged from the combustion chamber 4-2 of the internal circulation type fluidized bed gasification furnace 4, as will be described in detail later. . The dried raw material 100 is put into the raw material hopper 2, pushed into the raw material inlet of the raw material supply machine 3 by the pusher 5, and put into the gasification chamber 4-1 of the internal circulation type fluidized bed gasification furnace 4 by the raw material supply machine 3. Supplied. The fluidized bed 4-1b in which the fluidized medium is fluidized is formed in the gasification chamber 4-1, and the fluidized bed 4-2b in which the fluidized medium is fluidized is formed in the combustion chamber 4-2.

  The raw material 100 supplied to the upper part of the fluidized bed 4-1b (the upper part of the dense fluidized bed interface) of the gasification chamber 4-1 by the raw material feeder 3 is pyrolyzed and gasified in the fluidized bed 4-1b to produce a product gas Combustible gas) 101 and pyrolysis residues such as char are generated. The product gas 101 passes through the free board 4-1a and is sent to the gas reformer in the gas reforming process 6, and the product gas 101 reformed in the gas reforming process 6 is sent to the heat recovery process 7 to generate heat. In the recovery process 7, steam 102 is obtained by a waste heat boiler (not shown), preheated air 103 is obtained by an air preheater (not shown), and heat is recovered. The temperature of the product gas 101 is in the range of 800 ° C to 1200 ° C. To 200 ° C to 500 ° C. The product gas 101 whose temperature has dropped is sent to the gas cleaning / dedusting process 8, and the gas cleaning and drainage 104 and ash 105 are removed by water injection in the gas cleaning / dedusting process 8, and the cleaned product gas is cleaned. 101 becomes the product gas 106 through the gas purification step 9.

  The fluidized bed 4-1b in the gasification chamber 4-1 and the fluidized bed 4-2b in the combustion chamber 4-2 communicate with each other through an opening below the lower end of the partition wall 4-3, and the fluidized bed 4 in the gasification chamber 4-1 is connected. The thermal decomposition residue such as the fluidized medium and char moves from -1b to the fluidized bed 4-2b of the combustion chamber 4-2. In the combustion chamber 4-2, char or the like burns to generate combustion gas 107, and the generated combustion gas 107 is sent to the heat recovery step 11 through the free board 4-2a. Steam 108 is obtained with a boiler (not shown), preheated air 109 is obtained with an air preheater (not shown), and the heat is recovered. The temperature of the combustion gas 107 is in the range of 400 ° C. to 1000 ° C. to 150 ° C. to 500 ° C. Falls to the range. The combustion gas 107 whose temperature has been lowered is sent to an apparatus for the dust removal process 12, and the fly ash 110 is removed in the dust removal process 12, and passes through the apparatus for the desalination process 13 and the apparatus for the denitration process 14. Denitration treatment. The combustion gas 107 that has passed through the denitration process 14 is supplied to the raw material dryer 1 as a raw material drying gas. Of course, the gas reforming step 6, the heat recovery step 7, the gas cleaning / dedusting step 8, and the gas purification step 9 can be omitted depending on the properties and applications of the product gas 101. For example, when the product gas generated in the gasification chamber is used as it is as a fuel gas for a boiler, a cement firing furnace, a limestone firing furnace (also called a lime kiln) in a papermaking process, the gas reforming process 6 or the heat recovery process. 7 or the gas purification step 9 is not provided, and the generated gas is supplied to a boiler or a firing furnace after dust removal. Similarly, the heat recovery step 11, the dust removal step 12, the desalting step 13, and the denitration step 14 can be omitted if unnecessary due to the properties of the combustion gas 107. For example, when the raw material contains no chlorine, the desalting step 13 is not necessary.

  The raw material dryer 1 is a vertical dryer configured to supply a raw material drying gas from the lower end, contribute to the raw material drying while descending, and discharge from the upper end. The combustion gas 107 supplied to the raw material dryer 1 as a raw material drying gas contributes to the drying of the raw material 100 and is then sent to the cooling step 15 where the essential oil component and the wood vinegar component contained in the combustion gas (drying gas) 107 Is condensed and recovered. The essential oil component and / or the wood vinegar component are removed, and the combustion gas becomes exhaust gas 112 and is released to the outside of the system.

  The fluidized medium 113 moves into the fluidized bed 4-2b, is discharged from the bottom of the fluidized bed 4-2b, and is supplied into the raw material feeder 3 through the fluidized medium circulating means 16. The raw material feeder 3 has a configuration in which a screw 3-2 is rotatably arranged in a casing 3-1, and the casing 3-1 has a predetermined angle with respect to a horizontal plane, and the downstream side of the casing 3-1 is upward. So as to be inclined. Thereby, a high material sealing function can be exhibited by the raw material and the fluid medium 113 filled in the casing 3-1. On the other hand, if the material seal function is obtained so as to operate the system without causing a problem due to the lack of the seal function, the raw material supplier 3 may be arranged without being inclined.

  By supplying the raw material 100 having a low calorific value such as biomass dried by the raw material dryer 1 to the gasification chamber 4-1 as described above, the water contained in the raw material 100 evaporates and most of the hydrogen component is present. Is produced gas 101 as a volatile component and is discharged from gasification chamber 4-1, so that combustion gas 107 discharged from combustion chamber 4-2 contains almost no moisture and is high-grade such as kerosene. It has a drying capacity equivalent to a drying gas obtained by diluting a gas obtained by burning a hydrogen-containing fuel with a large amount of air. Accordingly, the combustion gas 107 is supplied to the raw material dryer 1 after being subjected to heat recovery, dedusting, desalting, and denitration processes through a heat recovery process 11, a dedusting process 12, a demineralization process 13, and a denitration process 14. , Low calorific value raw materials such as biomass, municipal solid waste, or organic sludge can be efficiently dried. Therefore, the product gas 106 can be recovered from the raw material 100 having a low calorific value with high efficiency and low cost. Energy may also be recovered from the raw material 100.

  Further, when gasifying a raw material having a high water content in the internal circulation type fluidized bed gasification furnace 4, the cold gas efficiency is lowered. That is, since the rate of burning the raw material 100 increases, the amount of the combustion gas 107 discharged from the combustion chamber 4-2 increases, and the drying capacity in the raw material dryer 1 also increases. As a result, the moisture content of the raw material 100 before being supplied to the gasification chamber 4-1 can be constantly stabilized, and the amount of generated gas 101 per unit raw material can be stabilized.

  Further, since the biomass raw material 100 contains an essential oil component and a wood vinegar component, the combustion gas 107 is adjusted to an appropriate temperature when the combustion gas 107 is introduced into the raw material dryer 1 in order to dry the biomass raw material, The essential oil component and the wood vinegar component in the biomass raw material can be selectively extracted into the combustion gas. The extracted essential oil component and wood vinegar component can be easily condensed and recovered by introducing the combustion gas to the cooling step 15 and cooling it. Since the recovered essential oil component and the wood vinegar component 111 are relatively expensive and can be sold, it can be expected to contribute to improving the profitability of the product gas and energy recovery business from biomass resources.

  Further, by using the sensible heat of the combustion gas 107 to dry the raw material 100 having a low calorific value, not only the cold gas efficiency can be improved and the energy recovery efficiency can be improved, but also the heat recovery and power recovery can be performed using a boiler. Therefore, the equipment cost can be suppressed, and an energy recovery device that can recover energy with high efficiency and low cost can be configured.

  Next, a gasification method and apparatus according to a second embodiment of the present invention will be described with reference to FIG. The gasifier of the second embodiment shown in FIG. 3 differs from the gasifier of the first embodiment shown in FIG. 2 in that the first embodiment shown in FIG. The mold material dryer 1 is arranged so that the dried material 100 can be directly fed into the material hopper 2, whereas in the second embodiment shown in FIG. The kiln type raw material dryer 20 is disposed. In the second embodiment shown in FIG. 3, the raw material 100 is introduced from the raw material supply port 20 a provided at the upper part of the end of the raw material dryer 20, and the raw material discharge provided at the lower part of the other end of the raw material dryer 20. The dried raw material 100 ′ is discharged from the outlet 20b.

  The combustion gas 107 which is a drying gas is supplied from one end on the downstream side of the raw material dryer 20 and is discharged from the other end on the upstream side. That is, the combustion gas 107 supplied from the combustion chamber 4-2 of the internal circulation type fluidized bed gasification furnace 4 undergoes a heat recovery process 11, a dust removal process 12, a desalting process 13, and a denitration process 14, and then a raw material dryer. 20 is supplied to the downstream end of the material 20, flows in the direction opposite to the moving direction of the raw material, contributes to the drying of the raw material 100, exits from the upstream end, and is supplied to the cooling step 15. . The dried raw material 100 'is supplied to the raw material hopper 2 by a conveying means (not shown). The other structure of the gasification apparatus shown in FIG. 3 is the same as that of the apparatus of FIG. 2, and has the same effect as the apparatus of FIG.

  FIG. 4 is a block diagram showing a gasification method and apparatus according to the third embodiment of the present invention. As shown in FIG. 4, an internal circulation type fluidized bed gasification furnace 4 in which the pyrolysis / gasification process and the pyrolysis residue combustion process according to the first and second embodiments of the present invention are performed in a single integrated furnace is provided. Furthermore, a drying / pretreatment chamber 4-4 for performing the “drying / pretreatment step” is provided.

  As shown in FIG. 4, the gasification furnace is a fluidized bed furnace, and the fluidized bed of the rich fluid medium is divided into three partition walls A, B, and C, and the drying / pretreatment chamber 4-4 and the gasification chamber 4. -1 and the combustion chamber 4-2. These three chambers 4-1, 4-2 and 4-3 are structured to be completely partitioned from the upper part of the fluidized bed to the top of the furnace by three partition walls A, B and C. Here, the upper part of the fluidized bed refers to the part above the surface part of the layer forming the dense fluidized bed. Specifically, these three partition walls A, B, and C have openings in the vicinity of the dispersion plate 4-6 at the bottom of the furnace and located in the dense fluidized bed so that the fluidized medium can move from the adjacent chamber. In addition to these openings, the walls are constructed so that there is no circulation with the next room. The fluid medium, raw material and pyrolysis residue forming the fluidized bed move to the next room through these openings. In this embodiment, the fluid medium 113 moves from the drying / pretreatment chamber 4-4 to the gasification chamber 4-1 together with the dried / pretreated raw material, and the fluid medium 113 is heated from the gasification chamber 4-1. It moves to the combustion chamber 4-2 together with the decomposition residue, and the fluid medium 113 moves from the combustion chamber 4-2 to the drying / pretreatment chamber 4-4 and the gasification chamber 4-1.

  By comprising in this way, the fluidized medium 113 heated by combustion of the thermal decomposition residue in the combustion chamber 4-2 is supplied to the drying / pretreatment chamber 4-4 and the gasification chamber 4-1, and the drying / pretreatment is performed. Heat necessary for the process and the gasification process can be moved by the fluidized medium 113. In order to move the fluid medium 113 (and the raw material and pyrolysis residue) in this way through the opening formed in the lower part of the partition wall, the fluidized state of the fluid medium on both sides of the partition wall of the opening, more specifically, Changes the superficial velocity of the fluidizing gas on both sides of the opening of the partition wall. That is, the fluidized state of the fluid medium on the downstream side of the opening is made relatively stronger than the fluidized state of the fluid medium on the upstream side of the opening. By doing so, the density difference between the fluidized beds on both sides of the partition wall opening occurs (the upstream fluidized bed is in a higher density state than the downstream fluidized bed), and the downstream flow velocity. The fluid medium moves due to the attraction effect due to the fact that is faster than the upstream flow velocity. The moving amount of the fluidized medium can be controlled by the difference in the fluidized state of the fluidized media on both sides of the opening, that is, the difference in the superficial velocity of the fluidized gas.

  Furthermore, a partition wall having a low height from the hearth such as D, E, and F to the vicinity of the surface of the dense fluidized bed is provided at least in the drying / pretreatment chamber 4-4, the gasification chamber 4-1, and the combustion chamber 4-2. It is good to provide one. These low partition walls are provided upstream of the opening of the partition wall that communicates with the downstream room in accordance with the flow of the fluid medium, and the partition walls (A, B, C) that partition the room and the low partition walls A region sandwiched between (D, E, F) is formed. In the region sandwiched between these two types of walls (for example, partition walls B and E), the other region in the room where the region is located (for example, other than the region sandwiched between partition walls B and E of gasification chamber 4-1). From the lower partition wall (for example, partition wall E), and the fluid medium passes through the lower opening of the partition wall (for example, partition wall B) that partitions the room, and the fluid medium passes through the lower chamber (for example, combustion chamber 4). -2). That is, a region sandwiched between these two types of walls (for example, partition walls B and E) has a function of sinking a fluid medium and sending it to an adjacent chamber, and is called a fluid medium sedimentation chamber. For example, the fluid medium settling chamber 4-5 is formed by the partition walls B and E. The fluid medium settling chamber is in a relatively weak fluidized state. When a low partition wall is provided to form a fluid medium settling chamber, the fluid medium that jumps into the fluid medium settling chamber accumulates in the fluid medium settling chamber due to weak fluidization of the fluid medium settling chamber. By appropriately setting the height of the low partition wall, the main body fluidized bed portion (portion other than the fluidized medium settling chamber) of the gasification chamber 4-1, the combustion chamber 4-2, and the drying / pretreatment chamber 4-4. High layer heights are possible. By making the bed height of the fluid medium settling chamber higher than the bed height of other regions, it becomes possible to increase the circulation amount of the fluid medium. That is, the circulation amount of the fluid medium can be controlled by the bed height of the fluid medium sedimentation chamber. Furthermore, since the fluidized medium settling chamber is in a relatively weak fluidized state, it has a fluidized bed with a higher density than other regions. Since the density can be increased, the circulating amount of the fluid medium can be controlled. Moreover, since a high-density layer is formed, it has a good gas sealing property that suppresses the inflow of gas from the adjacent chamber (downstream in the flow direction of the fluid medium) to the fluid medium sedimentation chamber.

  As described above, the combustion gas from the combustion chamber 4-2 is used as the fluidizing gas in the drying / pretreatment chamber 4-4, and the sensible heat of the combustion gas is preferably used for the drying / pretreatment of the raw material. In the gasification chamber 4-1, it is preferable to use a gas not containing oxygen such as water vapor or a gas having an oxygen content ratio of 5% or less, preferably 3% or less, for example, combustion exhaust gas. If a gas containing oxygen is supplied to the gasification chamber 4-1, the generated gas (combustible gas) generated by thermal decomposition is burned, and therefore, a part of the combustible gas component in the generated gas is lost. Absent. An oxygen-containing gas such as air or oxygen-enriched air is supplied to the combustion chamber 4-2.

  5A and 5B are horizontal cross-sectional conceptual diagrams showing an arrangement configuration of each chamber of the gasification furnace shown in FIG. The inside of one rectangular gasification furnace is partitioned into a drying / pretreatment chamber 4-4, a gasification chamber 4-1, and a combustion chamber 4-2 by partition walls A, B, C-1 and C-2, and a combustion chamber Two fluid medium settling chambers 4-5A and 4-5B, which are partitioned by low partition walls (F-1, F-2), are provided in 4-2. Partition walls A, B, C-1 and C-2 are partition walls from the bottom of the furnace to the top of the furnace, and an opening is provided in the vicinity of the bottom of the furnace so that the fluid medium, raw material and pyrolysis residue can move between the chambers. is there. The drying / pretreatment chamber 4-4 and the gasification chamber 4-1 are partitioned by a wall so as to be independent from any chamber except for the fluid medium moving opening provided in the vicinity of the bottom of the furnace. Since the opening for moving the fluidized medium is provided in the dense fluidized bed near the furnace bottom, the raw material and pyrolysis residue moving together with the fluidized medium and the fluidized medium can move to the adjacent chamber through the opening, but the drying / pretreatment chamber 4 -4, gas generated in each chamber of the gasification chamber 4-1 and the combustion chamber 4-2, that is, the gas generated by drying / pretreatment, the generated gas (combustible gas) and the combustion gas without moving to the adjacent chamber It is discharged independently from the outlet at the top of the furnace in the chamber. That is, the gas generated in each chamber can be taken out without being mixed with each other. Two low partition walls (F-1, F-2) are provided in the combustion chamber 4-2, and the fluid medium settling chamber 4-5A and the partition wall F partitioned by the partition walls F-1 and C-1. -2 and C-2 are formed as a fluid medium settling chamber 4-5B.

  Next, the movement (flow) of the fluidizing gas and the fluidized medium (including raw materials and pyrolysis residues that move with the fluidized medium) supplied to the fluidized bed will be described. The hatched areas in FIGS. 5A and 5B are fluidized areas that are relatively weaker than the adjacent white areas. The weak fluidized state of the fluidized medium is formed by supplying a fluidizing gas having a superficial velocity lower than the superficial velocity of the fluidizing gas supplied to the adjacent region.

  For example, the superficial velocity of the fluidized gas supplied to the left region in the combustion chamber 4-2 is set to the right side so that the left region in FIGS. 5A and 5B is weak and the right region is strong. It is relatively smaller than the superficial velocity of the fluidized gas supplied to the region. When fluidization regions having different velocities coexist in one chamber in this way, the flow settles in the weak fluidization region (the left region of the combustion chamber 4-2) and rises in the strong region (the right region of the combustion chamber 4-2). A medium flow occurs. This flow of the fluid medium is called a swirl flow. By forming a swirl flow in the gasification chamber 4-1 or combustion chamber 4-2, the raw materials and pyrolysis residue can be uniformly dispersed in the layer, and the pyrolysis and gasification reaction in the layer (In the case of the gasification chamber 4-1) and the combustion reaction (in the case of the combustion chamber 4-2) can be sufficiently caused.

  Movement of the fluid medium between the two chambers partitioned by the partition wall is caused by a pressure difference between both sides of the partition wall opening. That is, the fluid medium moves from the higher pressure to the lower pressure. The pressure in the region is the product of the density of the fluidized bed in the region, the fluidized bed height and the gravitational acceleration, so changing the density of the fluidized bed or the height of the fluidized bed in multiple regions (layer height) The amount of movement can be changed.

  For example, the movement of the fluid medium from the gasification chamber 4-1 to the combustion chamber 4-2 through the opening of the partition wall B between the gasification chamber 4-1 and the combustion chamber 4-2 occurs as follows. . The fluidization state on both sides of the partition wall B near the opening is weak on the gasification chamber 4-1 side and strong on the combustion chamber 4-2 side. Thereby, a sedimentation flow of the fluidized medium is formed on the gasification chamber 4-1 side, and an upward flow is formed on the combustion chamber 4-2 side. Furthermore, when the superficial velocity of the fluidized gas is different, the density of the fluidized bed is different. That is, the fluidized bed density in the weak fluidized region (region where the superficial velocity is relatively slow, the gasification chamber side) is the fluidized bed density in the strong fluidized region (region where the superficial velocity is relatively fast, the combustion chamber side). Higher than density. That is, the density of the fluidized bed is different on both sides of the partition wall of the opening. The fluid medium moves from the gasification chamber 4-1 side having a high fluidized bed density to the combustion chamber 4-2 side having a low fluidized bed density. In this way, by providing regions with different fluidization states on both sides of the partition wall opening, the fluid medium can be moved from a room with a weak fluidized region to a room with a strong fluidized region. Further, when the superficial velocity of the weak fluidization region on the gasification chamber side is decreased, the viscosity of the fluidized bed increases and the moving amount of the fluidized medium decreases. The moving amount of the fluidized medium can be changed by utilizing the change in the viscosity of the fluidized bed. In this configuration, the fluid medium and the raw material move from the drying / pretreatment chamber 4-4 to the gasification chamber 4-1 (hatched arrow a-1), and from the gasification chamber 4-1 to the combustion chamber 4-2. Of the fluidized medium and the pyrolysis residue (hatched arrow b-1), the fluidized medium from the fluidized medium sedimentation chambers 4-5A and 4-5B to the gasification chamber 4-1 (hatched arrow c- 1 and c-2), and the location where the fluid medium settling chambers 4-5A and 4-5B move to the drying and pretreatment chamber 4-4 (hatched arrows c-3 and c-4). In these places, the fluid medium moves, but it is better not to move the gas generated in each chamber to the adjacent chamber (the gases are not mixed with each other). . Thus, the amount of movement of the fluid medium passing through the partition wall opening can be changed depending on the difference in fluidization state in the vicinity of the opening between the two chambers. That is, the larger the difference between the fluidized state of the fluid medium on the upstream side of the opening and the fluidized state of the fluid medium on the downstream side, the larger the amount of fluid medium that moves. That is, if the upstream superficial velocity is decreased, the downstream superficial velocity is increased, or if the upstream side is slowed and the downstream side is accelerated, the amount of movement of the fluid medium increases.

  For example, the movement of the fluid medium from the combustion chamber 4-2 to the fluid medium sedimentation chamber 4-5A over the low partition wall F-1 between the combustion chamber 4-2 and the fluid medium sedimentation chamber 4-5A is as follows. To happen. The fluidized state of the fluid medium on both sides of the partition wall F-1 is relatively strong on the combustion chamber side and weak on the fluid medium sedimentation chamber side. Thereby, an upward flow of the fluid medium is formed on the combustion chamber side, and a downward flow of the fluid medium is formed on the fluid medium sedimentation chamber side. In the upward flow on the combustion chamber side, the fluid medium jumps out due to the burst of bubbles near the dense layer surface of the fluidized bed. Part of the fluid medium that has jumped out onto the bed jumps over the partition wall F-1 and enters the fluid medium sedimentation chamber 4-5A. The amount of the fluid medium that jumps into the fluid medium settling chamber 4-5A is the relationship between the layer height of the combustion chamber 4-2 and the height of the partition wall F-1, and the fluidization state on the combustion chamber side in the vicinity of the partition wall F-1. That is, it depends on the flow rate of the fluidizing gas. First, in a state where the bed height on the combustion chamber side is considerably lower than the height of the partition wall F-1, the partition wall is not changed even if the superficial velocity of the fluidized gas near the partition wall of the combustion chamber 4-2 is increased. The amount of the fluid medium that can be jumped over is small, but if the bed height of the combustion chamber 4-2 is close to the height of the partition wall F-1 and slightly lower than the height of the partition wall, the combustion chamber 4-2 layer Most of the fluid medium that has jumped up can be moved across the partition wall F-1 to the fluid medium sedimentation chamber 4-5A, and the amount of particles ejected onto the bed is higher as the superficial velocity of the fluidized gas is higher. Since a large amount of the fluid medium pops out, the amount of movement of the fluid medium can be changed by changing the superficial velocity on the combustion chamber 4-2 side near the partition wall F-1.

  Moreover, when the bed height of the combustion chamber 4-2 exceeds the height of the partition wall F-1, the fluid medium passes through the partition wall F-1 and the fluid medium sedimentation chamber 4-5A from the combustion chamber 4-2 side. Overflow to the side. In this case, regardless of the fluidized state, both the bed heights are the same at a position higher than the height of the partition wall F-1, or the bed height of the combustion chamber 4-2 is the same as that of the partition wall F-1. The fluidized medium moves from the combustion chamber 4-2 to the fluidized medium settling chamber 4-5A by overflow until it becomes the same. Note that there is no opening in the partition wall F-1, and the fluid medium does not move between the two chambers in the dense fluidized bed from the furnace bottom to the upper end of the partition wall.

In the gasification chamber shown in FIG. 5A, the fluid medium is supplied to both the drying / pretreatment chamber 4-4 and the gasification chamber 4-1, from both the fluid medium sedimentation chambers 4-5A, 4-5B. In the gasification chamber shown in FIG. 5B, from one fluid medium settling chamber 4-5B to the drying / pretreatment chamber 4-4 and from the other fluid medium settling chamber 4-5A to the gasification chamber 4- 1 has a structure in which a fluid medium is supplied to each.
As described above, the fluid medium can be moved in each partition wall, but the circulation of the fluid medium and the control of the circulation amount (movement amount) in the gasification furnace shown in FIGS. 5A and 5B are as follows. Do.

  In the case of the gasifier shown in FIG. 5A, the raw material is supplied to the drying / pretreatment chamber 4-4. The supplied raw material is settled in the fluidized bed by the swirling flow in which the hatched portion at the center of the drying / pretreatment chamber 4-4 is settled and the upper and lower white portions of the drying / pretreatment chamber 4-4 in FIG. Swallowed and evenly dispersed. The raw material is heated and dried by the sensible heat of the fluidized medium from the fluidized medium sedimentation chambers 4-5A and 4-5B supplied to the drying / pretreatment chamber 4-4 and the sensible heat of the combustion gas that is the fluidizing gas. -Pre-treated and separated into gas and other solids generated by drying / pre-treatment. A mixture of the drying / pretreatment gas and the gas generated from the raw material in the drying / pretreatment is discharged from the discharge port provided at the top of the furnace, sent to the cooling device, and cooled by the cooling device, and the essential oil component and / or the wood vinegar component and Harmful substances such as arsenic are collected. Thereafter, the exhaust gas is discharged outside the system. Solid content other than the gas component moves from the drying / pretreatment chamber 4-4 to the gasification chamber 4-1 as indicated by the hatched arrow a-1 through the opening of the partition wall A together with the fluid medium.

  The solid content moved to the gasification chamber 4-1 settles from the central portion of the gasification chamber 4-1 to the partition wall B side, and its peripheral portion is uniformly dispersed in the layer by the swirling flow of the fluidized medium, The main components are the product gas generated by pyrolysis and gasification, which is heated and decomposed by sensible heat from the fluid medium settling chambers 4-5A and 4-5B, and fixed carbon in the raw material. Divided into pyrolysis residues. The product gas generated in the gasification chamber 4-1 is discharged from an exhaust port provided at the top of the furnace, sent to the reforming process and reformed, and then heat recovered, washed, dedusted and purified to become a product gas. . The pyrolysis residue generated in the gasification chamber 4-1 moves from the gasification chamber 4-1 to the combustion chamber 4-2 as indicated by the hatched arrow b-1 through the opening of the partition wall B together with the fluid medium.

  The pyrolysis residue moved to the combustion chamber 4-2 is combusted by oxygen supplied to the combustion chamber 4-2, and the fluid medium is heated by the combustion heat of the pyrolysis residue. Combustion gas generated by combustion of pyrolysis residue is discharged from an exhaust port provided at the top of the furnace, and after heat recovery, dedusting, demineralization, and denitration, a part of the combustion gas is dried and pretreated chamber 4-4. Supplied as a heat source for drying and pretreatment. The heated fluid medium jumps over the partition walls F-1 and F-2 and moves to the fluid medium sedimentation chambers 4-5A and 4-5B as indicated by the white arrows f-1 and f-2.

  Part of the fluid medium that has moved to the fluid medium sedimentation chambers 4-5A and 4-5B flows as indicated by the arrows c-1 and c-2 hatched through the openings of the partition walls C-1 and C-2. The media settling chambers 4-5A, 4-5B move to the gasification chamber 4-1, and the remaining fluid medium is hatched through the other openings of the partition walls C-1 and C-2 and the arrows c-3 and As in c-4, the fluid medium settling chambers 4-5A and 4-5B move to the drying / pretreatment chamber 4-4.

  In summary, the circulation of the fluidized medium in the case of the gasification furnace shown in FIG. 5A is as follows: drying / pretreatment chamber 4-4 → gasification chamber 4-1 → combustion chamber 4-2 → fluid medium sedimentation chamber 4-5A. , 4-5B → drying / pretreatment chamber 4-4 → gasification chamber 4-1. That is, the fluidized media are pretreatment chamber 4-4, drying / pretreatment chamber 4-1, combustion chamber 4-2, fluid medium sedimentation chambers 4-5A, 4-5B, drying / pretreatment chamber 4-4, and It flows in the order of the gasification chamber 4-1. The circulation amount of the fluid medium in this circulation can be freely changed by changing the flow velocity of the fluid medium sedimentation chamber 4-5A or 4-5B, instead of changing the speed of each partition wall partitioning each chamber. First, since the drying / pretreatment chamber 4-4, the gasification chamber 4-1, and the combustion chamber 4-2 are all reaction sites, the amount of gas supplied to the chamber, that is, the amount of fluidized gas, is charged. If the type and amount of the raw material to be changed does not change, it is better to keep the reaction under certain conditions without changing it. When the input amount of the raw material changes, it is desirable to increase or decrease the amount of fluidized gas (reactive gas) supplied to these chambers relative to the change. In other words, the amount of fluidizing gas supplied to the drying / pretreatment chamber 4-4, gasification chamber 4-1, and combustion chamber 4-2 varies depending on the type of raw material and the input amount. Therefore, it is desirable not to increase or decrease.

  When the superficial velocity of the chambers other than the fluid medium sedimentation chambers 4-5A and 4-5B is constant, the fluid medium sedimentation chamber 4 can be obtained by reducing the superficial velocity of the fluid medium sedimentation chambers 4-5A and 4-5B. Since the difference in superficial velocity between the partition walls C-1 and C-2 between the -5A, 4-5B and the drying / pretreatment chamber 4-4 or the gasification chamber 4-1 increases, the fluid medium The amount of the fluid medium that moves from the settling chambers 4-5A and 4-5B to the drying / pretreatment chamber 4-4 or the gasification chamber 4-1 increases. On the contrary, if the superficial velocity of the fluid medium settling chambers 4-5A and 4-5B is increased, the flow medium settling chamber 4-5 and the drying / pretreatment chamber 4-4 or the gasification chamber 4-1 are arranged. Since the difference in the superficial velocity between the partition walls C-1 and C-2 is reduced, the fluid medium settling chambers 4-5A and 4-5B are moved to the drying / pretreatment chamber 4-4 or the gasification chamber 4-1. The amount of fluid medium that moves is reduced. When the amount of the flowing medium flowing into the drying / pretreatment chamber 4-4 or the gasification chamber 4-1 changes, the bed height of the drying / pretreatment chamber 4-4 or the gasification chamber 4-1 also changes. As described above, since the moving amount of the fluid medium also depends on the bed height, for example, if the amount of fluid medium flowing into the gasification chamber 4-1 from the fluid medium sedimentation chambers 4-5A and 4-5B increases. The bed height of the gasification chamber 4-1 is increased, and the amount of movement of the fluid medium from the gasification chamber 4-1 to the combustion chamber 4-2 is also increased. If the amount of flowing medium flowing into the combustion chamber 4-2 increases, the bed height of the combustion chamber 4-2 increases, so that the amount of flowing medium flowing from the combustion chamber 4-2 into the flowing medium settling chambers 4-5A and 4-5B also increases. . Thus, it is possible to change the circulation amount of the fluid medium to all the rooms only by changing the superficial velocity of the fluid medium sedimentation chamber 4-5A or 4-5B.

  In the case of the gasification furnace shown in FIG. 5B, the raw material is supplied to the drying / pretreatment chamber 4-4, settles on the partition wall side (partition wall A side), and rises on the partition wall side (partition wall C-2 side). It is swallowed into the fluidized bed by the swirling flow and uniformly dispersed. The raw material is heated, dried and pretreated by the sensible heat of the fluidized medium from the fluidized medium sedimentation chamber 4-5B supplied to the drying / pretreatment chamber 4-4 and the sensible heat of the combustion gas as the fluidizing gas. It is divided into gas generated by drying and pretreatment and other solid contents. A mixture of the drying / pretreatment gas and the gas generated from the raw material in the drying / pretreatment is discharged from the discharge port provided at the top of the furnace, sent to the cooling device, and cooled by the cooling device, and the essential oil component and / or the wood vinegar component and After collecting harmful substances such as arsenic, the exhaust gas is released outside the system. Solid content other than the gas component moves from the drying / pretreatment chamber 4-4 to the gasification chamber 4-1 as indicated by the hatched arrow a-1 through the opening of the partition wall A together with the fluid medium.

  The raw material solids moved to the gasification chamber 4-1 settle at the center of the gasification chamber 4-1, and rise on the upper and lower partition wall sides (upper and lower partition wall A side and partition wall C-1 side). And a product gas generated by pyrolysis and gasification, which is uniformly dispersed in the bed by the swirling flow of the fluid medium, heated by the sensible heat of the fluid medium from the fluid medium settling chamber 4-5A, and pyrolyzed and gasified. And pyrolysis residue mainly composed of fixed carbon in the raw material. The product gas generated in the gasification chamber 4-1 is discharged from an exhaust port provided at the top of the furnace, sent to the reforming process and reformed, and then heat recovered, washed, dedusted and purified to become a product gas. . The pyrolysis residue generated in the gasification chamber 4-1 moves from the gasification chamber 4-1 to the combustion chamber 4-2 as indicated by the hatched arrow b-1 through the opening of the partition wall B together with the fluid medium.

  The pyrolysis residue moved to the combustion chamber 4-2 is combusted by oxygen supplied to the combustion chamber 4-2, and the fluid medium is heated by the combustion heat of the pyrolysis residue. Combustion gas generated by combustion of pyrolysis residue is discharged from an exhaust port provided at the top of the furnace, and after heat recovery, dedusting, demineralization, and denitration, a part of the combustion gas is dried and pretreated chamber 4-4. Supplied as a heat source for drying and pretreatment. The fluid medium heated in the combustion chamber 4-2 jumps over the partition walls F-1 and F-2 and enters the fluid medium sedimentation chambers 4-5A and 4-5B as indicated by the white arrows f-1 and f-2. Moving.

  The fluid medium that has moved to one fluid medium sedimentation chamber 4-5A passes from the fluid medium sedimentation chamber 4-5A to the gasification chamber 4-1, as indicated by the arrow c-1 that is hatched through the opening of the partition wall C-1. Move to. The flowing medium that has moved to the flowing medium settling chamber 4-5A is transferred from the flowing medium settling chamber 4-5B to the drying / pretreatment chamber 4-4 as indicated by an arrow c-3 that is hatched through the opening of the partition wall C-2. Moving.

  In summary, the circulation of the fluidized medium in the case of the gasification furnace shown in FIG. 5B is as follows: drying / pretreatment chamber 4-4 → gasification chamber 4-1 → combustion chamber 4-2 → fluid medium sedimentation chamber 4-5A. , 4-5B → drying / pretreatment chamber 4-4 and gasification chamber 4-1. That is, the fluidized medium comprises a drying / pretreatment chamber 4-4, a gasification chamber 4-1, a combustion chamber 4-2, a fluid medium sedimentation chamber 4-5A, 4-5B, a drying / pretreatment chamber 4-4, and It flows in the order of the gasification chamber 4-1. The circulation amount of the fluid medium in this circulation can be controlled in the same manner as in the gasification furnace shown in FIG. 5A.

  Although the preferred embodiments of the present invention have been described in detail above, the present invention is not limited to the above-described embodiments, and various modifications can be made within the scope of the appended claims.

  INDUSTRIAL APPLICABILITY The present invention can be used for a gasification method and apparatus for generating combustible gas with high efficiency and low cost by gasifying a raw material such as biomass.

FIG. 1 is a block diagram showing the basic concept of the gasification method and apparatus of the present invention. FIG. 2 is a block diagram showing a gasification method and apparatus according to the first embodiment of the present invention. FIG. 3 is a block diagram showing a gasification method and apparatus according to the second embodiment of the present invention. FIG. 4 is a block diagram showing a gasification method and apparatus according to the third embodiment of the present invention. 5A and 5B are horizontal cross-sectional conceptual diagrams showing an arrangement configuration of each chamber of the gasification furnace shown in FIG.

Claims (23)

Raw material pretreatment process;
A gasification step in which a pretreated raw material is gasified in a gasification chamber to generate a combustible gas and a residue;
A combustion process for burning the residue in the combustion chamber and generating combustion gas;
A gasification method comprising: a supply step of supplying a combustion gas to the pretreatment step and separating a part of a volatile component from a raw material.   The gasification method according to claim 1, further comprising a cooling step of cooling the gaseous substance discharged from the pretreatment step and recovering an arsenic compound and / or a pyroligneous component.   The gasification chamber and the combustion chamber are provided in a fluidized bed gasification furnace so that a fluid medium can circulate between the gasification chamber and the combustion chamber. Item 2. The gasification method according to Item 1.   The gasification method according to claim 3, wherein the pretreatment step is performed in a pretreatment chamber, and the pretreatment chamber is provided in the fluidized bed gasification furnace.   5. The gasification method according to claim 3, further comprising at least one fluid medium sedimentation chamber that sediments the fluid medium and sends the fluid medium to at least one of the gasification chamber and the combustion chamber.   The gasification method according to claim 1, wherein the raw material is biomass. The raw material is dried with a drying device,
The dried raw material is gasified in the gasification chamber to produce combustible gas and residue,
The residue is burned in the combustion chamber to generate combustion gas,
A gasification method characterized by supplying combustion gas to the drying device and drying the raw material.   The gasification method according to claim 7, wherein the gaseous substance discharged from the drying device is cooled to recover an essential oil component and / or a wood vinegar component.   The gasification method according to claim 7, wherein the combustion gas is supplied to the drying device after recovering heat from the combustion gas discharged from the combustion chamber.   The gasification chamber and the combustion chamber are provided in a fluidized bed gasification furnace so that a fluid medium can circulate between the gasification chamber and the combustion chamber. Item 8. The gasification method according to Item 7.   The gasification method according to claim 10, further comprising at least one fluid medium sedimentation chamber that sediments the fluid medium and sends the fluid medium to at least one of the gasification chamber and the combustion chamber.   The gasification method according to claim 7, wherein the raw material is made of biomass. A pretreatment chamber for pretreatment of raw materials;
A gasification chamber for gasifying the pretreated raw material to produce a combustible gas and a residue;
A combustion chamber for burning residue and generating combustion gas,
A part of the volatile matter is separated from the raw material by supplying combustion gas from the combustion chamber to the pretreatment chamber.   The gasifier according to claim 13, further comprising a cooling device that cools the gaseous substance discharged from the pretreatment chamber and collects an arsenic compound and / or a pyroligneous component.   The gasification chamber and the combustion chamber are provided in a fluidized bed gasification furnace so that a fluid medium can circulate between the gasification chamber and the combustion chamber. Item 14. The gasifier according to Item 13.   The gasifier according to claim 15, wherein the pretreatment chamber is provided in the fluidized bed gasification furnace.   17. The gasifier according to claim 15, further comprising at least one fluid medium sedimentation chamber that sediments the fluid medium and sends the fluid medium to at least one of the gasification chamber and the combustion chamber. A drying device for drying the raw materials;
A gasification chamber for gasifying the dried raw material to produce a combustible gas and a residue;
A combustion chamber for burning residue and generating combustion gas,
The raw material is dried in the drying device by supplying combustion gas from the combustion chamber to the drying device.   The gasifier according to claim 18, further comprising a cooling device that cools the gaseous substance discharged from the drying device and collects an essential oil component and / or a wood vinegar component. A heat recovery device for recovering heat from the combustion gas discharged from the combustion chamber;
19. The gasifier according to claim 18, wherein the combustion gas discharged from the heat recovery device is supplied to the drying device.   The gasification chamber and the combustion chamber are provided in a fluidized bed gasification furnace so that a fluid medium can circulate between the gasification chamber and the combustion chamber. Item 19. The gasification method according to Item 18.   The gasification method according to claim 21, further comprising at least one fluid medium sedimentation chamber that sediments the fluid medium and sends the fluid medium to at least one of the gasification chamber and the combustion chamber. The gasifier according to claim 18, wherein the raw material is biomass.

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