JP3001190B2 - Jet type internal heat low temperature carbonization equipment - Google Patents
Jet type internal heat low temperature carbonization equipmentInfo
- Publication number
- JP3001190B2 JP3001190B2 JP9130997A JP13099797A JP3001190B2 JP 3001190 B2 JP3001190 B2 JP 3001190B2 JP 9130997 A JP9130997 A JP 9130997A JP 13099797 A JP13099797 A JP 13099797A JP 3001190 B2 JP3001190 B2 JP 3001190B2
- Authority
- JP
- Japan
- Prior art keywords
- jet
- furnace
- floating
- hydrocarbon
- raw material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、噴流型内熱流動乾
留装置に関するものであり、より詳細には、所定粒度に
調整された炭化水素系原料を７００℃以下の低温乾留雰
囲気にて浮遊（浮游）乾留せしめる希薄流動層を備える
とともに、空気流又は空気／水蒸気混合気流を噴出する
流動化装置を希薄流動層の下部域に配設してなる噴流型
内熱低温乾留装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a jet-type in-situ thermal fluidized-bed apparatus, and more particularly, to floating a hydrocarbon-based raw material adjusted to a predetermined particle size in a low-temperature carbonized atmosphere of 700 ° C. or lower. The present invention relates to a jet type internal thermal low-temperature carbonization apparatus having a thin fluidized bed to be carbonized and having a fluidizing device for jetting an air stream or an air / steam mixed gas stream disposed in a lower region of the lean fluidized bed.
【０００２】[0002]
【従来の技術】空気との接触を実質的に絶たれた不完全
燃焼雰囲気において石炭を加熱し、コークス、チャー、
ガス及び／又はタール等を生成する石炭乾留法が、知ら
れている。この種の石炭乾留法は、粉砕した所定粒径範
囲の原料炭、木粉、亜炭、モミガラ等の炭化水素系原料
を乾留炉に装入し、これを乾留炉内の高温雰囲気又は焼
成雰囲気にて乾留することにより実施される。乾留炉
は、一般に、ロストルにて区画された乾留室及び燃焼室
を有し、炭化水素系原料は、給炭量を制御可能な原料ホ
ッパー及びスクリュー式フィーダーを介して乾留室に装
入される。燃焼室にて生成した高温の燃焼ガス又は熱ガ
スは、ロストルを介して乾留室内に流入する。乾留室内
の炭化水素系原料は、燃焼ガスに浮遊懸吊され、炭化水
素系原料の所謂浮遊層を形成する。高温燃焼ガスの存在
下に乾留室において急速な乾留作用を受けた炭化水素系
原料は、乾留室上部の導出管を介して乾留ガスと共に系
外に送出され、サイクロン分離器に導入され、サイクロ
ン分離器において、コーライト又は半成コークス等の炭
化製品と、乾留ガスとに分離される。2. Description of the Prior Art Coal, char, and coal are heated in an incomplete combustion atmosphere substantially free of contact with air.
BACKGROUND ART A coal carbonization method for producing gas and / or tar or the like is known. In this type of coal carbonization method, a raw material coal, wood flour, lignite, peach and other hydrocarbon-based raw materials having a predetermined particle size range is charged into a carbonization furnace, and the raw material is heated to a high-temperature atmosphere or a firing atmosphere in the carbonization furnace. It is carried out by dry distillation. A carbonization furnace generally has a carbonization chamber and a combustion chamber partitioned by a rostre, and a hydrocarbon-based raw material is charged into the carbonization chamber via a raw material hopper and a screw-type feeder capable of controlling a coal supply amount. . The high-temperature combustion gas or hot gas generated in the combustion chamber flows into the carbonization chamber via the rostr. The hydrocarbon-based raw material in the carbonization chamber is suspended in the combustion gas and forms a so-called floating layer of the hydrocarbon-based raw material. The hydrocarbon-based raw material that has undergone rapid carbonization in the carbonization chamber in the presence of the high-temperature combustion gas is sent out of the system together with the carbonization gas through the outlet pipe at the top of the carbonization chamber, introduced into the cyclone separator, and subjected to cyclone separation. In the vessel, carbonized products such as colite or semi-coke and carbonized gas are separated.
【０００３】このような形式の乾留装置が、例えば、特
公昭５０−３７２０１号公報に開示されている。同公報
に開示された乾留装置は、農林産物の廃材等を連続的に
炭化／乾留反応せしめる高速内熱炉を有し、内熱炉は、
逆錐形の内熱炉本体および炉底ボックスを備える。炉底
ボックスは、炉内領域に生成した乾留ガスの再循環流
と、空気流又は空気／水蒸気混合流とを混合するととも
に、該混合ガスを炉底部から炉内領域に吹出す。炉内に
装入された炭化水素系原料は、内熱炉の炉床部に流動床
を形成し、乾留ガス及び空気／水蒸気を含む高温の混合
ガスは、炉底ボックスより吐出し、流動床を構成する炭
化水素系原料と均一に混合する。炭化水素系原料は、混
合ガスの燃焼により加熱され、乾留反応ないし炭化反応
する。混合ガスの上昇気流により希薄流動化した炭化水
素系原料は、炉内乾留反応又は炭化反応に伴って比重を
軽減し、炉内に生成した乾留ガスを含む炉内燃焼ガス
は、乾留された炭化水素系原料、即ち、半成コークス等
の炭化製品を系外に搬送する。炭化製品及び燃焼ガス
（乾留ガス）は、炉外のサイクロン装置等に導入され、
該サイクロン装置にて分離される。[0003] A carbonization apparatus of this type is disclosed, for example, in Japanese Patent Publication No. 50-37201. The carbonization apparatus disclosed in the publication has a high-speed internal heating furnace for continuously carbonizing / carbonizing a waste material of agricultural and forestry products, etc.
It includes an inverted pyramid-shaped inner heat furnace main body and a furnace bottom box. The hearth box mixes the recirculated flow of the carbonization gas generated in the furnace interior region with the air flow or the air / steam mixture flow, and blows out the mixed gas from the furnace bottom to the furnace interior region. The hydrocarbon-based raw material charged into the furnace forms a fluidized bed on the hearth of the internal heating furnace, and the high-temperature mixed gas containing the carbonization gas and air / steam is discharged from the furnace bottom box, Is uniformly mixed with the hydrocarbon-based raw material constituting the above. The hydrocarbon-based raw material is heated by the combustion of the mixed gas and undergoes a dry distillation reaction or a carbonization reaction. The hydrocarbon-based raw material diluted and fluidized by the ascending gas flow of the mixed gas reduces the specific gravity due to the in-furnace carbonization reaction or carbonization reaction, and the in-furnace combustion gas including the in-furnace gas generated in the furnace is carbonized by the carbonization. A hydrogen-based raw material, that is, a carbonized product such as semi-coke is conveyed out of the system. Carbonized products and combustion gas (carbonized gas) are introduced into cyclone equipment outside the furnace,
Separated by the cyclone device.
【０００４】[0004]
【発明が解決しよとうする課題】しかしながら、全体的
に逆錐形に形成された内熱炉構造体を有する従来の乾留
装置においては、上方に拡開した炉内領域を上昇する燃
焼ガス又は乾留ガスの流速を所望の如く設定し難く、従
って、炉内上部域におけるガス流速の不安定化又は極端
な低下等により、十分な炭化水素系原料の炉内滞在時間
又は浮遊時間を確保し難い事情がある。また、農林産物
の廃材等に混入した石片、金属片、不燃性物質又は無機
物片等の異物、或いは、炉内に生成した燃焼灰等は、上
記炭化水素系原料と共に内熱炉の炉底部に降下し、スロ
ート部を介して炉底ボックス内に自由落下し易く、この
結果、炉底ボックスの閉塞が生じ得る。同様に、炭化水
素系原料に含まれる比較的大粒径の原料炭、或いは、乾
留反応により溶着した大粒径の原料炭等は、内熱炉の炉
底部及びスロート部を介して炉底ボックス内に自由落下
し、炉底ボックス内にて燃焼反応し、この結果、炉底ボ
ックスに配設された空気吐出ノズル又は水蒸気吐出ノズ
ルの損傷又は破損等が生じ得る。かくして、これらの炉
内落下物に対する炉底ボックスの有効な保護対策を可能
にする内熱炉構造の研究・開発が要望される。However, in a conventional carbonization apparatus having an inner heat furnace structure formed in an inverted cone shape as a whole, the combustion gas or the ascending gas which rises in the furnace area expanded upward. It is difficult to set the flow rate of the carbonization gas as desired, and therefore, it is difficult to secure sufficient residence time or floating time of the hydrocarbon-based raw material in the furnace due to instability or extreme decrease in the gas flow rate in the upper part of the furnace. There are circumstances. In addition, foreign materials such as stone chips, metal chips, incombustible substances or inorganic chips mixed in waste materials of agricultural and forestry products, or combustion ash generated in the furnace, together with the hydrocarbon-based raw materials, are placed on the bottom of the inner heat furnace. , And easily fall into the hearth box via the throat portion, and as a result, the hearth box may be closed. Similarly, the relatively large-diameter coking coal contained in the hydrocarbon-based raw material or the large-diameter coking coal deposited by the dry distillation reaction is supplied to the furnace bottom box through the furnace bottom and the throat section of the inner heat furnace. , And a combustion reaction occurs in the hearth box. As a result, damage or breakage of the air discharge nozzle or the water vapor discharge nozzle provided in the hearth box may occur. Thus, there is a need for research and development of an inner heat furnace structure that enables effective protection of the hearth box against these falling objects in the furnace.
【０００５】本発明は、かかる課題に鑑みてなされたも
のであり、その目的とするところは、所定粒度に調整さ
れた炭化水素系原料を浮遊乾留せしめる希薄流動層を備
えた噴流型内熱低温乾留装置において、炉内上部域の上
昇気流速度を定常化し、必要且つ十分な炭化水素系原料
の炉内滞在時間を確保し得る噴流型内熱低温乾留装置を
提供することにある。本発明は又は、噴流層の下部域に
配置され、空気流又は空気／水蒸気混合気流を噴出する
流動化装置を備えた噴流型内熱低温乾留装置において、
流動化装置内に自由落下する金属片等の異物、燃焼灰又
は大粒径の粗大石炭粒子等に起因する流動化装置の閉
塞、或いは、流動化装置内における粗大石炭粒子等の燃
焼による給気流ノズル等の損傷を有効に防止し、継続的
な乾留装置の連続運転を可能にする噴流型内熱低温乾留
装置を提供することを目的とする。本発明は更に、上記
構成の噴流型内熱低温乾留装置において、流動化装置内
に落下ないし流入した異物、燃焼灰又は粗大石炭粒子等
を比較的容易に系外に排出し得るとともに、乾留装置の
運転初期に先混合型バーナノズルとして機能し得る流動
化装置を備えた噴流型内熱低温乾留装置を提供すること
を目的とする。The present invention has been made in view of the above-mentioned problems, and an object of the present invention is to provide a jet-type internal low-temperature type having a thin fluidized bed for floating-distilling a hydrocarbon-based raw material adjusted to a predetermined particle size. It is an object of the present invention to provide a jet type internal thermal low-temperature carbonization apparatus capable of stabilizing an ascending air flow velocity in an upper region in a furnace and securing a necessary and sufficient stay time of a hydrocarbon-based raw material in the furnace. The present invention is also directed to a jet-type internal thermal low-temperature carbonization apparatus provided with a fluidizing device that is disposed in a lower region of a spouted bed and ejects an air stream or an air / steam mixture stream,
Blockage of the fluidizer due to foreign matter such as metal pieces that fall freely into the fluidizer, combustion ash or large-sized coarse coal particles, or supply air flow due to combustion of coarse coal particles or the like in the fluidizer. It is an object of the present invention to provide a jet type internal thermal low-temperature carbonization apparatus that effectively prevents damage to nozzles and the like and enables continuous operation of the carbonization apparatus. The present invention further provides a jet-type internal heat low-temperature carbonization apparatus having the above-described configuration, in which foreign matter, combustion ash, or coarse coal particles, which have fallen or flowed into the fluidization apparatus, can be relatively easily discharged outside the system. It is an object of the present invention to provide a jet type internal heat low-temperature carbonization apparatus equipped with a fluidization apparatus which can function as a premixing type burner nozzle at the beginning of the operation.
【０００６】[0006]
【課題を解決するための手段及び作用】上記目的を達成
するために、本発明は、所定粒度に調整された炭化水素
系原料を７００℃以下の低温乾留雰囲気により浮遊乾留
し、嵩比重が低減した粒子を炉頂部より炉外に送出する
噴流内熱低温乾留装置において、噴流型流動炉を構成す
る内熱炉(10)と、所定粒度に調整された炭化水素系原料
を前記内熱炉に装入する給炭装置(20)と、前記内熱炉の
下部域に配設された流動化装置(30)とを有し、前記内熱
炉は、噴流層を構成する逆錐形の噴流部(11)と、前記炭
化水素系原料の粒子を炉内領域に浮遊せしめ、嵩比重の
低減に要する前記粒子の炉内滞在時間を確保するための
円筒形浮遊部とを有し、前記噴流部及び浮遊部は、上下
方向に延在する連続炉内領域(14)を形成し、前記噴流部
は、下方に向かって縮径する円錐形内壁面(18)を備える
とともに、前記炭化水素系原料の粒子を上方に吹上げる
空気及び／又は水蒸気の高速給気流を吐出するスロート
部(31)を下端部収束領域に備え、前記浮遊部(12)は、該
噴流部の上位大径部分と整合し且つ一体的に連接する所
定内径の円筒状内周壁面を備え、前記高速給気流にて浮
遊した前記炭化水素系原料の粒子を自由落下に抗して炉
内領域に所要時間滞在せしめる浮遊域を前記噴流部の上
方域に画成することを特徴とする噴流型内熱低温乾留装
置を提供する。SUMMARY OF THE INVENTION In order to achieve the above object, the present invention provides a method for producing a hydrocarbon having a predetermined particle size.
Floating carbonization of system raw materials in a low-temperature carbonization atmosphere of 700 ° C or less
And send the particles with reduced bulk specific gravity out of the furnace from the furnace top
In the jet internal heat low-temperature carbonization apparatus, an internal heat furnace (10) constituting a jet-type fluidized furnace, and a coal feeder (20) for charging a hydrocarbon-based raw material adjusted to a predetermined particle size into the internal heat furnace, A fluidizing device (30) disposed in a lower region of the internal heat furnace,
The furnace has an inverted cone-shaped jet part (11) constituting a spouted bed, and particles of the hydrocarbon-based raw material are floated in the furnace area, and the bulk specific gravity is
A cylindrical floating part for securing the residence time of the particles required for reduction in the furnace, wherein the jet part and the floating part are vertically
A continuous furnace region (14) extending in the direction, the jet portion has a conical inner wall surface (18) whose diameter is reduced downward, and the particles of the hydrocarbon-based raw material are blown upward. A throat portion (31) for discharging a high-speed supply flow of raising air and / or steam is provided in a lower end converging region, and the floating portion (12) is aligned with and integrally connected to the upper large-diameter portion of the jet flow portion. The floating area above the jet section is provided with a cylindrical inner peripheral wall having a predetermined inner diameter, and the floating area in which the particles of the hydrocarbon-based raw material floating in the high-speed supply flow are allowed to stay in the furnace area for a required time against free fall. The present invention provides a jet type internal heat low-temperature carbonization apparatus characterized by being defined in an area.
【０００７】本発明の上記構成によれば、６００℃乃至
７００℃以下の内熱低温乾留工程を実行する上記内熱炉
の炉内領域は、噴流層を構成する逆錐形噴流部と、炭化
水素系原料の乾留反応を促進する円筒状浮遊部とを備え
る。給炭装置により炉内領域に装入された炭化水素系原
料粒子は、噴流部の円錐状内周面に沿って降下し、流動
化装置から上方に噴出する高速給気流にて流動化され
る。原料粒子は更に、スロート部を吹き抜ける上昇給気
流の噴出作用ないし誘引作用により炉内領域を上昇し、
該給気流にて浮遊懸吊される。上昇給気流の流速は、上
方に拡開した噴流部にて漸減するとともに、上下方向に
均等化した横断面を有する浮遊部において均一化する。
炉内領域にて浮遊乾留作用を受け、嵩比重が低減した原
料粒子は、上昇給気流により炉頂部から系外に搬出され
る。他方、依然として過大な嵩比重を有する原料粒子
は、自由落下作用により噴流部に降下し、噴流部より噴
出する高速給気流にて再び上方に吹き上げられる。原料
粒子は、かかる自由落下及び上昇運動を反復し、この結
果、適切な浮遊乾留反応の進行に伴ってコークス化する
とともに、脱揮発作用により嵩比重を低減する。かくし
て所望の嵩比重に軽減した原料粒子は、上昇給気流に搬
送され、炉頂部より系外に搬出される。かかる乾留装置
の乾留工程においては、不活性ガス（イナートガス）な
いし乾留ガス再循環流等の炉内導入は、格別に必要とさ
れない。[0007] According to the above configuration of the present invention, the inner region of the inner heat furnace for performing the internal heat low-temperature carbonization step at a temperature of 600 ° C to 700 ° C or less is provided with an inverted cone-shaped jet forming a spouted bed, A cylindrical floating portion for promoting the dry distillation reaction of the hydrogen-based raw material. The hydrocarbon-based raw material particles charged into the furnace region by the coal supply device descend along the conical inner peripheral surface of the jet part, and are fluidized by the high-speed supply flow ejected upward from the fluidization device. . The raw material particles further rise in the furnace area by a blowing action or an inducing action of the rising supply air flowing through the throat portion,
The air is suspended in the air flow. The flow rate of the ascending supply flow gradually decreases at the jet part that expands upward, and becomes uniform at the floating part having a cross section that is equalized in the vertical direction.
The raw material particles having a reduced bulk specific gravity due to the floating carbonization in the furnace region are carried out of the furnace from the furnace top by the ascending air flow. On the other hand, the raw material particles still having an excessive bulk specific gravity fall to the jet part due to the free falling action, and are blown up again by the high-speed supply flow jetted from the jet part. The raw material particles repeat such free fall and ascending movements. As a result, coke is formed as the floating carbonization reaction proceeds, and the bulk density is reduced by devolatilization. The raw material particles thus reduced to the desired bulk specific gravity are conveyed to the ascending supply airflow and are carried out of the system from the furnace top. In the carbonization step of such a carbonization apparatus, introduction of an inert gas (inert gas) or a carbonization gas recirculation flow into the furnace is not particularly required.
【０００８】本発明は又、所定粒度に調整された炭化水
素系原料を７００℃以下の低温乾留雰囲気により浮遊乾
留し、嵩比重が低減した粒子を炉頂部より炉外に送出す
る噴流内熱低温乾留装置において、噴流型流動炉を構成
する内熱炉(10)と、所定粒度に調整された炭化水素系原
料を前記内熱炉に装入する給炭装置(20)と、前記内熱炉
の下部域に配設された流動化装置(30)とを有し、前記内
熱炉は、噴流層を構成する逆錐形の噴流部(11)と、前記
炭化水素系原料の粒子を炉内領域に浮遊せしめ、嵩比重
の低減に要する前記粒子の炉内滞在時間を確保するため
の円筒形浮遊部(12)とを有し、前記噴流部及び浮遊部
は、上下方向に延在する連続炉内領域(14)を形成し、前
記噴流部は、下方に向かって縮径する円錐形内壁面(18)
を備えるとともに、空気及び／又は水蒸気の噴出気流を
吐出するスロート部(31)を下端部収束領域に備え、該噴
出気流は、前記炭化水素系原料の粒子を上方に吹上げる
ように前記スロート部を吹抜け、前記浮遊部(12)は、該
噴流部の上位大径部分と整合し且つ一体的に連接する所
定内径の円筒状内周壁面を備え、前記スロート部の下方
域に配置された流動化装置(30)は、前記スロート部と連
通する給気流混合領域を形成するハウジング(32)と、前
記給気流混合領域に開口する空気流入口(33)と、前記給
気流混合領域に上下変位可能に支持された高さ調節可能
な水蒸気供給管(36)とを備え、前記水蒸気供給管の上端
部は、前記スロート部に隣接して開口する水蒸気吐出口
(37)を備えることを特徴とする噴流型内熱低温乾留装置
を提供する。．[0008] The present invention also relates to a hydrocarbon adjusted to a predetermined particle size.
Float dry raw materials in a low-temperature carbonization atmosphere of 700 ° C or less.
And send the particles with reduced bulk specific gravity out of the furnace from the furnace top.
That the jets in the heat low temperature carbonization device, heat furnaces among constituting the jet fluidized reactor (10), coal feed device for charging into said thermal reactor hydrocarbon feedstock which has been adjusted to a predetermined grain size and (20) A fluidizing device (30) disposed in a lower region of the inner heat furnace , wherein the inner heat furnace comprises an inverted cone-shaped jet part (11) constituting a spouted bed, and the hydrocarbon-based The particles of the raw material are suspended in the furnace area, and the bulk specific gravity
Reduced required to ensure the furnace residence time of the particles
A cylindrical floating part (12), and the jet part and the floating part
Forms a continuous furnace region (14) extending in the vertical direction, and the jet portion has a conical inner wall surface (18) whose diameter decreases downward.
And a throat section (31) for discharging a jet stream of air and / or water vapor is provided in a lower end converging region, and the jet stream is configured to blow up the particles of the hydrocarbon-based raw material upward. And the floating part (12) is
A place where it is aligned with the upper large-diameter part of the jet and is integrally connected
A fluidizing device (30) having a cylindrical inner peripheral wall surface having a constant inner diameter and disposed below the throat portion includes a housing (32) forming a supply air flow mixing region communicating with the throat portion; An air inlet (33) that opens into the airflow mixing area, and a height-adjustable steam supply pipe (36) that is supported in the supply airflow mixing area so as to be vertically displaceable, and an upper end of the steam supply pipe is provided. A steam outlet opening adjacent to the throat portion
(37) A jet type internal heat low-temperature carbonization apparatus characterized by comprising (37). .
【０００９】本発明の上記構成によれば、流動化装置を
構成する水蒸気供給管は、上下変位可能に支持され、水
蒸気吐出口とスロート部との間の距離は、水蒸気供給管
の高さ調節により、適切な間隙寸法に調整される。間隙
寸法は、噴流部に自由落下し得る原料粒子又は異物等の
ハウジング内流入を適切に阻止すべく、乾留装置の運転
条件、噴出給気流の混合割合、流量又は流速、炭化水素
系原料の物性、或いは、炭化水素系原料に混入し得る異
物の寸法・種類等に応じて適宜設定される。かくて、適
切な水蒸気供給管の高さ位置調節により、流動化装置の
閉塞、或いは、給気流ノズル等の損傷は、未然に防止さ
れる。According to the above configuration of the present invention, the steam supply pipe constituting the fluidizing device is supported so as to be vertically displaceable, and the distance between the steam discharge port and the throat portion is adjusted by adjusting the height of the steam supply pipe. Thereby, the gap size is adjusted to an appropriate value. The gap size depends on the operating conditions of the carbonization apparatus, the mixing ratio of the jet air supply flow, the flow rate or flow rate, and the physical properties of the hydrocarbon-based raw material in order to appropriately prevent the flow of raw material particles or foreign matter that can freely fall into the jet part into the housing. Alternatively, it is appropriately set according to the size and type of foreign matter that can be mixed into the hydrocarbon-based raw material. Thus, by appropriately adjusting the height position of the steam supply pipe, blockage of the fluidizer or damage to the air supply flow nozzle or the like is prevented beforehand.
【００１０】本発明は更に、上記構成の噴流型内熱低温
乾留装置において、上記流動化装置のハウジング内に自
由落下した異物又は粗大粒子等を排出可能な排出装置が
上記ハウジングに連結され、該排出装置は、上記異物又
は粗大粒子等の系外排出路を選択的に開閉可能な開閉弁
装置を有することを特徴とする噴流型内熱低温乾留装置
を提供する。本発明の上記構成によれば、スロート部を
介して流動化装置内に落下した異物又は粗大石炭粒子等
は、排出装置を介して系外に排出される。しかも、流動
化装置のハウジングに連結された開閉弁装置は、乾留装
置の運転・稼働中に開放し、異物ないし粗大粒子等を系
外に導出し得る。従って、予測し難い異物又は粗大石炭
粒子等の流動化装置内落下に適切に対処すべく、乾留装
置の連続操業中に流動化装置の異物排出工程又は機能復
元工程を実行することが可能となる。According to the present invention, there is further provided a jet type internal heat low-temperature carbonization apparatus having the above-mentioned structure, wherein a discharge device capable of discharging foreign matters or coarse particles which have fallen freely into the housing of the fluidizing apparatus is connected to the housing. The discharge device is provided with an on-off valve device capable of selectively opening and closing the external discharge path for the foreign matter or coarse particles, etc., to provide a jet type internal heat low temperature carbonization device. According to the above configuration of the present invention, foreign matter, coarse coal particles, and the like that have fallen into the fluidization device via the throat portion are discharged out of the system via the discharge device. In addition, the on-off valve device connected to the housing of the fluidizing device is opened during the operation and operation of the carbonization device, and foreign matter or coarse particles can be led out of the system. Therefore, it is possible to execute the foreign matter discharging step or the function restoring step of the fluidizing apparatus during the continuous operation of the carbonization apparatus in order to appropriately cope with the foreign matter or coarse coal particles that are difficult to predict and fall in the fluidizing apparatus. .
【００１１】本発明は又、上記構成の噴流型内熱低温乾
留装置において、燃焼用炭化水素系燃料を供給する燃料
供給手段が、上記流動化装置の水蒸気供給管に連結さ
れ、該燃料供給手段は、上記乾留装置の運転初期に上記
スロート部に燃焼用燃料を供給することを特徴とする噴
流型内熱低温乾留装置を提供する。流動化装置を構成す
る水蒸気供給管には、燃焼用燃料ガス等の炭化水素系燃
料が、乾留装置の運転初期に供給され、流動化装置は、
先混合型バーナノズルとして機能する。水蒸気供給管の
水蒸気吐出口を介してスロート部に流出した燃焼用燃料
は、空気流入口を介して供給される燃焼用空気又は助燃
空気の存在下にスロート部にて燃焼反応し、運転初期段
階に炉内雰囲気を所要温度に急速に昇温せしめる燃焼火
焔をスロート部及び／又は噴流部に形成する。The present invention also provides a jet type internal heat low temperature carbonization apparatus having the above-mentioned structure, wherein a fuel supply means for supplying hydrocarbon fuel for combustion is connected to a steam supply pipe of the fluidization apparatus. The present invention provides a jet type internal heat low temperature carbonization apparatus characterized in that a fuel for combustion is supplied to the throat portion at an early stage of operation of the carbonization apparatus. Hydrocarbon-based fuel, such as fuel gas for combustion, is supplied to the steam supply pipe constituting the fluidizing device in the early stage of operation of the carbonization device, and the fluidizing device is
Functions as a premix burner nozzle. The combustion fuel that has flowed out to the throat through the steam discharge port of the steam supply pipe undergoes a combustion reaction in the throat in the presence of combustion air or combustion air supplied through the air inlet, and the initial stage of operation. A combustion flame for rapidly raising the furnace atmosphere to a required temperature is formed in the throat portion and / or the jet portion.
【００１２】[0012]
【発明の実施の形態】本発明の好適な実施形態によれ
ば、上記スロート部、噴流部及び浮遊部の間で上昇及び
下降運動を反復する炭化水素系原料粒子の嵩比重は、乾
留反応により、初期比重の１／３乃至１／４に低減す
る。上記浮遊部の内径及び全高の寸法比は、かかる嵩比
重の低減に要する炉内滞在時間を確保するように設定さ
れる。流動部及び浮遊部の炉内温度条件および原料粒子
の炉内滞在時間は、炭化水素系原料素材の粒径分布又は
炭種等に相応して適宜設定される。或る好適な実施形態
において、上記噴流部の炉内温度条件及び温度分布は、
４００乃至７００℃の範囲内の温度域、更に好適には、
４５０乃至６００℃の範囲内の温度域に設定され、上記
炉内滞留時間は、５乃至６分間程度の時間に設定され
る。According to a preferred embodiment of the present invention, the bulk specific gravity of the hydrocarbon-based raw material particles, which repeatedly rise and fall between the throat section, the jet section and the floating section, is determined by a carbonization reaction. , To １ ／ to の of the initial specific gravity. The dimensional ratio of the inner diameter and the total height of the floating portion is set so as to secure the in-furnace stay time required for reducing the bulk specific gravity. The in-furnace temperature conditions of the flowing part and the floating part and the staying time of the raw material particles in the furnace are appropriately set according to the particle size distribution of the hydrocarbon-based raw material, the type of coal, and the like. In a preferred embodiment, the temperature condition and temperature distribution in the furnace of the jet section are as follows:
A temperature range in the range of 400 to 700 ° C., more preferably,
The temperature is set in the range of 450 to 600 ° C., and the residence time in the furnace is set to about 5 to 6 minutes.
【００１３】本発明の好適な実施形態において、内熱炉
の炉内容積は、給炭量又は給炭速度と、原料炭に含有さ
れる水分量に応じた適当な容積に設定され、噴流部にお
ける縮径下端部又はスロート部の内径と、拡径上端部の
内径との寸法比、或いは、噴流部の円錐形内壁面の傾斜
角度は、内熱乾留反応の要求酸素量に相応した適切な炉
内容積及び給気流速を実現し得る値に設定される。[0013] In a preferred embodiment of the present invention, the internal volume of the internal heating furnace is set to an appropriate volume according to the amount of coal supplied or the rate of coal supply and the amount of water contained in the raw coal, and The dimensional ratio between the inner diameter of the reduced diameter lower end or the throat part and the inner diameter of the enlarged diameter upper end, or the inclination angle of the conical inner wall surface of the jet part, is appropriate for the amount of oxygen required for the internal heat carbonization reaction. It is set to a value that can realize the furnace internal volume and the supply air flow rate.
【００１４】本発明の或る好適な実施形態によれば、例
えば、１乃至３mm粒径の褐炭を原料炭とする乾留装置に
おいて、浮遊部の内径Ｄ２を基準として、噴流部の縮径
下端部又はスロート部の内径Ｄ１は、好ましくは、０．
３×Ｄ２〜０．５×Ｄ２の範囲内、更に好ましくは、
０．３５×Ｄ２〜０．４５×Ｄ２の範囲内に設定され、
噴流部の全高Ｈ１は、好ましくは、１．３×Ｄ２〜１．
７×Ｄ２の範囲内、更に好ましくは、１．４×Ｄ２〜
１．６×Ｄ２の範囲内に設定され、浮遊部の全高Ｈ２
は、好ましくは、１．７×Ｄ２〜２．１×Ｄ２の範囲
内、更に好ましくは、１．８×Ｄ２〜２．０×Ｄ２の範
囲内に設定される。噴流部及び浮遊部の寸法比及び各部
寸法は、炭化水素系原料の種別及び物性、殊に、炭種に
適した適切な炉内ガス流速を確保し得る値に設定され
る。好ましくは、噴流部の縮径下端部又はスロート部の
給気流速は、炭種及び粒径分布に相応した適切な流速域
に設定され、更に好ましくは、レイノズル数のアレン領
域に相当する流速域に設定される。本発明の更に好適な
実施形態において、浮遊部の内径Ｄ２の３乗積、即ち、
（Ｄ２）3 [ｍ3]は、給炭量 [TON/hr] ×（０．４５〜
０．６５）の範囲内に設定され、更に好適には、給炭量
×（０．５〜０．６）の範囲内に設定される。According to a preferred embodiment of the present invention, for example, in a carbonization apparatus using lignite having a particle size of 1 to 3 mm as a raw coal, a reduced-diameter lower end portion of a jet portion is determined with reference to an inner diameter D2 of a floating portion. Alternatively, the inner diameter D1 of the throat portion is preferably set to 0.1.
Within the range of 3 × D2 to 0.5 × D2, more preferably,
It is set in the range of 0.35 × D2 to 0.45 × D2,
The total height H1 of the jet is preferably 1.3 × D2-1.
7 × D2, more preferably 1.4 × D2
It is set within the range of 1.6 × D2 and the total height H2 of the floating portion
Is preferably set in the range of 1.7 × D2 to 2.1 × D2, more preferably in the range of 1.8 × D2 to 2.0 × D2. The dimensional ratio of the jet part and the floating part and the dimensions of each part are set to values that can secure the appropriate gas flow rate in the furnace suitable for the type and physical properties of the hydrocarbon-based raw material, particularly, the type of coal. Preferably, the air supply flow velocity at the reduced diameter lower end part or the throat part of the jet part is set to an appropriate flow velocity area corresponding to the coal type and the particle size distribution, and more preferably, the flow velocity area corresponding to the Allen area of the number of Reynolds nozzles. Is set to In a further preferred embodiment of the present invention, the cube of the inner diameter D2 of the floating portion, that is,
(D2) 3 [m 3 ] is the amount of coal supply [TON / hr] × (0.45-
0.65), and more preferably, within a range of coal supply amount × (0.5 to 0.6).
【００１５】本発明の他の好ましい実施形態において、
上記水蒸気供給管に接続された蒸気供給系は、供給蒸気
流量を可変制御し得る蒸気流量制御手段を有し、上記空
気流入口に連結された空気供給系は、空気導入量を可変
制御可能な空気流量制御手段を備える。蒸気流量制御手
段および空気流量制御手段は、例えば、原料炭の湿分増
加等に伴って噴流部の温度が低下したとき、相対的に水
蒸気流量を低減し且つ空気流量を増大せしめ、これによ
り、噴流部及び浮遊部の内熱反応による発生熱量を増大
させる。In another preferred embodiment of the present invention,
The steam supply system connected to the steam supply pipe has a steam flow control means capable of variably controlling the supply steam flow, and the air supply system connected to the air inlet is capable of variably controlling the amount of introduced air. Air flow control means is provided. The steam flow rate control means and the air flow rate control means, for example, when the temperature of the jet section is reduced due to an increase in the moisture content of the coking coal, relatively reduce the steam flow rate and increase the air flow rate, whereby The amount of heat generated by the internal heat reaction of the jet part and the floating part is increased.
【００１６】本発明の更に好適な実施形態によれば、上
記給炭装置の原料装入口は、上記噴流部及び浮遊部の連
接部近傍に配置され、好ましくは、浮遊部内周壁面の下
端部に配置され、炉内に導入された炭化水素系原料は、
高速の上昇給気流と干渉せずに、噴流部の逆錐形内壁面
に沿ってスロート部に流下する。本発明の或る実施形態
によれば、上記空気流入口を介して上記噴流装置内に流
入した空気流は、ハウジング内領域において旋回流を形
成し、スロート部に上昇する。スロート部にて最大線速
度を呈する空気流は、希薄流動層の形成に要する所望の
初速を確保し、スロート部にて混合した空気流及び水蒸
気流は、噴流部の内周壁面に沿って旋回半径を漸増する
上昇給気流を内熱反応域に形成する。According to a further preferred embodiment of the present invention, the raw material charging port of the coal feeder is disposed near a connecting portion between the jet part and the floating part, and preferably at a lower end part of the inner peripheral wall surface of the floating part. The hydrocarbon-based raw materials placed and introduced into the furnace are:
It flows down to the throat section along the inverted conical inner wall surface of the jet without interfering with the high-speed rising air flow. According to an embodiment of the present invention, the air flow that has flowed into the jet device through the air inlet forms a swirling flow in the region inside the housing and rises to the throat. The air flow having the maximum linear velocity at the throat section secures the desired initial velocity required for forming a thin fluidized bed, and the mixed air stream and steam flow at the throat section swirl along the inner peripheral wall of the jet section. An ascending charge flow of increasing radius is formed in the internal heat reaction zone.
【００１７】本発明の或る実施形態において、１乃至１
０mmの粒径範囲に粉砕された原料炭が内熱炉に装入され
る。炉内領域の上昇気流速度は、赤熱した最小粒径１mm
の石炭粒子の飛散又は吹き飛びを防止するとともに、最
大粒径１０mmの粒子の浮遊運動を維持・管理し得る速度
に設定される。炉内領域の上昇気流速度は、好ましく
は、０．２５乃至０．５ｍ／ｓに設定される。In one embodiment of the present invention, 1 to 1
Coking coal pulverized to a particle size range of 0 mm is charged into an internal heating furnace. The ascending air velocity in the furnace area is 1 mm, the minimum particle size that glows red.
The speed is set so as to prevent the scattering or blowing of the coal particles and maintain and manage the floating motion of the particles having a maximum particle size of 10 mm. The updraft speed in the furnace area is preferably set to 0.25 to 0.5 m / s.
【００１８】[0018]
【実施例】以下、添付図面を参照して、本発明の実施例
に係る噴流型内熱低温乾留装置について、詳細に説明す
る。図１は、本発明の実施例に係る乾留装置の全体構成
を示す概略縦断面図であり、図２及び図３は、図１に示
す乾留装置のウィンドボックス構造及びスロート部構造
を示す横断面図及び縦断面図である。乾留装置１は、噴
流型流動炉を構成する内熱炉１０と、内熱炉１０に対し
て原料石炭を装入する給炭装置２０と、内熱炉１０の炉
底部に連結されたウィンドボックス３０と、ウィンドボ
ックス内の異物等を系外に排出する排出装置４０と、内
熱炉１０の上部域と連通するサイクロンホッパー５０と
を備える。乾留装置１による乾留操作又は乾留工程は、
燃焼反応を完結し得ない酸素不足又は低酸素濃度の不完
全燃焼反応により、石炭粒を所定温度範囲に加熱し、賦
活／炭化するためのものであり、内熱炉１０に導入され
る燃焼用空気流量は、炉内燃焼反応に要する理論空気比
未満の所定空気比に規制される。従って、給炭装置２０
を介して内熱炉１０内に装入された石炭粒は、完全燃焼
に要する空気比又は酸素濃度に達しない不完全燃焼雰囲
気において部分燃焼し、発熱する。かかる部分燃焼反応
は、石炭粒の燃焼反応により生成する徴粉炭、タール、
揮発分及び熱分解ガスと、ウィンドボックス３０より噴
出する上昇気流中の酸素との燃焼反応（酸化反応)によ
り助勢され、この結果、外部又は外界からの熱補給を実
質的に要しない部分燃焼反応、即ち、内熱反応が生起し
且つ維持される。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a perspective view showing a jet type internal low-temperature carbonization apparatus according to an embodiment of the present invention. FIG. 1 is a schematic vertical sectional view showing an entire configuration of a carbonization apparatus according to an embodiment of the present invention. FIGS. 2 and 3 are cross-sectional views showing a wind box structure and a throat structure of the carbonization apparatus shown in FIG. It is a figure and a longitudinal cross-sectional view. The carbonization apparatus 1 includes an inner heat furnace 10 constituting a jet flow furnace, a coal feeder 20 for charging raw coal into the inner heat furnace 10, and a wind box connected to a furnace bottom of the inner heat furnace 10. 30, a discharge device 40 that discharges foreign matter and the like in the wind box to the outside of the system, and a cyclone hopper 50 that communicates with an upper region of the internal heating furnace 10. The carbonization operation or the carbonization step by the carbonization apparatus 1 includes:
This is for heating coal particles to a predetermined temperature range and activating / carbonizing them by an oxygen-deficient or low-oxygen concentration incomplete combustion reaction that cannot complete the combustion reaction. The air flow rate is regulated to a predetermined air ratio less than the stoichiometric air ratio required for the in-furnace combustion reaction. Therefore, the coal feeder 20
The coal particles charged into the inner heat furnace 10 through the air burn partially in an incomplete combustion atmosphere that does not reach an air ratio or an oxygen concentration required for complete combustion and generate heat. Such a partial combustion reaction is made of coal dust, tar,
The combustion reaction (oxidation reaction) between the volatile matter and the pyrolysis gas and oxygen in the updraft jetted from the wind box 30 assists, and as a result, the partial combustion reaction that does not substantially require external or external heat supply. That is, an internal heat reaction occurs and is maintained.
【００１９】給炭装置２０は、原料石炭供給系に連結さ
れた給炭バンカー２１と、原料バンカー２１の下部域に
配置されたスクリュー式フィーダー２２とを備える。原
料石炭を受入れ可能な原炭受入装置（図示せず）に供給
された炭化水素系原料は、一次乾燥装置（図示せず）に
て所定の含水率、例えば、５％程度の含水率に水分量を
調整された後、粉砕機（図示せず）により所定粒径、例
えば、１０mm以下の粒径の炭化水素系原料に粉砕され、
しかる後、バケット・エレベ−タ−及び振動式フィ−ダ
−等を含む原料搬送装置（図示せず）により給炭バンカ
ー２１に投入される。スクリュー式フィーダー２２は、
螺旋形態の羽根部を有する回転スクリュー２３を備え、
回転スクリュー２３は、回転駆動装置２４に連結され
る。回転駆動装置２４は、給炭量制御装置（図示せず）
の制御下に作動する電動モータ及び減速機を備えてお
り、回転スクリュー５を所定速度で回転させる。かくし
て、給炭装置２０は、１０mm以下の所定粒度分布を有す
る粉砕炭を所定の給炭速度にて内熱炉１０内に装入す
る。The coal feeder 20 includes a coal feed bunker 21 connected to a raw coal supply system, and a screw feeder 22 disposed in a lower region of the raw coal bunker 21. The hydrocarbon-based raw material supplied to the raw coal receiving device (not shown) capable of receiving the raw coal is reduced to a predetermined moisture content, for example, about 5% by a primary drying device (not shown). After the amount is adjusted, it is pulverized by a pulverizer (not shown) into a hydrocarbon-based raw material having a predetermined particle size, for example, a particle size of 10 mm or less,
Thereafter, the raw material is charged into the coal supply bunker 21 by a raw material transporting device (not shown) including a bucket elevator, a vibratory feeder and the like. The screw type feeder 22
A rotary screw 23 having a helical blade,
The rotation screw 23 is connected to a rotation driving device 24. The rotation drive device 24 is a coal supply amount control device (not shown)
The electric motor and the speed reducer which operate under the control described above are provided, and the rotary screw 5 is rotated at a predetermined speed. Thus, the coal feeding device 20 charges the pulverized coal having a predetermined particle size distribution of 10 mm or less into the internal heating furnace 10 at a predetermined feeding speed.
【００２０】内熱炉１０は、逆錐形の噴流部１１及び直
胴形の浮遊部１２を備え、スクリュー式フィーダー２２
の吐出口２５は、噴流部１１及び浮遊部１２の連接部近
傍に配置され、浮遊部１２の下端部内周面に開口する。
内熱炉１０の壁体は、鋼板等の金属材料にて成形され、
噴流部１１及び浮遊部１２の内壁面１８、１９は、耐熱
性キャスタブル・ライニング材料、耐熱レンガ、耐火・
断熱レンガ又は耐熱性セラミックス材料等の各種耐火・
耐熱性被覆材にて被覆され、上下方向に延在する連続炉
内領域１４を画成する。噴流部１１は、全体的に逆錐形
に形成され、下方に向かって所定角度をなして縮径ない
し収束する錐面１８を炉内に形成し、ウィンドボックス
３０のスロート部３１が、噴流部１１の下端部に開口す
る。他方、浮遊部１２は、全体的に円筒形に形成され、
実質的に均一な内径を有する内周壁面１９を有し、耐火
ダクト５１の流入口５２に接続可能な導出ポート１５
が、浮遊部１２の炉頂部中央領域に配設される。スロー
ト部３１に隣接する噴流部１１の下端部内径Ｄ１と、噴
流部１１の上端部内径（浮遊部１２の内径）Ｄ２との寸
法比Ｄ１：Ｄ２は、Ｄ１：Ｄ２＝（０．３５〜０．４
５）：１の範囲内の所定比率に設定され、噴流部１１の
全高Ｈ１と浮遊部１２の全高Ｈ２との寸法比Ｈ１：Ｈ２
は、Ｈ１：Ｈ２＝（０．７５〜０．８５）：１の範囲内
の所定比率に設定される。また、上記高さ寸法Ｈ１は、
Ｈ１＝（１．４〜１．６）×Ｄ２の範囲内の所定値に設
定される。The internal heating furnace 10 has an inverted conical jet part 11 and a straight-body floating part 12, and a screw type feeder 22.
The discharge port 25 is disposed in the vicinity of the connection between the jet part 11 and the floating part 12 and opens at the inner peripheral surface at the lower end of the floating part 12.
The wall of the inner heat furnace 10 is formed of a metal material such as a steel plate,
The inner wall surfaces 18 and 19 of the jet part 11 and the floating part 12 are made of heat-resistant castable lining material, heat-resistant brick,
Various fireproof materials such as insulating bricks or heat-resistant ceramic materials
It defines a continuous furnace interior region 14 that is covered with a heat-resistant coating material and extends vertically. The jet part 11 is formed in the shape of an inverted cone as a whole, and forms a conical surface 18 converging or converging at a predetermined angle downward in the furnace, and the throat part 31 of the wind box 30 11 is opened at the lower end. On the other hand, the floating portion 12 is formed in a generally cylindrical shape,
An outlet port 15 having an inner peripheral wall 19 having a substantially uniform inner diameter and being connectable to an inlet 52 of a refractory duct 51.
Is disposed in the center region of the furnace top of the floating portion 12. The dimensional ratio D1: D2 between the lower end inner diameter D1 of the jet part 11 adjacent to the throat part 31 and the upper end inner diameter (inner diameter of the floating part 12) D2 of the jet part 11 is D1: D2 = (0.35-0) .4
5) The ratio is set to a predetermined ratio within the range of 1: 1, and the dimensional ratio H1: H2 between the total height H1 of the jet part 11 and the total height H2 of the floating part 12 is set.
Is set to a predetermined ratio in the range of H1: H2 = (0.75 to 0.85): 1. The height dimension H1 is:
H1 is set to a predetermined value within the range of (1.4 to 1.6) × D2.
【００２１】図２及び図３に示す如く、ウィンドボック
ス３０は、内熱炉１０と実質的に同一の耐火・耐熱構造
を有するハウジング３２と、ハウジング３２の周壁及び
底壁に配設された空気導入口３３及び蒸気導入装置３４
とを備える。ハウジング３２の内壁面は、噴流部１１及
び浮遊部１２と同様に、所定の耐火・耐熱性被覆材にて
被覆される。スロート部３１及びハウジング３２の中心
軸線は、内熱炉１０の中心軸線と一致し、ハウジング３
２内の給気流混合領域３５及びスロート部３１の噴流ポ
ートは、内熱炉１０の中心軸線を中心とする円形の横断
面形状を有する。As shown in FIGS. 2 and 3, the wind box 30 includes a housing 32 having substantially the same fire-resistant and heat-resistant structure as the internal heating furnace 10, and air provided on a peripheral wall and a bottom wall of the housing 32. Inlet 33 and steam inlet 34
And The inner wall surface of the housing 32 is coated with a predetermined fire-resistant and heat-resistant coating material, similarly to the jet part 11 and the floating part 12. The center axes of the throat portion 31 and the housing 32 coincide with the center axis of the internal heating furnace 10 and the housing 3
The supply air mixing region 35 and the jet port of the throat portion 31 in the inside 2 have a circular cross-sectional shape centered on the central axis of the internal heating furnace 10.
【００２２】ウィンドボックス３０の内周壁面に開口す
る空気導入口３３は、空気流量制御弁３９を備えた空気
導入管路ＯＡ（仮想線で示す）に連結され、所定流速の
空気流を実質的に水平にウィンドボックス３０内に導入
する。また、蒸気導入装置３４は、ウィンドボックス３
０の中心軸線を中心に垂直に配向された蒸気導入管３６
を備える。蒸気導入管３６は、ウィンドボックス３０の
傾斜底壁４１を貫通する円筒形垂直ガイド３８に気密状
態に支持され、給気流混合領域３５内に突出する。垂直
ガイド３８は、蒸気導入管３６の管体を上下変位可能に
支持する。ウィンドボックス３０から垂下する蒸気導入
管３６の下端部は、蒸気流量制御弁４５を介装した水蒸
気給送管路ＳＴ（仮想線で示す）に連結され、蒸気導入
管３６の上端部は、スロート部３１から所定間隔を隔て
て位置決めされた蒸気吐出口３７を備える。蒸気吐出口
３７は、水蒸気給送管路ＳＴにより供給された水蒸気を
上方に吐出する先端ノズルとして機能するとともに、ス
ロート部３１に対向する拡大部分を有し、流路面積を調
節可能な環状流路をスロート部３１及び蒸気吐出口３７
の間に画成する。An air inlet 33 opened on the inner peripheral wall surface of the wind box 30 is connected to an air inlet pipe OA (shown by a phantom line) provided with an air flow control valve 39 to substantially supply air at a predetermined flow rate. Into the wind box 30 horizontally. In addition, the steam introduction device 34 is
Vapor inlet pipe 36 oriented vertically about a central axis of zero
Is provided. The steam introduction pipe 36 is airtightly supported by a cylindrical vertical guide 38 penetrating the inclined bottom wall 41 of the wind box 30, and projects into the supply air mixing area 35. The vertical guide 38 supports the pipe of the steam introduction pipe 36 so as to be vertically displaceable. The lower end of the steam inlet pipe 36 hanging from the wind box 30 is connected to a steam feed line ST (shown by a phantom line) provided with a steam flow control valve 45, and the upper end of the steam inlet pipe 36 is a throat. A steam outlet 37 positioned at a predetermined distance from the section 31; The steam discharge port 37 functions as a tip nozzle that discharges the steam supplied from the steam supply pipe ST upward, has an enlarged portion facing the throat portion 31, and has an annular flow path whose flow path area can be adjusted. The throat section 31 and the steam outlet 37
Define between.
【００２３】ウィンドボックス３０の傾斜底壁４１は、
給気流混合領域３５内の異物、例えば、石炭原料に混入
した金属片、或いは、比較的大粒径の石炭粒塊等を系外
に排出する導出ノズル４２に連続する。排出装置４０を
構成する導出ノズル４２は、手動開閉操作可能なガスロ
ックダンパー又はロータリーバルブ等の開閉弁装置４３
に接続される。所望により、開閉弁装置４３の弁本体
は、弁体を開閉作動する開閉駆動装置（図示せず）に作
動的に連結され、開閉弁装置４３の流出端４４は、給気
流混合領域３５内の異物を排出可能な排出手段に連結さ
れる。The inclined bottom wall 41 of the wind box 30
The foreign matter in the air-flow mixing region 35, for example, a metal piece mixed in a coal raw material, or a coal particle lump having a relatively large particle diameter, etc., continues to the discharge nozzle 42 for discharging the coal to the outside. The outlet nozzle 42 constituting the discharge device 40 is provided with an opening / closing valve device 43 such as a gas lock damper or a rotary valve that can be manually opened / closed.
Connected to. If desired, the valve body of the on-off valve device 43 is operatively connected to an on-off drive device (not shown) that opens and closes the valve element. It is connected to a discharging means capable of discharging foreign matter.
【００２４】図１に示す如く、内熱炉１０の頂部導出ポ
ート１５に接続された耐火ダクト５１は、サイクロンホ
ッパー５０の上部流入ポート５３に連結される。下方に
収束する逆錐形態のサイクロンホッパー５０は、乾留ガ
スを系外に給送する乾留ガス送出ポート５４と、半成コ
ークスを導出するコークス導出ポート又はシュートノズ
ル５５とを備える。サイクロンホッパー５０の頂壁に配
置された乾留ガス送出ポート５４は、乾留ガスダクト５
６に連結され、乾留ガスダクト５６は、系外の燃焼装
置、乾留ガス回収装置又は乾留ガス循環装置等に接続さ
れる。他方、シュートノズル５５は、半成コークス送出
管路５７に連結され、半成コークス送出管路５７は、半
成コークスを回収するコ−クス回収装置（図示せず）に
接続される。As shown in FIG. 1, the refractory duct 51 connected to the top outlet port 15 of the inner heat furnace 10 is connected to the upper inlet port 53 of the cyclone hopper 50. The cyclone hopper 50 in the form of an inverted cone that converges downward includes a carbonized gas delivery port 54 for supplying the carbonized gas to the outside of the system, and a coke discharge port or chute nozzle 55 for discharging semi-coke. The carbonized gas delivery port 54 arranged on the top wall of the cyclone hopper 50 is connected to the carbonized gas duct 5.
The carbonization gas duct 56 is connected to a combustion device, a carbonization gas recovery device, a carbonization gas circulation device, or the like outside the system. On the other hand, the chute nozzle 55 is connected to a semi-coke delivery line 57, and the semi-coke delivery line 57 is connected to a coke recovery device (not shown) for recovering the semi-coke.
【００２５】次に、上記乾留装置１の作動について説明
する。原炭受入装置に供給された炭化水素系原料は、一
次乾燥装置において所定の含水率に調整され、粉砕機に
て所定粒径、例えば、１０mm以下の粒径に粉砕された
後、原料搬送装置により給炭バンカー２１内に投入され
る。スクリュー式フィーダー２２は、回転駆動装置２４
の作動により回転スクリュー２３を回転させ、所定の給
炭速度にて原料炭を内熱炉１０の炉内領域１４に装入
し、原料炭は、噴流部１１の円錐状内周面１８に沿って
降下する。空気導入管路ＯＡは、例えば、外界雰囲気の
常態空気を圧送し、空気導入口３３は、比較的高速の空
気流をウィンドボックス３０の給気流混合領域３５内に
吐出する。空気流は、蒸気導入管３６の外周領域を旋回
し、スロート部３１の狭小流路に向かって上昇する。水
蒸気給送管路ＳＴは、常圧下に生成した水蒸気を圧送
し、蒸気吐出口３７は、比較的高速の水蒸気流をスロー
ト部３１の狭小流路に向かって上方に吐出する。スロー
ト部３１において、空気流及び水蒸気流の混合気流が形
成され、該混合気流は、流動化剤として、噴流部１１内
に流入し、円錐状内周面１８に沿って下降する原料炭を
誘引し、該原料炭を上方に吹き上げる。原料炭は、空気
／水蒸気混合気流に同伴し、炉内領域１４にて浮遊し、
上昇する。Next, the operation of the carbonization apparatus 1 will be described. The hydrocarbon-based raw material supplied to the raw coal receiving device is adjusted to a predetermined moisture content in a primary drying device, crushed to a predetermined particle size by a crusher, for example, a particle size of 10 mm or less, and then fed to a raw material transfer device. Is charged into the coal bunker 21. The screw-type feeder 22 includes a rotary drive 24
By rotating the rotary screw 23 by the operation of the above, the raw coal is charged into the furnace region 14 of the internal heating furnace 10 at a predetermined coal feeding speed, and the raw coal is transferred along the conical inner peripheral surface 18 of the jet section 11. To descend. The air introduction pipe OA supplies, for example, normal air of the outside atmosphere under pressure, and the air introduction port 33 discharges a relatively high-speed air flow into the supply air mixing area 35 of the wind box 30. The air flow turns around the outer peripheral area of the steam introduction pipe 36 and rises toward the narrow flow path of the throat portion 31. The steam supply line ST feeds steam generated under normal pressure, and the steam discharge port 37 discharges a relatively high-speed steam flow upward toward the narrow flow path of the throat section 31. In the throat portion 31, a mixed airflow of an air flow and a steam flow is formed, and the mixed airflow flows into the jetting portion 11 as a fluidizing agent, and attracts the raw coal that descends along the conical inner peripheral surface 18. Then, the raw coal is blown up. The coking coal is entrained in the air / steam mixture stream and floats in the furnace area 14,
To rise.
【００２６】噴流部１１の温度は、低温乾留反応におい
て一般に必要とされる温度、即ち、４５０乃至７００℃
の範囲内の温度域に設定され、原料炭の炉内滞留時間
は、十分な乾留作用の進行を確保し得る時間、例えば、
約５乃至６分程度の時間に設定される。温度条件及び滞
留時間等の運転条件は、空気導入口３３及び蒸気吐出口
３７の空気流量及び水蒸気流量により可変制御され、炭
種に相応して適当に設定変更される。The temperature of the jet 11 is a temperature generally required in a low-temperature carbonization reaction, that is, 450 to 700 ° C.
Is set in a temperature range within the range, the coking coal residence time in the furnace is a time that can ensure the progress of sufficient carbonization, for example,
The time is set to about 5 to 6 minutes. The operating conditions such as the temperature condition and the residence time are variably controlled by the air flow rate and the steam flow rate of the air inlet 33 and the steam discharge port 37, and are appropriately set and changed according to the type of coal.
【００２７】炉内領域１４の水平断面積は、上方に拡開
する噴流部１１の形態に相応して増大するので、混合気
流の流速は、上方域に移行するにつれて漸減し、この結
果、混合気流中に浮遊した原料炭の上昇速度は低下し、
ついには、上昇速度を維持し得ず、重力作用により下降
する。降下した原料炭は、スロート部３１から噴出する
比較的高速の上昇混合気流により、再び上昇し、かくし
て、原料炭は、炉内領域１４にて上昇運動及び降下運動
を反復する。スロート部３１、噴流部１１及び浮遊部１
２の間における原料炭の上下動ないし浮遊運動の間に、
内熱が原料炭に伝熱し、原料炭は、乾留作用及び脱揮発
作用によりコークス化する。Since the horizontal cross-sectional area of the in-furnace region 14 increases in accordance with the shape of the jet part 11 expanding upward, the flow rate of the mixture gas gradually decreases as it moves to the upper region. The rising speed of the coking coal suspended in the air flow decreases,
Eventually, the ascending speed cannot be maintained and descends due to gravity. The lowered coking coal rises again by the relatively high-speed rising mixture gas jetted from the throat section 31, and thus the coking coal repeats the rising motion and the falling motion in the furnace region 14. Throat part 31, jet part 11, and floating part 1
During the vertical movement or floating movement of the coking coal between the two,
The internal heat is transferred to the coking coal, and the coking coal is coke by the carbonization and devolatilization.
【００２８】原料炭の嵩比重は、コークス化反応に伴っ
て低減し、初期の原炭嵩比重の１／３乃至１／４に減少
する。軽量化した原料炭は、浮遊部１２の上昇混合気流
により押上げられ、内熱反応により生成した乾留ガス
（分解ガス及び燃焼ガス) と一緒に、頂部導出ポート１
５、耐火ダクト５１及び上部流入ポート５３を介して、
サイクロンホッパー５０に流入する。内熱炉１０の乾留
作用により半成コークス化した原料炭は、サイクロンホ
ッパー５０における旋回流円心分離作用により、乾留ガ
スから分離され、半成コークスとしてシュートノズル５
５及び半成コークス送出管路５７により系外に導出さ
れ、回収装置にて回収される。他方、サイクロンホッパ
ー５０にて分離された乾留ガスは、乾留ガスダクト５６
を介して系外の乾留ガス回収装置又は乾留ガス循環装置
等に給送される。[0028] The bulk specific gravity of the raw coal decreases with the coking reaction and decreases to 1/3 to 1/4 of the initial bulk density of the raw coal. The light-weight coking coal is pushed up by the rising mixed gas flow in the floating portion 12 and is supplied to the top outlet port 1 together with the dry distillation gas (decomposed gas and combustion gas) generated by the internal heat reaction.
5, via the refractory duct 51 and the upper inflow port 53,
It flows into the cyclone hopper 50. The raw coal converted into semi-coke by the dry distillation operation of the internal heating furnace 10 is separated from the dry distillation gas by the swirling flow centrifugal separation operation in the cyclone hopper 50, and is converted into semi-coke by the chute nozzle 5.
5 and the semi-coke delivery line 57 lead out of the system and are recovered by a recovery device. On the other hand, the carbonized gas separated in the cyclone hopper 50 is supplied to the carbonized gas duct 56.
Is supplied to a dry distillation gas recovery device or a dry distillation gas circulating device outside the system.
【００２９】実運転において、石片、鉄片、ボルト、ナ
ット、或いは、各種金属塊等の異物が原料炭に混入して
おり、このような異物は、一般に、嵩比重が大きく、従
って、原料炭と一緒に炉内領域１４に装入された異物
は、噴流部１１を降下し、スロート部３１を介してウィ
ンドボックス３０内に落下し得る。また、原料炭に含有
され、或いは、乾留作用に伴う溶着現象により炉内領域
１４にて生成した比較的大粒径の原料炭も又、上記異物
と同様に噴流部１１を降下し、スロート部３１を介して
ウィンドボックス３０内に落下し、給気流混合領域３５
に堆積し得る。ウィンドボックス３０内に自由落下した
異物は、給気流混合領域３５の閉塞を生じさせる虞があ
り、また、ウィンドボックス３０内に落下した大粒径原
料炭は、給気流混合領域３５にて燃焼反応し、空気導入
口３３及び蒸気導入管３６の損傷又は破損等をもたらす
懸念があり、従って、これらの落下物は、乾留装置の連
続運転を阻害し得る。In actual operation, foreign materials such as stone pieces, iron pieces, bolts, nuts, and various metal lumps are mixed in the raw coal. Such foreign materials generally have a large bulk specific gravity, and The foreign matter charged into the furnace interior 14 together with the mist may descend the jet part 11 and fall into the wind box 30 via the throat part 31. In addition, the relatively large-diameter coking coal contained in the coking coal or generated in the furnace region 14 due to the welding phenomenon due to the carbonization action also descends the jet 11 in the same manner as the foreign matter, and the throat is formed. 31, falls into the wind box 30,
Can be deposited. Foreign matter that has fallen freely into the wind box 30 may cause blockage of the airflow mixing region 35, and large-diameter coking coal that has fallen into the windbox 30 may cause combustion reaction in the airflow mixing region 35. However, there is a concern that the air inlet 33 and the steam inlet pipe 36 may be damaged or broken, and therefore, these falling objects may hinder the continuous operation of the carbonization apparatus.
【００３０】本実施例において、円筒形垂直ガイド３８
により上下変位可能に支持された蒸気導入管３６は、適
切な蒸気導入管３６の高さ調整により、先端ノズル３７
とスロート部３１との間の距離を所望の如く調整し得
る。適切な蒸気導入管３６の高さ設定の結果、上記異物
及び上記大粒径原料炭のウィンドボックス３０内落下を
防止し得るとともに、適切な混合気流速度を確保し得る
適当な流路面積の間隙が、先端ノズル３７の外周領域に
形成される。かくして、異物又は大粒径原料炭のウィン
ドボックス内落下を未然に防止し、乾留装置１の連続操
業を確保することが可能となる。また、長時間の連続運
転によりウィンドボックス３０内に落下し得る予期せぬ
異物又は大径原料炭、或いは、燃焼灰等は、導出ノズル
４２を介してウィンドボックス３０に連結された開閉弁
装置４３の開放により、系外に排出される。開閉弁装置
４３は、乾留装置１の運転中に開閉作動し得るので、継
続的な乾留装置１の連続操業を確保しつつ、ウィンドボ
ックス３０内の堆積物を系外に導出することができる。In the present embodiment, the cylindrical vertical guide 38
The steam introduction pipe 36 supported so as to be vertically displaceable by the nozzle can be adjusted by adjusting the height of the steam introduction pipe 36 appropriately.
The distance between and the throat portion 31 can be adjusted as desired. As a result of the appropriate setting of the height of the steam introduction pipe 36, the foreign matter and the large-diameter coking coal can be prevented from falling into the wind box 30, and the gap having an appropriate flow area can ensure an appropriate mixed gas flow velocity. Are formed in the outer peripheral area of the tip nozzle 37. In this way, it is possible to prevent foreign matter or large-diameter coking coal from falling in the wind box, and to ensure continuous operation of the carbonization apparatus 1. In addition, unexpected foreign matter or large-diameter coking coal or combustion ash that may fall into the wind box 30 due to long-time continuous operation is supplied to the open / close valve device 43 connected to the wind box 30 through the outlet nozzle 42. Is discharged out of the system by opening the. The on-off valve device 43 can open and close during the operation of the carbonization device 1, so that the sediment in the wind box 30 can be led out of the system while ensuring continuous operation of the carbonization device 1.
【００３１】更に、乾留装置の連続運転の間に、原料炭
の湿分増加等に起因する噴流部１１の温度低下が生じた
とき、蒸気導入装置３４の水蒸気供給量を制限ないし低
減するとともに、空気導入口３３の空気導入量を相対的
に増大せしめ、これにより、内熱反応による炉内発生熱
量を増大させ、炉内温度を上昇させることができる。ま
た、乾留装置の運転開始時期に必要とされる昇温時に
は、過渡的に蒸気導入管３６に炭化水素系燃料ガスを導
入し、蒸気導入管３６を炉内昇温バーナーとして使用し
得る。なお、パイロットバーナー及び燃料供給制御弁等
の付帯設備が、蒸気導入管３６に関連して適宜配設され
るが、これらの付帯設備については、図を簡略化するた
めに図示を省略してある。Further, when the temperature of the jet section 11 decreases due to an increase in the moisture content of the coking coal during the continuous operation of the dry distillation apparatus, the amount of steam supplied from the steam introducing apparatus 34 is limited or reduced. The amount of air introduced into the air inlet 33 is relatively increased, whereby the amount of heat generated in the furnace due to the internal heat reaction can be increased, and the temperature in the furnace can be increased. In addition, at the time of temperature increase required at the start of operation of the carbonization apparatus, a hydrocarbon-based fuel gas can be transiently introduced into the steam introduction pipe 36, and the steam introduction pipe 36 can be used as a furnace heating burner. Ancillary facilities such as a pilot burner and a fuel supply control valve are appropriately arranged in relation to the steam introduction pipe 36, but these ancillary facilities are omitted from the drawings to simplify the drawing. .
【００３２】以上説明した如く、本実施例の乾留装置１
は、噴流型流動炉を構成する内熱炉１０と、所定粒度に
調整された原料炭を内熱炉１０に装入する給炭装置２０
と、内熱炉１０の下部域に配設された流動化装置、即
ち、ウィンドボックス３０とを備え、内熱炉１０の炉内
領域は、噴流層を構成する逆錐形の噴流部１１と、原料
炭粒子を炉内領域に浮遊せしめ、該粒子の所要の炉内滞
在時間を確保する円筒形浮遊部１２とにより構成され
る。噴流部１１は、下方に向かって縮径する円錐形内壁
面１８を備えるとともに、原料炭粒子を上方に吹上げ可
能な空気及び水蒸気の高速給気流を吐出するスロート部
３１を下端部収束領域に備える。浮遊部１２は、噴流部
１１の上位大径部分と整合し且つ一体的に連接するとと
もに、空気及び水蒸気の高速給気流にて浮遊した原料炭
粒子を自由落下に抗して炉内領域に所要時間滞在せしめ
る浮遊域を噴流部１１の上方域に画成する。スロート部
３１の下方域に配置されたウィンドボックス３０は、ス
ロート部３１と連通する給気流混合領域を形成するハウ
ジング３２と、ハウジング３２に開口する空気導入口３
３と、給気流混合領域に上下変位可能に支持された高さ
調節可能な蒸気導入管３６とを備え、蒸気導入管３６の
上端部は、スロート部３１に隣接して開口する先端ノズ
ル３７を備える。ハウジング内の異物又は粗大粒子等を
排出可能な排出装置４０がハウジング３２に連結され、
排出装置４０は、異物又は粗大粒子の系外排出路を選択
的に開閉可能な開閉弁装置４３を有する。As described above, the carbonization apparatus 1 of the present embodiment is used.
Is an inner heat furnace 10 constituting a jet-type fluidized-bed furnace, and a coal feeder 20 for charging coking coal adjusted to a predetermined particle size into the inner heat furnace 10.
And a fluidizing device disposed in a lower region of the inner heat furnace 10, that is, a wind box 30. The furnace region of the inner heat furnace 10 includes an inverted cone-shaped jet portion 11 forming a spouted bed. And a cylindrical floating portion 12 for suspending the raw coal particles in the furnace region and securing a required stay time of the particles in the furnace. The jet portion 11 has a conical inner wall surface 18 whose diameter is reduced downward, and a throat portion 31 that discharges a high-speed supply air flow of air and water vapor capable of blowing up the raw coal particles upward to a lower end converging region. Prepare. The floating part 12 is aligned with the upper large-diameter part of the jet part 11 and connected integrally therewith, and is required in the furnace area against the free fall of the raw coal particles suspended by the high-speed air and steam supply airflow. A floating area for staying for a time is defined above the jetting section 11. A wind box 30 disposed below the throat portion 31 includes a housing 32 forming a supply air flow mixing region communicating with the throat portion 31, and an air inlet 3 opening in the housing 32.
3 and a height-adjustable steam introduction pipe 36 supported vertically displaceable in the supply air mixing area, and the upper end of the steam introduction pipe 36 has a tip nozzle 37 that opens adjacent to the throat section 31. Prepare. A discharge device 40 capable of discharging foreign matters or coarse particles in the housing is connected to the housing 32,
The discharge device 40 has an on-off valve device 43 that can selectively open and close a discharge path for foreign matter or coarse particles outside the system.
【００３３】かかる構成の乾留装置１によれば、逆錐形
噴流部１１は、内熱反応の急激な進行により比較的多量
の乾留ガスを生成し且つ比較的大きな燃焼発熱を生起す
るのに対し、円筒形浮遊部１２においては、層高に比例
して炉内生成ガス量が増量することなく、しかも、熱放
散によりガス膨張作用が低下する結果、上昇気流のガス
流速が安定し、実質的に一定の上昇ガス流の速度分布が
得られる。従って、内熱炉全体が逆錐形に形成された従
来構造の乾留装置と対比し、炉内乾留作用により生成し
た浮遊半成コークスは、円筒形浮遊部１２に比較的長時
間滞留し、乾留反応の進行に伴う嵩比重の減少に従って
順次、上昇気流に同伴し、炉外に送出される。かかる浮
遊部１２の適切な寸法設定により、乾留工程の定性的な
制御をなし得るので、石炭の種類に相応して浮遊部１２
の全高を演算ないし推算し、原料炭粒の所望の炉内滞留
時間を確保することができ、しかも、酸素不足の雰囲気
下に十分な浮遊・流動操作及び内熱伝熱作用を発揮する
比較的簡素な内熱炉構造を提供し得るので、均一且つ安
価な半成コークスを大量生産することが可能となる。According to the carbonization apparatus 1 having such a configuration, the inverted conical jet section 11 generates a relatively large amount of carbonized gas due to rapid progress of the internal heat reaction and generates relatively large combustion heat. In the cylindrical floating portion 12, the amount of gas generated in the furnace does not increase in proportion to the bed height, and the gas expansion action is reduced by heat dissipation. A constant velocity distribution of the rising gas flow is obtained. Therefore, in contrast to the conventional structure of the carbonization apparatus in which the entire inner heat furnace is formed in the shape of an inverted cone, the floating semi-coke generated by the carbonization action in the furnace stays in the cylindrical floating portion 12 for a relatively long time, and As the bulk specific gravity decreases with the progress of the reaction, it is sequentially sent out of the furnace together with the rising airflow. By appropriately setting the size of the floating portion 12, qualitative control of the carbonization process can be performed.
The total height of the coal is calculated or estimated, and the desired residence time of the raw coal particles in the furnace can be ensured. In addition, a sufficient floating / fluidizing operation and an internal heat transfer effect can be exhibited in an oxygen-deficient atmosphere. Since a simple internal heating furnace structure can be provided, uniform and inexpensive semi-coke can be mass-produced.
【００３４】また、上記乾留装置による低温乾留法は、
乾留反応に要する有効な炉内滞留時間を比較的低圧の装
置系にて確保し、高速流動伝熱作用により石炭粒を低温
乾留し得る。従って、流動化剤として N2 、CO2 等のイ
ナートガス又は循環ガスを格別に要しない。しかも、灰
分の溶融に起因して従来の目皿型流動法において比較的
高頻度に生じ得た目詰り現象等を確実に回避し得るの
で、長時間の連続運転を要する工業的乾留装置、例え
ば、日産５０TON の生産量を要する連続稼働設備等とし
て好適に使用し得る。なお、上記乾留装置にて生産され
た均一な半成コークスは、煉炭・豆炭の原料、鋳物用コ
ークス原料、鉱炉用コークス原料、或いは、活性炭等の
原料として好適に利用し得る。The low-temperature carbonization method using the carbonization apparatus is as follows:
An effective furnace residence time required for the carbonization reaction is secured by a relatively low-pressure apparatus system, and coal particles can be carbonized at a low temperature by high-speed fluid heat transfer. Therefore, an inert gas such as N 2 or CO 2 or a circulating gas is not particularly required as a fluidizing agent. Moreover, since it is possible to reliably avoid the clogging phenomenon and the like which can occur relatively frequently in the conventional plate-type flow method due to the melting of the ash, an industrial carbonization apparatus requiring a long continuous operation, for example, It can be suitably used as continuous operation equipment requiring a production volume of 50 TON per day. The uniform semi-coke produced by the carbonization apparatus can be suitably used as a raw material for briquette / bean charcoal, a raw material for coke for casting, a raw material for coke for furnace, or a raw material for activated carbon.
【００３５】以上、本発明の好適な実施例について詳細
に説明したが、本発明は上記実施例に限定されるもので
はなく、特許請求の範囲に記載された本発明の範囲内で
種々の変形又は変更が可能であり、該変形例又は変更例
も又、本発明の範囲内に含まれるものであることは、い
うまでもない。例えば、上記乾留装置により多種多様の
農林産物の廃材、例えば、木材片又はモミガラ等の粒状
化物を低温乾留することができる。また、上記乾留装置
にて生成した乾留ガスを系外の熱利用プロセスに送出
し、乾留ガスの保有顕熱および乾留ガスの可燃成分の燃
焼熱量を熱交換器又は廃熱ボイラー等にて回収し、かか
る熱回収により生成された水蒸気等の熱媒体流体を各種
乾燥装置や、各種製造／精製プロセス等に供給しても良
い。Although the preferred embodiments of the present invention have been described in detail above, the present invention is not limited to the above embodiments, and various modifications may be made within the scope of the present invention described in the appended claims. It is needless to say that the modification or the modification is also included in the scope of the present invention. For example, the above-mentioned carbonization apparatus enables low-temperature carbonization of waste materials of a wide variety of agricultural and forestry products, for example, granulated materials such as wood chips and peaches. Further, the carbonized gas generated by the carbonized gas is sent to a heat utilization process outside the system, and the sensible heat of the carbonized gas and the combustion heat of the combustible components of the carbonized gas are recovered by a heat exchanger or a waste heat boiler. The heat medium fluid such as steam generated by the heat recovery may be supplied to various drying devices, various manufacturing / refining processes, and the like.
【００３６】[0036]
【発明の効果】以上説明した如く、請求項１に記載され
た本発明の上記構成によれば、所定粒度に調整された炭
化水素系原料を浮遊乾留せしめる希薄流動層を備えた噴
流型内熱低温乾留装置において、炉内上部域の上昇気流
速度を定常化し、必要且つ十分な炭化水素系原料の炉内
滞在時間を確保し得る噴流型内熱低温乾留装置を提供す
ることが可能となる。As described above, according to the first aspect of the present invention, a jet-type internal heat source having a dilute fluidized bed for floating-distilling a hydrocarbon-based raw material adjusted to a predetermined particle size is provided. In the low-temperature carbonization apparatus, it is possible to provide a jet-type internal heat low-temperature carbonization apparatus capable of stabilizing an ascending air flow velocity in an upper region in a furnace and securing a necessary and sufficient stay time of a hydrocarbon-based raw material in the furnace.
【００３７】また、請求項２に記載された本発明の上記
構成によれば、噴流層の下部域に配置され、空気流又は
空気／水蒸気混合気流を噴出する流動化装置を備えた噴
流型内熱低温乾留装置において、流動化装置内に自由落
下する金属片等の異物、燃焼灰又は大粒径の粗大石炭粒
子等に起因する流動化装置の閉塞、或いは、流動化装置
内における粗大石炭粒子等の燃焼による給気流ノズル等
の損傷を有効に防止し、継続的な乾留装置の連続運転を
可能にする噴流型内熱低温乾留装置を提供することが可
能となる。According to the second aspect of the present invention, there is provided a jet mold having a fluidizing device disposed in a lower region of a spouted bed and jetting an air flow or an air / steam mixed gas flow. In a thermal low-temperature carbonization apparatus, clogging of the fluidizer due to foreign matter such as metal pieces that fall freely into the fluidizer, combustion ash or large-size coarse coal particles, or coarse coal particles in the fluidizer Thus, it is possible to provide a jet-type internal heat low-temperature carbonization apparatus that effectively prevents damage to the air supply nozzle and the like due to combustion and enables continuous operation of the carbonization apparatus.
【００３８】更に、請求項３及び請求項４に記載された
本発明の上記構成によれば、上記構成の噴流型内熱低温
乾留装置において、流動化装置内に落下ないし流入した
異物、燃焼灰又は粗大石炭粒子等を比較的容易に系外に
排出し得るとともに、乾留装置の運転初期に先混合型バ
ーナノズルとして機能し得る流動化装置を備えた噴流型
内熱低温乾留装置を提供することが可能となる。According to the third aspect of the present invention, there is provided a jet type internal thermal low-temperature carbonization apparatus having the above-described configuration, wherein foreign matter and combustion ash that fall or flow into the fluidization apparatus. Alternatively, it is possible to relatively easily discharge coarse coal particles and the like out of the system, and to provide a jet-type internal heat low-temperature carbonization apparatus equipped with a fluidization apparatus capable of functioning as a premixing burner nozzle in the initial operation of the carbonization apparatus. It becomes possible.
【図１】本発明の実施例に係る噴流型内熱低温乾留装置
の全体構成を示す概略縦断面図である。FIG. 1 is a schematic longitudinal sectional view showing the entire configuration of a jet type internal heat low-temperature carbonization apparatus according to an embodiment of the present invention.
【図２】図１に示す噴流型内熱低温乾留装置におけるウ
ィンドボックスの構造を示す横断面図である。FIG. 2 is a cross-sectional view showing a structure of a wind box in the jet-type internal low-temperature dry distillation apparatus shown in FIG.
【図３】図１に示す噴流型内熱低温乾留装置におけるス
ロート部及びウィンドボックスの構造を示す縦断面図で
ある。FIG. 3 is a longitudinal sectional view showing a structure of a throat section and a wind box in the jet type internal thermal low-temperature carbonization apparatus shown in FIG.
１ 乾留装置 １０ 内熱炉 １１ 噴流部 １２ 浮遊部 １４ 連続炉内領域 １８ 円錐状内周面 １９ 円筒状内周面 ２０ 給炭装置 ２１ 給炭バンカー ２２ スクリュー式フィーダー ３０ ウィンドボックス ３１ スロート部 ３２ ハウジング ３３ 空気導入口 ３４ 蒸気導入装置 ３６ 蒸気導入管 ３７ 蒸気吐出口 ３８ 垂直ガイド ４０ 排出装置 ４３ 開閉弁装置 ５０ サイクロンホッパー ５１ 耐火ダクト DESCRIPTION OF SYMBOLS 1 Dry distillation apparatus 10 Inner heat furnace 11 Jet part 12 Floating part 14 Continuous furnace interior area 18 Conical inner peripheral surface 19 Cylindrical inner peripheral surface 20 Coal supply device 21 Coal supply bunker 22 Screw type feeder 30 Wind box 31 Throat part 32 Housing 33 Air Inlet 34 Steam Introducing Device 36 Steam Introducing Tube 37 Steam Outlet 38 Vertical Guide 40 Discharge Device 43 On-Off Valve Device 50 Cyclone Hopper 51 Refractory Duct
Claims (12)
７００℃以下の低温乾留雰囲気により浮遊乾留し、嵩比
重が低減した粒子を炉頂部より炉外に送出する噴流内熱
低温乾留装置において、 噴流型流動炉を構成する内熱炉(10)と、所定粒度に調整
された炭化水素系原料を前記内熱炉に装入する給炭装置
(20)と、前記内熱炉の下部域に配設された流動化装置(3
0)とを有し、前記内熱炉は、噴流層を構成する逆錐形の
噴流部(11)と、前記炭化水素系原料の粒子を炉内領域に
浮遊せしめ、嵩比重の低減に要する前記粒子の炉内滞在
時間を確保するための円筒形浮遊部(12)とを有し、前記噴流部及び浮遊部は、上下方向に延在する連続炉内
領域(14)を形成し、 前記噴流部は、下方に向かって縮径する円錐形内壁面(1
8)を備えるとともに、前記炭化水素系原料の粒子を上方
に吹上げる空気及び／又は水蒸気の高速給気流を吐出す
るスロート部(31)を下端部収束領域に備え、 前記浮遊部(12)は、該噴流部の上位大径部分と整合し且
つ一体的に連接する所定内径の円筒状内周壁面を備え、
前記高速給気流にて浮遊した前記炭化水素系原料の粒子
を自由落下に抗して炉内領域に所要時間滞在せしめる浮
遊域を前記噴流部の上方域に画成することを特徴とする
噴流型内熱低温乾留装置。(1)Hydrocarbon raw material adjusted to the specified particle size
Floating carbonization in a low-temperature carbonization atmosphere of 700 ° C or less, and the bulk ratio
Heat in the jet that sends particles with reduced weight out of the furnace from the furnace top
In low-temperature carbonization equipment, Adjusted to a predetermined particle size with the internal heating furnace (10) that composes the jet-type fluidized furnace
Coal feeder for charging the extracted hydrocarbon-based raw material into the internal heating furnace
(20) and a fluidization device (3
0) and the internal heatThe furnace, The inverse cone of the spouted bed
A jet part (11) and the particles of the hydrocarbon-based raw material
Let it float,Said required for reduction of bulk specific gravityParticle stay in furnace
Make timeforHaving a cylindrical floating portion (12),The jet part and the floating part are in a continuous furnace extending vertically.
Forming an area (14), The jet part has a conical inner wall surface (1
8) and the particles of the hydrocarbon-based raw material are
A high-speed supply stream of air and / or water vapor
The floating portion (12) is aligned with the upper large-diameter portion of the jet portion, and a throat portion (31) is provided in the lower end converging region.
A cylindrical inner peripheral wall of a predetermined inner diameter integrally connected to
Particles of the hydrocarbon-based raw material suspended in the high-speed supply flow
Floating in the furnace area for a required time against free fall
A play area is defined above the jet part.
Jet type internal low temperature carbonization equipment.
７００℃以下の低温乾留雰囲気により浮遊乾留し、嵩比
重が低減した粒子を炉頂部より炉外に送出する噴流内熱
低温乾留装置において、 噴流型流動炉を構成する内熱炉(10)と、所定粒度に調整
された炭化水素系原料を前記内熱炉に装入する給炭装置
(20)と、前記内熱炉の下部域に配設された流動化装置(3
0)とを有し、前記内熱炉は、噴流層を構成する逆錐形の
噴流部(11)と、前記炭化水素系原料の粒子を炉内領域に
浮遊せしめ、嵩比重の低減に要する前記粒子の炉内滞在
時間を確保するための円筒形浮遊部(12)とを有し、前記噴流部及び浮遊部は、上下方向に延在する連続炉内
領域(14)を形成し、 前記噴流部は、下方に向かって縮径する円錐形内壁面(1
8)を備えるとともに、空気及び／又は水蒸気の噴出気流
を吐出するスロート部(31)を下端部収束領域に備え、該
噴出気流は、前記炭化水素系原料の粒子を上方に吹上げ
るように前記スロート部を吹抜け、前記浮遊部(12)は、該噴流部の上位大径部分と整合し且
つ一体的に連接する所定内径の円筒状内周壁面を備え、 前記スロート部の下方域に配置された流動化装置(30)
は、前記スロート部と連通する給気流混合領域を形成す
るハウジング(32)と、前記給気流混合領域に開口する空
気流入口(33)と、前記給気流混合領域に上下変位可能に
支持された高さ調節可能な水蒸気供給管(36)とを備え、
前記水蒸気供給管の上端部は、前記スロート部に隣接し
て開口する水蒸気吐出口(37)を備えることを特徴とする
噴流型内熱低温乾留装置。(2)Hydrocarbon raw material adjusted to the specified particle size
Floating carbonization in a low-temperature carbonization atmosphere of 700 ° C or less, and the bulk ratio
Heat in the jet that sends particles with reduced weight out of the furnace from the furnace top
In low-temperature carbonization equipment, Adjusted to a predetermined particle size with the internal heating furnace (10) that composes the jet-type fluidized furnace
Coal feeder for charging the extracted hydrocarbon-based raw material into the internal heating furnace
(20) and a fluidization device (3
0) and the internal heatThe furnace, The inverse cone of the spouted bed
A jet part (11) and the particles of the hydrocarbon-based raw material
Let it float,Said required for reduction of bulk specific gravityParticle stay in furnace
Make timeforHaving a cylindrical floating portion (12),The jet part and the floating part are in a continuous furnace extending vertically.
Forming an area (14), The jet part has a conical inner wall surface (1
8) and the jet stream of air and / or steam
A throat section (31) for discharging the ink in the lower end convergence area,
The jet stream blows up the hydrocarbon-based material particles upward.
Blow through the throat part,The floating portion (12) is aligned with the upper large-diameter portion of the jet portion and
A cylindrical inner peripheral wall of a predetermined inner diameter integrally connected to Fluidization device (30) arranged in the lower area of the throat section
Form a supply air flow mixing region communicating with the throat portion.
Housing (32) and an air opening to the supply air mixing area.
Air flow inlet (33), so that it can be vertically displaced into the supply air mixing area
A supported height-adjustable steam supply pipe (36),
The upper end of the steam supply pipe is adjacent to the throat.
Characterized by having a water vapor discharge port (37) that opens
Jet type internal low temperature carbonization equipment.
下した異物又は粗大粒子等を排出可能な排出装置が前記
ハウジングに連結され、該排出装置は、前記異物又は粗
大粒子等の系外排出路を選択的に開閉可能な開閉弁装置
を有することを特徴とする請求項２に記載の噴流型内熱
低温乾留装置。3. A discharge device capable of discharging foreign matter or coarse particles which have fallen freely into the housing of the fluidizing device is connected to the housing, and the discharge device is provided with an external discharge path for the foreign matter or coarse particles. 3. The jet type internal heat low-temperature carbonization apparatus according to claim 2 , further comprising an on-off valve device capable of selectively opening and closing the jet.
には、燃焼用炭化水素系燃料を供給する燃料供給手段が
連結され、該燃料供給手段は、前記乾留装置の運転初期
に前記スロート部に燃焼用燃料を供給することを特徴と
する請求項２又は３に記載の噴流型内熱低温乾留装置。4. A fuel supply means for supplying a hydrocarbon-based fuel for combustion is connected to a steam supply pipe constituting the fluidizing device, and the fuel supply means is connected to the throat section at an early stage of operation of the dry distillation apparatus. 4. A jet type internal heat low temperature carbonization apparatus according to claim 2 , wherein a fuel for combustion is supplied to the fuel cell.
上昇及び下降運動を反復する炭化水素系原料粒子の嵩比
重は、乾留反応により、初期比重の１／３乃至１／４に
低減することを特徴とする請求項１乃至４のいずれか１
項に記載の噴流型内熱低温乾留装置。 5. Between the throat portion, the jet portion and the floating portion.
Bulk ratio of hydrocarbon-based raw material particles repeating reciprocating movements
Weight is reduced to 1/3 to 1/4 of initial specific gravity by dry distillation reaction.
The method according to claim 1, wherein the number is reduced.
Item 2. The jet-type internal heat low-temperature carbonization apparatus according to Item 1.
０℃の範囲内の温度に設定され、前記粒子の炉内滞留時
間は、５〜６分間の範囲に設定されることを特徴とする
請求項１乃至５のいずれか１項に記載の噴流型内熱低温
乾留装置。 6. The furnace temperature of the jet section is 450 ° C. to 60 ° C.
Set to a temperature within the range of 0 ° C., when the particles stay in the furnace
The interval is set in a range of 5 to 6 minutes.
The jet type internal low temperature according to any one of claims 1 to 5.
Carbonization equipment.
の内径寸法の０．３〜０．５倍の範囲の値に設定される
ことを特徴とする請求項１乃至６のいずれか１項に記載
の噴 流型内熱低温乾留装置。 7. An inner diameter of the throat portion is equal to the floating portion.
Set to a value within the range of 0.3 to 0.5 times the inner diameter of
The method according to any one of claims 1 to 6, wherein
Injection-flow in the heat cold carbonization apparatus.
径寸法の１．３〜１．７倍の範囲の値に設定されること
を特徴とする請求項１乃至７のいずれか１項に記載の噴
流型内熱低温乾留装置。 8. The height of the jet part is set within the floating part.
Be set to a value in the range of 1.3 to 1.7 times the diameter
The jet according to any one of claims 1 to 7, characterized in that:
Flow type internal heat low-temperature carbonization equipment.
給炭量 (TON/hr) の０．４５〜０．６５倍の範囲の値に
設定されることを特徴とする請求項１乃至８のいずれか
１項に記載の噴流型内熱低温乾留装置。 9. The cubic product (m 3 ) of the inner diameter of the floating portion is:
In the range of 0.45 to 0.65 times the coal supply (TON / hr)
9. The method according to claim 1, wherein the setting is performed.
Item 2. The jet type internal heat low-temperature carbonization apparatus according to Item 1.
系は、供給蒸気流量を可変制御可能な蒸気流量制御手段
を有し、前記空気流入口に連結された空気供給系は、空
気導入量を可変制御可能な空気流量制御手段を備えるこ
とを特徴とする請求項２乃至４のいずれか１項に記載の
噴流型内熱低温乾留装置。 10. A steam supply connected to the steam supply pipe.
The system is a steam flow control means that can variably control the supply steam flow.
Having an air supply system connected to the air inlet,
Air flow control means capable of variably controlling the amount of air
The method according to any one of claims 2 to 4, wherein
Jet type internal low temperature carbonization equipment.
内に流入した空気流は、前記ハウジング内に旋回流を形
成して前記スロート部に上昇することを特徴とする請求
項２乃至４のいずれか１項に記載の噴流型内熱低温乾留
装置 11. The jet device through the air inlet.
The air flow flowing into the housing forms a swirling flow in the housing.
And rising to the throat portion.
Item 5. Low-temperature carbonization of jet-type internal heat according to any one of Items 2 to 4
apparatus
２５〜０．５ｍ／ｓの範囲に設定されることを特徴とす
る請求項１乃至１１のいずれか１項に記載の噴流型内熱
低温乾留装置。 12. The furnace according to claim 1, wherein the ascending airflow velocity is in the range of 0.1.
It is set in the range of 25 to 0.5 m / s.
The jet-type internal heat according to any one of claims 1 to 11,
Low-temperature carbonization equipment .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9130997A JP3001190B2 (en) | 1997-05-21 | 1997-05-21 | Jet type internal heat low temperature carbonization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9130997A JP3001190B2 (en) | 1997-05-21 | 1997-05-21 | Jet type internal heat low temperature carbonization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH10316977A JPH10316977A (en) | 1998-12-02 |
| JP3001190B2 true JP3001190B2 (en) | 2000-01-24 |
Family
ID=15047533
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9130997A Expired - Fee Related JP3001190B2 (en) | 1997-05-21 | 1997-05-21 | Jet type internal heat low temperature carbonization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3001190B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5308795B2 (en) * | 2007-12-11 | 2013-10-09 | 住友化学株式会社 | Polyolefin production method and polyolefin production system provided with spouted bed apparatus |
| CN102616779B (en) * | 2011-10-25 | 2014-08-20 | 杭州星宇炭素科技有限公司 | Method for preventing material returning at feed end of rotary activated carbon activation furnace |
| CN105062529A (en) * | 2015-09-09 | 2015-11-18 | 陕西美斯林能源科技研究院 | Spouted fluidized bed powdered coal pyrolysis device and method |
| JP7051384B2 (en) * | 2017-11-17 | 2022-04-11 | 三菱重工業株式会社 | Biomass gasifier and its operation method |
-
1997
- 1997-05-21 JP JP9130997A patent/JP3001190B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH10316977A (en) | 1998-12-02 |
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