JPH0216191A - Rapid thermal decomposition apparatus for coal - Google Patents
Rapid thermal decomposition apparatus for coalInfo
- Publication number
- JPH0216191A JPH0216191A JP16726388A JP16726388A JPH0216191A JP H0216191 A JPH0216191 A JP H0216191A JP 16726388 A JP16726388 A JP 16726388A JP 16726388 A JP16726388 A JP 16726388A JP H0216191 A JPH0216191 A JP H0216191A
- Authority
- JP
- Japan
- Prior art keywords
- coke
- coal
- receiver
- reaction
- reactor tube
- 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.)
- Granted
Links
- 239000003245 coal Substances 0.000 title claims abstract description 32
- 238000005979 thermal decomposition reaction Methods 0.000 title abstract description 6
- 239000000571 coke Substances 0.000 claims abstract description 33
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 6
- 239000012263 liquid product Substances 0.000 claims description 7
- 238000000197 pyrolysis Methods 0.000 claims description 7
- 238000000354 decomposition reaction Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 239000002641 tar oil Substances 0.000 abstract description 4
- 239000000047 product Substances 0.000 abstract description 2
- 230000035484 reaction time Effects 0.000 abstract description 2
- 230000001105 regulatory effect Effects 0.000 abstract 2
- 238000010438 heat treatment Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000010742 number 1 fuel oil Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 239000003476 subbituminous coal Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Coke Industry (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、石炭の急速熱分解装置に係り、更に詳しくは
、低炭化度石炭からタール油等の高付加価値化学原料を
高収率で工業的有利に取得する装置に関するものである
。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a rapid pyrolysis device for coal, and more specifically, it is a method for producing high value-added chemical raw materials such as tar oil from low carbonization coal in high yield. The present invention relates to a device that can be obtained with industrial advantage.
従来は、何らかの形で高温ガス発生設備を設け、それか
ら発生せしめたホットガスと当該原料の微粉炭とを反応
器中で短時間接触させ、発生する生成物を逐次、チャー
タール油類、ガス等に分離して回収する方法が採られ
てきた。Conventionally, some form of high-temperature gas generation equipment was installed, and the hot gas generated was brought into contact with the raw material pulverized coal for a short time in a reactor, and the generated products were sequentially converted into coal oil, gas, etc. Methods have been adopted to separate and collect the
しかしながら、上記のような従来の方法は、新たに高温
ガス発生設備を設ける必要があることから設備コストが
高くつくばかりか、ガス加熱用の消費エネルギーの面で
のランニングコスト等も高くなる、などの問題点があっ
た。However, the conventional method described above not only requires high-temperature gas generation equipment to be installed, which not only increases equipment costs, but also increases running costs in terms of energy consumption for gas heating. There was a problem.
本発明は、上記のような従来の課題を解決して、高温ガ
ス発生設備及び予熱装置等の設備費を可及的低減すると
ともに、石炭の熱分解に要するエネルギーを大幅に節減
し得る、工業的有利な石炭の急速熱分解装置の提供を目
的とする。The present invention solves the above-mentioned conventional problems, reduces the cost of equipment such as high-temperature gas generation equipment and preheating equipment as much as possible, and provides an industrial solution that can significantly reduce the energy required for thermal decomposition of coal. The purpose of this invention is to provide a coal rapid pyrolysis device that is advantageous in terms of efficiency.
本発明者らは、かかる目的を達成すべく検討を進めた結
果、本発明に到達した。すな−わち、本発明は、コーク
ス炉からかま出しされる赤熱コークスを受けるコークス
受器、原料石炭を供給するフィーダー、該コークス受器
より供給された赤熱コークスと該フィーダーより供給さ
れた原料石炭とを接触させて熱分解反応を行う反応器、
反応生成物上りチャーを分離するチャー分離器、及び、
反応生成物より冷却器を介して液状生成物を分離する液
状生成物分離器を備えてなる石炭の急速熱分解装置を要
旨とするものである。The present inventors have conducted studies to achieve this objective, and as a result, have arrived at the present invention. In other words, the present invention provides a coke receiver for receiving red hot coke drawn out from a coke oven, a feeder for supplying coking coal, and a coke receiver for receiving red hot coke fed from the coke receiver and raw material supplied from the feeder. A reactor that performs a thermal decomposition reaction by contacting coal,
a char separator for separating reaction product char, and
The gist of this invention is a rapid pyrolysis apparatus for coal, which is equipped with a liquid product separator that separates a liquid product from a reaction product via a cooler.
以下、本発明を図面とともに詳細に説明する。Hereinafter, the present invention will be explained in detail with reference to the drawings.
第１図は本発明の詳細な説明するための概略図である。FIG. 1 is a schematic diagram for explaining the present invention in detail.
本発明装置は、例えば第１図に示すように、コークス炉
（１）からかま出しされる赤熱コークスを移動可能なコ
ークス受器（２）に受け、当該受器と反応管（３）とを
連結した後、所定粒度に粉砕調整された石炭を、フィー
ダー（４）を用い、連続的に反応管（３）へ供給し、同
時にコークス受器（２）から反応管（３）へ前記赤熱コ
ークスを送り、当該赤熱コークスと前記の調整された粉
炭とを接触させ急速に熱分解反応を行わせる。ついで反
応生成物は、チャー分離器（５）及び冷却器（７）を介
して液状生成物分離器（６）にてそれぞれ捕集される。As shown in FIG. 1, for example, the apparatus of the present invention receives red hot coke drawn out from a coke oven (1) in a movable coke receiver (2), and connects the receiver and a reaction tube (3). After the connection, coal that has been pulverized to a predetermined particle size is continuously supplied to the reaction tube (3) using a feeder (4), and at the same time the red hot coke is fed from the coke receiver (2) to the reaction tube (3). The red hot coke is brought into contact with the prepared pulverized coal to cause a rapid thermal decomposition reaction. The reaction products are then collected in a liquid product separator (6) via a char separator (5) and a cooler (7), respectively.
本発明において、フィーダー（４）より供給される原料
石炭としては、低石炭化度の弱粘結炭又は非粘結炭等の
低品位炭（亜歴青炭、ｍ炭）を使用することができる。In the present invention, low-grade coal (subbituminous coal, m coal) such as weakly caking coal or non-caking coal with a low degree of coalification may be used as the raw material coal supplied from the feeder (4). can.
又、石炭粒径としては、３ｆｌ以下のものが８０チ程度
以下であれば良いが、望ましくは２００メツシユ（７４
μ）以下が約７０％のボイラー用微粉炭程度の粒径のも
のが用いられる。In addition, the particle size of coal should be 3 fl or less and about 80 mesh or less, but preferably 200 mesh (74 mesh) or less.
The particle size of pulverized coal for boilers with about 70% of μ) or less is used.
また、反応管（５）における原料石炭の熱分解は、石炭
の種類にもよるが、約６５０℃付近からＣ−Ｃ結合の開
裂が激しくなり、炭化水素ガス。In addition, during the thermal decomposition of the raw coal in the reaction tube (5), although it depends on the type of coal, the C--C bonds begin to cleave violently from around 650°C, resulting in hydrocarbon gas.
液状生成物の収率が増大する。ところが、８５０℃程度
を超えると、−旦生成した分子量の大きいラジカル成分
の重縮合によるチャーへの転換が激しくなるため、炭素
の全転化率が再び低下し始める。したがって、反応温度
としては、６００〜１０００℃、望ましくは６５０〜８
５０℃程度が適当である。The yield of liquid product is increased. However, when the temperature exceeds about 850° C., the conversion of the previously generated radical component with a large molecular weight into char by polycondensation becomes intense, so that the total conversion rate of carbon starts to decrease again. Therefore, the reaction temperature is 600 to 1000°C, preferably 650 to 8°C.
Approximately 50°C is appropriate.
さらに、反応温度は温度、滞留時間等によって昇温速度
が変化するため決定しにくいが、本発明における反応時
間としては、〜１０秒程度で、石炭の昇温速度は数度〜
１０’℃／秒程度の急速加熱が適当である。Furthermore, it is difficult to determine the reaction temperature because the heating rate changes depending on the temperature, residence time, etc., but the reaction time in the present invention is about 10 seconds, and the heating rate of coal is several degrees or more.
Rapid heating at a rate of about 10'°C/sec is appropriate.
以上詳記した本発明の石炭の急速熱分解装置は、新人に
高温ガス発生設備を必要としないばかりでなく、反応に
必要なエネルギーとしてコークス炉からかま出しされる
赤熱コークスの顕熱を利用することができ、又コークス
の乾式消火（ＣＤＱ）設備と組合せて考えられる利点も
ある、などの特徴を有することから、新たに高温ガス発
生設備を必要とするためだけでもコスト的に高くつく前
記の従来の石炭の急速熱分解法に比べ、安価な低品位炭
から化学原料として有用なタール油類を格段に工業的有
利に安価で得られる、という工業的価値ある顕著な効果
を奏するものである。The rapid pyrolysis apparatus for coal of the present invention described in detail above not only does not require high-temperature gas generation equipment, but also utilizes the sensible heat of the red-hot coke ejected from the coke oven as the energy necessary for the reaction. It also has the advantage of being able to be combined with coke dry extinguishing (CDQ) equipment. Compared to the conventional rapid pyrolysis method of coal, this method has a remarkable effect of industrial value in that tar oil, which is useful as a chemical raw material, can be obtained from inexpensive low-rank coal at a much lower cost and with an industrial advantage. .
更に、本発明装置によれば、石炭の急速熱分解によって
生成するガス及びタール油類は、既設の化工品回収精製
設備をそのまま利用し、コークス製造時に発生する副産
物と共に回収精製を行うことができて好都合である。Furthermore, according to the device of the present invention, gas and tar oil produced by rapid pyrolysis of coal can be recovered and purified along with by-products generated during coke production by using existing chemical product recovery and refinement equipment as is. It's convenient.
第１図は本発明装置を説明する概略図である。
１・・・コークス炉、 ２・・・コークス受器、３・
・・反応管、 ４・・・石炭フィーダー５・・・
チャー分離器、６・・・液状生成物分離器、７・・・冷
却器、 ８・・・圧力制御バルン。FIG. 1 is a schematic diagram illustrating the apparatus of the present invention. 1... Coke oven, 2... Coke receiver, 3...
...Reaction tube, 4...Coal feeder 5...
Char separator, 6... Liquid product separator, 7... Cooler, 8... Pressure control balloon.
Claims (1)
けるコークス受器、原料石炭を供給するフィーダー、該
コークス受器より供給された赤熱コークスと該フィーダ
ーより供給された原料石炭とを接触させて熱分解反応を
行う反応器、反応生成物よりチャーを分離するチャー分
離器、及び、反応生成物より冷却器を介して液状生成物
を分離する液状生成物分離器を備えてなる石炭の急速熱
分解装置。(1) A coke receiver that receives the red hot coke drawn out from the coke oven, a feeder that supplies raw coal, and a coke receiver that brings the red hot coke supplied from the coke receiver into contact with the raw coal supplied from the feeder to heat the coke. Rapid pyrolysis of coal, comprising a reactor for performing a decomposition reaction, a char separator for separating char from a reaction product, and a liquid product separator for separating a liquid product from the reaction product via a cooler. Device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63167263A JP2564174B2 (en) | 1988-07-04 | 1988-07-04 | Coal rapid pyrolysis equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63167263A JP2564174B2 (en) | 1988-07-04 | 1988-07-04 | Coal rapid pyrolysis equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0216191A true JPH0216191A (en) | 1990-01-19 |
| JP2564174B2 JP2564174B2 (en) | 1996-12-18 |
Family
ID=15846492
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63167263A Expired - Lifetime JP2564174B2 (en) | 1988-07-04 | 1988-07-04 | Coal rapid pyrolysis equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2564174B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104449775A (en) * | 2014-12-17 | 2015-03-25 | 太原理工大成工程有限公司 | Method for directly using red coke obtained by high-temperature pyrolysis of pulverized coal |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57159886A (en) * | 1981-03-30 | 1982-10-02 | Hitachi Ltd | Spouted bed gasification of coal |
| JPS57205485A (en) * | 1981-03-27 | 1982-12-16 | Hartung Kuhn & Co Maschf | Process and equipment for obtaining water gas by utilizing exhaust gas upon cooling res heat coke extruded from furnace chamber |
| JPS5980492A (en) * | 1982-09-23 | 1984-05-09 | ハルトウング・ク−ン・ウント・コンパニ−・マシ−ネンフアブリク・ゲゼルシヤフト・ミツト・ベシユレンクテル・ハフトウング | Method and device for utilizing waste heat of coke cooling and manufacturing water gas |
-
1988
- 1988-07-04 JP JP63167263A patent/JP2564174B2/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS57205485A (en) * | 1981-03-27 | 1982-12-16 | Hartung Kuhn & Co Maschf | Process and equipment for obtaining water gas by utilizing exhaust gas upon cooling res heat coke extruded from furnace chamber |
| JPS57159886A (en) * | 1981-03-30 | 1982-10-02 | Hitachi Ltd | Spouted bed gasification of coal |
| JPS5980492A (en) * | 1982-09-23 | 1984-05-09 | ハルトウング・ク−ン・ウント・コンパニ−・マシ−ネンフアブリク・ゲゼルシヤフト・ミツト・ベシユレンクテル・ハフトウング | Method and device for utilizing waste heat of coke cooling and manufacturing water gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104449775A (en) * | 2014-12-17 | 2015-03-25 | 太原理工大成工程有限公司 | Method for directly using red coke obtained by high-temperature pyrolysis of pulverized coal |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2564174B2 (en) | 1996-12-18 |
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