JPH0759709B2 - How to control the humidity of coal - Google Patents

How to control the humidity of coal

Info

Publication number
JPH0759709B2
JPH0759709B2 JP21970988A JP21970988A JPH0759709B2 JP H0759709 B2 JPH0759709 B2 JP H0759709B2 JP 21970988 A JP21970988 A JP 21970988A JP 21970988 A JP21970988 A JP 21970988A JP H0759709 B2 JPH0759709 B2 JP H0759709B2
Authority
JP
Japan
Prior art keywords
tube
coal
dryer
humidity
dried
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
Application number
JP21970988A
Other languages
Japanese (ja)
Other versions
JPH01230916A (en
Inventor
克明 福永
勝久 松山
章 中村
啓一 駒井
武司 若林
文信 小野
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kawasaki Motors Ltd
Original Assignee
Kawasaki Jukogyo KK
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Kawasaki Jukogyo KK filed Critical Kawasaki Jukogyo KK
Priority to JP21970988A priority Critical patent/JPH0759709B2/en
Publication of JPH01230916A publication Critical patent/JPH01230916A/en
Publication of JPH0759709B2 publication Critical patent/JPH0759709B2/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
    • F26B11/02—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles
    • F26B11/04—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis
    • F26B11/0404—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis with internal subdivision of the drum, e.g. for subdividing or recycling the material to be dried
    • F26B11/0418—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis with internal subdivision of the drum, e.g. for subdividing or recycling the material to be dried the subdivision consisting of a plurality of parallel tubes, e.g. through which the material to be dried is conveyed in single or multi-pass fashion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B11/00—Machines or apparatus for drying solid materials or objects with movement which is non-progressive
    • F26B11/02—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles
    • F26B11/04—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis
    • F26B11/0404—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis with internal subdivision of the drum, e.g. for subdividing or recycling the material to be dried
    • F26B11/0418—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis with internal subdivision of the drum, e.g. for subdividing or recycling the material to be dried the subdivision consisting of a plurality of parallel tubes, e.g. through which the material to be dried is conveyed in single or multi-pass fashion
    • F26B11/0422—Machines or apparatus for drying solid materials or objects with movement which is non-progressive in moving drums or other mainly-closed receptacles rotating about a horizontal or slightly-inclined axis with internal subdivision of the drum, e.g. for subdividing or recycling the material to be dried the subdivision consisting of a plurality of parallel tubes, e.g. through which the material to be dried is conveyed in single or multi-pass fashion the tubes having internal members
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/18—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact
    • F26B3/22—Drying solid materials or objects by processes involving the application of heat by conduction, i.e. the heat is conveyed from the heat source, e.g. gas flame, to the materials or objects to be dried by direct contact the heat source and the materials or objects to be dried being in relative motion, e.g. of vibration

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Microbiology (AREA)
  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Coke Industry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)

Description

【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、コークス原料炭などの比較的石炭化度の高い
石炭類を、チューブ内側に被乾燥物を流通させ、チュー
ブ外側に加熱媒体を流通させる型式のチューブドライヤ
を使用して、効率よく調湿する方法に関するものであ
る。DETAILED DESCRIPTION OF THE INVENTION [Industrial field of application] The present invention relates to coals having a relatively high degree of coalification such as coke coking coal, in which a material to be dried is circulated inside the tube and a heating medium is arranged outside the tube. The present invention relates to a method for efficiently controlling humidity by using a tube dryer of a circulating type.

〔従来の技術〕[Conventional technology]

コークス原料炭などの比較的石炭化度の高い石炭類で
は、褐炭などの若年炭と異なり、露天積みの石炭であっ
ても、その水分は10〜20重量％程度である。上記原料炭
をコークス炉投入前に、原料炭の水分を調製すること
で、製品コークスの品質およびコークス炉の操業効率を
向上させ、省エネルギーを図るようにする方法が従来か
ら知られている。また一般炭においても、ボイラ投入前
に水分を減らし、ボイラ排ガス量を減らして排ガス処理
設備を小型化するとともに、省エネルギー対策とするこ
とも知られている。Coal, which has a relatively high degree of coalification such as coke coking coal, has a moisture content of about 10 to 20% by weight even in open-air coal, unlike young coal such as brown coal. A method has been conventionally known in which the quality of product coke and the operating efficiency of the coke oven are improved by adjusting the water content of the coke oven before the coke oven is charged into the coke oven to save energy. It is also known that steam coal is reduced in water content before it is charged into the boiler to reduce the amount of exhaust gas from the boiler to reduce the size of the exhaust gas treatment facility and also as an energy saving measure.

こうした石炭の調湿技術としては、つぎのようなものが
公知である。すなわち、石炭の乾燥装置としては、従
来、 （１） 熱風気流乾燥などを行う直接加熱型、 （２） 伝導受熱溝型撹拌装置、チューブドライヤなど
の間接加熱型、 が知られている。The following is known as such a humidity control technique for coal. That is, as a coal drying device, conventionally, (1) a direct heating type for performing hot air flow drying, etc., (2) a conduction heat receiving groove type stirring device, an indirect heating type such as a tube dryer are known.

上記のチューブドライヤは、傾斜回転円筒内に軸方向に
多数のチューブを配設して構成したもので、チューブ内
に被乾燥物を流通させ、チューブ外側にスチームなどの
加熱媒体を流通させて被乾燥物を間接加熱するマテリア
ルインチューブ型、および逆にチューブ内にスチームな
どの加熱媒体を流通させ、チューブ外側に被乾燥物を流
通させて被乾燥物を間接加熱するスチームインチューブ
型が用いられている。The above-mentioned tube dryer is configured by arranging a large number of tubes in an axial direction in an inclined rotary cylinder, and a material to be dried is circulated in the tube, and a heating medium such as steam is circulated on the outside of the tube to cover the material to be dried. Material-in-tube type that indirectly heats the dried product, and conversely, steam-in-tube type that heats the dried substance by circulating a heating medium such as steam in the tube and circulating the dried substance outside the tube is used. ing.

マテリアルインチューブ型のチューブドライヤとして、
従来、高水分褐炭の乾燥用に、フラットバー（幅20〜25
mm）をスパイラル状にした撹拌手段をチューブ内のほぼ
全長にわたって挿入し、チューブ内面（伝熱面）との接
触機会を増すようにしたものや、小チューブ外周に粒子
径程度の太さのワイヤを巻き付けた撹拌手段をチューブ
内のほぼ全長にわたつて挿入し、石炭とチューブ内面
（伝熱面）との接触機会を増すようにしたものが知られ
ている。As a material-in-tube type tube dryer,
Conventionally, a flat bar (width 20-25
(mm) spiral-shaped stirring means is inserted over almost the entire length of the tube to increase the chance of contact with the inner surface of the tube (heat transfer surface), or a wire with a particle diameter on the outer circumference of a small tube. It is known that a stirring means wound around is inserted over almost the entire length of the tube to increase the chance of contact between the coal and the tube inner surface (heat transfer surface).

またマテリアルインチューブ型の一例として、米国特許
第3,765,102号明細書および図面に示される構造のもの
が知られている。これは第９図および第10図に示すよう
に、チューブ１の内部に縦フイン状のフラツトバー２を
取り付け、粉粒体層を掻き上げて、伝熱面との接触面積
を拡げる作用をする撹拌手段を設けるものである。３は
管板、４は支持リング、５はせきである。またスチーム
インチューブ型の一例として、特開昭63−3089号公報に
示されるように、乾燥機の長手方向を三分割し、入口部
にオーステナイト系耐酸ステンレス材料、中間部に二相
ステンレス材料、出口部に炭素鋼を用いた石炭乾燥機が
知られている。Further, as an example of the material-in-tube type, one having a structure shown in US Pat. No. 3,765,102 and the drawings is known. As shown in FIG. 9 and FIG. 10, a vertical fin-shaped flat bar 2 is attached to the inside of the tube 1 to scrape up the powder / granular material layer and expand the contact area with the heat transfer surface. Means are provided. 3 is a tube sheet, 4 is a support ring, and 5 is a cough. Further, as an example of a steam-in-tube type, as shown in JP-A-63-3089, the longitudinal direction of the dryer is divided into three, the austenitic acid-resistant stainless steel material at the inlet, the duplex stainless steel material at the middle, A coal dryer using carbon steel at the outlet is known.

〔発明が解決しようとする問題点〕[Problems to be solved by the invention]

上記の熱風気流乾燥などを行う直接加熱型は、排ガスの
持去りエンタルピが大きく、間接加熱型に比較して熱効
率が低い。また処理風量が多いため、排ガス処理設備が
大型となり、またランニングコストも高い。さらに熱源
温度が高く、風量も多いので、発塵量が大きいなどの不
都合な点を有している。The direct heating type, which performs the above hot air flow drying, has a large enthalpy to carry away exhaust gas, and has a lower thermal efficiency than the indirect heating type. Further, since the amount of treated air is large, the exhaust gas treatment facility becomes large and the running cost is high. Further, since the heat source temperature is high and the air volume is large, there are disadvantages such as a large dust generation amount.

また伝導受熱溝型撹拌装置においては、充填率を高くす
ると、被乾燥物の混合が悪くなり、伝熱係数が低くなる
とともに、撹拌動力が多くなる反面、充填率を低くする
と、伝熱面積が相対的に少なくなり、いずれにせよ装置
容量が増大する。また回転部分の製作制度が要求され、
装置価格が割高である。In addition, in the conduction heat receiving groove type agitator, when the filling rate is increased, the mixing of the material to be dried is deteriorated and the heat transfer coefficient is lowered, while the stirring power is increased, but when the filling rate is decreased, the heat transfer area is reduced. It is relatively small and the device capacity increases anyway. In addition, a manufacturing system for rotating parts is required,
Equipment price is high.

スチームインチューブ型のチューブドライヤでは、材料
充填率は通常、10〜20％で伝熱面の利用率が少なくなる
こともあって、装置容量が大きくなる。また材料の流路
が複雑で、材料微粉の固着・堆積が生じて腐食のおそれ
がある。シェル内面では蒸発水分の再凝縮が生じ、上記
微粉が固着し腐食を誘発させる。そのため、チューブお
よびシェルに高価な材料を使用しなければならない。In the steam-in-tube type tube dryer, the material filling rate is usually 10 to 20%, and the utilization rate of the heat transfer surface may be reduced, so that the apparatus capacity is increased. Moreover, the flow path of the material is complicated, and the fine powder of the material may be fixed and deposited to cause corrosion. Re-condensation of evaporated water occurs on the inner surface of the shell, and the fine powder adheres to cause corrosion. Therefore, expensive materials have to be used for the tubes and shells.

また従来のマテリアルインチューブ型のチューブドライ
ヤでは、前述のフラットバーをスパイラル状にした撹拌
手段や、小チューブ外周に粒子径程度の太さのワイヤを
巻き付けた撹拌手段は、いずれも高水分褐炭（水分60〜
70重量％）を水分20〜30重量％に乾燥するために開発さ
れたもので、乾燥能力が大きい割にはチューブ内の石炭
流速を抑制して、処理可能な流量は低くなっており、比
較的乾燥負荷が小さく、処理量の大きい場合には、円筒
系が大きくなり製作、輸送上好ましくない。しかも撹拌
手段がチューブのほぼ全長にわたり、重量が大きく、交
換・清掃・メンテナンス作業も繁雑である。Further, in the conventional material-in-tube type tube dryer, the agitating means in which the flat bar is made into a spiral shape and the agitating means in which a wire having a particle diameter is wound around the outer circumference of the small tube are both high-moisture brown coal ( Water 60 ~
(70% by weight) was developed to dry the water to 20 to 30% by weight, and although the drying capacity is large, the flow rate of coal that can be processed is suppressed by suppressing the flow rate of coal in the tube. When the dynamic drying load is small and the processing amount is large, the cylindrical system becomes large, which is not preferable in manufacturing and transportation. Moreover, the agitation means is heavy over almost the entire length of the tube, and replacement, cleaning and maintenance work is complicated.

また米国特許第3,765,102号明細書および図面に示され
た、縦フィン状のフラットバーを取り付けたものは、流
動抵抗が大きくなり、上記の褐炭乾燥用の場合と同様に
好ましくない。さらに同米国特許明細書および図面に、
チューブ出口にせきを設けて、チューブ内滞留時間の調
整をはかる方式が開示されているが、粒子毎にバラツキ
があり、一部の材料は過乾燥となり、また完全排出が困
難で、微粉が固着し腐食を誘発する。Further, the one provided with the vertical fin-shaped flat bar shown in U.S. Pat. No. 3,765,102 and the drawings has a large flow resistance, which is not preferable as in the case of drying the brown coal described above. Further, in the US patent specification and drawings,
A method of adjusting the residence time in the tube by providing a weir at the tube outlet is disclosed, but there are variations in each particle, some materials become overdried, and complete discharge is difficult, and fine powder adheres. Induces corrosion.

上記のコークス原料炭は、発塵性の問題から、せいぜい
水分４〜７重量％程度まで乾燥すれば十分である。褐炭
の乾燥と比較すると、同じ原料に対して蒸発水分量は褐
炭の1/2〜1/3で済む。そのため処理量を２〜３倍量に増
大する必要があるが、従来タイプのチューブドライヤで
は、チューブ径が小さいとか、チューブ内に装填されて
いる撹拌手段が複雑な形状をしており、その流動抵抗に
よって十分な処理量を確保できなかった。From the problem of dusting properties, it is sufficient to dry the above coke raw coal to a water content of at most 4 to 7% by weight. Compared to the drying of brown coal, the amount of water vaporized for the same raw material is 1/2 to 1/3 that of brown coal. Therefore, it is necessary to increase the processing amount by 2 to 3 times, but in the conventional type tube dryer, the tube diameter is small or the stirring means loaded in the tube has a complicated shape, Due to the resistance, a sufficient amount of processing could not be secured.

コークス原料炭などの比較的石炭化度の高い石炭を、通
常、撹拌手段を廃したチューブに供給すると、石炭がチ
ューブの回転方向にせり上がり、かつせり上がり角が安
息角以上になることにより崩壊して撹拌させる現象（以
下、キルンアクションという）が生成せず、そのため流
速も速く、伝熱特性も悪くなる。When coal with a relatively high degree of coalification such as coke coking coal is supplied to a tube without a stirring means, the coal rises in the direction of rotation of the tube and collapses when the rising angle exceeds the repose angle. Therefore, the phenomenon of agitating (hereinafter, referred to as kiln action) is not generated, so that the flow velocity is high and the heat transfer characteristics are poor.

ところが、チューブ内の平均充填率を15％以上、望まし
くは30〜50％程度とすることにより、キルンアクション
を安定して生成せしめ、チューブ内の滞留時間を確保
し、また伝熱量を向上させることを、本発明者らは実験
によって見い出した。However, by setting the average filling rate in the tube to 15% or more, preferably about 30 to 50%, it is possible to stably generate the kiln action, secure the residence time in the tube, and improve the heat transfer amount. The present inventors found out by experiment.

また前記の特開昭63−3089号によれば、石炭層と接する
チューブ鉄皮温度（内面温度）が低温度域（120℃以
下、条件によっては130℃以下の場合もある）になる
と、石炭から遊離する成分（SO4 2-やCl-）による腐食が
発生することが知られている。Further, according to the above-mentioned JP-A-63-3089, when the temperature of the tube skin (inner surface temperature) in contact with the coal layer is in a low temperature range (120 ° C. or less, 130 ° C. or less depending on conditions), coal component free (SO 4 2-or Cl -) from corrosion by is known to occur.

さらに、前記の特開昭63−3089号では、このような腐食
に対して、二相ステンレス鋼やチタンなどの高級材料を
用いているが、腐食は軽減し、寿命は若干延びるもの
の、材料費が嵩み（約20倍となる）、経済的ではない。Further, in the above-mentioned JP-A-63-3089, high-grade materials such as duplex stainless steel and titanium are used for such corrosion, but the corrosion is reduced and the life is slightly extended, but the material cost is reduced. Is bulky (approx. 20 times) and not economical.

石炭の入口水分は平均９重量％程度であるが、天候や炭
塵飛散抑制のための散水、炭種差により、７〜12重量％
まで変動する。一方、出口水分は、乾燥炭のハンドリン
グ時の炭塵発生防止のため、５重量％前後の一定値を維
持する場合が多い。The average water content at the inlet of coal is about 9% by weight, but 7-12% by weight depending on the weather, watering to control the scattering of coal dust, and differences in coal types.
Fluctuates up to. On the other hand, the outlet water content often maintains a constant value of around 5% by weight in order to prevent the generation of coal dust when handling dry coal.

入口石炭水分の変動に応じて、乾燥能力を調節するに
は、従来、スチームの圧力制御により伝熱量調整を行っ
ていた。しかし、入口石炭が低水分の場合には、スチー
ムは低圧となってチューブ温度が120℃より低くなり、
腐食が生じるおそれがある。In order to adjust the drying capacity according to the fluctuation of the inlet coal moisture, the heat transfer amount has conventionally been adjusted by controlling the pressure of steam. However, when the inlet coal has low water content, the steam becomes low pressure and the tube temperature becomes lower than 120 ° C,
Corrosion may occur.

また、処理量が設計条件よりも低くなった場合にも、過
乾燥防止上、スチーム圧を低圧とすると、同様に腐食を
招来する温度域となってしまう。Further, even when the treatment amount is lower than the design condition, if the steam pressure is set to a low pressure in order to prevent overdrying, the temperature range similarly causes corrosion.

なお、マテリアルインチューブ型のドライヤは、高水分
褐炭用のドライヤとして、現在まで多くの実績がある
が、本発明において示す物性の石炭（主として原料炭）
と異なり、褐炭では成分の違いがあって、低温度域での
腐食例は見られていなかった。Note that the material-in-tube type dryer has many achievements up to the present as a dryer for high-moisture lignite, but it has the physical properties shown in the present invention (mainly coking coal).
In contrast to brown coal, there was no difference in the composition, and no corrosion cases were observed in the low temperature range.

また、スチームインチューブ型のドライヤでは、チュー
ブ内に石炭と熱交換し凝縮したスチームコンデンセート
が存在し、そのため、比較的伝熱抵抗の大きな凝縮水に
接する部分のチューブ鉄皮温度が低下して、腐食の発生
が見られる。Further, in the steam-in-tube type dryer, there is steam condensate that is heat-exchanged with coal and condensed in the tube, so the tube skin temperature of the part in contact with condensed water with a relatively large heat transfer resistance decreases, Corrosion is observed.

スチームインチューブ型は、構造上、凝縮水が伝熱面に
滞留するため、チューブを高級材料にするか、チューブ
鉄皮温度を高温に維持するためにスチーム圧力を上げる
かの方法を採らざるを得ず、経済的でない。In the steam-in-tube type, condensed water stays on the heat transfer surface due to its structure, so it is necessary to use a high-grade material for the tube or to increase the steam pressure to maintain the tube shell temperature at a high temperature. Not profitable and not economical.

本発明者らは、スチームのチューブドライヤ内の温度を
130℃以上として、チューブ鉄皮温度（内面温度）を120
℃以上、望ましくは130℃以上とすると、原料炭処理時
の腐食が抑えられ、SGPなどの低級材料で十分な耐食性
が得られることを利用して本発明に至つた。The present inventors have determined the temperature inside the steam tube dryer.
When the temperature is 130 ℃ or higher, the tube skin temperature (inner surface temperature) is 120
The present invention has been achieved by utilizing the fact that when the temperature is not lower than 130 ° C., preferably not lower than 130 ° C., the corrosion at the time of raw material coal treatment is suppressed and sufficient corrosion resistance can be obtained with a low-grade material such as SGP.

また、チューブドライヤの特性として、ドライヤ回転数
を上げると、チューブ内の石炭流速が増加すること、お
よび、さらに、石炭流速が上がっても、チューブを長く
して滞留時間を長く保つか、またはスチーム圧力（また
は温度）を高めるかの方法を採ることで、所望の乾燥能
力を維持できることが判明している。As a characteristic of the tube dryer, increasing the dryer rotation speed increases the coal flow rate in the tube, and even if the coal flow rate increases, the tube is lengthened to keep the residence time longer or the steam It has been found that the desired drying capacity can be maintained by increasing the pressure (or temperature).

本発明は上記の諸点に鑑みなされたもので、従来、褐炭
などの高水分炭の乾燥にしか使用されていなかったマテ
リアルインチューブ型のチューブドライヤを使用し、チ
ューブ径を従来型の２〜３倍とし、さらにチューブ内の
撹拌手段を廃し、または簡単な形状のものにすることに
より、必要な乾燥能力を維持した上で、処理量を上げる
ことができるようにした石炭の調湿方法を提供すること
を目的とするものである。The present invention has been made in view of the above points, and uses a material-in-tube type tube dryer which has been conventionally used only for drying high-moisture coal such as brown coal, and has a tube diameter of 2 to 3 of the conventional type. We provide a humidity control method for coal that doubles the number of times, by eliminating the stirring means inside the tube or making it into a simple shape, while maintaining the required drying capacity and increasing the throughput. The purpose is to do.

また本発明は、チューブドライヤの回転数を制御して
（高くして）、石炭の乾燥能力を維持したまま、スチー
ム温度を130℃以上の高温に保持し、チューブ鉄皮温度
を120℃、望ましくは130℃以上に保って、腐食温度域以
上とすることにより、SGP、STPGなどの普通のカーボン
スチール材でも、腐食のおそれのない石炭の調湿方法を
提供することを目的とするものである。In addition, the present invention controls the rotation speed of the tube dryer (increases) to maintain the steam drying capacity of coal and maintain the steam temperature at a high temperature of 130 ° C or higher, and the tube shell temperature of 120 ° C, preferably Is to keep the temperature above 130 ° C and keep it above the corrosion temperature range to provide a method for controlling the humidity of coal without the risk of corrosion even with ordinary carbon steel materials such as SGP and STPG. .

〔問題点を解決するための手段および作用〕[Means and Actions for Solving Problems]

上記の目的を達成するために、本発明の石炭の調湿方法
は、図面に示すように、純炭基準で揮発分含有率が45重
量％以下であり、粒径3mm以下の重量割合が75％以上で
あり、湿炭基準の水分含有率が20重量％以下である一種
類の石炭または数種類の石炭の混合物を、傾斜回転円筒
10内に軸方向に多数のチューブ１を配設し、該チューブ
内に被乾燥物を流通させ、チューブ外側にスチームなど
の加熱媒体を流通させて、被乾燥物を間接加熱するマテ
リアルインチューブ型のチューブドライヤに導入して、
湿炭基準の水分含有率が４〜７重量％になるように乾燥
させることを特徴としている。In order to achieve the above object, the method for controlling the humidity of coal of the present invention, as shown in the drawing, has a volatile content of 45% by weight or less based on pure coal, and a weight ratio of 3 mm or less with a particle diameter of 75%. % Or more and a wet coal-based water content of 20% by weight or less, one kind of coal or a mixture of several kinds of coal is used as an inclined rotary cylinder.
A material-in-tube type in which a large number of tubes 1 are axially arranged in the tube 10, a material to be dried is circulated in the tube, and a heating medium such as steam is circulated outside the tube to indirectly heat the material to be dried. Introduced into the tube dryer of
It is characterized by drying so that the moisture content based on wet coal is 4 to 7% by weight.

チューブ１の断面積に占める石炭層の割合が平均して15
〜40％となるように制御するのが望ましく、チューブの
入口部で50％以上となるように制御するのが望ましい。
15％未満では、キルンアクションが生成しない。そのた
めチューブ内面（伝達面）との接触面積が小さく、石炭
層の撹拌が十分に行われないために伝達効率が低い反
面、チューブ内流通がキルンアクションが生成した場合
に比べて大きくなるので、十分な乾燥を行うためにはチ
ューブ長が著しく長くなって不都合である。The average proportion of coal bed in the cross-sectional area of tube 1 is 15
It is desirable to control it so that it is -40%, and it is desirable to control it so that it is 50% or more at the inlet of the tube.
Below 15%, no kiln action will be generated. Therefore, the contact area with the inner surface of the tube (transfer surface) is small, and the transfer efficiency is low because the coal layer is not sufficiently stirred, but the flow in the tube is larger than when kiln action is generated, so it is sufficient. It is inconvenient because the tube length becomes extremely long in order to perform proper drying.

通常、チューブの入口側では石炭水分が高く、そのため
流速が小さく充填割合も高いのに対して、出口側では、
石炭水分が低くなって流速が大きく充填割合が低い。そ
のため出口側でキルンアクションを確保するためには、
出入口の石炭水分にもよるが、上記のような範囲の水分
に対しては、チューブの入口部で50％以上なければ不都
合である。Usually, coal moisture is high on the inlet side of the tube, so the flow rate is low and the filling rate is high, while on the outlet side,
The water content of coal is low, the flow velocity is high, and the filling rate is low. Therefore, in order to secure the kiln action at the exit side,
Although it depends on the water content of the coal at the entrance and exit, it is inconvenient for the water content in the above range to be 50% or more at the entrance of the tube.

また充填割合が50％を越えると、石炭の流動速度が減少
して行くため流動状態が不安定になり、チューブ内の詰
りや充填率のバラツキが発生する。よって局所的にも充
填割合が50％を越えることのないよう、平均充填率を40
％以下に抑えることが望ましい。Further, when the filling rate exceeds 50%, the flow rate of coal decreases and the flow state becomes unstable, causing clogging in the tube and variations in the filling rate. Therefore, make sure that the average filling rate is 40% so that the filling rate does not exceed 50% locally.
It is desirable to keep the percentage below.

また乾燥すべき材料のチューブドライヤへの供給量がほ
ぼ一定に制御された条件において、チューブドライヤ入
口フード11内の材料の粉体レベルが上昇しないよう、か
つチューブドライヤからの材料の排出量が減少しないよ
うに、これらを検出しながらチューブドライヤの回転数
を限界近くまで低下させることによって、チューブの断
面積に占める石炭量の割合を制御するのが望ましい。Also, under the condition that the supply amount of the material to be dried to the tube dryer is controlled to be almost constant, the powder level of the material in the tube dryer inlet hood 11 is not increased and the discharge amount of the material from the tube dryer is reduced. It is desirable to control the ratio of the amount of coal in the cross-sectional area of the tube by lowering the rotation speed of the tube dryer to the limit while detecting these so as not to do so.

また、本発明の石炭の調湿方法は、純炭基準で揮発分含
有率が45重量％以下であり、粒径3mm以下の重量割合が7
5％以上であり、湿炭基準の水分含有率が20重量％以下
である一種類の石炭または数種類の石炭の混合物を、傾
斜回転円筒内に軸方向に多数のチューブを配設し、該チ
ューブ内に撹拌手段16を装入し、チューブ内に被乾燥物
を流通させ、チューブ外側にスチームなどの加熱媒体を
流通させて、被乾燥物を間接加熱するマテリアルインチ
ューブ型のチューブドライヤに導入して、湿炭基準の水
分含有率が４〜７重量％になるように乾燥させることを
特徴としている。The coal humidity control method of the present invention has a volatile content of 45% by weight or less based on pure coal, and a weight ratio of 3 mm or less with a particle size of 7%.
One kind of coal or a mixture of several kinds of coal having a moisture content of 5% or more and a wet coal standard of 20% by weight or less is provided with a large number of tubes in an axial direction in an inclined rotary cylinder, and the tubes are The stirring means 16 is charged into the tube, the material to be dried is circulated in the tube, and a heating medium such as steam is circulated outside the tube, and the material is introduced into a tube dryer of the material-in-tube type that indirectly heats the material to be dried. And is dried so that the moisture content based on wet coal is 4 to 7% by weight.

撹拌手段としては、第１図〜第３図に示すような、スパ
イラル状の線材からなるもの、第４図および第５図に示
すような、チューブ横断面方向にリング状のせきを一定
間隔で数枚並べた形状のもの、第６図および第７図に示
すような、チューブ内面に接するようにフラットバー23
数条をチューブ軸方向に配列した形状のものなどを用い
るのが望ましい。As the stirring means, a spiral wire rod as shown in FIGS. 1 to 3 and ring-shaped weirs at regular intervals in the tube cross-sectional direction as shown in FIGS. 4 and 5 are provided. Several pieces arranged side by side, flat bar 23 as shown in FIGS. 6 and 7 so that it touches the inner surface of the tube.
It is desirable to use one having a shape in which several lines are arranged in the tube axial direction.

また本発明の石炭の調湿方法は、スチームなどの加熱媒
体のチューブドライヤ内における温度が130℃以上とな
るように、チューブドライヤ回転数を制御することを特
徴としている。Further, the method for controlling the humidity of coal of the present invention is characterized in that the number of rotations of the tube dryer is controlled so that the temperature of the heating medium such as steam in the tube dryer becomes 130 ° C or higher.

さらに本発明の石炭の調湿方法は、スチームなどの加熱
媒体のチューブドライヤ内における温度を130℃以上と
する代りに、チューブ鉄皮温度を120℃以上とすること
を特徴としている。Furthermore, the coal humidity control method of the present invention is characterized in that the tube iron shell temperature is set to 120 ° C. or higher instead of setting the temperature of the heating medium such as steam in the tube dryer to 130 ° C. or higher.

チューブの内面の腐食を抑制するためには、チューブの
鉄皮温度（内面温度）が120℃以上となるようにすれば
良いのであるが、回転しているドライヤ内のチューブ鉄
皮温度を測定するには工業的に簡便な方法がなく、信頼
性にも乏しい。マテリアルインチューブ型のチューブド
ライヤでは、スチーム圧力はドライヤ内のどの部分も一
定であって、またチューブ鉄皮内の温度降下も非常に小
さいため、チューブ鉄皮温度を測定する代りに、測定が
容易なドライヤ入口部のスチーム温度を検出して制御し
てもよい。発生した凝縮水も、チューブ鉄皮からすぐに
分離されてドライヤから排出されるため、ほぼドライヤ
内のスチーム温度と等しく、ドライヤ出口部の温度を測
定して制御してもよい。In order to suppress the corrosion of the inner surface of the tube, it is necessary to set the tube skin temperature (inner surface temperature) to 120 ° C or higher, but measure the tube skin temperature in the rotating dryer. There is no industrially convenient method, and reliability is poor. In the material-in-tube type tube dryer, the steam pressure is constant in all parts of the dryer, and the temperature drop in the tube shell is very small, so it is easy to measure instead of measuring the tube shell temperature. Alternatively, the steam temperature at the entrance of the dryer may be detected and controlled. The generated condensed water is also immediately separated from the tube shell and discharged from the dryer, so that the steam temperature in the dryer is substantially equal to the temperature of the dryer outlet, and the temperature may be measured and controlled.

定格乾燥能力のドライヤで、入口水分の低い石炭を処理
する場合、過乾燥を防ぐためにスチーム温度を下げる
と、チューブ材の腐食が生じる。When using a dryer with a rated drying capacity to process coal with a low inlet water content, lowering the steam temperature to prevent overdrying causes corrosion of the tube material.

そこで、スチーム温度を腐食のおそれのない130℃以上
に保った上で、出口石炭水分が所定水分となるように、
ドライヤ回転数を制御する。Therefore, keep the steam temperature at 130 ° C or higher, where there is no risk of corrosion, so that the water content of the coal at the outlet becomes the specified water content.
Controls the dryer speed.

石炭水分が低いと流動性が良好となり、チューブ内の石
炭充満率が低下するが、撹拌手段を装入していることに
よって、キルンアクションをより安定して生成せしめ、
充分な乾燥能力を保つことができる。When the water content of the coal is low, the fluidity is good, and the filling rate of the coal in the tube is reduced, but by installing the stirring means, the kiln action is generated more stably,
A sufficient drying ability can be maintained.

また原料石炭の純炭基準での揮発分含有率が30重量％以
下のものを用いるのが望ましく、かつ湿炭基準での水分
含有率が平均的には８〜12重量％のものを用いるのが望
ましい。It is desirable to use a raw coal having a volatile matter content of 30% by weight or less based on pure coal, and a water content of 8 to 12% by weight on average based on wet coal. Is desirable.

さらに傾斜回転円筒の傾斜角を５〜15゜とするのが望ま
しい。５゜未満では、チューブ内の石炭流速が小さく、
処理量が小さくなる反面、滞留時間が長くなるので、出
口の石炭は過乾燥となる。該水分範囲のものに５゜未満
の傾斜角のまま適用すると、円筒径の大きな、円筒長の
短い形状のドライヤとなり、製作・輸送上共不都合であ
る。また処理量を上げるために、回転数を大きくするこ
とは、後述のように問題がある。一方、15゜を越える
と、スラスターまたはシャフト軸受部のストッパ等のド
ライヤ軸方向の担持装置が大がかりなものとなり、製作
上、経済上好ましくない。Further, it is desirable that the inclination angle of the inclined rotary cylinder be 5 to 15 °. Below 5 °, the flow velocity of coal in the tube is low,
Although the treatment amount becomes small, the residence time becomes long, so the coal at the outlet is overdried. If the tilt angle of less than 5 ° is applied to those having a water content range, a dryer having a large cylinder diameter and a short cylinder length is formed, which is inconvenient for production and transportation. Further, increasing the number of rotations in order to increase the processing amount has a problem as described later. On the other hand, if the angle exceeds 15 °, the thruster or the stopper of the shaft bearing, etc., in the axial direction of the dryer will be large, which is economically unfavorable in production.

また傾斜回転円筒の回転数を５〜25rpm、直径を600〜60
00mm、チューブの本数を６本以上、チューブの内径を15
0mm以上とするのが望ましい。5rpm未満では、傾斜角５
゜未満の場合と同様に、チューブ一本当りの処理量が小
さくなるため、ドライヤが大径短筒の形状となって好ま
しくない。一方、25rpmを越えると、軸受等回転部の寿
命が短くなり、動力も大きくなるばかりでなく、特に回
転軸より離れた位置にあるチューブでは、遠心力の影響
が強くなり、キルンアクションが阻害される場合もあっ
て好ましくない。The rotation speed of the inclined rotary cylinder is 5 to 25 rpm, and the diameter is 600 to 60.
00mm, the number of tubes is 6 or more, the inner diameter of the tube is 15
It is desirable to set it to 0 mm or more. Below 5 rpm, inclination angle is 5
As in the case of less than 0 °, the amount of treatment per tube becomes small, so that the dryer becomes a large-diameter short tube shape, which is not preferable. On the other hand, if it exceeds 25 rpm, not only the life of rotating parts such as bearings will be shortened and power will be increased, but especially for tubes located far from the rotation axis, the influence of centrifugal force will be strong and the kiln action will be hindered. It may not be preferable.

本発明に係わる範囲においては、チューブの内径が150m
m未満では、チューブ一本当りの処理量が著しく過小と
なり、滞留時間も増大して乾燥能力が過大となる。その
ためドライヤは、傾斜角が５゜未満の場合より以上に製
作、輸送上不都合な形状となって好ましくない。In the range related to the present invention, the inner diameter of the tube is 150 m
If it is less than m, the amount of treatment per tube becomes extremely small, the residence time also increases, and the drying capacity becomes excessive. Therefore, the dryer is unfavorable because it is more inconvenient to manufacture and transport than when the inclination angle is less than 5 °.

直径が600未満では、150mm以上のチューブを複数配置す
ることが困難であり、6000mmを越えると、製作・輸送上
困難となり、またチューブ本数が余りにも多すぎて、チ
ューブへの均一な石炭投入が難しい。If the diameter is less than 600, it is difficult to place multiple tubes of 150 mm or more, and if it exceeds 6000 mm, it is difficult to manufacture and transport, and the number of tubes is too large, and uniform coal feeding into the tubes is not possible. difficult.

チューブの本数が５本以下では、ドライヤ断面に占める
チューブ断面積の総和の割合、すなわちドライヤ径に対
する石炭流路割合が低下して不経済である。When the number of tubes is 5 or less, the ratio of the total tube cross-sectional area in the dryer cross section, that is, the ratio of the coal flow path to the dryer diameter is reduced, which is uneconomical.

〔実施例〕〔Example〕

以下、図面を参照して本発明の好適な実施例を詳細に説
明する。ただしこの実施例に記載されている構成機器の
材質、形状、その相対配置などは、とくに特定的な記載
がない限りは、本発明の範囲をそれらのみに限定する趣
旨のものではなく、単なる説明例にすぎない。Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings. However, the materials, shapes, relative arrangements, and the like of the constituent devices described in this example are not intended to limit the scope of the present invention to them only unless otherwise specified, and are simply described. It's just an example.

第１図は本発明の方法を実施するチューブドライヤの一
例を示している。10は横型の傾斜回転円筒であり、駆動
手段（図示せず）により軸心周りに回転できるように構
成されている。この傾斜回転円筒10は、被乾燥物供給側
からみて、約10゜程度の下り勾配をもって設置されてい
る。FIG. 1 shows an example of a tube dryer for carrying out the method of the present invention. Reference numeral 10 denotes a horizontal inclined rotary cylinder, which is configured to be rotatable about its axis by a driving means (not shown). The inclined rotating cylinder 10 is installed with a downward slope of about 10 ° when viewed from the side of supplying the material to be dried.

石炭などの被乾燥物は入口フード11に供給され、傾斜回
転円筒10の両端の管板３に多数設置されているチューブ
１を通過する間に、チューブ１の外側を流れる加熱媒体
とチューブ壁を隔てて熱交換し乾燥されて、チューブ出
口端より排出される。熱媒体、たとえば数気圧のスチー
ムは、回転継手12を経て円筒10内に供給され、上記チュ
ーブ外側を加熱した後、凝縮して円筒下流の底部に流
れ、円筒の回転運転に従ってドレン管13を通り、回転継
手14を経て排出される。The material to be dried such as coal is supplied to the inlet hood 11, and while passing through the tubes 1 installed in the tube plates 3 at both ends of the inclined rotary cylinder 10, the heating medium flowing outside the tube 1 and the tube wall are separated. It is heat-exchanged and separated, dried, and discharged from the tube outlet end. The heat medium, for example, steam of several atm is supplied into the cylinder 10 through the rotary joint 12, heats the outside of the tube, then condenses and flows to the bottom of the cylinder downstream, and passes through the drain pipe 13 according to the rotation operation of the cylinder. , Is discharged through the rotary joint 14.

本発明の方法では、褐炭に比べて水分の低い石炭を乾燥
させるために、以下の処置を以ってより効率を高めるこ
とができる。まず、チューブ径は100mm前後の褐炭用に
対して、150〜300mm程度として処理量を高める。処理量
に応じてチューブドライヤ回転数を調整し、チューブの
石炭充填率が15〜40％としてキルンアクションを安定し
て生成させる。なお処理量が小さい時には、伝熱面積が
相対的に大きくなるので、加熱媒体の供給量（圧力）を
下げることにより、出口石炭の水分を制御する。In the method of the present invention, since coal having a lower water content than that of brown coal is dried, the efficiency can be increased by the following treatments. First, for brown coal with a tube diameter of around 100 mm, the throughput is increased to around 150-300 mm. The tube dryer rotation speed is adjusted according to the throughput, and the coal filling rate of the tube is set at 15 to 40% to stably generate the kiln action. When the treatment amount is small, the heat transfer area is relatively large, so the water content of the outlet coal is controlled by lowering the supply amount (pressure) of the heating medium.

さらに第２図〜第３図に示すように、チューブ内にスパ
イラル状に加工した丸鋼15からなる撹拌手段16を装入す
ることにより、被乾燥物層にキルンアクションを生成せ
しめ伝熱効果を高めるとともに、チューブ軸方向の流速
を抑制して滞留時間を確保し、これにより処理能力をさ
らに高める効果を発揮させる。この撹拌手段16は、チュ
ーブ出口端に設けられた押え具17にてチューブ１より抜
け落ちないようになっているが、チューブ内では自由に
回転運動できる。18は加熱媒体通路、20は乾燥物と排ガ
スとを分離して抜き出すためのホッパである。Further, as shown in FIG. 2 to FIG. 3, by inserting a stirring means 16 made of spirally processed round steel 15 into the tube, a kiln action is generated in the material layer to be dried, and a heat transfer effect is obtained. In addition to increasing the flow rate, the flow velocity in the tube axial direction is suppressed to secure the retention time, thereby exerting the effect of further increasing the processing capacity. The stirring means 16 is designed so as not to fall out of the tube 1 by a holding tool 17 provided at the tube outlet end, but can freely rotate in the tube. Reference numeral 18 is a heating medium passage, and 20 is a hopper for separating and extracting the dried material and the exhaust gas.

被乾燥物はチューブ内を進行するにつれ水分が低下し、
通常、流速が速くなる。そのため、チューブ内の乾燥物
充填率が低くなって、キルンアクションが生成しなくな
る場合がある。本発明における撹拌手段16によれば、低
水分、低充填率となってもキルンアクションを続行せし
め、調湿・乾燥能力を維持することが可能となる。撹拌
手段16のチューブ方向流さは被乾燥物の物性にもよる
が、コークス製造用原料炭の場合には、チューブの後半
1/2以下に装入すれば十分であり、スパイラル径もチュ
ーブ内径の1/2以上であれば良い。スパイラルピッチは
チューブ径の1/4〜２倍程度が望ましい。また撹拌手段1
6はチューブ内で回転する必要はなく、押え具17などに
よって固定しても差し支えない。As the material to be dried loses water content as it progresses in the tube,
Usually the flow velocity will be faster. Therefore, the filling rate of the dry matter in the tube becomes low, and the kiln action may not be generated. According to the stirring means 16 of the present invention, the kiln action can be continued even if the water content is low and the filling rate is low, and the humidity control / drying ability can be maintained. The flow of the stirring means 16 in the tube direction depends on the physical properties of the material to be dried, but in the case of coking coal, the latter half of the tube is used.
It suffices to charge it to 1/2 or less, and the spiral diameter may be 1/2 or more of the tube inner diameter. The spiral pitch is preferably about 1/4 to 2 times the tube diameter. Also stirring means 1
6 does not need to rotate in the tube, and may be fixed by a retainer 17 or the like.

また第１図〜第３図に示す撹拌手段16の代りに、第４図
および第５図に示うように、リング状のプレート21を数
百mmピッチに数枚並べ、スペーサーとして丸鋼22を渡し
た構造のものをチューブ内に装入する。リング状のプレ
ート21の大きさは、乾燥物の固着・堆積を防止する意味
から、チューブ径より若干小さく、回転するタイプが望
ましい。なおリング状のプレートは最下流の１枚のみで
はキルンアクションの生成が不安定であり、２枚以上必
要である。他の構成、作用は第１図〜第３図の場合と同
様である。Further, instead of the stirring means 16 shown in FIGS. 1 to 3, as shown in FIGS. 4 and 5, a plurality of ring-shaped plates 21 are arranged at a pitch of several hundreds mm, and a round steel 22 is used as a spacer. Insert the one with the passed structure into the tube. The size of the ring-shaped plate 21 is preferably a little smaller than the tube diameter and rotatable, in order to prevent the dried matter from sticking and accumulating. It should be noted that the production of the kiln action is unstable with only one ring-shaped plate at the most downstream side, and two or more plates are required. Other configurations and operations are the same as in the case of FIGS.

他の例として、第１図〜第３図に示す撹拌手段16の代り
に、第６図および第７図に示すように、フラットバー23
をチューブ１内面に密着させた状態で軸方向に数条並
べ、丸鋼24で固定した撹拌手段をチューブ１内に装入す
る。従来例として示した第９図および第10図のように乾
燥物を自ら掻き上げる型式ではなく、本例は粉体層の裾
野を支持し粉体のキルンアクションを助長せしめる構造
であるため、フラットバーの幅は小さく、本数も２〜３
条で済み、丸鋼24もたかだか数列であって流量を制限す
ることがない。他の構成、作用は第１図〜第３図の場合
と同様である。As another example, instead of the stirring means 16 shown in FIGS. 1 to 3, as shown in FIGS. 6 and 7, a flat bar 23 is used.
While being closely attached to the inner surface of the tube 1, several tubes are arranged in the axial direction, and the stirring means fixed with round steel 24 is charged into the tube 1. This is not a type of scraping dry matter by itself as shown in FIG. 9 and FIG. 10 shown as a conventional example, but this example has a structure that supports the foot of the powder layer and promotes the kiln action of the powder. The width of the bar is small and the number of bars is 2-3.
The round steel 24 has only a few rows and does not limit the flow rate. Other configurations and operations are the same as in the case of FIGS.

また本発明の方法では、以下の操作によってチューブ材
の腐食を防止することができる。まず、第８図に示すよ
うに、出口石炭水分に応じて、供給スチームの圧力を、
コントロール弁25などの手段により制御する。しかし、
スチーム温度が腐食発生温度以上の設定温度（たとえば
130℃）になると、コントロール弁25を制御して、スチ
ーム温度を腐食発生温度以上の設定温度に保ちながら、
出口石炭水分が所定の水分となるように、ドライヤ回転
数を、たとえば駆動モータ26用のインバータ27を用いて
制御する。28は水分検出器、29は温度検出器、30は回転
数調節器、31は回転駆動軸、32は軸受である。Moreover, in the method of the present invention, the corrosion of the tube material can be prevented by the following operations. First, as shown in FIG. 8, the pressure of the supply steam is changed according to the outlet coal moisture,
It is controlled by means such as the control valve 25. But,
The steam temperature is higher than the temperature at which corrosion occurs (for example,
130 ℃), while controlling the control valve 25 to keep the steam temperature above the corrosion generation temperature,
The dryer rotation speed is controlled by using, for example, the inverter 27 for the drive motor 26 so that the outlet coal water content becomes a predetermined water content. 28 is a moisture detector, 29 is a temperature detector, 30 is a rotation speed adjuster, 31 is a rotary drive shaft, and 32 is a bearing.

〔発明の効果〕〔The invention's effect〕

本発明の方法は上記のように、従来、褐炭にしか使用さ
れなかったマテリアルインチューブ型のチューブドライ
ヤを使用して、コークス原料炭などの比較的石炭化度の
高い石炭類の調湿を図るものであり、他の型式のチュー
ブドライヤや、他の乾燥方法に比較して、効率よく経済
性の高い調湿を行うことができるという効果を有してい
る。As described above, the method of the present invention uses a material-in-tube type tube dryer that has been conventionally used only for brown coal, and aims to regulate the humidity of coals having a relatively high degree of coalification, such as coke raw coal. It has the effect that humidity control can be performed efficiently and with high economic efficiency as compared with other types of tube dryers and other drying methods.

また、本発明の方法によって、スチームなどの加熱媒体
のチューブドライヤ内における温度を130℃以上に制御
すれば、またはチューブ内面温度が120℃以上とすれ
ば、チューブの腐食を防止することができ、チューブを
安価な材料で構成でき、効率よく、経済性に優れた石炭
の調湿を行うことができる。Further, by the method of the present invention, if the temperature in the tube dryer of the heating medium such as steam is controlled to 130 ° C or higher, or if the tube inner surface temperature is 120 ° C or higher, it is possible to prevent corrosion of the tube, The tube can be made of an inexpensive material, and the humidity of coal can be efficiently controlled with excellent economical efficiency.

【図面の簡単な説明】[Brief description of drawings]

第１図は本発明の石炭の調湿方法を実施するチューブド
ライヤの一例を示す縦断面説明図、第２図は第１図にお
けるチューブ出口端まわりの拡大断面図、第３図は同右
側面図、第４図はチューブの他の例を示す断面説明図、
第５図は同Ａ−Ａ線断面図、第６図はチューブのさらに
他の例を示す断面説明図、第７図は同Ｂ−Ｂ線断面図、
第８図は本発明の方法を実施するチューブドライヤの他
の例を示す説明図、第９図はチューブの従来例を示す断
面説明図、第10図は同Ｃ−Ｃ線断面図である。 １……チューブ、２……フラットバー、３……管板、４
……支持リング、５……せき、10……傾斜回転円筒、11
……入口フード、12、14……回転継手、13……ドレン
管、15……丸鋼、16……撹拌手段、17……押え具、18…
…加熱媒体通路、20……ホッパ、21……リング状のプレ
ート、22……丸鋼、23……フラットバー、24……丸鋼、
25……コントロール弁、26……駆動モータ、27……イン
バータ、28……水分検出器、29……温度検出器、30……
回転数調節器、31……回転駆動軸、32……軸受FIG. 1 is a vertical cross-sectional explanatory view showing an example of a tube dryer for carrying out the coal humidity control method of the present invention, FIG. 2 is an enlarged cross-sectional view around the tube outlet end in FIG. 1, and FIG. FIG. 4 is a cross-sectional explanatory view showing another example of the tube,
5 is a sectional view taken along the line AA, FIG. 6 is an explanatory sectional view showing still another example of the tube, and FIG. 7 is a sectional view taken along the line BB.
FIG. 8 is an explanatory view showing another example of a tube dryer for carrying out the method of the present invention, FIG. 9 is a sectional explanatory view showing a conventional example of a tube, and FIG. 10 is a sectional view taken along the line CC. 1 ... Tube, 2 ... Flat bar, 3 ... Tube plate, 4
…… Support ring, 5 …… Weep, 10 …… Inclined rotating cylinder, 11
...... Inlet hood, 12, 14 ...... Rotary joint, 13 …… Drain pipe, 15 …… Round steel, 16 …… Stirring means, 17 …… Pressing tool, 18 ・ ・ ・
… Heating medium passage, 20 …… Hopper, 21 …… Ring-shaped plate, 22 …… Round steel, 23 …… Flat bar, 24 …… Round steel,
25 …… Control valve, 26 …… Drive motor, 27 …… Inverter, 28 …… Moisture detector, 29 …… Temperature detector, 30 ……
Rotation speed regulator, 31 …… Rotary drive shaft, 32 …… Bearing

───────────────────────────────────────────────────── フロントページの続き (72)発明者 中村 章 兵庫県神戸市中央区東川崎町３丁目１番１ 号 川崎重工業株式会社神戸工場内 (72)発明者 駒井 啓一 兵庫県神戸市中央区東川崎町３丁目１番１ 号 川崎重工業株式会社神戸工場内 (72)発明者 若林 武司 兵庫県神戸市中央区東川崎町３丁目１番１ 号 川崎重工業株式会社神戸工場内 (72)発明者 小野 文信 兵庫県神戸市中央区東川崎町３丁目１番１ 号 川崎重工業株式会社神戸工場内 ─────────────────────────────────────────────────── ─── Continued Front Page (72) Inventor Akira Nakamura 3-1, 1-1 Higashikawasaki-cho, Chuo-ku, Kobe-shi, Hyogo Kawasaki Heavy Industries Ltd. Kobe factory (72) Keiichi Komai Higashi-kawasaki-cho, Chuo-ku, Kobe-shi, Hyogo 3-1-1 Kawasaki Heavy Industries, Ltd. Kobe Factory (72) Inventor Takeshi Wakabayashi 3-1-1 1-1 Higashikawasaki-cho, Chuo-ku, Kobe-shi, Hyogo Prefecture Kawasaki Heavy Industries Ltd. Kobe Factory (72) Inventor Fuminobu Ono Hyogo 3-1-1 Higashikawasaki-cho, Chuo-ku, Kobe-shi, Kawasaki

Claims (11)

【特許請求の範囲】[Claims] 【請求項１】純炭基準で揮発分含有率が45重量％以下で
あり、粒径3mm以下の重量割合が75％以上であり、湿炭
基準の水分含有率が20重量％以下である一種類の石炭ま
たは数種類の石炭の混合物を、傾斜回転円筒内に軸方向
に多数のチューブを配設し、該チューブ内に被乾燥物を
流通させ、チューブ外側にスチームなどの加熱媒体を流
通させて、被乾燥物を間接加熱するマテリアルインチュ
ーブ型のチューブドライヤに導入して、湿炭基準の水分
含有率が４〜７重量％になるように乾燥させることを特
徴とする石炭の調湿方法。1. A volatile matter content of 45% by weight or less based on pure coal, a weight ratio of 3 mm or less in particle size of 75% or more, and a water content of 20% by weight or less based on wet coal. Type of coal or a mixture of several types of coal, a large number of tubes are axially arranged in the inclined rotary cylinder, the material to be dried is circulated in the tube, and a heating medium such as steam is circulated outside the tube. A method for controlling humidity of coal, which comprises introducing a material to be dried into a tube dryer of a material-in-tube type that indirectly heats the material to be dried, and drying the material so that the moisture content based on wet coal is 4 to 7% by weight. 【請求項２】チューブ内に、撹拌手段を装入する請求項
１記載の石炭の調湿方法。2. The method for controlling the humidity of coal according to claim 1, wherein the tube is provided with a stirring means. 【請求項３】チューブ内に、スパイラル状の線材からな
る撹拌手段を装入する請求項２記載の石炭の調湿方法。3. The method for controlling the humidity of coal according to claim 2, wherein the tube is provided with stirring means made of a spiral wire. 【請求項４】チューブ内に、チューブ横断面方向にリン
グ状のせきを一定間隔で数枚並べた形状の撹拌手段を装
入する請求項２記載の石炭の調湿方法。4. The method for controlling the humidity of coal according to claim 2, wherein the tube is provided with a stirring means having a shape in which several ring-shaped coughs are arranged at regular intervals in the cross-sectional direction of the tube. 【請求項５】チューブ内に、チューブ内面に接するよう
にフラットバー数条をチューブ軸方向に配列した形状の
撹拌手段を装入する請求項２記載の石炭の調湿方法。5. The method for controlling humidity of coal according to claim 2, wherein a stirring means having a shape in which several flat bars are arranged in the tube axial direction so as to contact the inner surface of the tube is charged in the tube. 【請求項６】被乾燥物がコークス製造用の原料である請
求項１、２、３、４または５記載の石炭の調湿方法。6. The method for conditioning coal according to claim 1, wherein the material to be dried is a raw material for coke production. 【請求項７】チューブの断面積に占める石炭層の割合が
平均して15〜40％となるように制御する請求項１、２、
３、４、５または６記載の石炭の調湿方法。7. The control so that the proportion of the coal layer in the cross-sectional area of the tube is 15 to 40% on average.
The method for controlling humidity of coal according to 3, 4, 5 or 6. 【請求項８】チューブの断面積に占める石炭層の割合
が、チューブの入口部で50％以上となるように制御する
請求項１、２、３、４、５、６または７記載の石炭の調
湿方法。8. The coal according to claim 1, 2, 3, 4, 5, 6 or 7, wherein the proportion of the coal layer in the cross-sectional area of the tube is controlled to be 50% or more at the inlet of the tube. Humidification method. 【請求項９】乾燥すべき材料のチューブドライヤへの供
給量がほぼ一定に制御された条件において、チューブド
ライヤ入口フード内の材料の粉体レベルが上昇しないよ
う、かつチューブドライヤからの材料の排出量が減少し
ないように、これらを検出しながらチューブドライヤの
回転数を限界近くまで低下させることによって、チェー
ブの断面積に占める石炭量の割合を制御する請求項７ま
たは８記載の石炭の調湿方法。9. The discharge of the material from the tube dryer so that the powder level of the material in the tube dryer inlet hood does not rise under the condition that the supply amount of the material to be dried to the tube dryer is controlled to be substantially constant. The humidity control of coal according to claim 7 or 8, wherein the ratio of the amount of coal in the cross-sectional area of the chave is controlled by lowering the rotational speed of the tube dryer to the limit while detecting these so that the amount does not decrease. Method. 【請求項１０】スチームなどの加熱媒体のチューブドラ
イヤ内における温度が130℃以上となるように、チュー
ブドライヤ回転数を制御することを特徴とする請求項
１、２、３、４、５、６、７または８記載の石炭の調湿
方法。10. The tube dryer rotation speed is controlled so that the temperature of the heating medium such as steam in the tube dryer is 130 ° C. or higher. 7. The method for controlling humidity of coal according to 7 or 8. 【請求項１１】請求項10記載の石炭の調湿方法におい
て、スチームなどの加熱媒体のチューブドライヤ内にお
ける温度を130℃以上とする代りに、チューブ鉄皮温度
を120℃以上とすることを特徴とする石炭の調湿方法。11. The method for conditioning coal according to claim 10, wherein the temperature of the heating medium such as steam in the tube dryer is 130 ° C. or higher, and the tube shell temperature is 120 ° C. or higher. How to control the humidity of coal.
JP21970988A 1987-09-03 1988-09-02 How to control the humidity of coal Expired - Fee Related JPH0759709B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP21970988A JPH0759709B2 (en) 1987-09-03 1988-09-02 How to control the humidity of coal

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP22163287 1987-09-03
JP62-221632 1987-09-03
JP21970988A JPH0759709B2 (en) 1987-09-03 1988-09-02 How to control the humidity of coal

Publications (2)

Publication Number Publication Date
JPH01230916A JPH01230916A (en) 1989-09-14
JPH0759709B2 true JPH0759709B2 (en) 1995-06-28

Family

ID=16769810

Family Applications (1)

Application Number Title Priority Date Filing Date
JP21970988A Expired - Fee Related JPH0759709B2 (en) 1987-09-03 1988-09-02 How to control the humidity of coal

Country Status (3)

Country Link
EP (1) EP0370144B1 (en)
JP (1) JPH0759709B2 (en)
DE (1) DE3879948T2 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006292262A (en) * 2005-04-08 2006-10-26 Nippon Steel Engineering Co Ltd Fluidized bed dryer, and drying method of wet raw material by fluidized bed dryer
JP2011069609A (en) * 2010-10-25 2011-04-07 Nippon Steel Engineering Co Ltd Fluidized layer drying machine and drying method of wet raw material using fluidized bed drying machine

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IL97699A0 (en) * 1990-09-24 1992-06-21 Gaehler Franz Method and apparatus for reprocessing loose materials
DE4121873A1 (en) * 1991-07-02 1993-01-14 Braunschweigische Masch Bau Sugar beet dryer - has parallel tubes angled downwards in a rotating drying tube with hot steam fed between them
JPH0620446U (en) * 1992-03-31 1994-03-18 川崎重工業株式会社 Call-in-tube dryer
JP2515070Y2 (en) * 1993-01-18 1996-10-23 川崎重工業株式会社 Call in tube dryer
JP4858322B2 (en) * 2007-06-14 2012-01-18 Ｊｆｅエンジニアリング株式会社 Drying equipment
JP5535112B2 (en) * 2011-03-25 2014-07-02 月島機械株式会社 Coal thermal power generation facility and coal thermal power generation method
JP2015055375A (en) * 2013-09-10 2015-03-23 周南バルクターミナル株式会社 Power generation method
CN103591779B (en) * 2013-11-20 2015-10-07 韩旭新 Brown coal pipe drier
JP6245743B2 (en) 2013-12-06 2017-12-20 三菱重工業株式会社 Coal deactivation processing equipment
CN105157371A (en) * 2015-07-13 2015-12-16 华北电力大学 Revolving drum type fume-steam integrated raw coal drying equipment
DE102016213956A1 (en) * 2016-07-28 2018-02-01 Floradry Gmbh contact dryer
CN107314644A (en) * 2017-08-10 2017-11-03 阜阳华润电力有限公司 A kind of coal slime drier
CN109654527B (en) * 2018-12-10 2020-05-05 安徽金禾实业股份有限公司 Uniform coal feeding device of three-waste mixed combustion furnace
CN115388625B (en) * 2022-08-30 2023-06-13 湖南越洋药业有限公司 Backflushing rotary type drying equipment applied to methylprednisolone production

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE121763C (en) *
DE480573C (en) * 1929-08-05 Buckau R Wolf Akt Ges Maschf Helical winding strip for the tubes of tube dryers
DE171740C (en) *
DE112659C (en) *
DE481691C (en) * 1927-07-14 1929-08-27 Buckau R Wolf Akt Ges Maschf Process for drying fine-grained goods in circulating tube dryers
DE611988C (en) * 1933-09-19 1935-04-11 Buckau R Wolf Akt Ges Maschf Tube dryer
DE1023725B (en) * 1956-03-14 1958-01-30 Buckau Wolf Maschf R Storage and turning device for dryer tubes of steam-heated tube dryers
DE1256158B (en) * 1962-11-20 1967-12-07 Buckau Wolf Maschf R Method for feeding the material into the filling box of a pipe dryer
US3765102A (en) * 1972-09-21 1973-10-16 Patterson Kelley Co Rotary apparatus for treating particulate material
DE3027187A1 (en) * 1980-07-18 1982-02-11 Bayer Ag, 5090 Leverkusen PIPE FOR INDIRECT HEAT TREATMENT OF GIANT MATERIALS, HEAT EXCHANGERS COMPOSED FROM SUCH PIPES AND COMPONENTS FOR THE PRODUCTION OF THE TUBE BUNDLE
DE3033461C2 (en) * 1980-09-05 1982-11-04 Alfelder Eisenwerke Carl Heise, KG vorm. Otto Wesselmann & Cie., 3220 Alfeld Process for drying and preheating fine-grained hard coal using non-baking or only weakly baking coal and / or carbon carriers

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006292262A (en) * 2005-04-08 2006-10-26 Nippon Steel Engineering Co Ltd Fluidized bed dryer, and drying method of wet raw material by fluidized bed dryer
JP4653545B2 (en) * 2005-04-08 2011-03-16 新日鉄エンジニアリング株式会社 Fluidized bed dryer and method for drying wet raw material by fluidized bed dryer
JP2011069609A (en) * 2010-10-25 2011-04-07 Nippon Steel Engineering Co Ltd Fluidized layer drying machine and drying method of wet raw material using fluidized bed drying machine

Also Published As

Publication number Publication date
DE3879948D1 (en) 1993-05-06
EP0370144A1 (en) 1990-05-30
EP0370144B1 (en) 1993-03-31
JPH01230916A (en) 1989-09-14
DE3879948T2 (en) 1993-07-01

Similar Documents

Publication Publication Date Title
JPH0759709B2 (en) How to control the humidity of coal
TWI596311B (en) Indirect heating rotary dryer
US3245154A (en) Rotary driers
US2911730A (en) Drying of divided solid materials
US3765102A (en) Rotary apparatus for treating particulate material
JPS6330059B2 (en)
US7562465B2 (en) Process and means for drying of sticky materials
WO2008094466A1 (en) Counter flow air cooling drier with fluid heating and integrated heat recovery
CN203940692U (en) A kind of rotary flash distillation formula biomass powder raw material drying machine
HUT67647A (en) Method and device for drying wet materials
NO831254L (en) PROCEDURE AND APPARATUS FOR TREATMENT OF PARTICULATE MATERIAL.
US2628077A (en) Method of effecting indirect heat transfer
US3025611A (en) Drier with straight and sawtooth lifters
US4439932A (en) Method and apparatus for thermal treatment, especially drying, of finely comminuted bulk material
US3384974A (en) Process and apparatus for wet pellet drying
US3333344A (en) Rotary dryer
CN108106374A (en) Utilize the method for the wet charcoal of flue gas residual heat drying and its continuous drying equipment
JP2012233599A (en) Multitubular drying device
JPH07876Y2 (en) Tube dryer
CN212253487U (en) External heating type drying equipment heated by heat conduction oil
US2276589A (en) Drier
CN207741497U (en) A kind of continuous drying equipment using the wet charcoal of flue gas residual heat drying
TW201621246A (en) Indirect heating tube rotary dryer and drying method
JPS6234989Y2 (en)
US3490754A (en) Rotary kiln

Legal Events

Date Code Title Description
R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

S111 Request for change of ownership or part of ownership

Free format text: JAPANESE INTERMEDIATE CODE: R313115

R350 Written notification of registration of transfer

Free format text: JAPANESE INTERMEDIATE CODE: R350

R250 Receipt of annual fees

Free format text: JAPANESE INTERMEDIATE CODE: R250

LAPS Cancellation because of no payment of annual fees