JP2003105351A - Method and apparatus for quick thermal decomposition of coal - Google Patents
Method and apparatus for quick thermal decomposition of coalInfo
- Publication number
- JP2003105351A JP2003105351A JP2001300493A JP2001300493A JP2003105351A JP 2003105351 A JP2003105351 A JP 2003105351A JP 2001300493 A JP2001300493 A JP 2001300493A JP 2001300493 A JP2001300493 A JP 2001300493A JP 2003105351 A JP2003105351 A JP 2003105351A
- Authority
- JP
- Japan
- Prior art keywords
- coal
- thermal decomposition
- furnace
- pyrolysis
- gasification
- 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.)
- Withdrawn
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、石炭の熱分解によ
り高カロリーガスや高収率タール等の高価値の熱分解生
成物を得る石炭熱分解方法に関する。TECHNICAL FIELD The present invention relates to a coal pyrolysis method for obtaining a high-value pyrolysis product such as high-calorie gas or high-yield tar by pyrolysis of coal.
【０００２】[0002]
【従来の技術】石炭を利用価値の高いガス、液体および
固体に転換できる急速熱分解プロセスは石炭の新利用技
術として期待されている。2. Description of the Related Art A rapid pyrolysis process capable of converting coal into highly useful gas, liquid and solid is expected as a new coal utilization technology.
【０００３】熱分解方法に関して、従来は流動層やロー
タリーキルンを用いた方法が行われていた。しかし、こ
の方法では急速加熱することができず、有用な成分であ
る揮発分(ガス・タール)収率が低く、とりわけガス収率
が低いという問題があった。そのために、本発明者らは
特開平05-295371号公報において、微粉砕した石炭を急
速加熱して得られたチャーの一部を酸素でガス化し、そ
の高温ガス中に微粉炭を吹き込むことによって石炭の急
速熱分解を行う方法を提示している。Regarding the thermal decomposition method, conventionally, a method using a fluidized bed or a rotary kiln has been performed. However, this method has a problem that rapid heating cannot be performed, the yield of volatile components (gas / tar), which is a useful component, is low, and particularly the gas yield is low. Therefore, the inventors of the present invention, in JP 05-295371 A, by gasifying a portion of the char obtained by rapidly heating finely pulverized coal with oxygen, by blowing pulverized coal into the hot gas The method of rapid pyrolysis of coal is presented.
【０００４】[0004]
【発明が解決しようとする課題】特開平5-295371号公報
で提示した方法による石炭熱分解は、高温ガス発生部で
発生した高温ガス化ガス中に微粉炭を吹き込み急速熱分
解される。高温ガス化ガスの温度は、石炭またはチャー
中の灰分を溶融分離させるために、灰の溶融点以上の１
４００〜１７００℃に達し、その高温ガスが石炭熱分解
反応部下の導入口(スロート)より反応器内部に導入され
る。そのため、微粉炭を吹き込み混合された後のガスの
温度は６００〜１０００℃を示すが、吹き込んだ直後の
微粉炭は１４００〜１７００℃の高温ガスに晒される。
通常、石炭熱分解反応は、昇温とともに石炭中の揮発分
が分解する一次反応が起こり、さらに気相タール等の一
次反応生成物が雰囲気温度や組成に応じて二次反応によ
り分解する事が知られている。平均５０μｍ程度の微粉
炭の昇温および一次反応は１００ミリ秒以内で完了する
ものと推定されるために、この二次反応が極めて高温で
起きている可能性がある。二次反応が高温で起こること
により、一次反応生成物の分解が所望の炭化水素ガスに
留まらずにＣＯやＨ2ガスまで過度に進んだり、あるい
は重合反応が進展してススが生成したりして、熱分解生
成物の付加価値や有効成分の収率が下がるという問題が
ある。In the thermal decomposition of coal by the method disclosed in Japanese Unexamined Patent Publication No. 5-295371, pulverized coal is blown into the high temperature gasification gas generated in the high temperature gas generation section for rapid thermal decomposition. The temperature of the high-temperature gasification gas is 1 or higher than the melting point of ash in order to melt and separate the ash in coal or char.
The temperature reaches 400 to 1700 ° C., and the high temperature gas is introduced into the reactor through an inlet (throat) below the coal pyrolysis reaction section. Therefore, the temperature of the gas after the pulverized coal is blown and mixed is 600 to 1000 ° C., but the pulverized coal immediately after being blown is exposed to the high temperature gas of 1400 to 1700 ° C.
Usually, in a coal pyrolysis reaction, a primary reaction in which volatile matter in coal is decomposed as temperature rises, and a primary reaction product such as gas-phase tar may be decomposed by a secondary reaction depending on the ambient temperature and composition. Are known. Since it is estimated that the average temperature rise of the pulverized coal of about 50 μm and the primary reaction are completed within 100 milliseconds, there is a possibility that this secondary reaction occurs at an extremely high temperature. Since the secondary reaction occurs at a high temperature, the decomposition of the primary reaction product does not stay in the desired hydrocarbon gas but proceeds excessively to CO or H 2 gas, or the polymerization reaction progresses to form soot. As a result, there is a problem that the added value of the thermal decomposition product and the yield of the active ingredient are lowered.
【０００５】そこで、本発明は過度の熱分解二次反応を
抑制し、高価値の熱分解生成物を生成することができる
石炭熱分解方法を提供する。Therefore, the present invention provides a coal pyrolysis method capable of suppressing excessive pyrolysis secondary reactions and producing high-value pyrolysis products.
【０００６】[0006]
【課題を解決するための手段】上記課題を解決するため
の本発明は、熱分解ガス化チャーを酸素および水蒸気と
ともにガス化炉へ吹き込み、部分酸化反応を起こさせて
還元ガスを製造し、次いでガス化炉と直結した熱分解炉
に該還元ガスを導き、還元ガスの顕熱を利用して石炭を
急速熱分解する石炭の熱分解方法において、熱分解炉の
石炭供給口より下部に熱分解ガス化チャーの一部を吹き
込むことを特徴とする石炭の急速熱分解方法である。The present invention for solving the above-mentioned problems is to blow a pyrolysis gasification char together with oxygen and steam into a gasification furnace to cause a partial oxidation reaction to produce a reducing gas, and then to produce a reducing gas. In the thermal decomposition method of coal, in which the reducing gas is introduced into a thermal decomposition furnace directly connected to the gasification furnace, and the sensible heat of the reducing gas is used for rapid thermal decomposition of the coal, the thermal decomposition is performed below the coal supply port of the thermal decomposition furnace. It is a rapid coal pyrolysis method characterized by blowing a part of gasification char.
【０００７】また、ガス化炉とその上部にスロートを介
して設けられた熱分解炉と、熱分解炉で排出された熱分
解ガス化チャーのガス化炉への循環装置を備える石炭の
急速熱分解装置において、熱分解ガス化チャーの熱分解
炉への循環装置を設けたことを特徴とする石炭の急速熱
分解装置である。Further, the rapid heat of coal is provided with a gasification furnace and a pyrolysis furnace provided above the gasification furnace through a throat, and a circulation device for circulating the pyrolysis gasification char discharged in the pyrolysis furnace to the gasification furnace. This is a rapid coal pyrolysis apparatus characterized in that a pyrolysis gasification char is provided with a circulating device to the pyrolysis furnace.
【０００８】熱分解チャーは石炭中の揮発分が取り除か
れたもので、高温雰囲気に晒されても分解せずに、熱媒
体の役割を果たす。ガス化炉からスロートを介して導入
された高温ガス化ガスがこの熱分解チャーと混合して温
度を下げた後に、熱分解用石炭として供給される微粉炭
と接触することにより、熱分解二次反応温度が下がり、
過度の分解反応が抑制される。供給する熱分解チャーの
温度は、プロセスの熱効率を高めるためにもサイクロン
で回収された時点の温度をできるだけ維持することが望
ましい。Pyrolysis char is obtained by removing volatile components from coal and does not decompose even when exposed to a high temperature atmosphere, and serves as a heat medium. The high-temperature gasification gas introduced from the gasification furnace through the throat is mixed with this pyrolysis char to lower the temperature, and then comes into contact with the pulverized coal supplied as coal for pyrolysis, so that the pyrolysis secondary The reaction temperature goes down,
Excessive decomposition reaction is suppressed. It is desirable that the temperature of the pyrolysis char to be supplied be maintained as high as possible at the time of being recovered by the cyclone in order to enhance the thermal efficiency of the process.
【０００９】熱分解チャーは、また熱分解一次反応生成
物を適度に分解させる触媒的作用も果たし、温度が下が
ることによる二次反応の低下を防ぐ効果もある。従っ
て、熱分解チャーを熱分解反応部の微粉炭供給口の下部
から吹き込む方法は、高価値の熱分解生成物を得る有効
な手段である。The pyrolysis char also acts as a catalyst for appropriately decomposing the pyrolysis primary reaction product, and also has an effect of preventing a decrease in secondary reaction due to a decrease in temperature. Therefore, the method of blowing the pyrolysis char from the lower part of the pulverized coal supply port of the pyrolysis reaction section is an effective means for obtaining a high-value pyrolysis product.
【００１０】[0010]
【発明の実施の形態】次に、本発明の実施の形態につい
て図面に基づいて説明する。図１は、本発明の石炭熱分
解装置のフロー図である。石炭熱分解装置は炉本体とチ
ャーを炉本体へ供給する循環装置とに分けられる。炉本
体は、酸素および水蒸気５でガス化チャー６を部分酸化
反応によりガス化し、ＣＯ、Ｈ2、ＣＯ2、Ｈ2Ｏを主成
分の高温還元ガスを発生させるガス化炉２と、熱分解用
石炭４を供給しガス化炉２からの高温還元ガスと熱分解
用石炭４を混合して熱分解する熱分解炉１と、ガス化炉
２と熱分解炉１とを繋ぐスロート３とで構成される。さ
らに高さ方向として熱分解反応部の熱分解用石炭供給口
とスロート３との間に、循環チャー供給口が円周方向に
１個または２個以上設けられ、循環チャー７が供給され
る。ここで循環チャーの供給口は石炭供給口よりも少し
でも下部からスロートのすぐ上までの範囲に設置するも
のとする。ガス化炉２内で生成した高温還元ガスは1400
〜1700℃程度であり、スロート３を通って石炭熱分解炉
１に送られる。石炭熱分解炉１内部では、熱分解炉下部
のチャー供給口から循環チャー７が供給され、高温還元
ガスが１０００〜１２００℃まで冷却されるとともに炉
内のチャー密度が高められる。冷却された還元ガスと循
環チャーとの混合物の中に微粉砕された熱分解用石炭４
が供給され、急速に加熱されて熱分解反応を起こしチャ
ー、ガス、タール等の熱分解生成物が生成する。しか
し、循環チャー７により還元ガスの温度は低下している
ために、石炭の熱分解生成物の温度は高々１０００〜１
２００℃までしか上昇せず、しかもチャー密度の濃厚な
雰囲気での熱分解反応であることから、一次熱分解生成
物の二次反応は促進されるが過度には進行せず、熱分解
カーボン生成の抑制、炭化水素系ガス収率の増加等、高
価値の熱分解生成物を得ることができる。BEST MODE FOR CARRYING OUT THE INVENTION Next, embodiments of the present invention will be described with reference to the drawings. FIG. 1 is a flow chart of the coal pyrolysis apparatus of the present invention. The coal pyrolyzer is divided into a furnace body and a circulation device for supplying char to the furnace body. The furnace body gasifies the gasification char 6 with oxygen and water vapor 5 by a partial oxidation reaction to generate a high-temperature reducing gas containing CO, H 2 , CO 2 , and H 2 O as main components, and a pyrolysis furnace. The pyrolysis furnace 1 that supplies the coal for use 4 and mixes the high-temperature reducing gas from the gasifier 2 with the coal for pyrolysis 4 to pyrolyze, and the throat 3 that connects the gasifier 2 and the pyrolysis furnace 1 together. Composed. Further, one or more circulation char supply ports are provided in the circumferential direction between the pyrolysis coal supply port of the pyrolysis reaction section and the throat 3 in the height direction, and the circulation char 7 is supplied. Here, the supply port of the circulation char is to be installed in the range from the lower part to just above the throat, even a little than the coal supply port. The high-temperature reducing gas generated in the gasification furnace 2 is 1400
The temperature is about 1700 ° C. and is sent to the coal pyrolysis furnace 1 through the throat 3. In the coal pyrolysis furnace 1, the circulating char 7 is supplied from the char supply port at the lower part of the pyrolysis furnace, the high-temperature reducing gas is cooled to 1000 to 1200 ° C, and the char density in the furnace is increased. Pyrolysis coal 4 pulverized in a mixture of cooled reducing gas and circulating char
Is supplied and heated rapidly to cause a thermal decomposition reaction to generate thermal decomposition products such as char, gas and tar. However, since the temperature of the reducing gas is lowered by the circulating char 7, the temperature of the thermal decomposition products of coal is at most 1000-1.
Since the temperature rises only up to 200 ° C and the pyrolysis reaction is carried out in a dense char density atmosphere, the secondary reaction of the primary pyrolysis product is promoted but does not proceed excessively, resulting in pyrolysis carbon formation. It is possible to obtain a high-value thermal decomposition product such as the suppression of the above and the increase of the yield of hydrocarbon gas.
【００１１】供給された循環チャー７および熱分解用石
炭４の熱分解により生成されたチャーは石炭熱分解反応
部出口から排出され、固気分離装置（サイクロン８）で
ガス１０と分離されチャーホッパー９に貯留される。高
温ガス発生部２へは１４００〜１７００℃に制御できる
量のガス化チャー６が供給され、また熱分解反応部１へ
は高温還元ガスを１０００〜１２００℃に冷却できる量
の循環チャー７が供給される。過剰のチャーは製品チャ
ー１１として系外へ排出される。ここで、チャー循環装
置とは、固気分離装置８、チャーホッパー９、および熱
分解炉１へ循環チャー７を供給する装置の組み合わせで
ある。一般に、熱分解石炭の約５０％がチャーに転換さ
れ、その大部分はガス化チャー６となる。熱分解反応部
１への循環チャー７は系内をリサイクルするもので、予
め貯留されたチャーが用いられる。チャーリサイクル量
はチャーの温度が高いほど多くなる。Chars produced by the pyrolysis of the supplied circulating char 7 and the pyrolysis coal 4 are discharged from the coal pyrolysis reaction section outlet, separated from the gas 10 by the solid-gas separation device (cyclone 8), and the char hopper. 9 is stored. An amount of gasification char 6 that can be controlled to 1400 to 1700 ° C. is supplied to the high temperature gas generation unit 2, and a circulating char 7 that is capable of cooling the high temperature reducing gas to 1000 to 1200 ° C. is supplied to the thermal decomposition reaction unit 1. To be done. Excess char is discharged outside the system as product char 11. Here, the char circulation device is a combination of the solid-gas separation device 8, the char hopper 9, and a device for supplying the circulation char 7 to the thermal decomposition furnace 1. Generally, about 50% of pyrolyzed coal is converted to char, and most of it becomes gasification char 6. The circulating char 7 to the thermal decomposition reaction part 1 is for recycling the inside of the system, and a char stored in advance is used. The amount of char recycling increases as the temperature of char rises.
【００１２】[0012]
【実施例】石炭の熱分解試験は、熱分解用微粉炭供給量
150kg/hの大型試験装置を用いて行った。この大型試験
装置は図１のフロー図と同じ構造を有している。石炭熱
分解炉での熱分解反応条件は温度800℃、圧力０.３ＭＰ
ａ、ガス化条件は温度1550℃、圧力０.３ＭＰａであ
る。石炭熱分解炉への微粉炭供給量は0〜150kg/h、チャ
ー供給量は0〜150kg/h、またガス化炉へのチャー供給量
は100kg/hである。実験には、Ａ炭(インドネシア炭)を
平均粒径は約40μmに調整したものを使用した。また、
チャーは予め生成し、貯留していたものを用いた。[Example] Pyrolysis test for coal is based on the amount of pulverized coal supplied for pyrolysis
The test was carried out using a large test apparatus of 150 kg / h. This large-scale test apparatus has the same structure as the flow chart of FIG. Pyrolysis reaction conditions in the coal pyrolysis furnace are temperature 800 ℃, pressure 0.3MP.
a, the gasification conditions are a temperature of 1550 ° C. and a pressure of 0.3 MPa. The pulverized coal supply rate to the coal pyrolysis furnace is 0 to 150 kg / h, the char supply rate is 0 to 150 kg / h, and the char supply rate to the gasification furnace is 100 kg / h. In the experiment, coal A (Indonesian coal) having an average particle size adjusted to about 40 μm was used. Also,
Char used was previously generated and stored.
【００１３】石炭熱分解炉下部へのチャー供給量を３段
階に変化させ、１０時間操業を行った時点での生成ガス
中の炭化水素ガス収率を表１に示す。炭化水素ガス収率
は熱分解により生成したガス中のメタン、エチレンなど
の炭化水素ガス成分の総質量を熱分解に供給した石炭の
質量で除した値であり、その値が大きいほどガスの熱量
は高くなる。石炭熱分解炉下部へ供給するチャーの量を
増加させると、生成ガス中の炭化水素ガス収率が増える
結果が得られ、石炭熱分解部下部へチャーを供給するこ
とにより高価値の熱分解生成物が得られることを確認で
きた。Table 1 shows the yield of hydrocarbon gas in the produced gas when the char supply amount to the lower part of the coal pyrolysis furnace was changed in three stages and the operation was carried out for 10 hours. The hydrocarbon gas yield is the value obtained by dividing the total mass of hydrocarbon gas components such as methane and ethylene in the gas produced by pyrolysis by the mass of coal supplied for pyrolysis.The larger the value, the calorific value of the gas. Will be higher. Increasing the amount of char supplied to the lower part of the coal pyrolysis furnace has the effect of increasing the hydrocarbon gas yield in the product gas, and by supplying char to the lower part of the coal pyrolysis part, high-value pyrolysis production It was confirmed that the product was obtained.
【００１４】[0014]
【表１】 [Table 1]
【００１５】[0015]
【発明の効果】本発明の石炭熱分解操業方法によって、
過度の熱分解二次反応を抑制でき、高価値の熱分解生成
物を生成することが可能となった。According to the coal pyrolysis operation method of the present invention,
Excessive thermal decomposition secondary reactions can be suppressed and high-value thermal decomposition products can be produced.
【図1】本発明例の石炭熱分解プロセスのフロー図であ
る。FIG. 1 is a flow diagram of a coal pyrolysis process of an example of the present invention.
１ 熱分解炉 ２ ガス化炉 ３ スロート ４ 熱分解石炭 ５ 酸素、水蒸気 ６ ガス化チャー ７ 循環チャー ８ サイクロン ９ チャーホッパー 10 生成ガス 11 製品チャー 1 Pyrolysis furnace 2 gasification furnace 3 throat 4 Pyrolysis coal 5 oxygen and water vapor 6 gasification char 7 circulation char 8 cyclones 9 Char Hopper 10 Product gas 11 Product char
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ１０Ｊ 3/46 Ｃ１０Ｊ 3/46 Ｍ (71)出願人 000004123 日本鋼管株式会社 東京都千代田区丸の内一丁目１番２号 (71)出願人 000001199 株式会社神戸製鋼所 兵庫県神戸市中央区脇浜町二丁目10番26号 (72)発明者 小野田 正己 富津市新富20−１ 新日本製鐵株式会社技 術開発本部内 (72)発明者 小水流 広行 富津市新富20−１ 新日本製鐵株式会社技 術開発本部内 (72)発明者 橋本 茂 富津市新富20−１ 新日本製鐵株式会社技 術開発本部内 (72)発明者 藤川 淳 北九州市戸畑区大字中原46−59 新日本製 鐵株式会社エンジニアリング事業本部内─────────────────────────────────────────────────── ─── Continuation of front page (51) Int.Cl. 7 Identification code FI theme code (reference) C10J 3/46 C10J 3/46 M (71) Applicant 000004123 Nippon Steel Tube Co., Ltd. 1-chome, Marunouchi, Chiyoda-ku, Tokyo No. 2 (71) Applicant 000001199 Kobe Steel, Ltd. 2-10-10 Wakihama-cho, Chuo-ku, Kobe-shi, Hyogo Prefecture (72) Inventor Masami Onoda 20-1 Shintomi, Futtsu-shi Nippon Steel Co., Ltd. Technical development Headquarters (72) Inventor Komizu-ryu Hiroyuki 20-1 Shintomi, Futtsu City Nippon Steel Corporation Technology Development Headquarters (72) Inventor Shigeru Hashimoto 20-1 Shintomi Futtsu City Nippon Steel Corporation Technology Development Headquarters (72) Inventor Atsushi Fujikawa 46-59 Nakahara, Tobata-ku, Kitakyushu City Nippon Steel Corporation Engineering Division
Claims (2)
とともにガス化炉へ吹き込み、部分酸化反応を起こさせ
て還元ガスを製造し、次いでガス化炉と直結した熱分解
炉に該還元ガスを導くとともに石炭を吹き込み、還元ガ
スの顕熱を利用して石炭を急速熱分解する石炭の熱分解
方法において、熱分解炉の石炭供給口より下部に熱分解
ガス化チャーの一部を吹き込むことを特徴とする石炭の
急速熱分解方法。1. A pyrolysis gasification char is blown into a gasification furnace together with oxygen and water vapor to cause a partial oxidation reaction to produce a reduction gas, and then the reduction gas is introduced into a pyrolysis furnace directly connected to the gasification furnace. In the pyrolysis method of coal, in which coal is blown in and the sensible heat of the reducing gas is used to rapidly pyrolyze the coal, a part of the pyrolysis gasification char is blown below the coal feed port of the pyrolysis furnace. Method for rapid pyrolysis of coal.
設けられた熱分解炉と、熱分解炉で排出された熱分解ガ
ス化チャーのガス化炉への循環装置を備える石炭の急速
熱分解装置において、熱分解ガス化チャーの熱分解炉へ
の循環装置を設けたことを特徴とする石炭の急速熱分解
装置。2. Rapid heat of coal comprising a gasification furnace, a pyrolysis furnace provided above the gasification furnace via a throat, and a circulation device for circulating the pyrolysis gasification char discharged in the pyrolysis furnace to the gasification furnace. A rapid thermal decomposition apparatus for coal, characterized in that a circulation apparatus for the thermal decomposition gasification char to the thermal decomposition furnace is provided in the decomposition apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001300493A JP2003105351A (en) | 2001-09-28 | 2001-09-28 | Method and apparatus for quick thermal decomposition of coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001300493A JP2003105351A (en) | 2001-09-28 | 2001-09-28 | Method and apparatus for quick thermal decomposition of coal |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JP2003105351A true JP2003105351A (en) | 2003-04-09 |
Family
ID=19121059
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2001300493A Withdrawn JP2003105351A (en) | 2001-09-28 | 2001-09-28 | Method and apparatus for quick thermal decomposition of coal |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2003105351A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101123385B1 (en) | 2009-11-06 | 2012-03-23 | 한국에너지기술연구원 | 2 stages pyrolysis and gasification hybrid system of high viscosity oilsand bitumen for synthetic liquid fuel and syngas production method using it |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| US9175226B2 (en) | 2007-12-12 | 2015-11-03 | Outotec Oyj | Process and plant for producing char and fuel gas |
| JP5816770B1 (en) * | 2015-05-22 | 2015-11-18 | 新日鉄住金エンジニアリング株式会社 | Operation method of coal gasification system |
-
2001
- 2001-09-28 JP JP2001300493A patent/JP2003105351A/en not_active Withdrawn
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9175226B2 (en) | 2007-12-12 | 2015-11-03 | Outotec Oyj | Process and plant for producing char and fuel gas |
| US9371487B2 (en) | 2007-12-12 | 2016-06-21 | Outotec Oyj | Process and plant for producing char and fuel gas |
| KR101123385B1 (en) | 2009-11-06 | 2012-03-23 | 한국에너지기술연구원 | 2 stages pyrolysis and gasification hybrid system of high viscosity oilsand bitumen for synthetic liquid fuel and syngas production method using it |
| CN103980948A (en) * | 2014-06-11 | 2014-08-13 | 华东理工大学 | Coal powder pyrolysis and gasification method |
| JP5816770B1 (en) * | 2015-05-22 | 2015-11-18 | 新日鉄住金エンジニアリング株式会社 | Operation method of coal gasification system |
| WO2016190028A1 (en) * | 2015-05-22 | 2016-12-01 | 新日鉄住金エンジニアリング株式会社 | Method for operating coal gasification system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP5763618B2 (en) | Two-stage dry feed gasifier and method | |
| JP5630626B2 (en) | Organic raw material gasification apparatus and method | |
| CN1018449B (en) | Production for fuel gas | |
| CN104342212B (en) | PC-FB hydropyrolysis and gasification coupling method | |
| JP2003041268A (en) | Method for gasifying biomass | |
| KR20100125428A (en) | Method and device for producing synthesis gas from biomass | |
| JPH0668108B2 (en) | Gasification method and equipment for carbonaceous material | |
| JPH0649874B2 (en) | Coal spouted bed gasification method | |
| CN103589459B (en) | Coal gasification method and device employing plasma torch heating technology | |
| JPH0454601B2 (en) | ||
| JP7192899B2 (en) | Blast Furnace Operation Method and Blast Furnace Incidental Equipment | |
| CN109054901A (en) | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device | |
| JP4731988B2 (en) | Gasification method and apparatus for carbonaceous resources | |
| JP2003105351A (en) | Method and apparatus for quick thermal decomposition of coal | |
| JP7192900B2 (en) | Blast Furnace Operation Method and Blast Furnace Incidental Equipment | |
| JP2012514078A (en) | Tar-free gasification system and method | |
| JPS5832196B2 (en) | Coal gasification method | |
| JP2006291134A (en) | Gasification method for biomass | |
| JP3559163B2 (en) | Gasification method using biomass and fossil fuel | |
| JP4334326B2 (en) | Coal hydropyrolysis apparatus and method | |
| GB1565034A (en) | Process of removing fines in fluidized coal gasification | |
| JP7192901B2 (en) | Blast Furnace Operation Method and Blast Furnace Incidental Equipment | |
| CN117701308A (en) | Biomass gasification device and gasification method | |
| EP2705120B1 (en) | Process and plant for the production and further treatment of fuel gas | |
| JP3287603B2 (en) | Coal rapid pyrolysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A711 | Notification of change in applicant |
Free format text: JAPANESE INTERMEDIATE CODE: A712 Effective date: 20060808 |
|
| RD02 | Notification of acceptance of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7422 Effective date: 20061002 |
|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 20081202 |