WO2021200425A1

WO2021200425A1 - Method and facility for manufacturing reformed coal

Info

Publication number: WO2021200425A1
Application number: PCT/JP2021/012113
Authority: WO
Inventors: 小水流　広行; 亘谷奥; 兼井　玲; 小菅　克志; 淳志小林; 白水　渡
Original assignee: 日鉄エンジニアリング株式会社
Priority date: 2020-03-30
Filing date: 2021-03-24
Publication date: 2021-10-07
Also published as: CN115349007A; AU2021247761A1; JP7416654B2; AU2021247761B2; CN115349007B; JP2021161144A

Abstract

Provided is a facility for manufacturing reformed coal, comprising an inner cylinder that rotates about an axis, a heating chamber that covers the inner cylinder from the radial outside of the inner cylinder, and a plurality of exhaust pipes arranged in the axial direction that penetrate through the inner cylinder in the radial direction and open into the heating chamber, coal being supplied from the end part that is positioned on the upstream side along the axial direction in the inner cylinder, and modified coal being discharged from the end part that is positioned on the downstream side along the axial direction in the inner cylinder, wherein the facility for manufacturing modified coal further comprises a temperature control unit for supplying an oxygen-containing gas to the heating chamber and controlling the temperature in the heating chamber, and a flue for discharging gas from the heating chamber, the flue being connected only to the end part that is positioned on the upstream side in the heating chamber.

Description

改質石炭の製造方法および製造設備Reformed coal manufacturing method and manufacturing equipment

　本発明は、改質石炭の製造方法および製造設備に関する。 The present invention relates to a method for producing reformed coal and a production facility.

　従来から、石炭を乾留して改質石炭を製造する改質石炭の製造方法として、下記特許文献１に記載の方法が知られている。この製造方法では、乾留ガスを乾留の熱源として使用することで、熱効率を高めている。
　ところで、この種の改質石炭の製造方法において、乾留ガスには高沸点成分のタールが含まれていることから、例えば、このタールが配管に付着して配管を閉塞する等し、乾留設備の稼働率が低下するおそれがある。
　そこで、下記特許文献１に記載の製造方法では、低温加熱ガスおよび廃熱ガスを乾留ガスに混合することで、タールの配管などへの付着を抑制している。 Conventionally, as a method for producing reformed coal by carbonizing coal to produce reformed coal, the method described in Patent Document 1 below is known. In this production method, the thermal efficiency is improved by using the carbonization gas as a heat source for carbonization.
By the way, in the method for producing this kind of reformed coal, since the dry distillation gas contains tar as a high boiling point component, for example, this tar adheres to the pipe to block the pipe, and the dry distillation equipment is used. The operating rate may decrease.
Therefore, in the production method described in Patent Document 1 below, adhesion of tar to piping or the like is suppressed by mixing low-temperature heating gas and waste heat gas with dry distillation gas.

特開２０１３－１７３８３１号公報Japanese Unexamined Patent Publication No. 2013-173831

　しかしながら、前記従来の改質石炭の製造方法では、石炭を乾留させる乾留装置の装置構成が複雑となり、運転が煩雑となるといった課題がある。 However, the conventional method for producing reformed coal has a problem that the configuration of a carbonization device for carbonizing coal becomes complicated and the operation becomes complicated.

　本発明は、前述した事情に鑑みてなされたものであって、改質石炭の製造設備における乾留装置の装置構成を簡素化し、運転も容易にすることを目的とする。 The present invention has been made in view of the above-mentioned circumstances, and an object of the present invention is to simplify the device configuration of a carbonization device in a reformed coal manufacturing facility and facilitate operation.

　前記課題を解決するために、本発明は以下の手段を提案している。
［１］軸線の回りに回転する内筒と、内筒を、内筒の径方向の外側から覆う加熱室と、内筒に、軸線方向に複数配置され、内筒を径方向に貫通して加熱室内に開口する排気管と、を有する乾留装置を備え、内筒において、軸線方向に沿った上流側に位置する端部から石炭が供給され、軸線方向に沿った下流側に位置する端部から改質石炭が排出される改質石炭の製造設備であって、加熱室内に酸素含有ガスを供給して加熱室内の温度を制御する温度制御部と、加熱室内のガスを排出する煙道と、を更に備え、煙道は、加熱室において上流側に位置する端部にのみ接続されている、改質石炭の製造設備。
［２］温度制御部は、煙道内の温度が６００℃以上を維持し、かつ加熱室内の温度を６００℃以上となるように制御する、［１］に記載の改質石炭の製造設備。
［３］温度制御部は、加熱室内を軸線方向に複数に区画してなる制御ゾーンごとに温度を制御し、煙道は、複数の制御ゾーンのうち、最も上流側の制御ゾーンに接続されている、［１］または［２］に記載の改質石炭の製造設備。
［４］内筒の内周面から軸線に向かって突出し、石炭を撹拌する撹拌部材をさらに備える、［１］から［３］のいずれか１項に記載の改質石炭の製造設備。
［５］内筒の内部で下流側の熱分解ゾーンに配置される撹拌部材は、上流側の水分蒸発ゾーンに配置される撹拌部材よりも、軸線に対する傾斜角が大きい、［４］に記載の改質石炭の製造設備。
［６］水分蒸発ゾーンに配置される撹拌部材の軸線に対する傾斜角が０である、［５］に記載の改質石炭の製造設備。
［７］撹拌部材は、軸線方向について、水分蒸発ゾーンおよび熱分解ゾーンからなる加熱領域の９０％を超える範囲に配置される、［５］または［６］に記載の改質石炭の製造設備。
［８］撹拌部材と内筒の内周面との間に隙間が形成されている、［４］から［７］のいずれか１項に記載の改質石炭の製造設備。
［９］隙間の大きさは、内筒の径方向における撹拌部材の寸法の１０％～２５％である、［８］に記載の改質石炭の製造設備。
［１０］撹拌部材は、内筒の径方向に対して傾斜する折り曲げ部を有する、［４］から［８］のいずれか１項に記載の改質石炭の製造設備。
［１１］折り曲げ部は、撹拌部材の軸線側で内筒の内周面を基準にした撹拌部材の高さの３０％以上～７０％以下の範囲に形成され、
　折り曲げ部の内筒の径方向に対する傾斜角は１０°以上４５°以下である、［１０］に記載の改質石炭の製造設備。
［１２］軸線の回りに回転する内筒と、内筒を、内筒の径方向の外側から覆う加熱室と、内筒に、軸線方向に複数配置され、内筒を径方向に貫通して加熱室内に開口する排気管と、を有する乾留装置を用いて、内筒において軸線方向に沿った上流側に位置する端部から石炭を供給し、軸線方向に沿った下流側に位置する端部から改質石炭を排出する改質石炭の製造方法であって、加熱室内に酸素含有ガスを供給して加熱室内の温度を制御する温度制御工程と、加熱室内のガスを排出するガス排出工程と、を含み、ガス排出工程では、加熱室において上流側に位置する端部からのみガスを排出する、改質石炭の製造方法。
［１３］温度制御工程は、加熱室内の温度を６００℃以上となるように制御する、［１２］に記載の改質石炭の製造方法。
［１４］温度制御工程は、加熱室内を軸線方向に複数に区画してなる制御ゾーンごとに温度を制御し、
　ガス排出工程は、複数の制御ゾーンのうち、最も上流側の制御ゾーンからガスを排出する、［１２］または［１３］に記載の改質石炭の製造方法。
［１５］内筒の内周面から軸線に向かって突出する撹拌部材を用いて石炭を撹拌する、［１２］から［１４］のいずれか１項に記載の改質石炭の製造方法。
［１６］少なくとも内筒の内部で下流側の熱分解ゾーンに配置される撹拌部材が軸線に対する傾斜角を有し、石炭を上流側に押し戻すように撹拌する、［１５］に記載の改質石炭の製造方法。
［１７］撹拌部材と内筒の内周面との間に隙間が形成され、撹拌部材によって撹拌された石炭を隙間から落下させる、［１５］または［１６］に記載の改質石炭の製造方法。
［１８］撹拌部材は内筒の径方向に対して傾斜する折り曲げ部を有し、撹拌部材によって撹拌された石炭を折り曲げ部から落下させる、［１５］から［１７］のいずれか１項に記載の改質石炭の製造方法。 In order to solve the above problems, the present invention proposes the following means.
[1] An inner cylinder that rotates around the axis, a heating chamber that covers the inner cylinder from the outside in the radial direction of the inner cylinder, and a plurality of inner cylinders are arranged in the axial direction and penetrate the inner cylinder in the radial direction. A dry distillation device having an exhaust pipe that opens into a heating chamber is provided, and coal is supplied from an end located on the upstream side along the axial direction in the inner cylinder, and coal is supplied from an end located on the downstream side along the axial direction. A temperature control unit that supplies oxygen-containing gas to the heating chamber to control the temperature in the heating chamber, and a flue that discharges the gas in the heating chamber. A modified coal production facility in which the flue is connected only to the upstream end of the heating chamber.
[2] The modified coal manufacturing equipment according to [1], wherein the temperature control unit controls the temperature in the flue to be 600 ° C. or higher and the temperature in the heating chamber to be 600 ° C. or higher.
[3] The temperature control unit controls the temperature for each control zone formed by dividing the heating chamber into a plurality of control zones in the axial direction, and the flue is connected to the most upstream control zone among the plurality of control zones. The modified coal production facility according to [1] or [2].
[4] The equipment for producing reformed coal according to any one of [1] to [3], further comprising a stirring member that protrudes from the inner peripheral surface of the inner cylinder toward the axis and stirs the coal.
[5] The stirring member arranged in the thermal decomposition zone on the downstream side inside the inner cylinder has a larger inclination angle with respect to the axis than the stirring member arranged in the water evaporation zone on the upstream side, according to [4]. Modified coal manufacturing equipment.
[6] The modified coal manufacturing facility according to [5], wherein the inclination angle of the stirring member arranged in the water evaporation zone with respect to the axis is 0.
[7] The equipment for producing reformed coal according to [5] or [6], wherein the stirring member is arranged in a range exceeding 90% of a heating region including a water evaporation zone and a thermal decomposition zone in the axial direction.
[8] The equipment for producing reformed coal according to any one of [4] to [7], wherein a gap is formed between the stirring member and the inner peripheral surface of the inner cylinder.
[9] The modified coal manufacturing equipment according to [8], wherein the size of the gap is 10% to 25% of the size of the stirring member in the radial direction of the inner cylinder.
[10] The equipment for producing modified coal according to any one of [4] to [8], wherein the stirring member has a bent portion inclined in the radial direction of the inner cylinder.
[11] The bent portion is formed on the axis side of the stirring member in a range of 30% or more to 70% or less of the height of the stirring member with respect to the inner peripheral surface of the inner cylinder.
The modified coal manufacturing equipment according to [10], wherein the inclination angle of the inner cylinder of the bent portion with respect to the radial direction is 10 ° or more and 45 ° or less.
[12] An inner cylinder that rotates around the axis, a heating chamber that covers the inner cylinder from the outside in the radial direction of the inner cylinder, and a plurality of inner cylinders are arranged in the axial direction and penetrate the inner cylinder in the radial direction. Using a carbonization device having an exhaust pipe that opens into the heating chamber, coal is supplied from the end located on the upstream side along the axial direction in the inner cylinder, and the end located on the downstream side along the axial direction. A method for producing reformed coal that discharges reformed coal from a coal, a temperature control step that supplies oxygen-containing gas to the heating chamber to control the temperature in the heating chamber, and a gas discharge step that discharges the gas in the heating chamber. A method for producing reformed coal, which comprises, and in the gas discharge process, discharges gas only from the end located on the upstream side in the heating chamber.
[13] The method for producing reformed coal according to [12], wherein the temperature control step controls the temperature in the heating chamber to be 600 ° C. or higher.
[14] In the temperature control step, the temperature is controlled for each control zone formed by dividing the heating chamber into a plurality of parts in the axial direction.
The method for producing reformed coal according to [12] or [13], wherein the gas discharge step discharges gas from the most upstream control zone among the plurality of control zones.
[15] The method for producing modified coal according to any one of [12] to [14], wherein the coal is agitated using a stirring member protruding from the inner peripheral surface of the inner cylinder toward the axis.
[16] The modified coal according to [15], wherein the stirring member arranged in the thermal decomposition zone on the downstream side at least inside the inner cylinder has an inclination angle with respect to the axis and stirs the coal so as to push it back to the upstream side. Manufacturing method.
[17] The method for producing modified coal according to [15] or [16], wherein a gap is formed between the stirring member and the inner peripheral surface of the inner cylinder, and the coal stirred by the stirring member is dropped from the gap. ..
[18] The item according to any one of [15] to [17], wherein the stirring member has a bent portion that is inclined with respect to the radial direction of the inner cylinder, and coal that has been stirred by the stirring member is dropped from the bent portion. How to make reformed coal.

　上記の構成によれば、改質石炭の製造設備における乾留装置の稼働率を確保しつつ、改質石炭の製造設備における乾留装置の装置構成を簡素化し、運転も容易にすることができる。 According to the above configuration, it is possible to simplify the equipment configuration of the carbonization device in the reformed coal manufacturing facility and facilitate the operation while ensuring the operating rate of the carbonization device in the reformed coal manufacturing facility.

本発明の第１の実施形態に係る改質石炭の製造設備のブロック図である。It is a block diagram of the production facility of reformed coal which concerns on 1st Embodiment of this invention. 図１に示す改質石炭の製造設備を構成する乾留装置の模式図である。It is a schematic diagram of the carbonization apparatus which constitutes the manufacturing facility of the reformed coal shown in FIG. 本発明の第２の実施形態に係る乾留装置の内筒の展開内面図である。It is a developed inner view of the inner cylinder of the carbonization apparatus which concerns on 2nd Embodiment of this invention. 図３に示す内筒の非展開状態のＡ－Ａ線に沿った断面図である。FIG. 3 is a cross-sectional view taken along the line AA of the inner cylinder shown in FIG. 3 in an unexpanded state. 図３に示す内筒の非展開状態のＢ－Ｂ線に沿った断面図である。FIG. 3 is a cross-sectional view taken along line BB of the inner cylinder shown in FIG. 3 in an unexpanded state. 図３に示す例における撹拌板の正面図である。It is a front view of the stirring plate in the example shown in FIG. 図３に示す例における撹拌板の側面図である。It is a side view of the stirring plate in the example shown in FIG. 本発明の第２の実施形態の変形例に係る乾留装置の内筒の断面図である。It is sectional drawing of the inner cylinder of the dry distillation apparatus which concerns on the modification of the 2nd Embodiment of this invention. 本発明の第２の実施形態の変形例による撹拌板の正面図である。It is a front view of the stirring plate by the modification of the 2nd Embodiment of this invention. 本発明の第２の実施形態の変形例による撹拌板の側面図である。It is a side view of the stirring plate by the modification of the 2nd Embodiment of this invention. 検証試験における石炭の昇温速度と温度と揮発分との関係を示すグラフである。It is a graph which shows the relationship between the temperature rise rate of coal, the temperature, and the volatile matter in the verification test. 検証試験における総括伝熱係数の測定結果を示すグラフである。It is a graph which shows the measurement result of the total heat transfer coefficient in a verification test. 検証試験における隙間の大きさと飛散率および総括伝熱係数との関係を示すグラフである。It is a graph which shows the relationship between the size of a gap in a verification test, a scattering rate, and a total heat transfer coefficient.

　以下に添付図面を参照しながら、本発明の好適な実施形態について詳細に説明する。なお、本明細書および図面において、実質的に同一の機能構成を有する構成要素については、同一の符号を付することにより重複説明を省略する。 A preferred embodiment of the present invention will be described in detail below with reference to the accompanying drawings. In the present specification and the drawings, components having substantially the same functional configuration are designated by the same reference numerals, so that duplicate description will be omitted.

　（第１の実施形態）
　以下、図面を参照し、本発明の第１の実施形態に係る改質石炭の製造設備を説明する。
　図１に示すように、改質石炭の製造設備１０は、乾燥装置１１と、乾留装置１２と、冷却装置１３と、排ガスシステム１４と、を備えている。この製造設備１０は、例えば、褐炭や亜瀝青炭のような水分含有量の多い低品位炭を改質するのに好適に用いることができる。 (First Embodiment)
Hereinafter, the modified coal manufacturing equipment according to the first embodiment of the present invention will be described with reference to the drawings.
As shown in FIG. 1, the reformed coal production facility 10 includes a drying device 11, a carbonization device 12, a cooling device 13, and an exhaust gas system 14. This production facility 10 can be suitably used for reforming low-grade coal having a high water content, such as lignite and subbituminous coal.

　乾燥装置１１は、石炭を乾燥する。乾燥装置１１は、例えば石炭の水分含有量が１５重量％以下、好ましくは、１０重量％以下になるまで、石炭を乾燥させる。乾留装置１２は、乾燥された石炭を乾留する。乾留装置１２は、例えば石炭の温度が５００℃以上、具体的には５５０℃～８００℃になるまで、石炭を乾留し、改質石炭にする。冷却装置１３は、乾留された改質石炭を冷却する。冷却装置１３は、例えば石炭の温度が７０℃以下、好ましくは６０℃以下になるまで、石炭を冷却させる。 The drying device 11 dries coal. The drying device 11 dries the coal until, for example, the water content of the coal is 15% by weight or less, preferably 10% by weight or less. The carbonization device 12 dry-distills the dried coal. The carbonization apparatus 12 dry-distills the coal until, for example, the temperature of the coal reaches 500 ° C. or higher, specifically 550 ° C. to 800 ° C., to obtain reformed coal. The cooling device 13 cools the reformed coal that has been carbonized. The cooling device 13 cools the coal until, for example, the temperature of the coal is 70 ° C. or lower, preferably 60 ° C. or lower.

　排ガスシステム１４は、乾留装置１２から排出される水蒸気および部分燃焼（酸化）により一次燃焼された乾留ガスおよび同ガスに少量同伴される微粉炭を完全燃焼後に排ガスとして大気に放出する。排ガスシステム１４は、二次燃焼装置１５と、蒸気発生装置１６と、除塵装置１７と、吸引ファン１８と、排ガス処理装置１９と、を備えている。 The exhaust gas system 14 releases the dry distillation gas discharged from the dry distillation apparatus 12, the dry distillation gas primarily burned by partial combustion (oxidation), and the pulverized coal accompanying a small amount of the gas to the atmosphere as exhaust gas after complete combustion. The exhaust gas system 14 includes a secondary combustion device 15, a steam generator 16, a dust removing device 17, a suction fan 18, and an exhaust gas treatment device 19.

　二次燃焼装置１５は、一次燃焼された乾留ガスを二次燃焼させて完全燃焼させる。完全燃焼の段階でＮＯ_ｘが環境基準を上回るまで発生する場合には、後段に脱ＮＯ_ｘ装置を設置することが好ましい。
　蒸気発生装置１６は、水蒸気および完全燃焼された乾留ガスからの廃熱回収により蒸気を発生させる。蒸気発生装置１６は、回収した蒸気の一部もしくは全部を乾燥装置１１に石炭の乾燥用熱源として供給する。除塵装置１７は、蒸気発生装置１６を通過したガスに同伴する微粉灰などを除去する。吸引ファン１８は、除塵装置１７からのガスを乾留装置１２の加熱室内の圧力が一定となるように吸引し、排ガス処理装置１９に送出する。排ガス処理装置１９は、ガスからＳＯ_ｘ等を除去することで排ガスを精製し、この排ガスを大気に放出する。 The secondary combustion device 15 secondarily burns the primary burned carbonization gas to completely burn it. _{If NO x} is generated until it exceeds the environmental standard at the stage of complete combustion, it is preferable to install a _{NO x removal device in the subsequent stage.}
The steam generator 16 generates steam by recovering waste heat from steam and dry distillation gas that has been completely burned. The steam generator 16 supplies a part or all of the recovered steam to the drying device 11 as a heat source for drying coal. The dust remover 17 removes fine ash and the like accompanying the gas that has passed through the steam generator 16. The suction fan 18 sucks the gas from the dust removing device 17 so that the pressure in the heating chamber of the carbonization device 12 becomes constant, and sends it to the exhaust gas treatment device 19. The exhaust gas treatment device 19 _{purifies the exhaust gas by removing SO x and the} like from the gas, and releases the exhaust gas to the atmosphere.

　ところで乾留装置１２は、いわゆる外熱式ロータリーキルンである。図２に示すように、乾留装置１２は、内筒２１と、加熱室２２と、温度制御部２３と、を備えている。 By the way, the carbonization device 12 is a so-called external heat type rotary kiln. As shown in FIG. 2, the carbonization device 12 includes an inner cylinder 21, a heating chamber 22, and a temperature control unit 23.

　乾留装置１２において、石炭は、内筒２１の内部を、内筒２１の軸線Ｏ方向に通過する。内筒２１において、軸線Ｏ方向に沿った上流側Ｄ１に位置する端部から石炭が定量で供給され、下流側Ｄ２に位置する端部から改質石炭が排出される。内筒２１の上流側Ｄ１の端部は、乾燥装置１１に接続され、内筒２１の下流側Ｄ２の端部は、冷却装置１３に接続されている。 In the carbonization device 12, coal passes through the inside of the inner cylinder 21 in the axis O direction of the inner cylinder 21. In the inner cylinder 21, coal is supplied in a fixed amount from an end located on the upstream side D1 along the axis O direction, and reformed coal is discharged from an end located on the downstream side D2. The end of the upstream side D1 of the inner cylinder 21 is connected to the drying device 11, and the end of the downstream side D2 of the inner cylinder 21 is connected to the cooling device 13.

　内筒２１の軸線Ｏは、水平方向に傾斜して延びている。具体的には、内筒２１の軸線Ｏには、軸線Ｏ方向に沿った上流側Ｄ１から下流側Ｄ２に向かう下り緩勾配がつけられている。内筒２１は、軸線Ｏ回りに回転可能に形成されている。内筒２１の上流側Ｄ１の端部から供給された石炭は、内筒２１が下流に向けて傾斜していること、軸線Ｏ回りに回転することで、内筒２１の内周面を伝って所定の滞留時間をかけて徐々に下流側Ｄ２に向けて移動する。 The axis O of the inner cylinder 21 is inclined and extends in the horizontal direction. Specifically, the axis O of the inner cylinder 21 is provided with a gentle downward slope from the upstream side D1 to the downstream side D2 along the axis O direction. The inner cylinder 21 is formed so as to be rotatable around the axis O. The coal supplied from the end of the upstream side D1 of the inner cylinder 21 is transmitted along the inner peripheral surface of the inner cylinder 21 by the inner cylinder 21 being inclined toward the downstream side and rotating around the axis O. It gradually moves toward the downstream side D2 over a predetermined residence time.

　加熱室２２は、内筒２１を、内筒２１の径方向（以下、「径方向」という）の外側から覆っている。加熱室２２には、内筒２１が、軸線Ｏ方向に挿通されていて、内筒２１の軸線Ｏ方向の両端部は、加熱室２２から軸線Ｏ方向に突出している。 The heating chamber 22 covers the inner cylinder 21 from the outside in the radial direction (hereinafter, referred to as “diameter direction”) of the inner cylinder 21. An inner cylinder 21 is inserted into the heating chamber 22 in the axis O direction, and both ends of the inner cylinder 21 in the axis O direction project from the heating chamber 22 in the axis O direction.

　ここで内筒２１には、排気管２４が設けられていて、乾留装置１２として、いわゆる角（つの）付きキルンが採用されている。
　排気管２４は、内筒２１に、軸線Ｏ方向に複数配置されている。排気管２４は、内筒２１を径方向に貫通して加熱室２２内に開口している。排気管２４は、内筒２１において、加熱室２２内に位置する部分である加熱室内部分の２１ａに設けられている。図示された例において、排気管２４は、加熱室内部分２１ａにおける軸線Ｏ方向の全長にわたって設けられている。排気管２４は、軸線Ｏ方向に同等の間隔をあけて複数配置されている。排気管２４は、内筒２１の内部で石炭から発生したガスである水蒸気や高沸点成分のタールを含む乾留ガスを、加熱室２２内に排出する。 Here, the inner cylinder 21 is provided with an exhaust pipe 24, and a so-called cornered kiln is adopted as the carbonization device 12.
A plurality of exhaust pipes 24 are arranged in the inner cylinder 21 in the axis O direction. The exhaust pipe 24 penetrates the inner cylinder 21 in the radial direction and opens into the heating chamber 22. The exhaust pipe 24 is provided in the heating chamber portion 21a, which is a portion of the inner cylinder 21 located in the heating chamber 22. In the illustrated example, the exhaust pipe 24 is provided over the entire length of the heating chamber portion 21a in the axis O direction. A plurality of exhaust pipes 24 are arranged at equal intervals in the axis O direction. The exhaust pipe 24 discharges the dry distillation gas containing water vapor, which is a gas generated from coal inside the inner cylinder 21, and tar, which is a high boiling point component, into the heating chamber 22.

　温度制御部２３は、加熱室２２内に空気を供給して加熱室２２内の温度を制御する。温度制御部２３は、排気管２４から加熱室２２内に排出された高沸点成分のタールを含む乾留ガスを、空気により部分燃焼（酸化）させることで、加熱室２２内を加熱する。なお空気と同様に、空気とは異なる酸素含有ガスを加熱室２２内に供給することも可能である。ここで酸素含有ガスとは、酸素を含有し、乾留ガスを燃焼（酸化）させることができるガスを意味する。酸素含有ガスとしては、空気の他に、例えば酸素を含有する排ガス、酸素富化空気などが使用できる。さらに本実施形態では、温度制御部２３は、加熱室２２内を、加熱室２２外の熱源すなわち燃料ガスにより加熱可能に形成されている。また、燃料ガスは、天然ガスやＬＰＧガス等を使用することができ、立ち上げ時の系の予熱にも使用される。 The temperature control unit 23 supplies air into the heating chamber 22 to control the temperature inside the heating chamber 22. The temperature control unit 23 heats the inside of the heating chamber 22 by partially burning (oxidizing) the dry distillation gas containing tar, which is a high boiling point component, discharged from the exhaust pipe 24 into the heating chamber 22 by air. As with air, it is also possible to supply an oxygen-containing gas different from air into the heating chamber 22. Here, the oxygen-containing gas means a gas that contains oxygen and can burn (oxidize) the carbonization gas. As the oxygen-containing gas, in addition to air, for example, oxygen-containing exhaust gas, oxygen-enriched air, and the like can be used. Further, in the present embodiment, the temperature control unit 23 is formed so that the inside of the heating chamber 22 can be heated by a heat source outside the heating chamber 22, that is, fuel gas. Further, as the fuel gas, natural gas, LPG gas, or the like can be used, and it is also used for preheating the system at the time of start-up.

　温度制御部２３は、制御ゾーンＺ１～Ｚ３ごとに温度を制御する。制御ゾーンＺ１～Ｚ３は、加熱室２２内が軸線Ｏ方向に複数に区画されてなる。図示の例では、制御ゾーンＺ１～Ｚ３は、３つに区画されており、上流側Ｄ１から下流側Ｄ２に向けて、第１制御ゾーンＺ１、第２制御ゾーンＺ２、第３制御ゾーンＺ３の順に区画されている。 The temperature control unit 23 controls the temperature for each of the control zones Z1 to Z3. The control zones Z1 to Z3 are divided into a plurality of control zones Z1 to Z3 in the axis O direction in the heating chamber 22. In the illustrated example, the control zones Z1 to Z3 are divided into three, and the first control zone Z1, the second control zone Z2, and the third control zone Z3 are in this order from the upstream side D1 to the downstream side D2. It is partitioned.

　温度制御部２３には、複数の制御ゾーンＺ１～Ｚ３にそれぞれに対応する複数の制御系２５が備えられている。各制御系２５は、空気供給部２６と、加熱部２７と、温度検出部２９と、制御本体部３０と、を少なくとも備えている。図示の例では、上記に加え、制御ゾーンＺ１～Ｚ３に蒸気供給部２８も備えた例を示す。なお空気供給部２６は、空気以外の酸素含有ガスを供給する場合も含めると、酸素含有ガス供給部と言い換えることができる。 The temperature control unit 23 is provided with a plurality of control systems 25 corresponding to the plurality of control zones Z1 to Z3, respectively. Each control system 25 includes at least an air supply unit 26, a heating unit 27, a temperature detection unit 29, and a control main body unit 30. In the illustrated example, in addition to the above, an example in which the steam supply unit 28 is also provided in the control zones Z1 to Z3 is shown. The air supply unit 26 can be rephrased as an oxygen-containing gas supply unit, including the case where an oxygen-containing gas other than air is supplied.

　空気供給部２６は、加熱室２２内に空気を供給する。空気供給部２６は、加熱室２２に空気を供給する打ち込み空気ファン３１と、打ち込み空気ファン３１を加熱室２２内に接続する第１配管３２と、第１配管３２に介装された第１制御弁３３と、を備えている。第１配管３２は、加熱室２２の上壁および下壁部分に、上壁側および下壁側の配管が対向方向となるように、かつ上壁と下壁の配管を複数に分岐した後に接続されている。なお第１制御弁３３に代わり、打ち込み空気ファン３１のモーターをインバーターを用いて回転数変更する供給空気量制御方式も適用可能である。 The air supply unit 26 supplies air into the heating chamber 22. The air supply unit 26 includes a driving air fan 31 that supplies air to the heating chamber 22, a first pipe 32 that connects the driving air fan 31 into the heating chamber 22, and a first control interposed in the first pipe 32. It is provided with a valve 33. The first pipe 32 is connected to the upper wall and the lower wall portion of the heating chamber 22 so that the pipes on the upper wall side and the lower wall side face each other and after the pipes on the upper wall and the lower wall are branched into a plurality of pipes. Has been done. Instead of the first control valve 33, a supply air amount control method in which the motor of the driving air fan 31 is changed in rotation speed by using an inverter can also be applied.

　加熱部２７は、加熱室２２内を、加熱室２２外の燃料ガス（熱源）により加熱する。加熱部２７は、加熱室２２を加熱するバーナー３４と、バーナー３４に空気を供給するバーナーファン３６と、バーナーファン３６をバーナー３４に接続する第２配管３７と、第２配管３７に介装された第２制御弁３８と、バーナー３４に燃料ガスを供給する第３配管３９と、第３配管３９に介装された第３制御弁４０と、を備えている。バーナー３４は、供給部から供給された空気と燃料ガスとを混合して燃料ガスを燃焼させる。バーナー３４は、加熱室２２の下壁部分に設けられ、第１配管３２の下壁部分設置配管と同じ方向に設けられている。 The heating unit 27 heats the inside of the heating chamber 22 with the fuel gas (heat source) outside the heating chamber 22. The heating unit 27 is interposed in a burner 34 that heats the heating chamber 22, a burner fan 36 that supplies air to the burner 34, a second pipe 37 that connects the burner fan 36 to the burner 34, and a second pipe 37. A second control valve 38, a third pipe 39 for supplying fuel gas to the burner 34, and a third control valve 40 interposed in the third pipe 39 are provided. The burner 34 mixes the air supplied from the supply unit with the fuel gas and burns the fuel gas. The burner 34 is provided on the lower wall portion of the heating chamber 22, and is provided in the same direction as the lower wall portion installation pipe of the first pipe 32.

　蒸気供給部２８は、加熱室２２内に蒸気を供給し、加熱室２２内を冷却する。蒸気供給部２８は、例えば１５０℃程度の蒸気を加熱室２２内に供給する。蒸気供給部２８は、加熱室２２内に蒸気を供給する第４配管４１と、第４配管４１に介装された第４制御弁４２と、を備えている。第４配管４１は、加熱室２２の下壁に第１配管３２の下壁部分設置配管と同じ方向に接続されている。 The steam supply unit 28 supplies steam into the heating chamber 22 to cool the inside of the heating chamber 22. The steam supply unit 28 supplies steam of, for example, about 150 ° C. into the heating chamber 22. The steam supply unit 28 includes a fourth pipe 41 that supplies steam into the heating chamber 22, and a fourth control valve 42 interposed in the fourth pipe 41. The fourth pipe 41 is connected to the lower wall of the heating chamber 22 in the same direction as the lower wall portion installation pipe of the first pipe 32.

　温度検出部２９は、加熱室２２内の温度を検出する。温度検出部２９は、例えば温度センサにより構成することができる。
　制御本体部３０は、温度検出部２９の検出結果に基づいて、空気供給部２６、加熱部２７および蒸気供給部２８を制御する。図示の例では、制御本体部３０は、第１～第４制御弁３３、３８、４０、４２を制御することで、空気供給部２６、加熱部２７および蒸気供給部２８を制御する。制御本体部３０は、例えばＰＬＣ（Programmable Logic Controller）などの制御装置により構成され、分散制御システム（ＤＣＳ：Distributed Control System）として実装されてもよい。 The temperature detection unit 29 detects the temperature inside the heating chamber 22. The temperature detection unit 29 can be configured by, for example, a temperature sensor.
The control main body 30 controls the air supply unit 26, the heating unit 27, and the steam supply unit 28 based on the detection result of the temperature detection unit 29. In the illustrated example, the control main body 30 controls the air supply unit 26, the heating unit 27, and the steam supply unit 28 by controlling the first to

fourth control valves

33, 38, 40, and 42. The control main body 30 may be configured by a control device such as a PLC (Programmable Logic Controller) and may be implemented as a distributed control system (DCS).

　ここで加熱室２２には、加熱室２２からガスを排出する煙道４３が設けられている。煙道４３は、加熱室２２に接続され、加熱室２２内と二次燃焼装置１５とを接続する。このとき、煙道４３は、加熱室２２における上流側Ｄ１に位置する端部にのみ接続されている。これにより、加熱室２２内のガスは、加熱室２２において上流側Ｄ１に位置する端部からのみ排出される。煙道４３は、複数の制御ゾーンＺ１～Ｚ３のうち、最も上流側Ｄ１に位置する第１制御ゾーンＺ１に接続されている。 Here, the heating chamber 22 is provided with a flue 43 for discharging gas from the heating chamber 22. The flue 43 is connected to the heating chamber 22 and connects the inside of the heating chamber 22 to the secondary combustion device 15. At this time, the flue 43 is connected only to the end portion of the heating chamber 22 located on the upstream side D1. As a result, the gas in the heating chamber 22 is discharged only from the end located on the upstream side D1 in the heating chamber 22. The flue 43 is connected to a first control zone Z1 located on the most upstream side D1 among the plurality of control zones Z1 to Z3.

　次に、改質石炭の製造設備１０および乾留装置１２の作用について説明する。
　改質石炭の製造設備１０を用いた改質石炭の製造方法は、石炭を乾燥する乾燥工程と、乾燥した石炭を乾留する乾留工程と、乾留した石炭を冷却する冷却工程と、を備えている。乾燥工程は乾燥装置１１により実施され、乾留工程は乾留装置１２により実施され、冷却工程は冷却装置１３により実施される。 Next, the operations of the reformed coal production facility 10 and the carbonization device 12 will be described.
The method for producing reformed coal using the reformed coal production facility 10 includes a drying step for drying the coal, a carbonization step for carbonizing the dried coal, and a cooling step for cooling the carbonized coal. .. The drying step is carried out by the drying device 11, the dry distillation step is carried out by the dry distillation device 12, and the cooling step is carried out by the cooling device 13.

　ここで乾留工程では、まず、加熱室２２を予熱する予熱工程を実施する。このとき、温度制御部２３の加熱部２７により、加熱室２２内を加熱する。
　また、内筒２１の上流側Ｄ１の端部から石炭を供給し、下流側Ｄ２の端部から改質石炭を排出する。このとき、内筒２１の内部を通過する石炭から高沸点成分のタールを含む乾留ガスが発生すると、この乾留ガスが、内筒２１の内部から排気管２４を通して加熱室２２内に排出される。 Here, in the carbonization step, first, a preheating step of preheating the heating chamber 22 is carried out. At this time, the inside of the heating chamber 22 is heated by the heating unit 27 of the temperature control unit 23.
Further, coal is supplied from the end of D1 on the upstream side of the inner cylinder 21, and reformed coal is discharged from the end of D2 on the downstream side. At this time, when the dry distillation gas containing tar having a high boiling point component is generated from the coal passing through the inside of the inner cylinder 21, the dry distillation gas is discharged from the inside of the inner cylinder 21 into the heating chamber 22 through the exhaust pipe 24.

　そこで、加熱室２２内に空気を供給して加熱室２２内の温度を制御する温度制御を実施する（温度制御工程）。このとき、空気により乾留ガスを加熱室２２内で部分燃焼（酸化）させることで、加熱室２２内の温度を高め、内筒２１の内部を通過する石炭を、内筒２１を介して加熱することができる。また加熱室２２内の温度を、加熱室２２の壁面や煙道４３の壁面にタールが付着しない程度に高めることができる。 Therefore, temperature control is performed by supplying air into the heating chamber 22 to control the temperature inside the heating chamber 22 (temperature control step). At this time, the dry distillation gas is partially burned (oxidized) in the heating chamber 22 by air to raise the temperature in the heating chamber 22 and heat the coal passing through the inside of the inner cylinder 21 through the inner cylinder 21. be able to. Further, the temperature inside the heating chamber 22 can be raised to such an extent that tar does not adhere to the wall surface of the heating chamber 22 or the wall surface of the flue 43.

　本実施形態では、加熱室２２の温度制御の際には、加熱室２２内の全体の温度を６００℃以上に制御する。このとき温度制御部２３は、複数の制御ゾーンＺ１～Ｚ３のいずれの温度も６００℃以上に制御する。温度制御部２３は、加熱室２２内の温度を過度に高めることなく、乾留装置１２が操業可能な範囲で加熱室２２内の温度を制御する。なお温度制御部２３は、空気供給部２６からの空気の供給量のみを制御することで、加熱室２２の温度を制御することができる。また温度制御部２３は、空気供給部２６のみならず、加熱部２７や蒸気供給部２８を制御することで、加熱室２２の温度を制御することも可能である。さらに、温度制御部２３は、煙道４３内の温度が６００℃以上を維持するように温度制御を実施してもよい。 In the present embodiment, when controlling the temperature of the heating chamber 22, the overall temperature inside the heating chamber 22 is controlled to 600 ° C. or higher. At this time, the temperature control unit 23 controls all the temperatures of the plurality of control zones Z1 to Z3 to 600 ° C. or higher. The temperature control unit 23 controls the temperature inside the heating chamber 22 within the range in which the carbonization device 12 can operate without excessively increasing the temperature inside the heating chamber 22. The temperature control unit 23 can control the temperature of the heating chamber 22 by controlling only the amount of air supplied from the air supply unit 26. Further, the temperature control unit 23 can control the temperature of the heating chamber 22 by controlling not only the air supply unit 26 but also the heating unit 27 and the steam supply unit 28. Further, the temperature control unit 23 may perform temperature control so that the temperature in the flue 43 is maintained at 600 ° C. or higher.

　ここで、加熱室２２内の温度は、例えば製造される改質石炭の用途などに応じて適宜変更することができる。加熱室２２内の温度は、例えば、内筒２１から排出される改質石炭の目標温度である改質石炭目標温度に基づいて設定することができる。具体的には、加熱室２２内の温度を、改質石炭目標温度に対して１００℃～１５０℃高い範囲で設定することが可能である。なお、改質石炭目標温度に対して、１００℃～１５０℃高い範囲であることは、必須条件ではなく、改質石炭目標温度以上の温度であれば適用可能である。 Here, the temperature in the heating chamber 22 can be appropriately changed depending on, for example, the use of the reformed coal to be produced. The temperature in the heating chamber 22 can be set based on, for example, the target temperature of the reformed coal, which is the target temperature of the reformed coal discharged from the inner cylinder 21. Specifically, the temperature in the heating chamber 22 can be set in a range of 100 ° C. to 150 ° C. higher than the target temperature of the reformed coal. It should be noted that the range of 100 ° C. to 150 ° C. higher than the target temperature of reformed coal is not an essential condition, and can be applied as long as the temperature is equal to or higher than the target temperature of reformed coal.

　なお、例えば改質石炭目標温度を６５０℃～８５０℃とすることで、石炭の揮発分（ＶＭ）を５～１５質量％にして、改質石炭を無煙炭相当炭または半無煙炭相当炭とすることができる。さらに例えば、改質石炭目標温度を５５０℃～７５０℃とすることで、石炭の揮発分（ＶＭ）を１０～３０質量％にして、改質石炭を一般炭相当炭として好適に用いることができる。 For example, by setting the target temperature of reformed coal to 650 ° C to 850 ° C, the volatile content (VM) of coal is set to 5 to 15% by mass, and the reformed coal is anthracite equivalent coal or semi-anthracite equivalent coal. Can be done. Further, for example, by setting the target temperature of the reformed coal to 550 ° C to 750 ° C, the volatile content (VM) of the coal can be set to 10 to 30% by mass, and the reformed coal can be suitably used as steam coal equivalent coal. ..

　ところで、加熱室２２の温度制御の際、内筒２１に上流側Ｄ１の端部から供給される石炭が１５０℃程度まで加熱される段階で石炭中の水分が蒸発する。その結果、内筒２１において、上流側Ｄ１に位置する部分では、水分の蒸発に必要な熱量が加わるために石炭の加熱に必要な熱量が大きくなり、下流側Ｄ２に位置する部分では水分の蒸発がなくなるので石炭の加熱に必要な熱量が小さくなる。したがって、内筒２１の内部では、上流側Ｄ１に位置する部分では石炭および雰囲気の温度が上昇し難い。また、内筒２１の上流側Ｄ１に位置する部分では石炭中の水分の蒸発により水蒸気が多く発生し、下流側Ｄ２に向かうに連れて、乾留ガスの発生量が多くなる。その結果、排気管２４から加熱室２２内に排出される乾留ガスは、上流側Ｄ１において下流側Ｄ２より少なくなる。従って、加熱室２２内についても、上流側Ｄ１に位置する部分では雰囲気ガスのカロリーが低いために温度が上昇し難い。 By the way, when the temperature of the heating chamber 22 is controlled, the water content in the coal evaporates at the stage where the coal supplied from the end of the upstream side D1 to the inner cylinder 21 is heated to about 150 ° C. As a result, in the inner cylinder 21, the amount of heat required for heating coal increases in the portion located on the upstream side D1 because the amount of heat required for evaporation of water is added, and the amount of heat required for heating coal increases in the portion located on the downstream side D2. The amount of heat required to heat the coal is reduced because the amount of heat required for heating the coal is reduced. Therefore, inside the inner cylinder 21, the temperature of coal and the atmosphere is unlikely to rise in the portion located on the upstream side D1. Further, in the portion of the inner cylinder 21 located on the upstream side D1, a large amount of water vapor is generated due to the evaporation of water in the coal, and the amount of carbonization gas generated increases toward the downstream side D2. As a result, the amount of carbonization gas discharged from the exhaust pipe 24 into the heating chamber 22 is less on the upstream side D1 than on the downstream side D2. Therefore, even in the heating chamber 22, the temperature of the portion located on the upstream side D1 is difficult to rise because the calorie of the atmospheric gas is low.

　そこで、本実施形態では、加熱室２２において上流側Ｄ１に位置する端部からのみガスを排出するようにガス排出を実施する（ガス排出工程）。つまり、加熱室２２内のガスを上流側Ｄ１に位置する端部に設置した煙道４３からのみ排出する。これにより、加熱室２２内の下流側Ｄ２に位置する部分において多量に発生する乾留ガスが、加熱室２２から排出される過程で、加熱室２２内において上流側Ｄ１に位置する部分を通過する。このとき、乾留ガスに空気を供給して乾留ガスを部分燃焼（酸化）させることで、加熱室２２内において上流側Ｄ１に位置する部分の温度を確実に上昇させることができる。 Therefore, in the present embodiment, the gas is discharged so that the gas is discharged only from the end located on the upstream side D1 in the heating chamber 22 (gas discharge step). That is, the gas in the heating chamber 22 is discharged only from the flue 43 installed at the end located on the upstream side D1. As a result, a large amount of carbonization gas generated in the portion located on the downstream side D2 in the heating chamber 22 passes through the portion located on the upstream side D1 in the heating chamber 22 in the process of being discharged from the heating chamber 22. At this time, by supplying air to the carbonization gas to partially burn (oxidize) the carbonization gas, the temperature of the portion located on the upstream side D1 in the heating chamber 22 can be surely raised.

　以上説明したように、本実施形態に係る改質石炭の製造設備１０、乾留装置１２、改質石炭の製造方法および乾留方法によれば、乾留ガスを加熱室２２内で部分燃焼（酸化）させることで、加熱室２２内の温度を高めることができる。したがって、加熱室２２内の温度を、加熱室２２の壁面や煙道４３の壁面にタールが付着しない程度に高めることで、改質石炭の製造設備１０における乾留装置１２の稼働率を確保しつつ、改質石炭の製造設備１０における乾留装置１２の装置構成を簡素化し、運転も容易にすることができる。 As described above, according to the reformed coal production facility 10, the carbonization device 12, the carbonization method, and the carbonization method according to the present embodiment, the carbonization gas is partially burned (oxidized) in the heating chamber 22. As a result, the temperature inside the heating chamber 22 can be raised. Therefore, by raising the temperature in the heating chamber 22 to such an extent that tar does not adhere to the wall surface of the heating chamber 22 and the wall surface of the flue 43, the operating rate of the carbonization device 12 in the reformed coal production facility 10 is secured. , The apparatus configuration of the carbonization apparatus 12 in the reformed coal production facility 10 can be simplified and the operation can be facilitated.

　また温度制御部２３が、煙道４３内の温度が６００℃以上を維持し、かつ加熱室２２内の温度を６００℃以上になるように制御するので、加熱室２２の壁面や煙道４３の壁面にタールが付着するのを確実に抑えることができる。これにより、改質石炭の製造設備１０における乾留装置１２の稼働率を確実に確保することができる。 Further, since the temperature control unit 23 controls the temperature inside the flue 43 to be 600 ° C. or higher and the temperature inside the heating chamber 22 to be 600 ° C. or higher, the wall surface of the heating chamber 22 or the flue 43 It is possible to reliably prevent tar from adhering to the wall surface. As a result, the operating rate of the carbonization device 12 in the reformed coal manufacturing facility 10 can be reliably secured.

　さらに温度制御部２３が、制御ゾーンＺ１～Ｚ３ごとに温度を制御するので、加熱室２２内の温度を、加熱室２２の壁面や煙道４３の壁面にタールが付着しない程度に確実に高めることができる。例えば、複数の制御ゾーンＺ１～Ｚ３のうち、温度が上昇し易い下流側Ｄ２の第３制御ゾーンＺ３において、乾留ガスが過剰に部分燃焼（酸化）するのを抑えて、未燃ガスを上流側へと移動させ、温度が上昇し難い上流側Ｄ１の第１制御ゾーンＺ１において、下流側からの未燃ガスを含んだ乾留ガスを積極的に部分燃焼（酸化）させることができる。これにより、改質石炭の製造設備１０における乾留装置１２の稼働率を確実に確保することができる。 Further, since the temperature control unit 23 controls the temperature for each of the control zones Z1 to Z3, the temperature inside the heating chamber 22 is surely raised to the extent that tar does not adhere to the wall surface of the heating chamber 22 or the wall surface of the flue 43. Can be done. For example, among the plurality of control zones Z1 to Z3, in the third control zone Z3 of the downstream side D2 where the temperature tends to rise, the dry distillation gas is suppressed from being excessively partially burned (oxidized), and the unburned gas is transferred to the upstream side. In the first control zone Z1 of the upstream side D1 where the temperature does not easily rise, the dry distillation gas containing the unburned gas from the downstream side can be positively partially burned (oxidized). As a result, the operating rate of the carbonization device 12 in the reformed coal manufacturing facility 10 can be reliably secured.

　なお、本実施形態については、以下に例示するように種々の変更を加えることが可能である。 It should be noted that various changes can be made to this embodiment as illustrated below.

　例えば、上述した例では蒸気発生装置１６が回収した蒸気を乾燥装置１１に熱源として供給するが、蒸気発生装置１６とは異なる装置から乾燥装置１１に熱源が供給されてもよい。また、例えば、上述した例では温度制御部２３が制御ゾーンＺ１～Ｚ３ごとに温度を制御しているが、温度制御部２３が加熱室２２内の温度を一体に制御してもよい。さらに、例えば、上述した例では加熱室２２内に空気を供給するが、空気と同様に、空気とは異なる酸素含有ガスを加熱室２２内に供給してもよい。ここで酸素含有ガスとは、酸素を含有し、乾留ガスを燃焼（酸化）させることができるガスを意味する。酸素含有ガスとしては、空気の他に、例えば酸素を含有する排ガス、酸素富化空気などが使用できる。その他、本発明の趣旨に逸脱しない範囲で、上述した例における構成要素を周知の構成要素に置き換えることは適宜可能であり、また、変形例を適宜組み合わせてもよい。 For example, in the above example, the steam recovered by the steam generator 16 is supplied to the drying device 11 as a heat source, but the heat source may be supplied to the drying device 11 from a device different from the steam generator 16. Further, for example, in the above-described example, the temperature control unit 23 controls the temperature for each of the control zones Z1 to Z3, but the temperature control unit 23 may integrally control the temperature in the heating chamber 22. Further, for example, in the above-described example, air is supplied into the heating chamber 22, but like air, an oxygen-containing gas different from air may be supplied into the heating chamber 22. Here, the oxygen-containing gas means a gas that contains oxygen and can burn (oxidize) the carbonization gas. As the oxygen-containing gas, in addition to air, for example, oxygen-containing exhaust gas, oxygen-enriched air, and the like can be used. In addition, it is possible to replace the constituent elements in the above-mentioned examples with well-known constituent elements as appropriate without departing from the spirit of the present invention, and modified examples may be appropriately combined.

　次に、上記の第１の実施形態の作用効果を検証する第１～第３の検証試験を実施した。なお以下の第１～第３の検証試験では、加熱室２２内に、酸素含有ガスとしての空気を供給した。 Next, the first to third verification tests for verifying the action and effect of the above first embodiment were carried out. In the following first to third verification tests, air as an oxygen-containing gas was supplied into the heating chamber 22.

　（第１の検証試験）
　第１の検証試験では、煙道４３の軸線Ｏ方向の位置の違いに基づく加熱室２２内の温度について検証した。第１の検証試験では、試験例Ａ１および試験例Ｂ１として２種類の乾留装置１２を用いた。これらの２つの乾留装置１２はいずれも、内筒２１の直径は５００ｍｍとし、内筒２１の加熱室内部分２１ａの軸線Ｏ方向の大きさは３０００ｍｍとし、内筒２１の軸線Ｏの水平方向に対する傾斜角度は１．０度とし、内筒２１の回転速度は３．１ｒｐｍとした。また、内筒２１に供給される石炭の水分を１１．８重量％とし、内筒２１に供給される石炭の供給速度を、２８０ｋｇ／ｈ～２９０ｋｇ／ｈとした。さらに、第２制御ゾーンＺ２の温度に基づいて、各制御系２５から制御ゾーンＺ１～Ｚ３それぞれに供給される空気量の供給速度を設定した。このとき、各制御ゾーンＺ１～Ｚ３に供給する空気量の供給速度を同等とし、３ゾーン合計の空気量の供給速度は２８０Ｎｍ^３／ｈ～２８５Ｎｍ^３／ｈとした。 (First verification test)
In the first verification test, the temperature inside the heating chamber 22 based on the difference in the position of the flue 43 in the axis O direction was verified. In the first verification test, two types of carbonization devices 12 were used as Test Example A1 and Test Example B1. In both of these two carbonization devices 12, the diameter of the inner cylinder 21 is 500 mm, the size of the heating chamber portion 21a of the inner cylinder 21 in the axis O direction is 3000 mm, and the inclination of the axis O of the inner cylinder 21 with respect to the horizontal direction. The angle was 1.0 degree, and the rotation speed of the inner cylinder 21 was 3.1 rpm. Further, the water content of the coal supplied to the inner cylinder 21 was set to 11.8% by weight, and the supply speed of the coal supplied to the inner cylinder 21 was set to 280 kg / h to 290 kg / h. Further, based on the temperature of the second control zone Z2, the supply rate of the amount of air supplied from each control system 25 to each of the control zones Z1 to Z3 was set. At this time, the supply speed of the amount of air supplied to each control zone Z1 to Z3 was set to be the same, and the supply speed of the total amount of air in the three zones was set ^{to 280 Nm 3} / h to 285 Nm ³ / h.

　ここで、試験例Ａ１と試験例Ｂ１とでは、煙道４３の軸線Ｏ方向の位置を異ならせた。
試験例Ａ１では、上記の実施形態と同様に、煙道４３を、加熱室２２の上流側Ｄ１の端部の制御ゾーンＺ１のみに接続した。試験例Ｂ１では、煙道４３を、加熱室２２の下流側Ｄ２の端部の制御ゾーンＺ３のみに接続した。
　この第１の検証試験では、第１～第３制御ゾーンＺ３それぞれの温度と、内筒２１から排出される石炭の温度である排出石炭温度と、を測定した。結果を以下表１に示す。 Here, the positions of the flue 43 in the axis O direction were different between Test Example A1 and Test Example B1.
In Test Example A1, the flue 43 was connected only to the control zone Z1 at the end of the upstream side D1 of the heating chamber 22, as in the above embodiment. In Test Example B1, the flue 43 was connected only to the control zone Z3 at the end of D2 on the downstream side of the heating chamber 22.
In this first verification test, the temperature of each of the first to third control zones Z3 and the discharged coal temperature, which is the temperature of the coal discharged from the inner cylinder 21, were measured. The results are shown in Table 1 below.

　この結果から、試験例Ａ１では、試験例Ｂ１よりも加熱室２２内の温度にばらつきが生じ難くなっていて、排出石炭温度も高められていることが確認された。 From this result, it was confirmed that in Test Example A1, the temperature in the heating chamber 22 was less likely to vary than in Test Example B1, and the discharged coal temperature was also raised.

　（第２の検証試験）
　第２の検証試験では、加熱室２２内の温度の違いに基づくタールの付着について検証した。第２の検証試験では、試験例Ａ２および試験例Ｂ２として２種類の乾留装置１２を用いた。これらの２つの乾留装置１２はいずれも、内筒２１の直径は５００ｍｍとし、内筒２１の加熱室内部分２１ａの軸線Ｏ方向の大きさは３０００ｍｍとし、内筒２１の軸線Ｏの水平方向に対する傾斜角度は１．０度とし、内筒２１の回転速度は３．１ｒｐｍとした。また、内筒２１に供給される石炭の水分を１２．３重量％とし、内筒２１に供給される石炭の供給速度を、２７５ｋｇ／ｈ～２８０ｋｇ／ｈとした。さらに、煙道４３を、加熱室２２の上流側Ｄ１の端部の制御ゾーンＺ１のみに接続した。 (Second verification test)
In the second verification test, the adhesion of tar based on the difference in temperature in the heating chamber 22 was verified. In the second verification test, two types of carbonization devices 12 were used as Test Example A2 and Test Example B2. In both of these two carbonization devices 12, the diameter of the inner cylinder 21 is 500 mm, the size of the heating chamber portion 21a of the inner cylinder 21 in the axis O direction is 3000 mm, and the inclination of the axis O of the inner cylinder 21 with respect to the horizontal direction. The angle was 1.0 degree, and the rotation speed of the inner cylinder 21 was 3.1 rpm. Further, the water content of the coal supplied to the inner cylinder 21 was set to 12.3% by weight, and the supply speed of the coal supplied to the inner cylinder 21 was set to 275 kg / h to 280 kg / h. Further, the flue 43 was connected only to the control zone Z1 at the end of the upstream side D1 of the heating chamber 22.

　試験例Ａ２と試験例Ｂ２とでは、加熱室２２の運転温度によるタール付着の影響を比較するために、第２制御ゾーンＺ２の目標温度を異ならせた。試験例Ａ２では第２制御ゾーンＺ２の温度が６３０℃程度とし、試験例Ｂ２では第２制御ゾーンＺ２の温度が５５０℃程度とした。試験例Ａ２および試験例Ｂ２では、それぞれの第２制御ゾーンＺ２の目標温度に基づいて、各制御系２５から制御ゾーンＺ１～Ｚ３それぞれに供給される空気量の供給速度を設定した。このとき、試験例Ａ２および試験例Ｂ２それぞれにおいて、各制御ゾーンＺ１～Ｚ３に供給する空気量の供給速度を同等とした。具体的には、試験例Ａ２では各制御ゾーンＺ１～Ｚ３の空気量の供給速度の合計を２１５Ｎｍ^３／ｈとし、試験例Ｂ２では各制御ゾーンＺ１～Ｚ３の空気量の供給速度の合計を１６３Ｎｍ^３／ｈとした。なお、この場合における第１～第３制御ゾーンＺ３それぞれの温度および排出石炭温度を、以下表２に示す。 In Test Example A2 and Test Example B2, the target temperature of the second control zone Z2 was made different in order to compare the influence of tar adhesion on the operating temperature of the heating chamber 22. In Test Example A2, the temperature of the second control zone Z2 was set to about 630 ° C, and in Test Example B2, the temperature of the second control zone Z2 was set to about 550 ° C. In Test Example A2 and Test Example B2, the supply speed of the amount of air supplied from each control system 25 to each of the control zones Z1 to Z3 was set based on the target temperature of each of the second control zones Z2. At this time, in each of Test Example A2 and Test Example B2, the supply speed of the amount of air supplied to each of the control zones Z1 to Z3 was set to be the same. Specifically, in Test Example A2, the total supply rate of air in each of the control zones Z1 to Z3 is 215 Nm ³ / h, and in Test Example B2, the total supply rate of air in each of the control zones Z1 to Z3 is 163 Nm. ^{It was set to 3} / h. The temperature and the discharged coal temperature of each of the first to third control zones Z3 in this case are shown in Table 2 below.

　この第２の検証試験では、試験例Ａ２および試験例Ｂ２それぞれについて、５日間連続して操業し、１日目における内筒２１から二次燃焼装置１５までの間の圧力損失と、５日目における内筒２１から二次燃焼装置１５までの間の圧力損失とを測定した。ここで、内筒２１から二次燃焼装置１５までの間の圧力損失は、内筒２１の下流側Ｄ２の端部と二次燃焼装置１５側の端部との間のガスの圧力差によって測定する。 In this second verification test, each of Test Example A2 and Test Example B2 was operated continuously for 5 days, and the pressure loss between the inner cylinder 21 and the secondary combustion device 15 on the first day and the pressure loss on the fifth day The pressure loss between the inner cylinder 21 and the secondary combustion device 15 was measured. Here, the pressure loss between the inner cylinder 21 and the secondary combustion device 15 is measured by the pressure difference of the gas between the end of the downstream side D2 of the inner cylinder 21 and the end of the secondary combustion device 15 side. do.

　試験例Ａ２および試験例Ｂ２とも、１日目の運転開始直後における煙道４３の圧力損失は、０．０２ｋＰａであった。試験例Ａ２では、５日目における煙道４３の圧力損失は、０．０３ｋＰａであるのに対して、試験例Ｂ２では、５日目における煙道４３の圧力損失は、１．４５ｋＰａであった。
　この結果から、試験例Ａ２では、試験例Ｂ１よりも煙道４３の圧力損失が小さく、タールの付着が抑えられていることが確認された。 In both Test Example A2 and Test Example B2, the pressure loss of the flue 43 immediately after the start of operation on the first day was 0.02 kPa. In Test Example A2, the pressure loss of the flue 43 on the 5th day was 0.03 kPa, whereas in Test Example B2, the pressure loss of the flue 43 on the 5th day was 1.45 kPa. ..
From this result, it was confirmed that in Test Example A2, the pressure loss of the flue 43 was smaller than that of Test Example B1, and the adhesion of tar was suppressed.

　（第３の検証試験）
　第３の検証試験では、制御ゾーンＺ１～Ｚ３ごとに温度を制御することによる石炭の揮発分の違いについて検証した。第３の検証試験では、試験例Ａ３および試験例Ｂ３として２種類の乾留装置１２を用いた。これらの２つの乾留装置１２はいずれも、内筒２１の直径は５００ｍｍとし、内筒２１の加熱室内部分２１ａの軸線Ｏ方向の大きさは３０００ｍｍとし、内筒２１の軸線Ｏの水平方向に対する傾斜角度は１．０度とし、内筒２１の回転速度は３．１ｒｐｍとした。また、内筒２１に供給される石炭の水分を１２．１重量％とし、内筒２１に供給される石炭の供給速度を、２２０ｋｇ／ｈ～２２５ｋｇ／ｈとした。さらに、煙道４３を、加熱室２２の上流側Ｄ１の端部の制御ゾーンＺ１のみに接続した。そして、排出改質石炭温度に基づいて、各制御系２５から制御ゾーンＺ１～Ｚ３それぞれに供給される空気の供給速度を設定した。このとき、排出石炭温度が６５５℃前後となるように、各制御系２５を制御した。 (Third verification test)
In the third verification test, the difference in the volatile content of coal by controlling the temperature in each of the control zones Z1 to Z3 was verified. In the third verification test, two types of carbonization devices 12 were used as Test Example A3 and Test Example B3. In both of these two carbonization devices 12, the diameter of the inner cylinder 21 is 500 mm, the size of the heating chamber portion 21a of the inner cylinder 21 in the axis O direction is 3000 mm, and the inclination of the axis O of the inner cylinder 21 with respect to the horizontal direction. The angle was 1.0 degree, and the rotation speed of the inner cylinder 21 was 3.1 rpm. Further, the water content of the coal supplied to the inner cylinder 21 was set to 12.1% by weight, and the supply speed of the coal supplied to the inner cylinder 21 was set to 220 kg / h to 225 kg / h. Further, the flue 43 was connected only to the control zone Z1 at the end of the upstream side D1 of the heating chamber 22. Then, based on the emission reformed coal temperature, the supply speed of the air supplied from each control system 25 to each of the control zones Z1 to Z3 was set. At this time, each control system 25 was controlled so that the discharged coal temperature was around 655 ° C.

　試験例Ａ３と試験例Ｂ３とでは、加熱室２２内における温度の分布を異ならせた。
　すなわち、試験例Ａ３では、温度制御部２３により、各制御ゾーンＺ１～Ｚ３の温度がほぼ同等になるように、加熱室２２の温度を制御した（表３参照）。このとき試験例Ａ３では、各制御系２５からの空気量の供給速度を異ならせて、第１制御ゾーンＺ１には１２０Ｎｍ^３／ｈで空気を供給し、第２制御ゾーンＺ２には７０Ｎｍ^３／ｈで空気を供給し、第３制御ゾーンＺ３には３５Ｎｍ^３／ｈで空気を供給した。
　一方、試験例Ｂ３では、各制御系２５からの空気の供給速度を同等にして、各制御ゾーンＺ１～Ｚ３に各々７５Ｎｍ^３／ｈで空気量の供給速度で空気を供給した。その結果、各制御ゾーンＺ１～Ｚ３の温度は、表３に示すように各ゾーンの温度がばらついた。 The temperature distribution in the heating chamber 22 was different between Test Example A3 and Test Example B3.
That is, in Test Example A3, the temperature control unit 23 controlled the temperature of the heating chamber 22 so that the temperatures of the control zones Z1 to Z3 were substantially the same (see Table 3). At this time, in Test Example A3, the supply speed of the amount of air from each control system 25 is changed ^{to supply air to the first control zone Z1 at 120 Nm 3} / h and to the second control zone Z2 at 70 Nm ³ /. Air was supplied at h, and air was supplied to the third control zone Z3 at 35 Nm ³ / h.
On the other hand, in Test Example B3, the air supply speed from each control system 25 was made equal, and air was supplied to each of the control zones Z1 to Z3 at a supply speed of ^{75 Nm 3 / h.} As a result, the temperatures of the control zones Z1 to Z3 varied as shown in Table 3.

　この第３の検証試験では、試験例Ａ３および試験例Ｂ３それぞれについて、内筒２１から排出される改質石炭の揮発分を測定した。試験例Ａ３では揮発分が６．２重量％であるのに対し、試験例Ｂ３では揮発分が９．２重量％であった。
　この結果から、試験例Ａ３では、排出石炭温度が試験例Ｂ３と同等であるにも関わらず試験例Ｂ３よりも揮発度が小さく、効果的に乾留されていることが確認された。 In this third verification test, the volatile content of the reformed coal discharged from the inner cylinder 21 was measured for each of Test Example A3 and Test Example B3. In Test Example A3, the volatile content was 6.2% by weight, whereas in Test Example B3, the volatile content was 9.2% by weight.
From this result, it was confirmed that in Test Example A3, although the discharged coal temperature was the same as that of Test Example B3, the volatility was smaller than that of Test Example B3 and carbonization was effectively performed.

　（第２の実施形態）
　次に、本発明の第２の実施形態について説明する。本実施形態でも上記の第１の実施形態と同様の外熱式ロータリーキルンの乾留装置を含む製造設備を用いて改質石炭が製造される。本実施形態では、以下で説明するように乾留装置の内筒の中で石炭を撹拌するための撹拌部材が設けられる。なお、それ以外の点については上記の第１の実施形態の例に限らず一般的な外熱式ロータリーキルンの構成を採用することが可能であり、例えば加熱室において煙道は必ずしも上流側の端部にのみ接続されなくてもよい。 (Second Embodiment)
Next, a second embodiment of the present invention will be described. In this embodiment as well, reformed coal is produced using a production facility including a carbonization device for an externally heated rotary kiln similar to that in the first embodiment. In the present embodiment, as described below, a stirring member for stirring coal in the inner cylinder of the carbonization device is provided. Regarding other points, it is possible to adopt a general external heat type rotary kiln configuration, not limited to the example of the first embodiment described above. For example, in a heating chamber, the flue is not necessarily the upstream end. It does not have to be connected only to the unit.

　図３は、本発明の第２の実施形態に係る乾留装置における内筒の内周面の展開図である。図示された例において、内筒２１の内部は上流側から下流側に向けて送り領域２１１と加熱領域２１２に区分され、加熱領域２１２は水分蒸発ゾーン２１２Ａおよび熱分解ゾーン２１２Ｂにさらに区分される。また、熱分解ゾーン２１２Ｂの下流側は出口領域２１３である。本実施形態では、石炭を撹拌するための撹拌板５１，５２が、それぞれ水分蒸発ゾーン２１２Ａおよび熱分解ゾーン２１２Ｂで内筒２１の内周面２１ｃから軸線Ｏ（図２参照）に向かって突出して設けられる。送り領域２１１には石炭を加熱領域２１２に送り込むための送りリフター２１１Ｌが設けられ、出口領域２１３には撹拌板およびリフターは設けられない。 FIG. 3 is a developed view of the inner peripheral surface of the inner cylinder in the carbonization device according to the second embodiment of the present invention. In the illustrated example, the inside of the inner cylinder 21 is further divided into a feed region 211 and a heating region 212 from the upstream side to the downstream side, and the heating region 212 is further divided into a water evaporation zone 212A and a thermal decomposition zone 212B. Further, the downstream side of the thermal decomposition zone 212B is the outlet region 213. In the present embodiment, the stirring

plates

51 and 52 for stirring coal project from the inner peripheral surface 21c of the inner cylinder 21 toward the axis O (see FIG. 2) in the water evaporation zone 212A and the thermal decomposition zone 212B, respectively. Provided. The feed region 211 is provided with a feed lifter 211L for feeding coal to the heating region 212, and the outlet region 213 is not provided with a stirring plate and a lifter.

　撹拌板５１，５２は、内筒２１の周方向について９０°間隔で方向を変えて配列された排気管２４とは別に、内筒２１の周方向について所定間隔（図示された例では４５°間隔）で配列される。水分蒸発ゾーン２１２Ａでは、周方向に配列される複数の撹拌板５１のそれぞれが軸線Ｏに対して平行に延びている。つまり、水分蒸発ゾーン２１２Ａの撹拌板５１の軸線Ｏに対する傾斜角は０である。図４Ａは図３のＡ－Ａ線に沿った断面図、すなわち展開されていない状態の内筒２１の水分蒸発ゾーン２１２Ａにおける断面図であり、各撹拌板５１が内筒２１の内周面２１ｃから軸線Ｏに向かって突出し、かつ内筒２１の周方向に等間隔に配列される例が示されている。撹拌板５１は、軸線Ｏとは反対側の端部でブラケット５３を介して内周面２１ｃに取り付けられている。軸線Ｏの方向で隣接する撹拌板５１は内筒２１の周方向について間隔の１／２（図示された例では２２．５°）だけ互いにずれて配列されている。本実施形態において、水分蒸発ゾーン２１２Ａの撹拌板５１は軸線Ｏの方向に例えば４列配列されている。 The stirring

plates

51 and 52 are separated from the exhaust pipes 24 arranged by changing the direction of the inner cylinder 21 at 90 ° intervals, and at predetermined intervals (45 ° intervals in the illustrated example) in the circumferential direction of the inner cylinder 21. ). In the water evaporation zone 212A, each of the plurality of stirring plates 51 arranged in the circumferential direction extends parallel to the axis O. That is, the inclination angle of the stirring plate 51 of the water evaporation zone 212A with respect to the axis O is 0. FIG. 4A is a cross-sectional view taken along the line AA of FIG. 3, that is, a cross-sectional view of the inner cylinder 21 in an undeveloped state in the water evaporation zone 212A, and each stirring plate 51 is an inner peripheral surface 21c of the inner cylinder 21. An example is shown in which the inner cylinder 21 protrudes from the axis O toward the axis O and is arranged at equal intervals in the circumferential direction of the inner cylinder 21. The stirring plate 51 is attached to the inner peripheral surface 21c via the bracket 53 at the end opposite to the axis O. The stirring plates 51 adjacent to each other in the direction of the axis O are arranged so as to be offset from each other by 1/2 (22.5 ° in the illustrated example) of the circumferential direction of the inner cylinder 21. In the present embodiment, the stirring plates 51 of the water evaporation zone 212A are arranged in, for example, four rows in the direction of the axis O.

　一方、熱分解ゾーン２１２Ｂでは、水分蒸発ゾーン２１２Ａにおける撹拌板５１の配列と同様な周方向の間隔（図では４５°間隔）および長さ方向の間隔で、複数の撹拌板５２が配列されている。熱分解ゾーン２１２Ｂでは、周方向に配列される複数の撹拌板５２のそれぞれが軸線Ｏに対して傾斜角β（図３参照）を有する。傾斜角βの大きさは、例えば４．３°～４．５°程度である。熱分解ゾーン２１２Ｂでは、撹拌板５２が傾斜角βを有することによって、内筒２１を所定の向きに回転させた場合に通過する石炭を上流側に押し戻すように撹拌することができる。その一方で、水分蒸発ゾーン２１２Ａでは傾斜角を有さない撹拌板５１によって石炭が熱分解ゾーン２１２Ｂ側に送り出されるため、熱分解ゾーン２１２Ｂ内での石炭の充填率がより均一になり、滞留時間を長く設定することができる。図４Ｂは図３のＢ－Ｂ線に沿った断面図、すなわち展開されていない状態の内筒２１の熱分解ゾーン２１２Ｂにおける断面図であり、各撹拌板５２が内筒２１の内周面２１ｃから軸線Ｏに向かって突出し、かつ内筒２１の周方向に等間隔に配列され、かつ軸線Ｏに対して傾斜角βを有するために端面だけではなく板面が見えている例が示されている。本実施形態において、熱分解ゾーン２１２Ｂの撹拌板５２は軸線Ｏの方向に例えば８列配列されている。 On the other hand, in the thermal decomposition zone 212B, a plurality of stirring plates 52 are arranged at intervals in the circumferential direction (45 ° intervals in the figure) and intervals in the length direction similar to the arrangement of the stirring plates 51 in the water evaporation zone 212A. .. In the thermal decomposition zone 212B, each of the plurality of stirring plates 52 arranged in the circumferential direction has an inclination angle β (see FIG. 3) with respect to the axis O. The magnitude of the inclination angle β is, for example, about 4.3 ° to 4.5 °. In the thermal decomposition zone 212B, since the stirring plate 52 has an inclination angle β, the coal passing through when the inner cylinder 21 is rotated in a predetermined direction can be stirred so as to be pushed back to the upstream side. On the other hand, in the moisture evaporation zone 212A, the coal is sent out to the pyrolysis zone 212B side by the stirring plate 51 having no inclination angle, so that the filling rate of the coal in the pyrolysis zone 212B becomes more uniform and the residence time becomes more uniform. Can be set longer. FIG. 4B is a cross-sectional view taken along the line BB of FIG. 3, that is, a cross-sectional view of the inner cylinder 21 in an undeveloped state in the thermal decomposition zone 212B, and each stirring plate 52 is an inner peripheral surface 21c of the inner cylinder 21. An example is shown in which not only the end face but also the plate surface is visible because the inner cylinder 21 is arranged at equal intervals in the circumferential direction of the inner cylinder 21 and has an inclination angle β with respect to the axis O. There is. In the present embodiment, the stirring plates 52 of the thermal decomposition zone 212B are arranged in, for example, eight rows in the direction of the axis O.

　加えて、熱分解ゾーン２１２Ｂにおける撹拌板５２は、図５Ａおよび図５Ｂに示すようにブラケット５３を介して内周面２１ｃに取り付けられ、撹拌板５２と内筒２１の内周面２１ｃとの間には隙間５４が形成されている。このような隙間５４が形成されることで、内筒２１の回転時に撹拌板５２によって撹拌された石炭の一部を隙間５４から内周面２１ｃに沿って落下させることができ、石炭の粒子が軸線Ｏ側に飛散して排気管２４に吸い込まれるのを防止しつつ、内筒２１の内部での石炭の混合を促進させることができる。 In addition, the stirring plate 52 in the thermal decomposition zone 212B is attached to the inner peripheral surface 21c via the bracket 53 as shown in FIGS. 5A and 5B, and is between the stirring plate 52 and the inner peripheral surface 21c of the inner cylinder 21. A gap 54 is formed in the. By forming such a gap 54, a part of the coal stirred by the stirring plate 52 when the inner cylinder 21 is rotated can be dropped from the gap 54 along the inner peripheral surface 21c, and the coal particles can be formed. It is possible to promote the mixing of coal inside the inner cylinder 21 while preventing the coal from being scattered toward the axis O side and being sucked into the exhaust pipe 24.

　本実施形態において、上記のような撹拌板５１，５２は、軸線Ｏの方向について、水分蒸発ゾーン２１２Ａおよび熱分解ゾーン２１２Ｂからなる加熱領域２１２の全体に配置されている。石炭の飛散を防止しながら均一に撹拌混合するためには、撹拌板５１，５２を加熱領域２１２の９０％を超える範囲に設置することが好ましい。 In the present embodiment, the stirring

plates

51 and 52 as described above are arranged in the entire heating region 212 including the water evaporation zone 212A and the thermal decomposition zone 212B in the direction of the axis O. In order to uniformly stir and mix while preventing coal from scattering, it is preferable to install the

stir plates

51 and 52 in a range exceeding 90% of the heating region 212.

　次に、上記の第１の実施形態で説明した図１もあわせて参照して、本実施形態における乾留装置を用いた改質石炭の製造方法について説明する。まず、図示しない駆動部を駆動させることで内筒２１を軸線Ｏ回りに回転させるとともに、加熱部２７によって加熱室２２内を加熱する。そして、内筒２１の内部が所定の高温になると石炭を内筒２１の内部に投入し、加熱室２２内の高熱によって乾留させる。 Next, a method for producing reformed coal using the carbonization apparatus in the present embodiment will be described with reference to FIG. 1 described in the first embodiment above. First, the inner cylinder 21 is rotated around the axis O by driving a drive unit (not shown), and the inside of the heating chamber 22 is heated by the heating unit 27. Then, when the inside of the inner cylinder 21 reaches a predetermined high temperature, coal is put into the inside of the inner cylinder 21 and carbonized by the high heat in the heating chamber 22.

　回転する内筒２１の内部に石炭を投入すると、送り領域２１１の送りリフター２１１Ｌによって加熱領域２１２の水分蒸発ゾーン２１２Ａに搬送され、石炭に含まれる水分が蒸発させられる。水分蒸発ゾーン２１２Ａにおいて、撹拌板５１は内筒２１の軸線Ｏと平行に配列されているため、石炭の粒子は撹拌板５１によって撹拌されながら内筒２１の内周面２１ｃに沿って搬送され、熱分解ゾーン２１２Ｂに搬送される。 When coal is put into the rotating inner cylinder 21, the coal is conveyed to the water evaporation zone 212A of the heating region 212 by the feed lifter 211L of the feed region 211, and the water contained in the coal is evaporated. In the water evaporation zone 212A, since the stirring plate 51 is arranged parallel to the axis O of the inner cylinder 21, coal particles are conveyed along the inner peripheral surface 21c of the inner cylinder 21 while being stirred by the stirring plate 51. It is transported to the thermal decomposition zone 212B.

　熱分解ゾーン２１２Ｂでは、内筒２１の回転によって撹拌板５２が回転させられ、内筒２１の内部で石炭が撹拌板５２によって撹拌混合される。その際、一部の石炭は撹拌板５２によって持ち上げられ、他の一部の石炭は撹拌板５２で持ち上げられずに隙間５４から落下して内周面２１ｃ上を流動する。撹拌板５２上の石炭の全体が軸線Ｏ側に落下するのではないことによって、撹拌に伴う飛散量を抑制できる。 In the thermal decomposition zone 212B, the stirring plate 52 is rotated by the rotation of the inner cylinder 21, and coal is stirred and mixed by the stirring plate 52 inside the inner cylinder 21. At that time, some coal is lifted by the stirring plate 52, and some other coal is not lifted by the stirring plate 52 but falls from the gap 54 and flows on the inner peripheral surface 21c. Since the entire coal on the stirring plate 52 does not fall to the axis O side, the amount of scattering due to stirring can be suppressed.

　ここで、図４Ｂに示すように、熱分解ゾーン２１２Ｂに配置される撹拌板５２は、撹拌板５２の高さｈａ（内周面２１ｃを基準にした、内筒２１の径方向における寸法）が石炭の充填高さｈｍに対して６０％～９０％となるように設計されることが好ましい。石炭の充填高さｈｍが撹拌板５２の高さｈａに対して小さすぎると撹拌効果が小さく、逆に大きすぎると石炭の飛散が増大する。内筒２１への石炭の投入量を、撹拌板５２の高さｈａが石炭の充填高さｈｍに対して上記の範囲になるように調節してもよい。また、図５Ａに示されるように、内周面２１ｃと撹拌板５２の延長面との交点（ブラケット５３が内周面２１ｃに接合される位置）から撹拌板５２の軸線Ｏ側の端部までの距離を高さｈａとし、隙間５４の高さ、すなわち内周面２１ｃと撹拌板５２の延長面との交点から撹拌板５２の内周面２１ｃ側の端部までの距離を高さｈｂとした場合、隙間５４の高さｈｂは撹拌板５２の高さｈａの１０％～２５％の範囲、より好ましくは１０％～２０％の範囲にあることが好ましい。 Here, as shown in FIG. 4B, the stirring plate 52 arranged in the thermal decomposition zone 212B has a height ha of the stirring plate 52 (dimension in the radial direction of the inner cylinder 21 with reference to the inner peripheral surface 21c). It is preferably designed to be 60% to 90% with respect to the filling height hm of coal. If the filling height hm of the coal is too small with respect to the height ha of the stirring plate 52, the stirring effect is small, and conversely, if it is too large, the scattering of coal increases. The amount of coal charged into the inner cylinder 21 may be adjusted so that the height ha of the stirring plate 52 is within the above range with respect to the filling height hm of coal. Further, as shown in FIG. 5A, from the intersection of the inner peripheral surface 21c and the extension surface of the stirring plate 52 (the position where the bracket 53 is joined to the inner peripheral surface 21c) to the end of the stirring plate 52 on the axis O side. The height ha is defined as the height ha, and the height of the gap 54, that is, the distance from the intersection of the inner peripheral surface 21c and the extension surface of the stirring plate 52 to the end of the stirring plate 52 on the inner peripheral surface 21c side is defined as the height hb. If so, the height hb of the gap 54 is preferably in the range of 10% to 25%, more preferably 10% to 20% of the height ha of the stirring plate 52.

　このように、本実施形態では、内筒２１の熱分解ゾーン２１２Ｂで石炭を乾留するにあたり、撹拌板５２による撹拌によって、石炭の融着や塊状化を防止できる。これによって、内筒２１の内部に堆積した石炭の温度偏差が小さくなり、加熱室２２からの熱が効率的に伝達される。また、隙間５４を設けることによって撹拌時における石炭の飛散を抑え、不揮発成分である炭化物の粒子が排気管２４から排出されるのを抑制できる。 As described above, in the present embodiment, when the coal is carbonized in the thermal decomposition zone 212B of the inner cylinder 21, the coal can be prevented from being fused or agglomerated by stirring with the stirring plate 52. As a result, the temperature deviation of the coal deposited inside the inner cylinder 21 is reduced, and the heat from the heating chamber 22 is efficiently transferred. Further, by providing the gap 54, it is possible to suppress the scattering of coal during stirring and to prevent the particles of carbide, which is a non-volatile component, from being discharged from the exhaust pipe 24.

　また、上述のように内筒２１の軸線Ｏには下り緩勾配がつけられているため、内筒２１の全体を通じて石炭は下流側に向かって移動するが、熱分解ゾーン２１２Ｂの撹拌板５２が傾斜角βを有することによって、撹拌板５２で撹拌された石炭の下流側への移動はある程度妨げられ、一部が上流側に押し戻される。その一方で、水分蒸発ゾーン２１２Ａでは石炭が傾斜角を有さない撹拌板５１によって下流側に送り出されるため、熱分解ゾーン２１２Ｂ内の石炭の充填率がより均一になり、滞留時間が長くなる。例えば、熱分解ゾーン２１２Ｂにおける温度を６５０℃とし、本実施形態とは異なり熱分解ゾーン２１２Ｂでも傾斜角を有さない撹拌板を設けた場合、内筒２１に投入された石炭が熱分解ゾーン２１２Ｂに滞留する時間は例えば５０分間程度である。他の条件は同様にして、本実施形態のように熱分解ゾーン２１２Ｂに傾斜角βを有する撹拌板５２を設けた場合、石炭が熱分解ゾーン２１２Ｂに滞留する時間は約２０％延長されて６０分程度になり、これによって石炭の受熱面積が約８％向上する。つまり、上記の例では、撹拌板５２が傾斜角βを有することによって乾留装置における石炭への伝熱効率が約８％向上する。 Further, as described above, since the axis O of the inner cylinder 21 has a gentle downward slope, coal moves toward the downstream side throughout the inner cylinder 21, but the stirring plate 52 of the thermal decomposition zone 212B By having the inclination angle β, the movement of the coal stirred by the stirring plate 52 to the downstream side is hindered to some extent, and a part of the coal is pushed back to the upstream side. On the other hand, in the water evaporation zone 212A, the coal is sent to the downstream side by the stirring plate 51 having no inclination angle, so that the filling rate of the coal in the pyrolysis zone 212B becomes more uniform and the residence time becomes longer. For example, when the temperature in the pyrolysis zone 212B is set to 650 ° C. and a stirring plate having no inclination angle is provided in the pyrolysis zone 212B unlike the present embodiment, the coal charged into the inner cylinder 21 is the pyrolysis zone 212B. The time to stay in the water is, for example, about 50 minutes. Under other conditions, when the stirring plate 52 having the inclination angle β is provided in the pyrolysis zone 212B as in the present embodiment, the time for coal to stay in the pyrolysis zone 212B is extended by about 20% to 60. This will increase the heat receiving area of coal by about 8%. That is, in the above example, the heat transfer efficiency to coal in the carbonization apparatus is improved by about 8% because the stirring plate 52 has the inclination angle β.

　なお、本実施形態については、上記の第１の実施形態との組み合わせが可能である他、以下に例示するように種々の変更を加えることが可能である。また、上記で説明した撹拌板５２が傾斜角βをもって配置される構成と、撹拌板５２と内筒２１の内周面２１ｃとの間に隙間５４を設ける構成とは、それぞれ別個に効果を奏するため、いずれか一方のみが採用されてもよい。 It should be noted that this embodiment can be combined with the above-mentioned first embodiment, and various changes can be made as illustrated below. Further, the configuration in which the stirring plate 52 described above is arranged with an inclination angle β and the configuration in which the gap 54 is provided between the stirring plate 52 and the inner peripheral surface 21c of the inner cylinder 21 are effective separately. Therefore, only one of them may be adopted.

　例えば、上述した例では、水分蒸発ゾーン２１２Ａの撹拌板５１を軸線Ｏに対して平行に設置したが、水分蒸発ゾーン２１２Ａにおける撹拌板５１も軸線Ｏに対して傾斜角をもって配置してもよい。この場合、軸線Ｏに対する撹拌板５１の傾斜角は、撹拌板５２の傾斜角βより小さく設定することが好ましい。 For example, in the above example, the stirring plate 51 of the water evaporation zone 212A is installed parallel to the axis O, but the stirring plate 51 in the water evaporation zone 212A may also be arranged with an inclination angle with respect to the axis O. In this case, the inclination angle of the stirring plate 51 with respect to the axis O is preferably set smaller than the inclination angle β of the stirring plate 52.

　また、内筒２１の周方向に配列される撹拌板５２の設置間隔は、等間隔であることが好ましいが、不等間隔であってもよい。撹拌板５２は、内筒２１の内径に応じて４枚～１２枚、より好ましくは６枚～１０枚の範囲で設置できる。内周面２１ｃの周方向に設置する撹拌板５２の数は、石炭の混合撹拌効果を向上できる範囲で適宜設定できるが、撹拌板５２の設置数を増やし過ぎると石炭の粒子が撹拌板５２間で細かく区画されてしまい、混合割合が低下するので好ましくない。 Further, the installation intervals of the stirring plates 52 arranged in the circumferential direction of the inner cylinder 21 are preferably equal intervals, but may be unequal intervals. The stirring plate 52 can be installed in the range of 4 to 12, more preferably 6 to 10, depending on the inner diameter of the inner cylinder 21. The number of stirring plates 52 installed in the circumferential direction of the inner peripheral surface 21c can be appropriately set within a range in which the mixing and stirring effect of coal can be improved. It is not preferable because it is divided into small pieces and the mixing ratio is lowered.

　次に、図６、図７Ａおよび図７Ｂを参照して、本発明の第２の実施形態の変形例について説明する。本変形例では、撹拌板５２に、内筒２１の径方向に対して傾斜する折り曲げ部５２ｂが形成される。具体的には、図７Ａに示されるように、内周面２１ｃと撹拌板５２の延長面との交点（ブラケット５３が内周面２１ｃに接合される位置）から撹拌板５２の軸線Ｏ側の端部までの距離を高さｈａとし、隙間５４の高さ、すなわち内周面２１ｃと撹拌板５２の延長面との交点から撹拌板５２の内周面２１ｃ側の端部までの距離を高さｈｂとし、撹拌板５２の軸線Ｏ側に形成される折り曲げ部５２ｂとそれ以外の部分との境界の内周面２１ｃからの距離を高さｈｃとした場合、高さｈｃは高さｈａの３０％～７０％の範囲であることが好ましい。つまり、折り曲げ部５２ｂは、撹拌板５２の軸線Ｏ側で内筒２１の内周面２１ｃを基準にした撹拌板５２の高さの３０％以上～７０％以下の範囲に形成されることが好ましい。また、折り曲げ部５２ｂの内筒２１の径方向に対する傾斜角γは１０°以上４５°以下であることが好ましい。上記の例では、撹拌板５２によって撹拌された石炭のうち、折り曲げ部５２ｂ上にあるものが先行して落下することで、例えば折り曲げ部が形成されない撹拌板５２の端部から石炭が（内筒２１の回転によって撹拌板５２の角度が水平を超えた時点で）一度に落下する場合に比べて石炭の飛散を抑制できる。 Next, a modified example of the second embodiment of the present invention will be described with reference to FIGS. 6, 7A and 7B. In this modification, the stirring plate 52 is formed with a bent portion 52b that is inclined with respect to the radial direction of the inner cylinder 21. Specifically, as shown in FIG. 7A, from the intersection of the inner peripheral surface 21c and the extension surface of the stirring plate 52 (the position where the bracket 53 is joined to the inner peripheral surface 21c) on the axis O side of the stirring plate 52. The distance to the end is defined as the height ha, and the height of the gap 54, that is, the distance from the intersection of the inner peripheral surface 21c and the extension surface of the stirring plate 52 to the end of the stirring plate 52 on the inner peripheral surface 21c side is increased. When the height hc is defined as the distance from the inner peripheral surface 21c of the boundary between the bent portion 52b formed on the axis O side of the stirring plate 52 and the other portion, the height hc is the height ha. It is preferably in the range of 30% to 70%. That is, the bent portion 52b is preferably formed in a range of 30% or more to 70% or less of the height of the stirring plate 52 with respect to the inner peripheral surface 21c of the inner cylinder 21 on the axis O side of the stirring plate 52. .. Further, the inclination angle γ of the bent portion 52b with respect to the radial direction of the inner cylinder 21 is preferably 10 ° or more and 45 ° or less. In the above example, among the coal agitated by the agitating plate 52, the coal on the bent portion 52b falls in advance, so that, for example, the coal is removed from the end of the agitated plate 52 in which the bent portion is not formed (inner cylinder). It is possible to suppress the scattering of coal as compared with the case where the stirring plate 52 is dropped all at once (when the angle of the stirring plate 52 exceeds the horizontal due to the rotation of 21).

　（第４の検証試験）
　次に、本発明の第２の実施形態に係る検証試験の結果について説明する。第４の検証試験では、試験例Ａ４および試験例Ａ５として、揮発分が５０ｗｔ％程度の褐炭を５ｍｍ以下に粉砕して乾燥させたものを原料炭として用いて熱分解試験を実施した。原料炭の加熱温度と生成された改質石炭のＶＭ値（揮発分）との関係を図８のグラフに示す。試験例Ａ４では石炭の昇温速度を７℃／分とし、試験例Ａ５では２５℃／分とした、それぞれ１分間保持した。試験例Ａ４，Ａ５のそれぞれで石炭温度が５５０℃、６５０℃、７５０℃の時にＶＭ値を測定すると、昇温速度が低い試験例Ａ４の場合の方が試験例Ａ５と比較してＶＭ値が低いという結果が得られた。この結果から、石炭の最終到達温度が同じであっても、昇温速度を比較的低く設定して熱分解ゾーンでの加熱（滞留）時間を長く維持することによって石炭のＶＭ値を低減し、乾留炭の揮発を促進できることがわかる。 (Fourth verification test)
Next, the result of the verification test according to the second embodiment of the present invention will be described. In the fourth verification test, as Test Example A4 and Test Example A5, a thermal decomposition test was carried out using lignite having a volatile content of about 50 wt% crushed to 5 mm or less and dried as a coking coal. The relationship between the heating temperature of the coking coal and the VM value (volatile matter) of the produced reformed coal is shown in the graph of FIG. In Test Example A4, the rate of temperature rise of coal was set to 7 ° C./min, and in Test Example A5, the rate of temperature rise was 25 ° C./min. When the VM value was measured when the coal temperatures were 550 ° C, 650 ° C, and 750 ° C in each of Test Examples A4 and A5, the VM value in Test Example A4, which had a lower heating rate, was higher than that in Test Example A5. The result was low. From this result, even if the final temperature of coal is the same, the VM value of coal is reduced by setting the heating rate relatively low and maintaining the heating (retention) time in the pyrolysis zone for a long time. It can be seen that the volatilization of dry distillation coal can be promoted.

　（第５の検証試験）
　第５の検証試験では、内筒の内径φ５００ｍｍ×加熱長Ｌ＝３０００ｍｍ（水分蒸発ゾーンおよび熱分解ゾーンを合わせた加熱領域の長さ）の外熱式ロータリーキルンを用いて石炭の乾留を行った。加熱領域の全長にわたって内筒の内周面周方向について４枚の撹拌板を配置し、撹拌板の傾斜角が０．０°（試験例Ｂ４）、４．０°（試験例Ａ６）、６．０°（試験例Ａ７）の３通りについて実験を行った。実験では、石炭投入量２８０ｋｇ／ｈ、内筒の回転数を３．１ｒｐｍ、内筒の下り勾配角度１．０°、撹拌板の高さｈａ＝９０ｍｍとし、試験例Ｂ４および試験例Ａ６，Ａ７について、実測滞留時間（ｍｉｎ）および総括伝熱係数（ｋｃａｌ／ｍ^２ｈ℃）とを測定した。結果を表４に示す。 (Fifth verification test)
In the fifth verification test, coal was carbonized using an externally heated rotary kiln having an inner cylinder inner diameter of φ500 mm × heating length L = 3000 mm (the length of the heating region including the water evaporation zone and the pyrolysis zone). Four stirring plates are arranged in the circumferential direction of the inner peripheral surface of the inner cylinder over the entire length of the heating region, and the inclination angles of the stirring plates are 0.0 ° (Test Example B4), 4.0 ° (Test Example A6), 6 Experiments were carried out in three ways of 0.0 ° (Test Example A7). In the experiment, the amount of coal input was 280 kg / h, the rotation speed of the inner cylinder was 3.1 rpm, the downward gradient angle of the inner cylinder was 1.0 °, and the height of the stirring plate was ha = 90 mm. The measured residence time (min) and the overall heat transfer coefficient (kcal / m ² h ° C.) were measured. The results are shown in Table 4.

　表４に示す試験結果から、内筒の加熱領域に配置される撹拌板に傾斜角をもたせた試験例Ａ６，Ａ７において、傾斜角がない試験例Ｂ４と比較して実測滞留時間が長くなり、総括伝熱係数が大きくなることを確認できた。 From the test results shown in Table 4, in Test Examples A6 and A7 in which the stirring plate arranged in the heating region of the inner cylinder was provided with an inclination angle, the measured residence time was longer than that in Test Example B4 having no inclination angle. It was confirmed that the overall heat transfer coefficient increased.

　（第６の検証試験）
　第６の検証試験では、内筒の内径φ５００ｍｍ、加熱長Ｌ＝３０００ｍｍ、内筒の下り勾配角度１．０°の外熱式ロータリーキルンを用いて石炭の乾留を行った。試験例Ｂ５では加熱領域の全長に渡って軸線に対して傾斜角をもたない撹拌板を設置し、試験例Ａ８では加熱領域のうち内筒の上流側の端部から６００ｍｍの範囲までは傾斜角のない撹拌板を設置し、それ以降は傾斜角４°の撹拌板を設置した。試験例Ａ９では加熱領域のうち内筒の上流側の端部から６００ｍｍの範囲までは傾斜角のない撹拌板を設置し、それ以降は傾斜角６°の撹拌板を設置した。実験では、石炭投入量２８０ｋｇ／ｈ、内筒の回転数を３．１ｒｐｍ、撹拌板の高さｈａ＝９０ｍｍ、内筒の下流側の端部における炭化物の目標温度を６４０℃とし、試験例Ｂ５および試験例Ａ８，Ａ９について、実測滞留時間（ｍｉｎ）、総括伝熱係数（ｋｃａｌ／ｍ^２ｈ℃）および乾留後の石炭揮発分（％）を測定した。結果を表５に示す。 (6th verification test)
In the sixth verification test, coal was carbonized using an externally heated rotary kiln having an inner cylinder having an inner diameter of φ500 mm, a heating length of L = 3000 mm, and an inner cylinder having a downward gradient angle of 1.0 °. In Test Example B5, a stirring plate having no inclination angle with respect to the axis is installed over the entire length of the heating region, and in Test Example A8, the heating region is inclined up to a range of 600 mm from the upstream end of the inner cylinder. A stirring plate without an angle was installed, and thereafter, a stirring plate with an inclination angle of 4 ° was installed. In Test Example A9, a stirring plate having no inclination angle was installed up to a range of 600 mm from the upstream end of the inner cylinder in the heating region, and after that, a stirring plate having an inclination angle of 6 ° was installed. In the experiment, the coal input amount was 280 kg / h, the rotation speed of the inner cylinder was 3.1 rpm, the height of the stirring plate was 90 mm, the target temperature of the charcoal at the downstream end of the inner cylinder was 640 ° C., and Test Example B5 For Test Examples A8 and A9, the measured residence time (min), the overall heat transfer coefficient (kcal / m ² h ° C.), and the coal volatilization content (%) after carbonization were measured. The results are shown in Table 5.

　表５に示す試験結果から、水分蒸発ゾーンには傾斜角のない撹拌板を、熱分解ゾーンには傾斜角をもった撹拌板をそれぞれ設置した試験例Ａ８，Ａ９では、加熱領域の全長に傾斜角をもった撹拌板を設置した上記の試験例Ａ６，Ａ７に比べて主に水分蒸発ゾーンで実測滞留時間が若干短くなる。ただし、水分蒸発ゾーンでは石炭に含まれる水分が蒸発しきっていないために内筒の内外での温度差が大きく、滞留時間が長くなっても総括伝熱係数の増加にはつながらない。従って、熱分解ゾーンでの滞留時間が同程度である試験例Ａ６，Ａ７と試験例Ａ８，Ａ９の間で総括伝熱係数はほとんど変わらなかった。また、内筒の下流側の端部における炭化物の目標温度が同じである場合、実測滞留時間の長い試験例Ａ６，Ａ７の方がより揮発分の低い改質石炭が得られた。 From the test results shown in Table 5, in Test Examples A8 and A9 in which a stirring plate having no inclination angle was installed in the moisture evaporation zone and a stirring plate having an inclination angle was installed in the thermal decomposition zone, the stirring plate was inclined to the entire length of the heating region. Compared with the above-mentioned Test Examples A6 and A7 in which the stirring plate having corners is installed, the measured residence time is slightly shorter mainly in the water evaporation zone. However, in the water evaporation zone, since the water contained in the coal has not completely evaporated, the temperature difference between the inside and outside of the inner cylinder is large, and even if the residence time is long, the total heat transfer coefficient does not increase. Therefore, the overall heat transfer coefficient was almost the same between Test Examples A6 and A7 and Test Examples A8 and A9, which had similar residence times in the pyrolysis zone. Further, when the target temperature of the carbide at the downstream end of the inner cylinder was the same, the modified coal having a lower volatile content was obtained in Test Examples A6 and A7 having a longer actual measurement residence time.

　（第７の検証試験）
　第７の検証試験では、内筒の内径φ５００ｍｍ、加熱長Ｌ＝３０００ｍｍ、内筒の下り勾配角度１．０°の外熱式ロータリーキルンを用いて石炭の乾留を行い、撹拌板の有無と設置数の違いによる内筒の内部の総括伝熱係数の測定値について試験した。石炭投入量１９０ｋｇ／ｈ～２８０ｋｇ／ｈ、内筒の回転数を２．２ｒｐｍ～３．０ｒｐｍ、加熱室の燃焼温度を７９０℃～８４０℃、内筒の内部における石炭の充填高さｈｍを１００ｍｍ～１４０ｍｍの範囲に設定した。試験例Ｂ６では撹拌板を設けず、試験例Ａ１０では撹拌板を周方向に２枚（１８０°間隔）で配置し、試験例Ａ１１では撹拌板を周方向に４枚（９０°間隔）で配置し、試験例Ａ１２では撹拌板を周方向に８枚（４５°間隔）で配置した。撹拌板の高さｈａはいずれも７５ｍｍとした。各試験例について、撹拌板の配置長さを変更し、撹拌板の周方向の枚数×撹拌板の全長を加熱長Ｌで除した値Ｋを変化させながら石炭の乾留を行い、内筒の全内周面の面積を基準とする総括伝熱係数Ｕ（ｋｃａｌ／ｍ^２ｈ℃）を測定した。 (7th verification test)
In the seventh verification test, coal was carbonized using an externally heated rotary kiln with an inner cylinder inner diameter of φ500 mm, a heating length of L = 3000 mm, and an inner cylinder with a downward gradient angle of 1.0 °. The measured values of the total heat transfer coefficient inside the inner cylinder were tested. The amount of coal input is 190 kg / h to 280 kg / h, the rotation speed of the inner cylinder is 2.2 rpm to 3.0 rpm, the combustion temperature of the heating chamber is 790 ° C to 840 ° C, and the filling height hm of coal inside the inner cylinder is 100 mm. It was set in the range of ~ 140 mm. In Test Example B6, no stirring plate is provided, in Test Example A10, two stirring plates are arranged in the circumferential direction (180 ° interval), and in Test Example A11, four stirring plates are arranged in the circumferential direction (90 ° interval). Then, in Test Example A12, eight stirring plates (45 ° intervals) were arranged in the circumferential direction. The height ha of the stirring plate was 75 mm in each case. For each test example, the arrangement length of the stirring plates was changed, and carbonization was performed while changing the value K obtained by dividing the number of stirring plates in the circumferential direction × the total length of the stirring plates by the heating length L, and carbonizing the entire inner cylinder. The overall heat transfer coefficient U (kcal / m ² h ° C.) based on the area of the inner peripheral surface was measured.

　図９は、第７の検証試験に係る総括伝熱係数の測定結果を示すグラフである。グラフに示されるように、撹拌板を設置することによって、また撹拌板の周方向の枚数および総面積が増大するに従って総括伝熱係数が大きくなることを確認できた。この結果は、撹拌板を設置し、周方向の枚数および総面積を増大させることで、内筒の内部における石炭の撹拌混合が促進されることを示している。 FIG. 9 is a graph showing the measurement results of the overall heat transfer coefficient according to the seventh verification test. As shown in the graph, it was confirmed that the total heat transfer coefficient increased by installing the stirring plate and as the number of stirring plates in the circumferential direction and the total area increased. This result shows that the stirring and mixing of coal inside the inner cylinder is promoted by installing the stirring plate and increasing the number of sheets and the total area in the circumferential direction.

　（第８の検証試験）
　第８の検証試験では、内筒の内径φ２７００ｍｍ、加熱長Ｌ＝３０００ｍｍの外熱式ロータリーキルンにおける撹拌板の折り曲げ部の有無による石炭の飛散位置の違いをＤＥＭ（Discrete Element Method）による計算で求めた。内筒の回転数は２．７ｒｐｍ、内筒の内部における石炭模擬粒子の充填高さｈｍは６９０ｍｍとした。撹拌板は試験例Ｂ７、試験例Ａ１３ともに周方向に６０°間隔で６枚配置した。試験例Ｂ７の撹拌板は内筒の径方向に延びる平板形状であり、試験例Ａ１３の撹拌板は図６に示すように撹拌板の上部に折り曲げ部を有する形状である。試験例Ｂ７、試験例Ａ１３とも、撹拌板と内筒の内周面との間には隙間が形成されない。試験例Ｂ７、試験例Ａ１３のそれぞれで、内筒が３回転する間に撹拌板によって撹拌された石炭の粒子が飛散する量を、内筒の中心軸線から内周面までの距離の関数として演算した。その結果を表６に示す。 (8th verification test)
In the eighth verification test, the difference in the scattering position of coal depending on the presence or absence of a bent portion of the stirring plate in an externally heated rotary kiln having an inner cylinder inner diameter of φ2700 mm and a heating length of L = 3000 mm was calculated by DEM (Discrete Element Method). .. The rotation speed of the inner cylinder was 2.7 rpm, and the filling height hm of the coal simulated particles inside the inner cylinder was 690 mm. Six stirring plates were arranged at intervals of 60 ° in the circumferential direction in both Test Example B7 and Test Example A13. The stirring plate of Test Example B7 has a flat plate shape extending in the radial direction of the inner cylinder, and the stirring plate of Test Example A13 has a shape having a bent portion at the upper part of the stirring plate as shown in FIG. In both Test Example B7 and Test Example A13, no gap is formed between the stirring plate and the inner peripheral surface of the inner cylinder. In each of Test Example B7 and Test Example A13, the amount of coal particles agitated by the stirring plate while the inner cylinder rotates three times is calculated as a function of the distance from the central axis of the inner cylinder to the inner peripheral surface. bottom. The results are shown in Table 6.

　表６に示す結果から、試験例Ｂ７に比べて試験例Ａ１３では、石炭の粒子が飛散する範囲が軸線付近から内周面付近に移動していることがわかる。この結果は、撹拌板に折り曲げ部を設けることによって、内筒の軸線付近に飛散して排気管から排出される石炭の粒子を減少させられることを示している。 From the results shown in Table 6, it can be seen that in Test Example A13, the range in which coal particles are scattered has moved from the vicinity of the axis to the vicinity of the inner peripheral surface as compared with Test Example B7. This result shows that by providing the bending portion in the stirring plate, the coal particles scattered near the axis of the inner cylinder and discharged from the exhaust pipe can be reduced.

　（第９の検証試験）
　第９の検証試験では、内筒の内径φ５００ｍｍ、加熱長Ｌ＝３０００ｍｍの外熱式ロータリーキルンを用いて石炭の乾留を行い、撹拌板と内筒の内周面との間の隙間の有無による石炭の飛散状況を試験した。それぞれの例において撹拌板は内筒の内周面から上端までの高さｈａが９０ｍｍであり、上部に折り曲げ部を有する形状である。撹拌板と内周面との間の隙間の大きさは、試験例Ｂ８では０（隙間なし）、試験例Ａ１４では１５ｍｍ、試験例Ｂ９では高さ３５ｍｍとした。内筒に投入される石炭の含有水分を１２．５０％とし、内筒の回転数を３．１ｒｐｍとした。試験では、石炭の投入量および加熱後の温度から既知の収率関数を用いて、乾留後の改質石炭の排出量の予測値を計算した。この予測値と、内筒から排出された改質石炭の排出量の実測値との差分を、内筒の内部で飛散して排気管から排出された石炭粒子の量であるとみなして飛散率を算出した。結果を表７に示す。 (9th verification test)
In the ninth verification test, coal was carbonized using an externally heated rotary kiln having an inner cylinder inner diameter of φ500 mm and a heating length of L = 3000 mm, and coal was carbonized by the presence or absence of a gap between the stirring plate and the inner peripheral surface of the inner cylinder. The scattering situation was tested. In each example, the stirring plate has a height ha from the inner peripheral surface to the upper end of the inner cylinder of 90 mm, and has a shape having a bent portion at the upper portion. The size of the gap between the stirring plate and the inner peripheral surface was 0 (no gap) in Test Example B8, 15 mm in Test Example A14, and 35 mm in height in Test Example B9. The water content of the coal charged into the inner cylinder was set to 12.50%, and the rotation speed of the inner cylinder was set to 3.1 rpm. In the test, predicted values of reformed coal emissions after carbonization were calculated using a known yield function from the coal input and the temperature after heating. The difference between this predicted value and the measured value of the amount of reformed coal discharged from the inner cylinder is regarded as the amount of coal particles scattered inside the inner cylinder and discharged from the exhaust pipe, and the scattering rate Was calculated. The results are shown in Table 7.

　表７に示す結果から、撹拌板と内筒の内周面との間の隙間を大きくすることによって石炭の飛散量を低下させられることがわかる。ただし、以下の検証試験で示すように、隙間が大きすぎると石炭への伝熱係数が減少する場合があるため、隙間の大きさは適切な範囲で設定することが望ましい。 From the results shown in Table 7, it can be seen that the amount of coal scattered can be reduced by increasing the gap between the stirring plate and the inner peripheral surface of the inner cylinder. However, as shown in the verification test below, if the gap is too large, the heat transfer coefficient to coal may decrease, so it is desirable to set the size of the gap within an appropriate range.

　（第１０の検証試験）
　第１０の検証試験では、内筒の内径φ５００ｍｍ、加熱長Ｌ＝３０００ｍｍの外熱式ロータリーキルンを用いて石炭の乾留を行い、撹拌板と内筒の内周面との間に隙間がある場合とない場合とにおける総括伝熱係数を実測した。それぞれの例において撹拌板は内筒の内周面から上端までの高さｈａが９０ｍｍであり、撹拌板と内周面との間の隙間の大きさは、試験例Ｂ１０では０（隙間なし）、試験例Ａ１５では１５ｍｍ、試験例Ｂ１１では３５ｍｍである。内筒の回転数は２．７ｒｐｍ、石炭投入量は２８０ｋｇ／ｈ、内筒の内部における石炭の充填高さｈｍは１５０ｍｍとした。それぞれの例における総括伝熱係数の算出結果を表８に示す。 (10th verification test)
In the tenth verification test, coal was carbonized using an externally heated rotary kiln with an inner cylinder inner diameter of φ500 mm and a heating length of L = 3000 mm, and there was a gap between the stirring plate and the inner peripheral surface of the inner cylinder. The overall heat transfer coefficient was measured with and without it. In each example, the height ha of the stirring plate from the inner peripheral surface to the upper end of the inner cylinder is 90 mm, and the size of the gap between the stirring plate and the inner peripheral surface is 0 (no gap) in Test Example B10. , 15 mm in Test Example A15 and 35 mm in Test Example B11. The rotation speed of the inner cylinder was 2.7 rpm, the coal input amount was 280 kg / h, and the coal filling height hm inside the inner cylinder was 150 mm. Table 8 shows the calculation results of the overall heat transfer coefficient in each example.

　表８に示す結果から、隙間の大きさを１５ｍｍとした試験例Ａ１５では隙間のない試験例Ｂ１０に比べて総括伝熱係数が上昇するものの、隙間の大きさを３５ｍｍとした試験例Ｂ１１ではかえって隙間のない試験例Ｂ１０よりも総括伝熱係数が低下した。この結果から、撹拌板と内筒の内周面との間に適切な大きさの隙間を設けることによって石炭の撹拌の効率が向上するが、隙間が大きすぎると撹拌の効率が低下することがわかる。 From the results shown in Table 8, in Test Example A15 with a gap size of 15 mm, the overall heat transfer coefficient was higher than in Test Example B10 with no gap, but in Test Example B11 with a gap size of 35 mm, instead. The overall heat transfer coefficient was lower than that of Test Example B10 having no gap. From this result, the efficiency of stirring coal can be improved by providing a gap of an appropriate size between the stirring plate and the inner peripheral surface of the inner cylinder, but if the gap is too large, the efficiency of stirring may decrease. Recognize.

　図１０は、上記の第９および第１０の検証試験の結果について、内筒の内周面と撹拌板との間の隙間の大きさと石炭の飛散率および総括伝熱係数との関係を示すグラフである。グラフに示されるように、石炭粒子の飛散率は隙間が大きいほど少なくなる一方で、伝熱係数は隙間が所定の値（この例では１５ｍｍ）の場合に最大になり、隙間が大きくなりすぎると低下する。例えば、グラフにおいて総括伝熱係数が１０ｋｃａｌ／ｍ^２ｈ℃を上回る範囲を適切な範囲とすると、隙間の大きさについては９ｍｍ～２３ｍｍ、すなわち撹拌板の高さｈａの１０％～２５％の範囲が好ましく、高さｈａの１０％～２０％の範囲がより好ましいといえる。 FIG. 10 is a graph showing the relationship between the size of the gap between the inner peripheral surface of the inner cylinder and the stirring plate, the scattering rate of coal, and the overall heat transfer coefficient for the results of the ninth and tenth verification tests. Is. As shown in the graph, the scattering rate of coal particles decreases as the gap becomes larger, while the heat transfer coefficient becomes maximum when the gap is a predetermined value (15 mm in this example), and when the gap becomes too large. descend. For example, assuming ^{that the range in which the total heat transfer coefficient exceeds 10 kcal / m 2} h ° C in the graph is an appropriate range, the size of the gap is 9 mm to 23 mm, that is, the range of 10% to 25% of the height ha of the stirring plate. Is preferable, and it can be said that a range of 10% to 20% of the height ha is more preferable.

　以上、添付図面を参照しながら本発明の好適な実施形態について詳細に説明したが、本発明はかかる例に限定されない。本発明の属する技術の分野における通常の知識を有する者であれば、特許請求の範囲に記載された技術的思想の範疇内において、各種の変更例または修正例に想到し得ることは明らかであり、これらについても、当然に本発明の技術的範囲に属するものと了解される。 Although the preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, the present invention is not limited to such examples. It is clear that a person having ordinary knowledge in the field of technology to which the present invention belongs can come up with various modifications or modifications within the scope of the technical ideas described in the claims. , These are also naturally understood to belong to the technical scope of the present invention.

　１０…製造設備、１１…乾燥装置、１２…乾留装置、１３…冷却装置、１４…排ガスシステム、１５…二次燃焼装置、１６…蒸気発生装置、１７…除塵装置、１８…吸引ファン、１９…排ガス処理装置、２１…内筒、２１ａ…加熱室内部分、２１ｃ…内周面、２１１…送り領域、２１１Ｌ…送りリフター、２１２…加熱領域、２１２Ａ…水分蒸発ゾーン、２１２Ｂ…熱分解ゾーン、２１３…出口領域、２２…加熱室、２３…温度制御部、２４…排気管、２５…制御系、２６…空気供給部、２７…加熱部、２８…蒸気供給部、２９…温度検出部、３０…制御本体部、３１…打ち込み空気ファン、３２…第１配管、３３…第１制御弁、３４…バーナー、３６…バーナーファン、３７…第２配管、３８…第２制御弁、３９…第３配管、４０…第３制御弁、４１…第４配管、４２…第４制御弁、４３…煙道、５１…撹拌板、５２…撹拌板、５２ｂ…折り曲げ部、５３…ブラケット、５４…隙間、Ｄ１…上流側、Ｄ２…下流側、Ｏ…軸線、Ｚ１…第１制御ゾーン、Ｚ２…第２制御ゾーン、Ｚ３…第３制御ゾーン。 10 ... Manufacturing equipment, 11 ... Drying device, 12 ... Drying device, 13 ... Cooling device, 14 ... Exhaust system, 15 ... Secondary combustion device, 16 ... Steam generator, 17 ... Dust removal device, 18 ... Suction fan, 19 ... Exhaust gas treatment device, 21 ... Inner cylinder, 21a ... Heating chamber part, 21c ... Inner peripheral surface, 211 ... Feed area, 211L ... Feed lifter, 212 ... Heating area, 212A ... Moisture evaporation zone, 212B ... Thermal decomposition zone, 213 ... Outlet area, 22 ... heating chamber, 23 ... temperature control unit, 24 ... exhaust pipe, 25 ... control system, 26 ... air supply unit, 27 ... heating unit, 28 ... steam supply unit, 29 ... temperature detection unit, 30 ... control Main body, 31 ... Driven air fan, 32 ... 1st pipe, 33 ... 1st control valve, 34 ... Burner, 36 ... Burner fan, 37 ... 2nd pipe, 38 ... 2nd control valve, 39 ... 3rd pipe, 40 ... 3rd control valve, 41 ... 4th pipe, 42 ... 4th control valve, 43 ... flue, 51 ... stirring plate, 52 ... stirring plate, 52b ... bent part, 53 ... bracket, 54 ... gap, D1 ... Upstream side, D2 ... downstream side, O ... axis, Z1 ... first control zone, Z2 ... second control zone, Z3 ... third control zone.

Claims

　軸線の回りに回転する内筒と、
　前記内筒を、前記内筒の径方向の外側から覆う加熱室と、
　前記内筒に、前記軸線方向に複数配置され、前記内筒を前記径方向に貫通して前記加熱室内に開口する排気管と、を有する乾留装置を備え、
　前記内筒において、前記軸線方向に沿った上流側に位置する端部から石炭が供給され、前記軸線方向に沿った下流側に位置する端部から改質石炭が排出される改質石炭の製造設備であって、
　前記加熱室内に酸素含有ガスを供給して前記加熱室内の温度を制御する温度制御部と、
　前記加熱室内のガスを排出する煙道と、を更に備え、
　前記煙道は、前記加熱室において前記上流側に位置する端部にのみ接続されている、改質石炭の製造設備。 An inner cylinder that rotates around the axis and
A heating chamber that covers the inner cylinder from the outside in the radial direction of the inner cylinder, and
The inner cylinder is provided with a carbonization device having a plurality of exhaust pipes arranged in the axial direction and having an exhaust pipe that penetrates the inner cylinder in the radial direction and opens into the heating chamber.
Production of reformed coal in which coal is supplied from an end located on the upstream side along the axial direction of the inner cylinder and reformed coal is discharged from an end located on the downstream side along the axial direction. It ’s a facility,
A temperature control unit that supplies oxygen-containing gas to the heating chamber to control the temperature in the heating chamber,
Further provided with a flue for discharging gas in the heating chamber.
A facility for producing reformed coal, wherein the flue is connected only to an end located on the upstream side in the heating chamber.
　前記温度制御部は、前記煙道内の温度が６００℃以上を維持し、かつ前記加熱室内の温度を６００℃以上となるように制御する、請求項１に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to claim 1, wherein the temperature control unit controls the temperature in the flue to be 600 ° C. or higher and the temperature in the heating chamber to be 600 ° C. or higher.
　前記温度制御部は、前記加熱室内を前記軸線方向に複数に区画してなる制御ゾーンごとに温度を制御し、
　前記煙道は、複数の前記制御ゾーンのうち、最も前記上流側の制御ゾーンに接続されている、請求項１または請求項２に記載の改質石炭の製造設備。 The temperature control unit controls the temperature for each control zone formed by dividing the heating chamber into a plurality of sections in the axial direction.
The modified coal manufacturing facility according to claim 1 or 2, wherein the flue is connected to the most upstream control zone among the plurality of control zones.
　前記内筒の内周面から前記軸線に向かって突出し、前記石炭を撹拌する撹拌部材をさらに備える、請求項１から請求項３のいずれか１項に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to any one of claims 1 to 3, further comprising a stirring member that protrudes from the inner peripheral surface of the inner cylinder toward the axis and stirs the coal.
　前記内筒の内部で前記下流側の熱分解ゾーンに配置される前記撹拌部材は、前記上流側の水分蒸発ゾーンに配置される前記撹拌部材よりも、前記軸線に対する傾斜角が大きい、請求項４に記載の改質石炭の製造設備。 4. The stirring member arranged in the thermal decomposition zone on the downstream side inside the inner cylinder has a larger inclination angle with respect to the axis than the stirring member arranged in the water evaporation zone on the upstream side. The modified coal manufacturing equipment described in.
　前記水分蒸発ゾーンに配置される前記撹拌部材の前記軸線に対する傾斜角が０である、請求項５に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to claim 5, wherein the inclination angle of the stirring member arranged in the water evaporation zone with respect to the axis is 0.
　前記撹拌部材は、前記軸線方向について、前記水分蒸発ゾーンおよび前記熱分解ゾーンからなる加熱領域の９０％を超える範囲に配置される、請求項５または請求項６に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to claim 5 or 6, wherein the stirring member is arranged in a range exceeding 90% of a heating region including the water evaporation zone and the thermal decomposition zone in the axial direction. ..
　前記撹拌部材と前記内筒の内周面との間に隙間が形成されている、請求項４から請求項７のいずれか１項に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to any one of claims 4 to 7, wherein a gap is formed between the stirring member and the inner peripheral surface of the inner cylinder.
　前記隙間の大きさは、前記内筒の径方向における前記撹拌部材の寸法の１０％～２５％である、請求項８に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to claim 8, wherein the size of the gap is 10% to 25% of the dimension of the stirring member in the radial direction of the inner cylinder.
　前記撹拌部材は、前記内筒の径方向に対して傾斜する折り曲げ部を有する、請求項４から請求項８のいずれか１項に記載の改質石炭の製造設備。 The modified coal manufacturing equipment according to any one of claims 4 to 8, wherein the stirring member has a bent portion that is inclined with respect to the radial direction of the inner cylinder.
　前記折り曲げ部は、前記撹拌部材の前記軸線側で前記内筒の内周面を基準にした前記撹拌部材の高さの３０％以上～７０％以下の範囲に形成され、
　前記折り曲げ部の前記内筒の径方向に対する傾斜角は１０°以上４５°以下である、請求項１０に記載の改質石炭の製造設備。 The bent portion is formed on the axis side of the stirring member in a range of 30% or more to 70% or less of the height of the stirring member with respect to the inner peripheral surface of the inner cylinder.
The modified coal manufacturing equipment according to claim 10, wherein the inclination angle of the bent portion with respect to the radial direction of the inner cylinder is 10 ° or more and 45 ° or less.
　軸線の回りに回転する内筒と、前記内筒を、前記内筒の径方向の外側から覆う加熱室と、前記内筒に、前記軸線方向に複数配置され、前記内筒を前記径方向に貫通して前記加熱室内に開口する排気管と、を有する乾留装置を用いて、前記内筒において前記軸線方向に沿った上流側に位置する端部から石炭を供給し、前記軸線方向に沿った下流側に位置する端部から改質石炭を排出する改質石炭の製造方法であって、
　前記加熱室内に酸素含有ガスを供給して前記加熱室内の温度を制御する温度制御工程と、
　前記加熱室内のガスを排出するガス排出工程と、を含み、
　前記ガス排出工程では、前記加熱室において前記上流側に位置する端部からのみガスを排出する、改質石炭の製造方法。 A plurality of inner cylinders that rotate around an axis, a heating chamber that covers the inner cylinders from the outside in the radial direction of the inner cylinders, and a plurality of the inner cylinders are arranged in the inner cylinders in the axial direction, and the inner cylinders are arranged in the radial direction. Using a carbonization device having an exhaust pipe that penetrates and opens into the heating chamber, coal is supplied from an end located on the upstream side of the inner cylinder along the axial direction, and coal is supplied along the axial direction. It is a method for producing reformed coal that discharges reformed coal from the end located on the downstream side.
A temperature control step of supplying an oxygen-containing gas to the heating chamber to control the temperature in the heating chamber, and
Including a gas discharge step of discharging gas in the heating chamber.
In the gas discharge step, a method for producing reformed coal, in which gas is discharged only from an end located on the upstream side in the heating chamber.
　前記温度制御工程は、前記加熱室内の温度を６００℃以上となるように制御する、請求項１２に記載の改質石炭の製造方法。 The method for producing reformed coal according to claim 12, wherein the temperature control step controls the temperature in the heating chamber to be 600 ° C. or higher.
　前記温度制御工程は、前記加熱室内を前記軸線方向に複数に区画してなる制御ゾーンごとに温度を制御し、
　前記ガス排出工程は、複数の前記制御ゾーンのうち、最も前記上流側の制御ゾーンからガスを排出する、請求項１２または請求項１３に記載の改質石炭の製造方法。 In the temperature control step, the temperature is controlled for each control zone formed by dividing the heating chamber into a plurality of parts in the axial direction.
The method for producing reformed coal according to claim 12 or 13, wherein the gas discharge step discharges gas from the most upstream control zone among the plurality of control zones.
　前記内筒の内周面から前記軸線に向かって突出する撹拌部材を用いて前記石炭を撹拌する、請求項１２から請求項１４のいずれか１項に記載の改質石炭の製造方法。 The method for producing modified coal according to any one of claims 12 to 14, wherein the coal is agitated using a stirring member protruding from the inner peripheral surface of the inner cylinder toward the axis.
　少なくとも前記内筒の内部で前記下流側の熱分解ゾーンに配置される前記撹拌部材が前記軸線に対する傾斜角を有し、前記石炭を前記上流側に押し戻すように撹拌する、前記請求項１５に記載の改質石炭の製造方法。 13. How to make reformed coal.
　前記撹拌部材と前記内筒の内周面との間に隙間が形成され、前記撹拌部材によって撹拌された石炭を前記隙間から落下させる、請求項１５または請求項１６に記載の改質石炭の製造方法。 The production of the modified coal according to claim 15 or 16, wherein a gap is formed between the stirring member and the inner peripheral surface of the inner cylinder, and the coal stirred by the stirring member is dropped from the gap. Method.
　前記撹拌部材は前記内筒の径方向に対して傾斜する折り曲げ部を有し、前記撹拌部材によって撹拌された石炭を前記折り曲げ部から落下させる、請求項１５から請求項１７のいずれか１項に記載の改質石炭の製造方法。 The stirring member has a bent portion inclined in the radial direction of the inner cylinder, and the coal stirred by the stirring member is dropped from the bent portion, according to any one of claims 15 to 17. The method for producing reformed coal according to the description.