JPH057795A - Coal grade discrimination using spiral discriminator - Google Patents
Coal grade discrimination using spiral discriminatorInfo
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- JPH057795A JPH057795A JP16465391A JP16465391A JPH057795A JP H057795 A JPH057795 A JP H057795A JP 16465391 A JP16465391 A JP 16465391A JP 16465391 A JP16465391 A JP 16465391A JP H057795 A JPH057795 A JP H057795A
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Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明はスパイラル選鉱機を用い
た石炭の選別方法に関し、詳しくは粒径２mm以下の高灰
分の微粉炭をスパイラル選鉱機で処理して効率よく選別
する方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for sorting coal using a spiral beneficiation machine, and more particularly to a method for efficiently treating pulverized coal having a high ash content of 2 mm or less with a spiral beneficiation machine.
【０００２】[0002]
【従来の技術及び発明が解決しようとする課題】スパイ
ラル選鉱機は、設置面積の割に処理能力が高く、操業コ
ストも低く抑えられることから、微粉炭の選別に盛んに
実用化されている。しかしその一方で、選別精度がシャ
ープでなく、特に高灰分の石炭が供給された場合には、
紛れ込みにより精炭品位が大幅に悪化してしまう問題が
あった。すなわち、低灰分の精炭を収率を下げることな
く回収するためには、高比重分の紛れ込みを抑えると同
時にシャープな分離を行い、低比重分がボタ側に逃げる
のを制御することが重要であるが、スパイラル選鉱機に
供給するスラリー流量を増すと高比重分の紛れ込みが激
しくなり、スラリー濃度を増すと分離のシャープさが損
なわれてしまう。2. Description of the Related Art Spiral beneficiation machines are widely used for the selection of pulverized coal because they have a high processing capacity for their installation area and a low operating cost. However, on the other hand, the sorting accuracy is not sharp, especially when high ash coal is supplied,
There was a problem that the quality of clean coal would be greatly deteriorated due to the inclusion. In other words, in order to recover clean coal with low ash content without lowering the yield, it is possible to suppress the mixing of the high specific gravity and at the same time perform sharp separation to control the escape of the low specific gravity to the button side. It is important to note that increasing the flow rate of the slurry supplied to the spiral concentrator increases the mixing of the high specific gravity, and increasing the slurry concentration impairs the sharpness of separation.
【０００３】そのため、選別精度を向上させ、鉱物質の
紛れ込みを極力抑えることにより、原炭の灰分に関係な
く低灰分の精炭を安定して生産することのできるプロセ
スが求められている。Therefore, there is a demand for a process capable of stably producing clean ash having a low ash content regardless of the ash content of raw coal by improving the sorting accuracy and suppressing the mixture of mineral substances as much as possible.
【０００４】一方、上述のスパイラル選鉱機は、通常、
一段の処理で用いられるが、中間産物から精炭を回収す
るため、これをもう一度スパイラル選鉱することは一般
的に知られている。またクロマイト，ルチル，ジルコ
ン，イルメナイト等の重鉱物を回収する際に、精鉱を二
段処理する方法が提唱されている（Ritchie, I.C., and
Glen, J., 1983 "Testwork with FGL and CC Spirals o
n Heavy Mineral Sands"Vickers Fine Minerals Engine
ering, Internal Report No.61) 。On the other hand, the above spiral beneficiation machine is usually
It is used in a one-step process, but it is generally known that spiral coal processing is performed once again to recover clean coal from an intermediate product. In addition, a method of treating the concentrate in two stages has been proposed when recovering heavy minerals such as chromite, rutile, zircon, and ilmenite (Ritchie, IC, and
Glen, J., 1983 "Testwork with FGL and CC Spirals o
n Heavy Mineral Sands "Vickers Fine Minerals Engine
ering, Internal Report No. 61).
【０００５】しかしながら、スパイラル選鉱機を複数段
用いて選鉱処理を行っても、各段のスラリー濃度，スラ
リー流量を同一として行う通常の多段処理では、精炭品
位の向上には寄与するが、スパイラルの設置基数が多く
なるのが問題であった。However, even if a plurality of stages of the spiral beneficiation machine are used for the beneficiation treatment, the ordinary multi-stage treatment in which the slurry concentration and the slurry flow rate at each stage are the same contributes to the improvement of clean coal quality, but the spiral It was a problem that the number of installed bases increased.
【０００６】そこで本発明者は、上記従来技術の問題点
を解消し、簡単な装置構成で選別精度を向上することが
でき、高灰分の石炭が供給された場合でも、低灰分の精
炭を安定して生産できる石炭の選別方法を開発すべく鋭
意研究を重ねた。その結果、スパイラル選鉱機の二段処
理において、供給する原料炭のスラリー流量及びスラリ
ー濃度を制御することにより、上記目的を達成できるこ
とを見出した。本発明はかかる知見に基づいて完成され
たものである。Therefore, the inventor of the present invention can solve the above-mentioned problems of the prior art and improve the sorting accuracy with a simple apparatus configuration. Even when high ash content coal is supplied, low ash content clean coal can be obtained. We have conducted intensive research to develop a method for selecting coal that can be stably produced. As a result, it has been found that the above object can be achieved by controlling the slurry flow rate and slurry concentration of the feed coal to be supplied in the two-stage treatment of the spiral beneficiation machine. The present invention has been completed based on such findings.
【０００７】[0007]
【課題を解決するための手段】すなわち、本発明は、粒
径２mm以下の高灰分の微粉炭をスパイラル選鉱機で処理
して選別するにあたり、スパイラル選鉱処理を二段で行
い、その１段目におけるスパイラル単位長さあたりのス
ラリー流量を１５〜２５トン／時・ｍ，スラリー濃度を
２０〜５０重量％に、２段目におけるスパイラル単位長
さあたりのスラリー流量を２０〜３０トン／時・ｍ，ス
ラリー濃度を５〜３０重量％にするとともに、１段目の
スラリー流量を２段目のスラリー流量より少なくするこ
とを特徴とするスパイラル選鉱機を用いた石炭の選別方
法を提供するものである。[Means for Solving the Problems] That is, according to the present invention, when a fine ash coal with a high ash content having a particle diameter of 2 mm or less is processed and sorted by a spiral beneficiation machine, a spiral beneficiation treatment is performed in two stages, and the first stage thereof. The slurry flow rate per spiral unit length is 15 to 25 tons / hour · m, the slurry concentration is 20 to 50% by weight, and the slurry flow rate per spiral unit length in the second stage is 20 to 30 tons / hour · m. And a slurry concentration of 5 to 30% by weight and a slurry flow rate of the first stage lower than the slurry flow rate of the second stage. .
【０００８】本発明の対象となる石炭は、通常の炭鉱か
ら採掘された原炭である。この原炭には、一般に炭質分
以外に土砂をはじめとする鉱物質（ボタ）が含まれてい
るが、このようなボタが多量に含まれていると、分離除
去するのが困難である。本発明は、比重2.０以上の高比
重物が２０重量％以上含まれ、灰分の高い石炭に対して
特に有効である。The coal that is the subject of the present invention is raw coal mined from ordinary coal mines. Generally, this raw coal contains mineral substances (bottoms) such as earth and sand in addition to the carbonaceous matter, but if a large amount of such botts is contained, it is difficult to separate and remove them. INDUSTRIAL APPLICABILITY The present invention contains 20% by weight or more of a high specific gravity material having a specific gravity of 2.0 or more and is particularly effective for coal having a high ash content.
【０００９】図１は本発明の選別方法を示す工程図であ
る。まず高灰分の原炭は、適当な粉砕装置で粒径２mm以
下の微粉炭に粉砕され、低濃度の水スラリーとしてサイ
クロン１に供給される。サイクロン１では、次の第１ス
パイラル選鉱機２における選鉱処理に適したスラリー濃
度に調節される。すなわち、サイクロン１に供給する水
スラリーの流入圧力を調整することにより、過剰の水を
サイクロン上部から系外に排出し、適度なスラリー濃度
として次の第１スパイラル選鉱機２に原料を供給するこ
とができる。FIG. 1 is a process diagram showing the selection method of the present invention. First, raw coal with a high ash content is pulverized by a suitable pulverizing device into pulverized coal having a particle size of 2 mm or less, and is supplied to the cyclone 1 as a low-concentration water slurry. In the cyclone 1, the slurry concentration is adjusted to be suitable for the beneficiation process in the next first spiral beneficiation machine 2. That is, by adjusting the inflow pressure of the water slurry supplied to the cyclone 1, the excess water is discharged from the upper part of the cyclone to the outside of the system, and the raw material is supplied to the next first spiral beneficiation machine 2 as an appropriate slurry concentration. You can
【００１０】ここで、スパイラル選鉱機は、図２に示す
ように、螺旋状の流路１０にスラリー状の原料混合物を
流下させ、そのときの遠心力により外側に低比重の石炭
を濃縮し、内側に灰分の高い高比重の粒子を濃縮して分
離するように形成されている。螺旋状の流路１０の途中
には、流路の幅方向を仕切る分離板（スプリッター）１
１，１２が設けられており、外側の精炭Ｃと、中間部の
中間産物Ｍと、内側のボタＲとの３成分に分離される。
なお、本発明においては、スパイラル選鉱機の形式は特
に限定されるものではなく、各種形式のスパイラル選鉱
機を用いることが可能である。Here, as shown in FIG. 2, the spiral beneficiation machine causes a slurry-like raw material mixture to flow down in a spiral flow path 10 and concentrates coal having a low specific gravity to the outside by centrifugal force at that time. It is formed to concentrate and separate particles having a high specific gravity and a high ash content inside. A separation plate (splitter) 1 for partitioning the width direction of the flow path 1 is provided in the middle of the spiral flow path 10.
1, 12 are provided, and are separated into three components, an outer clean coal C, an intermediate intermediate product M, and an inner button R.
In the present invention, the type of spiral beneficiation machine is not particularly limited, and various types of spiral beneficiation machine can be used.
【００１１】このスパイラル選鉱機におけるスラリー流
量は、スパイラル選鉱機の形式により異なるが、ここで
は、単位長さあたりの流量で規定する。単位長さあたり
の流量とは、スパイラル１巻へのスラリー供給量を、ス
パイラル下端のスプリッター直前の半径（スラリーが流
れる部分のみ）で割った値と定義する。単位はトン／時
・ｍで表わす。The slurry flow rate in this spiral beneficiation machine differs depending on the type of the spiral beneficiation machine, but here it is defined by the flow rate per unit length. The flow rate per unit length is defined as a value obtained by dividing the amount of slurry supplied to one spiral by the radius of the lower end of the spiral immediately before the splitter (only the portion where the slurry flows). The unit is ton / hour · m.
【００１２】前記第１スパイラル選鉱機２にスラリー流
量は、単位長さあたり１５〜２５トン／時・ｍ、好まし
くは１５〜２０トン／時・ｍである。このスラリー流量
は、高比重物の紛れ込みに大きく影響するので、正常な
流れを保てる範囲でできるだけ低い方が好ましい。スラ
リー流量が１５トン／時・ｍ未満だと、スラリー層の厚
さが薄くなりすぎて流れが不安定になる。The flow rate of the slurry in the first spiral beveling machine 2 is 15 to 25 tons / hour · m, preferably 15 to 20 tons / hour · m per unit length. Since the flow rate of the slurry has a great influence on the mixing of the high specific gravity material, it is preferable that the flow rate of the slurry is as low as possible within a range in which a normal flow can be maintained. When the slurry flow rate is less than 15 tons / hour · m, the thickness of the slurry layer becomes too thin and the flow becomes unstable.
【００１３】また、スラリー濃度は、２０〜５０重量
％、好ましくは４０〜５０重量％の範囲とする。スラリ
ー濃度は５０重量％を超えると、スラリーの粘度が増し
てスパイラル表面を正常に流れなくなり、また２０重量
％未満では水が多すぎて効率が低下する。The slurry concentration is in the range of 20 to 50% by weight, preferably 40 to 50% by weight. If the slurry concentration exceeds 50% by weight, the viscosity of the slurry will increase and the slurry will not flow normally on the spiral surface, and if it is less than 20% by weight, the amount of water will be too much and the efficiency will decrease.
【００１４】第１スパイラル選鉱機２で選別された精炭
Ｃは、一旦タンク３に貯留される。また、ボタＲは廃石
として廃棄され、中間産物Ｍは品位により精炭として回
収するか除去するかが決定される。タンク３では、次工
程の第２スパイラル選鉱機４における選鉱処理に適した
スラリー濃度に調節される。すなわち、第２スパイラル
選鉱機４の運転条件であるスラリー流量２０〜３０トン
／時・ｍ、好ましくは２５〜３０トン／時・ｍと、スラ
リー濃度５〜３０重量％、好ましくは５〜２０重量％に
調整するために、通常は水が注入される。The clean coal C selected by the first spiral beveling machine 2 is temporarily stored in the tank 3. Further, the button R is discarded as a waste stone, and the intermediate product M is determined to be recovered or removed as clean coal depending on the quality. In the tank 3, the slurry concentration is adjusted to be suitable for the beneficiation process in the second spiral beneficiation machine 4 in the next step. That is, a slurry flow rate of 20 to 30 tons / hour · m, preferably 25 to 30 tons / hour · m, which is the operating condition of the second spiral beveling machine 4, and a slurry concentration of 5 to 30% by weight, preferably 5 to 20% by weight. Water is usually injected to adjust to%.
【００１５】第２スパイラル選鉱機４では、原炭処理量
を上げるためにスラリー流量を１段目より大きくすると
ともに、シャープな分離を行うためにスラリー濃度を極
力下げることが必要である。したがって、スラリー流量
及びスラリー濃度の上限値は第１スパイラル選鉱機２の
運転条件により定まる。またスラリー流量が低すぎる
と、前述のようにスラリー層の厚さが薄くなりすぎて流
れが不安定になり、スラリー濃度が低すぎると効率が低
下する。このようにして第２スパイラル選鉱機４で選別
することにより、低灰分の精炭を高収率で得ることがで
きる。In the second spiral beneficiation machine 4, it is necessary to increase the slurry flow rate from the first stage in order to increase the amount of raw coal to be processed, and to reduce the slurry concentration as much as possible in order to perform sharp separation. Therefore, the upper limits of the slurry flow rate and the slurry concentration are determined by the operating conditions of the first spiral beneficiation machine 2. Further, if the slurry flow rate is too low, the thickness of the slurry layer becomes too thin as described above to make the flow unstable, and if the slurry concentration is too low, the efficiency will decrease. In this way, by sorting with the second spiral beneficiation machine 4, low ash content clean coal can be obtained in high yield.
【００１６】すなわち、本発明は、スパイラル選鉱機を
二段とし、１段目におけるスラリー流量を小さくするこ
とで紛れ込みの原因となる高比重物を効果的に除去し、
２段目ではスラリー濃度を下げることでシャープな分離
を行うようにしたものである。このように、１段目と２
段目とのスパイラル選鉱機の選別目的を分けたことによ
り、従来法よりも選別効率を大幅に向上させ、より低灰
分の精炭を得ることができる。That is, according to the present invention, the spiral beneficiation machine is provided in two stages, and the slurry flow rate in the first stage is reduced to effectively remove the high specific gravity substance which causes the mixing,
In the second stage, the slurry concentration is reduced to achieve sharp separation. In this way,
By separating the sorting purpose of the spiral beneficiation machine from the stage, the sorting efficiency can be greatly improved as compared with the conventional method, and clean coal with a lower ash content can be obtained.
【００１７】なお、第１，第２スパイラル選鉱機は、同
一のものでも異なる形式のものを組み合わせてもよく、
１段目と２段目とを上下に設置すれば、タンク３を省略
することもできる。The first and second spiral beneficiation machines may be the same or different types may be combined,
The tank 3 can be omitted by installing the first stage and the second stage up and down.
【００１８】[0018]
【実施例】次に、本発明を実施例及び比較例によりさら
に詳しく説明する。
実施例１
（１）実験用試料の調製
エベネザ炭（豪州クイーンズランド州産）をロータービ
ーターミルで2.０mm以下に粉砕した後、0.１２５mm以下
の微粉をふるい分けて除去した。ＪＩＳ−Ｍ−８８１２
に従い分析した結果、灰分は２0.７重量％（無水ベー
ス）であった。なお、以後灰分はすべて無水ベースで表
記する。また、ＪＩＳ−Ｍ−８８０１に従い浮沈試験を
行った結果、比重構成は第１表に示す通りであった。EXAMPLES Next, the present invention will be described in more detail with reference to Examples and Comparative Examples. Example 1 (1) Preparation of Experimental Sample Eveneza charcoal (made in Queensland, Australia) was crushed to 2.0 mm or less by a rotor beater mill, and then fine powder of 0.125 mm or less was removed by sieving. JIS-M-8812
The ash content was 20.7% by weight (anhydrous basis). In addition, hereinafter, all the ash content will be described on an anhydrous basis. In addition, as a result of a floating-sink test according to JIS-M-8801, the specific gravity constitution was as shown in Table 1.
【表１】 [Table 1]
【００１９】このエベネザ炭１４3.４kgに市販の砂（灰
分９6.４重量％）6.６kgを混合して、灰分２4.０重量％
の実験用原炭（低灰分原灰）を調製した。比重構成を図
３に示す。143.4 kg of this Ebeneza charcoal was mixed with 6.6 kg of commercially available sand (ash content: 96.4% by weight) to obtain an ash content of 24.0% by weight.
An experimental raw coal (low ash raw ash) was prepared. The specific gravity structure is shown in FIG.
【００２０】（２）選鉱処理
実験に用いたスパイラル選鉱機は MINERAL DEPOSIT社製
ＬＤ２型である。１段目では（１）で得られた実験用原
炭１５０kgに水２００kgを加えてスラリー濃度４３重量
％とし、スラリー流量4.０トン／時（単位長さあたりの
流量１8.２トン／時・ｍ）でスパイラル選別を行った。
次に得られた１段目精炭 1２1.２kgと中間産物２0.６kg
に水６４６kgを加え、スラリー濃度１８重量％とし、ス
ラリー流量6.０トン／時（単位長さあたりの流量２7.３
トン／時・ｍ）で２段目の選別を行った。その結果、２
段の選鉱処理で得られた精炭の灰分は１3.７重量％，収
率は７9.１重量％であった。得られた精炭の比重構成を
図４に示す。(2) The spiral beneficiation machine used for the beneficiation treatment experiment is LD2 type manufactured by MINERAL DEPOSIT. In the first step, 200 kg of water was added to 150 kg of the experimental raw coal obtained in (1) to make the slurry concentration 43% by weight, and the slurry flow rate was 4.0 tons / hour (flow rate per unit length was 18.2 tons / hour). • Spiral selection was performed in m).
Next obtained 1st stage clean coal 121.2kg and intermediate product 20.6kg
Add 646 kg of water to make the slurry concentration 18% by weight, slurry flow rate 6.0 tons / hour (flow rate per unit length 27.3
The second stage of sorting was performed at ton / hour / m). As a result, 2
The ash content of the clean coal obtained by the beneficiation treatment was 13.7% by weight, and the yield was 79.1% by weight. The specific gravity composition of the obtained clean coal is shown in FIG.
【００２１】実施例２
実施例１と同様の方法で粉砕、ふるい分けされたエベネ
ザ炭（灰分２0.７重量％）１２3.８kgに市販の砂（灰分
９6.４重量％）２6.２ｋｇを混合して灰分３3.９重量％
の実験用原炭（中灰分原炭）を調製した。比重構成を図
５に示す。この原炭を、実施例１と同様の条件で２段階
のスパイラル選別を行った。なお２段目には、１段目で
得られた精炭１００kgと中間産物１7.４kgに水５３５kg
を加えて供給した。得られた精炭の灰分は１4.０重量
％，収率は６8.３重量％であった。得られた精炭の比重
構成を図６に示す。Example 2 123.8 kg of Ebeneza charcoal (ash content: 20.7% by weight) pulverized and sieved in the same manner as in Example 1 was mixed with 26.2 kg of commercially available sand (ash content: 96.4% by weight). Ash content 33.9% by weight
An experimental raw coal (medium ash raw coal) was prepared. The specific gravity structure is shown in FIG. This raw coal was subjected to two-step spiral screening under the same conditions as in Example 1. In the second stage, 100 kg of clean coal obtained in the first stage, 17.4 kg of intermediate product and 535 kg of water.
Was added and supplied. The ash content of the obtained clean coal was 14.0% by weight, and the yield was 68.3% by weight. The specific gravity structure of the obtained clean coal is shown in FIG.
【００２２】実施例３
実施例１と同様の方法で粉砕，ふるい分けされたエベネ
ザ炭（灰分２0.７重量％）９8.６kgに市販の砂（灰分９
6.４重量％）５1.４kgを混合して灰分４6.７重量％の実
験用原炭（中灰分原炭）を調製した。比重構成を図７に
示す。この原炭を、実施例１と同様の条件で２段階のス
パイラル選別を行った。なお２段目には、１段目で得ら
れた精炭７7.９kgと中間産物１4.４kgに水４２０kgを加
えて供給した。得られた精炭の灰分は１4.４重量％，収
率は５4.７重量％であった。得られた精炭の比重構成を
図８に示す。Example 3 Eveneza charcoal (ash content 20.7% by weight) pulverized and sieved in the same manner as in Example 1 was added to 98.6 kg of commercially available sand (ash content 9
(6.4 wt%) 51.4 kg was mixed to prepare an experimental raw coal (medium ash raw coal) having an ash content of 46.7 wt%. The specific gravity structure is shown in FIG. This raw coal was subjected to two-step spiral screening under the same conditions as in Example 1. In addition, in the second stage, the clean coal 77.9 kg obtained in the first stage and the intermediate product 14.4 kg were added with 420 kg of water and supplied. The ash content of the obtained clean coal was 14.4% by weight, and the yield was 54.7% by weight. The specific gravity structure of the obtained clean coal is shown in FIG.
【００２３】比較例１
実施例１に用いた実験用原炭（低灰分原炭）１５０kgに
水７２２kgを加えてスラリー濃度１7.２重量％とし、ス
ラリー流量5.０トン／時（単位長さあたりの流量２2.７
トン／時・ｍ）でスパイラル選別を行った。２基のスパ
イラル選鉱機に同時にスラリーを供給し、実施例１と供
給量が同じになるようにした。得られた精炭の灰分は１
5.８重量％，収率は７9.６重量％であった。精炭の比重
構成を図９に示す。Comparative Example 1 150 kg of the experimental raw coal (low ash raw coal) used in Example 1 was mixed with 722 kg of water to obtain a slurry concentration of 17.2% by weight, and the slurry flow rate was 5.0 tons / hour (unit length: Flow rate per 22.7
Spiral selection was performed at ton / hour / m). The slurry was simultaneously supplied to the two spiral beneficiation machines so that the supply amount was the same as in Example 1. The ash content of the obtained clean coal is 1
It was 5.8% by weight and the yield was 79.6% by weight. The specific gravity composition of clean coal is shown in FIG.
【００２４】比較例２
実施例２に用いた実験用原炭（中灰分原炭）を、比較例
１と同様の方法でスパイラル選別を行った。得られた精
炭の灰分は１7.０重量％，収率は６9.７重量％であっ
た。精炭の比重構成を図１０に示す。Comparative Example 2 The experimental raw coal (medium ash raw coal) used in Example 2 was subjected to spiral screening in the same manner as in Comparative Example 1. The ash content of the obtained clean coal was 17.0% by weight, and the yield was 69.7% by weight. The specific gravity structure of clean coal is shown in FIG.
【００２５】比較例３
実施例３に用いた実験用原炭（高灰分原炭）を、比較例
１と同様の方法でスパイラル選別を行った。得られた精
炭の灰分は１9.２重量％，収率は５7.０重量％であっ
た。精炭の比重構成を図１１に示す。Comparative Example 3 The experimental raw coal (high ash raw coal) used in Example 3 was subjected to spiral screening in the same manner as in Comparative Example 1. The ash content of the obtained clean coal was 19.2% by weight, and the yield was 57.0% by weight. The specific gravity structure of clean coal is shown in FIG.
【００２６】以上の結果から、各比較例に示す１段処理
では、特に高灰分の原炭において比重2.０以上の高比重
分が除去されずに残ってしまい、精炭品位を悪化させて
いることがわかる。一方、各実施例では比重2.０以上の
高比重分が殆ど分離除去されていることが分かる。From the above results, in the one-step treatment shown in each comparative example, particularly in the high ash content raw coal, the high specific gravity of 2.0 or more remains without being removed, which deteriorates the quality of clean coal. You can see that On the other hand, in each of the examples, it can be seen that the high specific gravity components having a specific gravity of 2.0 or more are almost separated and removed.
【００２７】比較例４
実施例３に用いた実験用原炭（高灰分原炭）１５０kgに
水３０３kgを加えてスラリー濃度を３3.１重量％とし、
スラリー流量5.２トン／時（単位長さあたりの流量２3.
６トン／時・ｍ）で１段目のスパイラル選別を行った。
次に得られた１段目の精炭１１8.５kgと中間産物１4.１
kgに水２６８kgを加え、スラリー濃度３3.１重量％と
し、スラリー流量5.２トン／時（単位長さあたりの流量
２3.６トン／時・ｍ）で２段目の選別を行った。なお、
１段目のスラリー供給量は実施例１と同じである。得ら
れた２段目精炭の灰分は１6.９重量％，収率は５6.３重
量％であった。精炭の比重構成を図１２に示す。Comparative Example 4 To 150 kg of the experimental raw coal (high ash raw coal) used in Example 3, 303 kg of water was added to make a slurry concentration 33.1% by weight,
Slurry flow rate 5.2 tons / hour (flow rate per unit length 23.
The first stage of spiral sorting was performed at 6 tons / hour / m).
Next, the obtained first-stage clean coal 118.5 kg and intermediate product 14.1
268 kg of water was added to kg to make the slurry concentration 33.1% by weight, and the second stage selection was performed at a slurry flow rate of 5.2 tons / hour (flow rate per unit length of 23.6 tons / hour · m). In addition,
The amount of slurry supplied in the first stage is the same as in Example 1. The ash content of the obtained second-stage clean coal was 16.9% by weight, and the yield was 56.3% by weight. The specific gravity composition of clean coal is shown in FIG.
【００２８】実施例１〜３及び比較例１〜４の結果を第
２表にまとめて示す。The results of Examples 1 to 3 and Comparative Examples 1 to 4 are summarized in Table 2.
【表２】 [Table 2]
【００２９】[0029]
【発明の効果】以上説明したように、本発明によれば、
選別精度を大幅に向上させることができるので、通常の
２段処理に比べて少ないスパイラル選鉱機の設置基数
で、収率を下げることなく、より低灰分の精炭を生産す
ることができる。As described above, according to the present invention,
Since the sorting accuracy can be significantly improved, it is possible to produce a clean coal with a lower ash content without lowering the yield with a smaller number of spiral beneficiation machines installed as compared with the normal two-stage treatment.
【図１】 本発明の処理工程の概略図である。FIG. 1 is a schematic view of the processing steps of the present invention.
【図２】 スパイラル選鉱機の要部を示す斜視図であ
る。FIG. 2 is a perspective view showing a main part of a spiral beneficiation machine.
【図３】 実施例１における実験用原炭の比重構成を示
す図である。FIG. 3 is a diagram showing a specific gravity structure of an experimental raw coal in Example 1.
【図４】 実施例１で得られた精炭の比重構成を示す図
である。FIG. 4 is a diagram showing a specific gravity structure of the clean coal obtained in Example 1.
【図５】 実施例２における実験用原炭の比重構成を示
す図である。FIG. 5 is a diagram showing a specific gravity structure of an experimental raw coal in Example 2.
【図６】 実施例２で得られた精炭の比重構成を示す図
である。FIG. 6 is a view showing a specific gravity structure of clean coal obtained in Example 2.
【図７】 実施例３における実験用原炭の比重構成を示
す図である。FIG. 7 is a diagram showing a specific gravity structure of an experimental raw coal in Example 3.
【図８】 実施例３で得られた精炭の比重構成を示す図
である。FIG. 8 is a diagram showing a specific gravity structure of clean coal obtained in Example 3.
【図９】 比較例１で得られた精炭の比重構成を示す図
である。FIG. 9 is a view showing a specific gravity structure of clean coal obtained in Comparative Example 1.
【図１０】 比較例２で得られた精炭の比重構成を示す
図である。FIG. 10 is a diagram showing a specific gravity structure of clean coal obtained in Comparative Example 2.
【図１１】 比較例３で得られた精炭の比重構成を示す
図である。FIG. 11 is a diagram showing a specific gravity structure of clean coal obtained in Comparative Example 3.
【図１２】 比較例４で得られた精炭の比重構成を示す
図である。FIG. 12 is a view showing a specific gravity structure of clean coal obtained in Comparative Example 4.
１：サイクロン ２：第１スパイラル選鉱機 ３：タンク ４：第２スパイラル選鉱機 １０：螺旋状の流路 １１，１２：分離板（スプリッター） Ｃ：精炭 Ｍ：中間産物 Ｒ：ボタ 1: Cyclone 2: 1st spiral beneficiation machine 3: Tank 4: Second spiral beneficiation machine 10: spiral flow path 11, 12: Separation plate (splitter) C: clean coal M: Intermediate product R: Bota
Claims (2)
ラル選鉱機で処理して選別するにあたり、スパイラル選
鉱処理を二段で行い、その１段目におけるスパイラル単
位長さあたりのスラリー流量を１５〜２５トン／時・
ｍ，スラリー濃度を２０〜５０重量％に、２段目におけ
るスパイラル単位長さあたりのスラリー流量を２０〜３
０トン／時・ｍ，スラリー濃度を５〜３０重量％にする
とともに、１段目のスラリー流量を２段目のスラリー流
量より少なくすることを特徴とするスパイラル選鉱機を
用いた石炭の選別方法。1. When treating a high ash pulverized coal having a particle size of 2 mm or less with a spiral beneficiation machine for selection, a spiral beneficiation process is performed in two stages, and the slurry flow rate per spiral unit length in the first stage is 15-25 tons / hour
m, the slurry concentration is 20 to 50% by weight, and the slurry flow rate per spiral unit length in the second stage is 20 to 3
Coal sorting method using a spiral beneficiation machine, characterized in that the tonnage is 0 ton / hour · m, the slurry concentration is 5 to 30% by weight, and the first stage slurry flow rate is lower than the second stage slurry flow rate. .
ラリー濃度より低くすることを特徴とする請求項１記載
の石炭の選別方法。2. The method for selecting coal according to claim 1, wherein the second stage slurry concentration is lower than the first stage slurry concentration.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16465391A JPH057795A (en) | 1991-07-04 | 1991-07-04 | Coal grade discrimination using spiral discriminator |
| AU17235/92A AU638376B2 (en) | 1991-07-04 | 1992-05-29 | Coal preparation method for producing high quality clean coal with spiral separators |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16465391A JPH057795A (en) | 1991-07-04 | 1991-07-04 | Coal grade discrimination using spiral discriminator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH057795A true JPH057795A (en) | 1993-01-19 |
Family
ID=15797270
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16465391A Pending JPH057795A (en) | 1991-07-04 | 1991-07-04 | Coal grade discrimination using spiral discriminator |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPH057795A (en) |
| AU (1) | AU638376B2 (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5470691A (en) * | 1993-04-10 | 1995-11-28 | Taiyo Yuden, Co., Ltd. | Optical information medium |
| US5549952A (en) * | 1992-06-13 | 1996-08-27 | Sony Corporation | Optical information medium and method for printing on the surface of the medium |
| JP2008137003A (en) * | 2006-11-30 | 2008-06-19 | Palo Alto Research Center Inc | Method for treating particle in liquid and method for forming spiral separation device |
| JP2009274066A (en) * | 2008-05-13 | 2009-11-26 | Palo Alto Research Center Inc | Particle separation system |
| CN102410745A (en) * | 2011-10-31 | 2012-04-11 | 天津三泰晟驰科技股份有限公司 | Protecting sheath for high-temperature-resistant camera shooting device in heating furnace |
| US8276760B2 (en) | 2006-11-30 | 2012-10-02 | Palo Alto Research Center Incorporated | Serpentine structures for continuous flow particle separations |
| US9862624B2 (en) | 2007-11-07 | 2018-01-09 | Palo Alto Research Center Incorporated | Device and method for dynamic processing in water purification |
| US10052571B2 (en) | 2007-11-07 | 2018-08-21 | Palo Alto Research Center Incorporated | Fluidic device and method for separation of neutrally buoyant particles |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113769884B (en) * | 2021-08-27 | 2023-10-03 | 杨高灵 | Coal washing and dressing process |
-
1991
- 1991-07-04 JP JP16465391A patent/JPH057795A/en active Pending
-
1992
- 1992-05-29 AU AU17235/92A patent/AU638376B2/en not_active Ceased
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5549952A (en) * | 1992-06-13 | 1996-08-27 | Sony Corporation | Optical information medium and method for printing on the surface of the medium |
| US5470691A (en) * | 1993-04-10 | 1995-11-28 | Taiyo Yuden, Co., Ltd. | Optical information medium |
| JP2008137003A (en) * | 2006-11-30 | 2008-06-19 | Palo Alto Research Center Inc | Method for treating particle in liquid and method for forming spiral separation device |
| US8276760B2 (en) | 2006-11-30 | 2012-10-02 | Palo Alto Research Center Incorporated | Serpentine structures for continuous flow particle separations |
| US9486812B2 (en) | 2006-11-30 | 2016-11-08 | Palo Alto Research Center Incorporated | Fluidic structures for membraneless particle separation |
| US9862624B2 (en) | 2007-11-07 | 2018-01-09 | Palo Alto Research Center Incorporated | Device and method for dynamic processing in water purification |
| US10052571B2 (en) | 2007-11-07 | 2018-08-21 | Palo Alto Research Center Incorporated | Fluidic device and method for separation of neutrally buoyant particles |
| JP2009274066A (en) * | 2008-05-13 | 2009-11-26 | Palo Alto Research Center Inc | Particle separation system |
| CN102410745A (en) * | 2011-10-31 | 2012-04-11 | 天津三泰晟驰科技股份有限公司 | Protecting sheath for high-temperature-resistant camera shooting device in heating furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| AU1723592A (en) | 1993-01-07 |
| AU638376B2 (en) | 1993-06-24 |
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