JPH109511A5 - - Google Patents
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- JPH109511A5 JPH109511A5 JP1996181478A JP18147896A JPH109511A5 JP H109511 A5 JPH109511 A5 JP H109511A5 JP 1996181478 A JP1996181478 A JP 1996181478A JP 18147896 A JP18147896 A JP 18147896A JP H109511 A5 JPH109511 A5 JP H109511A5
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- fluidized bed
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Description
【０００８】
【発明が解決しようとする課題】
上記の従来技術では、旋回流を用いることにより、炉の底部で中央部から周辺部への強力な流れを形成するため、サイズの大きい不燃物を炉底に堆積させることなく炉周辺部の排出口より外部へ排出できる。また旋回流により、可燃物を破砕し、炉内を流動媒体とともに可燃物が循環する間に、可燃物が可能な限り酸化またはガス化される。また原料を無破砕状態でガス化炉へ投入しても旋回流により破砕、ガス化可能であるが、一方、流動層炉の水平断面がほぼ円形で、移動層が炉の中央部に形成される構成になっているため、比較的粒径の大きなチャー（カーボン質）は、炉の底部に下降し、不燃物と共に排出される割合が増えてくるため、熔融炉へ飛散する可燃物が少なくなり、システム全体の熱効率が低下するおそれがある。また不燃物と共に系外へ排出されたチャーを系内に戻す必要がある。
[0008]
[Problem to be solved by the invention]
In the above-mentioned conventional technology, a swirling flow creates a powerful flow from the center to the periphery at the bottom of the furnace, allowing large non-combustible materials to be discharged from outlets around the furnace periphery without depositing at the bottom. The swirling flow also crushes combustible materials, oxidizing or gasifying them as much as possible as they circulate through the furnace with the bed material. While the swirling flow allows for crushing and gasification of raw materials even when they are not crushed, the horizontal cross section of the fluidized-bed furnace is nearly circular, and the moving bed is formed in the center of the furnace. Therefore, relatively large particles of char (carbonaceous material) tend to descend to the bottom of the furnace, increasing the proportion of these particles discharged with the non-combustible materials. This reduces the amount of combustible material dispersed into the melting furnace, potentially reducing the overall thermal efficiency of the system. Furthermore, the char discharged with the non-combustible materials must be returned to the system.
【００１１】
【課題を解決するための手段】
上記課題を解決するために本発明の可燃物の処理方法の一態様は、流動層炉において可燃物をガス化し、熔融燃焼炉において灰分を熔融する可燃物の処理方法において、前記流動層炉内に流動媒体の旋回流を形成し、前記可燃物を該流動層炉に供給して該流動媒体の旋回流中でガス化して生成ガスを生成し、前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保ち、該生成ガスを熔融燃焼炉に供給して灰分を熔融することを特徴とする。
本発明の可燃物の処理装置の一態様は、可燃物をガス化する流動層炉と、灰分を熔融する熔融燃焼炉を備えた可燃物の処理装置において、前記流動層炉の流動層中に流動媒体の旋回流を形成し、前記可燃物を該旋回流中でガス化して生成ガスを生成し、前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保つことを特徴とする。
本発明の可燃物の処理装置の一態様は、可燃物をガス化する流動層炉と、灰分を熔融する熔融燃焼炉を備えた可燃物の処理装置において、前記流動層炉は、炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層炉炉底より供給するための流動化ガス分散機構と、前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、前記炉底第二領域付近から不燃物を排出するための不燃物排出口とを備え、前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、前記可燃物を前記流動層炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保ち、該生成ガスを前記熔融燃焼炉に供給し灰分を熔融することを特徴とする。
本発明の流動層ガス化炉の一態様は、可燃物をガス化する流動層ガス化炉において、前記流動層ガス化炉は炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層ガス化炉の炉底より供給するための流動化ガス分散機構と、前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、前記炉底第二領域の外側から不燃物を排出するための不燃物排出口を備え、流動媒体を前記第一領域から前記第二領域へと前記流動化ガス分散機構に沿って移動させ、前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、前記可燃物を前記流動層ガス化炉に供給し、該流動層ガス化炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、前記生成ガスを８００℃以下になるよう保ちつつ前記流動層上方のフリーボードから前記生成ガスを排出することを特徴とする。
本発明の流動層ガス化炉の一態様は、可燃物をガス化する流動層ガス化炉において、前記流動層ガス化炉は、炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層ガス化炉の炉底より供給するための流動化ガス分散機構と、前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、前記炉底第二領域の外側から不燃物を排出するための不燃物排出口を備え、前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、前記可燃物を前記流動層ガス化炉に供給し、該流動層ガス化炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、前記生成ガスを８００℃以下になるよう保ちつつ前記流動層上方のフリーボードから前記生成ガスを排出することを特徴とする。
本発明の流動層ガス化炉の一態様は、流動層の温度が４５０℃〜６５０℃に維持されるよう温度制御する構成を設けたことを特徴とする。
本発明の流動層ガス化炉の一態様は、前記流動層ガス化炉内において熱回収する構成を設けたことを特徴とする。
本発明の可燃物の処理方法の一態様は、可燃物を流動層炉にてガス化して可燃ガス及びチャーを生成し、該可燃ガス及びチャーを熔融燃焼炉にて燃焼し灰分を熔融する可燃物の処理方法において、該流動層炉は、流動層の温度が４５０〜６５０℃に維持されるように温度制御され、該流動層炉で生成された可燃ガス及びチャーを流動層上部のフリーボードから該熔融燃焼炉へ８００℃以下の状態で送り、該熔融燃焼炉で燃焼し灰分を熔融することを特徴とする。
本発明の好ましい一態様は、可燃物が流動層炉において、可燃ガスにガス化される方法において、流動層炉は、流動層の温度が４５０〜６５０℃に維持されるように温度制御され、流動層炉で生成された可燃ガス及び微粒子は流動層上部のフリーボードから熔融燃焼炉へ８００℃以下の状態で送られ、熔融燃焼炉で１３００℃以上で燃焼され、灰分が熔融されるようにしてもよい。
本発明の好ましい一態様は、可燃物が並設される２つの領域に分けられる流動層炉において可燃ガスにガス化される方法において、流動層炉へ供給される流動化ガスは、炉底第１領域付近から炉内へ上向き流として供給される第１流動化ガスと、炉底第２領域から炉内へ上向き流として供給される第２流動化ガスとからなり、第１流動化ガスの質量速度は第２流動化ガスの質量速度より小にされ、それによって、炉内の第１領域に流動媒体が沈降拡散する移動層が形成されると共に、炉内の第２領域に流動媒体が活発に流動化している流動層が形成され、炉内へ供給される可燃物が、移動層の下部から流動層へ及び流動層頂部から移動層へ、流動媒体と共に循環する間に可燃ガスにガス化され、第１流動化ガスの酸素含有量が、第２流動化ガスの酸素含有量以下であり、かつ流動層の温度が４５０〜６５０℃に維持されるようにしてもよい。
本発明の好ましい一態様は、上記可燃物が流動層炉において、可燃ガスにガス化される方法又は可燃物が並設される２つの領域に分けられる流動層炉において可燃ガスにガス化される方法において、流動層炉へ供給される流動化ガスは、可燃物の燃焼に必要な理論燃焼空気量の３０％以下の空気量を含むようにしてもよい。
本発明の好ましい一態様は、上記可燃物が並設される２つの領域に分けられる流動層炉において可燃ガスにガス化される方法において、流動層炉の炉底第２領域付近から不燃物が取り出され、分級され、得られた砂が流動層炉内へ戻されるようにしてもよい。
本発明の好ましい一態様は、上記可燃物が流動層炉において、可燃ガスにガス化される方法又は可燃物が並設される２つの領域に分けられる流動層炉において可燃ガスにガス化される方法において、流動層炉で生成された可燃ガス及び微粒子は熔融燃焼炉で１３００℃以上で高温燃焼され、灰分が熔融されるようにしてもよい。
すなわち、本発明の好ましい一態様では、流動層炉内の空気量制御や、熱回収等により、ダクト内のガスが８００℃以下になるようにし、ダクト内にクリンカが生じないようにしてもよい。
[0011]
[Means for solving the problem]
In order to solve the above problems, one aspect of the method for treating combustibles of the present invention is a method for treating combustibles by gasifying the combustibles in a fluidized bed furnace and melting the ash in a melting combustion furnace, characterized in that a swirling flow of a bed material is formed in the fluidized bed furnace, the combustibles are supplied to the fluidized bed furnace and gasified in the swirling flow of the bed material to generate a generated gas, the generated gas is sent from a freeboard above the fluidized bed to a duct at the inlet of the melting combustion furnace at a temperature of 800°C or less, and the generated gas is supplied to the melting combustion furnace to melt the ash.
One aspect of the present invention is a combustible material treatment device equipped with a fluidized bed furnace for gasifying combustible materials and a melting combustion furnace for melting ash, characterized in that a swirling flow of a bed material is formed in the fluidized bed of the fluidized bed furnace, the combustible materials are gasified in the swirling flow to generate a generated gas, and the generated gas is maintained at 800°C or less in the section from the freeboard above the fluidized bed to the duct at the inlet of the melting combustion furnace.
One aspect of the present invention is a combustible material treatment device including a fluidized bed furnace for gasifying combustible materials and a melting combustion furnace for melting ash, wherein the fluidized bed furnace comprises a fluidizing gas dispersion mechanism for supplying, from the bottom of the fluidized bed furnace, a first fluidizing gas supplied as an upward flow from a first hearth region into the furnace interior and a second fluidizing gas supplied as an upward flow from a second hearth region into the furnace interior; a hearth inclined from the first hearth region to the second hearth region; and a non-combustible material discharge port, wherein a fluidizing gas is supplied to the fluidized-bed gasification furnace so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of bed material, the combustible material is gasified in the swirling flow of the bed material in the fluidized-bed gasification furnace to generate a generated gas, the generated gas being sent from a freeboard above the fluidized bed to a duct at the inlet of the smelting combustion furnace is kept at 800°C or less, and the generated gas is supplied to the smelting combustion furnace to melt the ash.
One aspect of the fluidized-bed gasifier of the present invention is a fluidized-bed gasifier for gasifying combustibles, the fluidized-bed gasifier comprising a fluidizing gas dispersion mechanism for supplying a first fluidizing gas, which is supplied as an upward flow from a first hearth region into the furnace, and a second fluidizing gas, which is supplied as an upward flow from a second hearth region into the furnace, from the furnace bottom of the fluidized-bed gasifier; a hearth inclined from the first hearth region to the second hearth region; and an incombustible material discharge port for discharging incombustible material from the outside of the second hearth region, the first fluidizing gas is moved from the first region to the second region along the fluidizing gas dispersion mechanism, a fluidizing gas is supplied to the fluidized-bed gasification furnace so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of bed material, the combustible material is supplied to the fluidized-bed gasification furnace, and is gasified in the swirling flow of the bed material in the fluidized-bed gasification furnace to generate a product gas, and the product gas is discharged from a freeboard above the fluidized bed while maintaining the temperature of the product gas at 800°C or less.
One aspect of the fluidized-bed gasifier of the present invention is a fluidized-bed gasifier that gasifies combustibles, the fluidized-bed gasifier comprising: a fluidizing gas dispersion mechanism for supplying, from the bottom of the fluidized-bed gasifier, a first fluidizing gas that is supplied as an upward flow from a first hearth region into the furnace interior and a second fluidizing gas that is supplied as an upward flow from a second hearth region into the furnace interior; a hearth that slopes from the first hearth region to the second hearth region; and a non-combustible material discharge port for discharging non-combustibles from the outside of the second hearth region, wherein fluidizing gas is supplied to the fluidized-bed gasifier so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of bed material, the combustibles are supplied to the fluidized-bed gasifier, and are gasified in the swirling flow of the bed material in the fluidized-bed gasifier to generate a produced gas, and the produced gas is discharged from a freeboard above the fluidized bed while maintaining the produced gas at 800°C or less.
One aspect of the fluidized bed gasification furnace of the present invention is characterized by being provided with a temperature control configuration so that the temperature of the fluidized bed is maintained at 450°C to 650°C.
One aspect of the fluidized-bed gasification furnace of the present invention is characterized in that a heat recovery system is provided within the fluidized-bed gasification furnace.
One aspect of the method for treating combustible material of the present invention is a method for treating combustible material, which comprises gasifying the combustible material in a fluidized bed furnace to generate combustible gas and char, and burning the combustible gas and char in a melting combustion furnace to melt the ash, characterized in that the fluidized bed furnace is temperature controlled to maintain the temperature of the fluidized bed at 450 to 650°C, and the combustible gas and char generated in the fluidized bed furnace are sent from a freeboard above the fluidized bed to the melting combustion furnace at a temperature of 800°C or less, and are burned in the melting combustion furnace to melt the ash.
In a preferred embodiment of the present invention, in a method for gasifying combustible materials into combustible gas in a fluidized bed furnace, the temperature of the fluidized bed furnace is controlled so that the temperature of the fluidized bed is maintained at 450 to 650°C, and the combustible gas and fine particles generated in the fluidized bed furnace are sent from a freeboard above the fluidized bed to a melting combustion furnace at a temperature of 800°C or less, and are combusted in the melting combustion furnace at a temperature of 1300°C or more, thereby melting the ash.
In a preferred embodiment of the present invention, in a method for gasifying combustible materials into a combustible gas in a fluidized-bed furnace divided into two zones arranged side by side, the fluidizing gases supplied to the fluidized-bed furnace comprise a first fluidizing gas supplied as an upward flow from near the first zone at the furnace bottom into the furnace, and a second fluidizing gas supplied as an upward flow from the second zone at the furnace bottom into the furnace, the mass velocity of the first fluidizing gas being smaller than the mass velocity of the second fluidizing gas, thereby forming a moving bed in the first zone in the furnace where the fluidizing material settles and diffuses, and forming a fluidized bed in the second zone in the furnace where the fluidizing material is actively fluidized, the combustible materials supplied into the furnace are gasified into a combustible gas while circulating together with the fluidizing material from the bottom to the fluidized bed and from the top to the fluidized bed, the oxygen content of the first fluidizing gas may be equal to or less than the oxygen content of the second fluidizing gas, and the temperature of the fluidized bed may be maintained at 450 to 650°C.
In a preferred aspect of the present invention, in the method for gasifying combustible materials into combustible gas in a fluidized bed furnace or in the method for gasifying combustible materials into combustible gas in a fluidized bed furnace divided into two regions arranged side by side, the fluidizing gas supplied to the fluidized bed furnace may contain an air amount that is 30% or less of the theoretical combustion air amount required for combustion of the combustible materials.
In a preferred embodiment of the present invention, in the method for gasifying the combustible material into a combustible gas in a fluidized bed furnace divided into two parallel zones, non-combustible material may be removed from near the second zone at the bottom of the fluidized bed furnace and classified, and the resulting sand may be returned to the fluidized bed furnace.
In a preferred embodiment of the present invention, in the method for gasifying combustible materials into combustible gas in a fluidized bed furnace or in the method for gasifying combustible materials into combustible gas in a fluidized bed furnace divided into two regions arranged side by side, the combustible gas and fine particles produced in the fluidized bed furnace may be combusted at a high temperature of 1300°C or higher in a melting combustion furnace to melt the ash.
That is, in a preferred embodiment of the present invention, the gas in the duct may be kept at 800°C or less by controlling the amount of air in the fluidized bed furnace or by heat recovery, etc., to prevent clinker from being generated in the duct.
Claims (8)
前記流動層炉内に流動媒体の旋回流を形成し、前記可燃物を該流動層炉に供給して該流動媒体の旋回流中でガス化して生成ガスを生成し、
前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保ち、該生成ガスを熔融燃焼炉に供給して灰分を熔融することを特徴とする可燃物の処理方法。 A method for treating combustible materials by gasifying combustible materials in a fluidized bed furnace and melting the ash in a melting combustion furnace,
forming a swirling flow of a bed material in the fluidized bed furnace, supplying the combustible material to the fluidized bed furnace and gasifying it in the swirling flow of the bed material to generate a product gas;
A method for treating combustibles, characterized in that the generated gas sent from the freeboard above the fluidized bed to the duct at the entrance of the melting combustion furnace is kept at 800°C or less, and the generated gas is supplied to the melting combustion furnace to melt the ash.
前記流動層炉の流動層中に流動媒体の旋回流を形成し、前記可燃物を該旋回流中でガス化して生成ガスを生成し、
前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保つことを特徴とする可燃物の処理装置。 A combustible material treatment device equipped with a fluidized bed furnace for gasifying combustible materials and a melting combustion furnace for melting ash,
forming a swirling flow of a bed material in a fluidized bed of the fluidized bed furnace, and gasifying the combustible material in the swirling flow to generate a product gas;
A combustibles treatment device characterized in that the generated gas sent from the freeboard above the fluidized bed to the duct at the inlet of the molten combustion furnace is kept at 800°C or less.
前記流動層炉は、炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層炉炉底より供給するための流動化ガス分散機構と、
前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、
前記炉底第二領域付近から不燃物を排出するための不燃物排出口とを備え、
前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、
前記可燃物を前記流動層炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、
前記流動層上方のフリーボードから前記熔融燃焼炉入口のダクトに至る部分で送られる前記生成ガスが８００℃以下になるよう保ち、該生成ガスを前記熔融燃焼炉に供給し灰分を熔融することを特徴とする可燃物の処理装置。 A combustible material treatment device equipped with a fluidized bed furnace for gasifying combustible materials and a melting combustion furnace for melting ash,
The fluidized bed furnace comprises a fluidizing gas dispersion mechanism for supplying, from the bottom of the fluidized bed furnace, a first fluidizing gas supplied as an upward flow from a first hearth region into the furnace interior and a second fluidizing gas supplied as an upward flow from a second hearth region into the furnace interior;
a hearth inclined from the first hearth region to the second hearth region;
a non-combustible material discharge port for discharging non-combustible material from the vicinity of the second furnace bottom region,
supplying a fluidizing gas to the fluidized-bed gasification furnace so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of the bed material;
gasifying the combustible material in the swirling flow of the bed material in the fluidized bed furnace to generate a product gas;
A combustible material treatment device characterized in that the generated gas sent from the freeboard above the fluidized bed to the duct at the entrance of the melting combustion furnace is kept at 800°C or less, and the generated gas is supplied to the melting combustion furnace to melt the ash.
前記流動層ガス化炉は炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層ガス化炉の炉底より供給するための流動化ガス分散機構と、
前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、
前記炉底第二領域の外側から不燃物を排出するための不燃物排出口を備え、
流動媒体を前記第一領域から前記第二領域へと前記流動化ガス分散機構に沿って移動させ、前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、
前記可燃物を前記流動層ガス化炉に供給し、該流動層ガス化炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、
前記生成ガスを８００℃以下になるよう保ちつつ前記流動層上方のフリーボードから前記生成ガスを排出することを特徴とする流動層ガス化炉。 In a fluidized bed gasifier that gasifies combustible materials,
The fluidized-bed gasification furnace comprises a fluidizing gas dispersion mechanism for supplying, from the bottom of the fluidized-bed gasification furnace, a first fluidizing gas supplied as an upward flow from a first region at the bottom of the furnace into the furnace and a second fluidizing gas supplied as an upward flow from a second region at the bottom of the furnace into the furnace;
a hearth inclined from the first hearth region to the second hearth region;
a non-combustible material discharge port for discharging non-combustible material from the outside of the second hearth region;
moving the bed material from the first region to the second region along the fluidizing gas dispersion mechanism, and supplying a fluidizing gas to the fluidized-bed gasification furnace so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of the bed material;
The combustible material is supplied to the fluidized-bed gasification furnace and gasified in the swirling flow of the bed material in the fluidized-bed gasification furnace to generate a product gas;
A fluidized bed gasification furnace, characterized in that the generated gas is discharged from a freeboard above the fluidized bed while maintaining the generated gas at 800°C or less.
前記流動層ガス化炉は、炉底第一領域から炉内へ上向き流として供給される第一流動化ガスと、炉底第二領域から炉内へ上向き流として供給される第二流動化ガスとを該流動層ガス化炉の炉底より供給するための流動化ガス分散機構と、
前記炉底第一領域から前記炉底第二領域にかけて傾斜した炉底と、
前記炉底第二領域の外側から不燃物を排出するための不燃物排出口を備え、
前記第一流動化ガスの質量速度を前記第二流動化ガスの質量速度より小となるよう流動化ガスを前記流動層ガス化炉に供給して流動媒体の旋回流を形成し、
前記可燃物を前記流動層ガス化炉に供給し、該流動層ガス化炉内の前記流動媒体の旋回流中でガス化して生成ガスを生成し、
前記生成ガスを８００℃以下になるよう保ちつつ前記流動層上方のフリーボードから前記生成ガスを排出することを特徴とする流動層ガス化炉。 In a fluidized bed gasifier that gasifies combustible materials,
The fluidized-bed gasification furnace includes a fluidizing gas dispersion mechanism for supplying, from the bottom of the fluidized-bed gasification furnace, a first fluidizing gas supplied as an upward flow from a first furnace bottom region into the furnace interior and a second fluidizing gas supplied as an upward flow from a second furnace bottom region into the furnace interior;
a hearth inclined from the first hearth region to the second hearth region;
a non-combustible material discharge port for discharging non-combustible material from the outside of the second hearth region;
supplying a fluidizing gas to the fluidized-bed gasification furnace so that the mass velocity of the first fluidizing gas is smaller than the mass velocity of the second fluidizing gas to form a swirling flow of the bed material;
The combustible material is supplied to the fluidized-bed gasification furnace and gasified in the swirling flow of the bed material in the fluidized-bed gasification furnace to generate a product gas;
A fluidized bed gasification furnace, characterized in that the generated gas is discharged from a freeboard above the fluidized bed while maintaining the generated gas at 800°C or less.
該流動層炉は、流動層の温度が４５０〜６５０℃に維持されるように温度制御され、The fluidized bed furnace is temperature-controlled so that the temperature of the fluidized bed is maintained at 450 to 650°C;
該流動層炉で生成された可燃ガス及びチャーを流動層上部のフリーボードから該熔融燃焼炉へ８００℃以下の状態で送り、該熔融燃焼炉で燃焼し灰分を熔融することを特徴とする可燃物の処理方法。A method for treating combustibles, characterized in that the combustible gas and char produced in the fluidized bed furnace are sent from the freeboard above the fluidized bed to the melting combustion furnace at a temperature of 800°C or less, and are burned in the melting combustion furnace to melt the ash.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18147896A JPH109511A (en) | 1996-06-21 | 1996-06-21 | Fluidized bed gasification and melting combustion method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18147896A JPH109511A (en) | 1996-06-21 | 1996-06-21 | Fluidized bed gasification and melting combustion method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH109511A JPH109511A (en) | 1998-01-16 |
| JPH109511A5 true JPH109511A5 (en) | 2005-06-02 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP18147896A Pending JPH109511A (en) | 1996-06-21 | 1996-06-21 | Fluidized bed gasification and melting combustion method |
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| JP (1) | JPH109511A (en) |
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| US6315390B1 (en) | 1999-04-05 | 2001-11-13 | Seiko Epson Corporation | Line ink jet head and a printer using the same |
| JP2002219417A (en) * | 2001-01-30 | 2002-08-06 | Mitsui Eng & Shipbuild Co Ltd | Fluidized bed separator for pyrolysis residue |
| JP2005055508A (en) | 2003-08-05 | 2005-03-03 | Fujikura Ltd | Optical component manufactured using grating type optical component manufacturing method, grating type optical component manufacturing apparatus, grating type optical component manufacturing method, or grating type optical component manufacturing apparatus |
| JP5694690B2 (en) * | 2010-06-22 | 2015-04-01 | 株式会社神鋼環境ソリューション | Fluidized bed furnace and waste treatment method |
| CN103238028B (en) * | 2010-11-19 | 2015-09-23 | 荏原环境工程有限公司 | Fluidized bed furnace and waste disposal method |
| JP5462214B2 (en) * | 2011-03-31 | 2014-04-02 | 株式会社神鋼環境ソリューション | Fluidized bed furnace |
| JP2015045422A (en) * | 2013-08-27 | 2015-03-12 | 株式会社Ihi | Fluidized bed boiler |
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1996
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