JPS6258398B2 - - Google Patents
Info
- Publication number
- JPS6258398B2 JPS6258398B2 JP56024732A JP2473281A JPS6258398B2 JP S6258398 B2 JPS6258398 B2 JP S6258398B2 JP 56024732 A JP56024732 A JP 56024732A JP 2473281 A JP2473281 A JP 2473281A JP S6258398 B2 JPS6258398 B2 JP S6258398B2
- Authority
- JP
- Japan
- Prior art keywords
- coal
- ash
- pulverized coal
- lipophilic
- water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003245 coal Substances 0.000 claims description 142
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 65
- 239000002002 slurry Substances 0.000 claims description 51
- 239000007787 solid Substances 0.000 claims description 47
- 238000009835 boiling Methods 0.000 claims description 35
- 238000005469 granulation Methods 0.000 claims description 32
- 230000003179 granulation Effects 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 30
- 239000008187 granular material Substances 0.000 claims description 29
- 238000000034 method Methods 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 9
- 238000010298 pulverizing process Methods 0.000 claims description 5
- 229920003002 synthetic resin Polymers 0.000 claims description 5
- 239000000057 synthetic resin Substances 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 2
- 239000003921 oil Substances 0.000 description 44
- 239000003502 gasoline Substances 0.000 description 13
- 238000002156 mixing Methods 0.000 description 8
- 239000002245 particle Substances 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000011343 solid material Substances 0.000 description 3
- 239000011230 binding agent Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000004533 oil dispersion Substances 0.000 description 2
- 229920000915 polyvinyl chloride Polymers 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 239000004094 surface-active agent Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003250 coal slurry Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000005115 demineralization Methods 0.000 description 1
- 230000002328 demineralizing effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- GNVXPFBEZCSHQZ-UHFFFAOYSA-N iron(2+);sulfide Chemical compound [S-2].[Fe+2] GNVXPFBEZCSHQZ-UHFFFAOYSA-N 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000002562 thickening agent Substances 0.000 description 1
- 239000010409 thin film Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Description
【発明の詳細な説明】
産業上の利用分野
この発明は、脱灰炭の段階的製造方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application This invention relates to a method for the stepwise production of deashed coal.
従来の技術
天然に産出する石炭中には灰分が比較的多く含
まれているが、これらの灰分はシリカ（SiO2）、
硫化鉄（FeS）およびアルミナ（Al2O3）等を主成
分とするものであり、通常石炭中に７〜25％程度
の割合で含まれている。このような石炭中の灰分
をＸ線マイクロアナライザで観察すると、灰分は
５μｍ〜数十μｍの大きさの粒状で偏在している
ことが明らかである。このような灰分を石炭から
除去する方法としては、従来灰分を含む原炭を粉
砕し、得られた粉炭を水と混合して粉炭スラリー
をつくつたのち、このスラリーに結合剤として油
を添加して、粉炭と油をそのまま造粒し、ついで
造粒物と、灰分を含むスラリーとを分離する方法
がすでに知られている。灰分が除去せられた造粒
物はペレツト状の含油脱灰炭であり、これは燃料
として使用せられる。しかしながら、このような
従来の方法では、石炭より充分に灰分を除去する
ことができないという問題があつた。というの
は、石炭中の灰分を充分除去するためには、石炭
をこれに含まれる灰分と同程度の大きさに、すな
わち５μｍ〜数十μｍの大きさに非常に細かく粉
砕する必要があるが、石炭をあまり細かく粉砕す
ると、粉炭の表面積が増大し、結合剤としての油
を多く使用しなければならないし、また造粒時間
が非常に長くかかるといううらみがあり、このた
め石炭をあまり細かく粉砕することができず、結
局石炭から灰分を充分に除去することができない
という問題があつた。Conventional technology Naturally produced coal contains a relatively large amount of ash, but this ash contains silica (SiO 2 ),
It is mainly composed of iron sulfide (FeS) and alumina (Al 2 O 3 ), and is usually contained in coal at a ratio of about 7 to 25%. When the ash content in such coal is observed using an X-ray microanalyzer, it is clear that the ash content is unevenly distributed in the form of particles with a size of 5 μm to several tens of μm. The conventional method for removing ash from coal is to crush raw coal containing ash, mix the resulting powdered coal with water to create a powdered coal slurry, and then add oil as a binder to this slurry. A method is already known in which pulverized coal and oil are granulated as they are, and then the granulated material is separated from a slurry containing ash. The granulated material from which the ash content has been removed is pellet-shaped oil-impregnated deashed coal, which is used as fuel. However, such conventional methods have a problem in that ash cannot be removed more fully than from coal. This is because, in order to sufficiently remove the ash content in coal, it is necessary to grind the coal very finely to a size comparable to that of the ash contained in the coal, that is, to a size of 5 μm to several tens of μm. However, if the coal is pulverized too finely, the surface area of the pulverized coal will increase, more oil must be used as a binder, and the granulation time will be very long. However, there was a problem that the ash content could not be sufficiently removed from the coal.
発明の目的
この発明の目的は、上記の問題を解決し、石炭
から灰分を充分に除去することができて、灰分の
含有量が非常に少ない脱灰炭を製造することがで
きるとともに、対象とする燃焼装置によつて選択
的に使用し得るように高品位の脱灰炭から比較的
低品位の脱灰炭までを段階的に製造することがで
きる方法を提供しようとするにある。Purpose of the Invention The purpose of the present invention is to solve the above-mentioned problems, to be able to sufficiently remove ash from coal, to produce deashed coal with a very low ash content, and to The present invention aims to provide a method that can step-by-step produce from high-grade deashed coal to comparatively low-grade deashed coal so that it can be selectively used in a combustion device that uses deashed coal.
発明の構成
この発明は、上記の目的を達成するために、灰
分を含む石炭を粉砕して微粉炭をつくり、この灰
分を含む微粉炭の水スラリーに、すべての微粉炭
を造粒するには少ない所要量の液状低沸点油、お
よび造粒核となる合成樹脂製親油性粒状固形物を
混合して造粒する工程と、造粒物を水スラリー中
より取出して水で洗浄することにより、造粒物
と、未造粒微粉炭および灰分を含む水スラリーと
を分離する分離工程と、造粒物を加熱して、液状
低沸点油と水分とを蒸発せしめる工程と、低沸点
油を含まない造粒物を分解してペレツト状の脱灰
炭と親油性粒状固形物とに分離し、脱灰炭を得る
とともに、親油性粒状固形物を回収して上記造粒
工程に返送する工程と、ガス状低沸点油と水とを
含む蒸発ガスを凝縮したのち、液状低沸点油と水
とに分離し、液状低沸点油を上記造粒工程に返送
する工程とよりなる第１段階の脱灰操作を実施
し、つぎに、この第１段階の脱灰操作の分離工程
から取り出した未造粒微粉炭と灰分とを含む水ス
ラリーについて濃度を調整したのち微粉炭の造粒
を行なう第２段階以降の脱灰操作を上記第１段階
の脱灰操作と同様に親油性粒状固形物を用いて実
施して、灰分含有量の非常に少ない脱灰炭から比
較的灰分除去率の低い脱灰炭までを段階的に取得
することを特徴とする脱灰炭の段階的製造方法を
要旨としている。Composition of the Invention In order to achieve the above object, the present invention involves pulverizing coal containing ash to produce pulverized coal, and granulating all of the pulverized coal into a water slurry of the pulverized coal containing ash. By mixing and granulating a small amount of liquid low-boiling oil and a lipophilic granular solid made of synthetic resin that will serve as granulation nuclei, and by taking out the granules from the water slurry and washing them with water, a separation step of separating the granules from a water slurry containing ungranulated pulverized coal and ash; a step of heating the granules to evaporate liquid low-boiling oil and water; a step of decomposing the unused granules and separating them into pellet-like deashed coal and lipophilic granular solids to obtain deashed coal, and collecting the lipophilic granular solids and returning them to the granulation process; The first step of desorption consists of condensing the evaporated gas containing gaseous low-boiling oil and water, separating it into liquid low-boiling oil and water, and returning the liquid low-boiling oil to the granulation process. Ash operation is carried out, and then the concentration of the water slurry containing ungranulated pulverized coal and ash taken out from the separation step of the first stage deashing operation is adjusted, and then pulverized coal is granulated. The subsequent deashing operations are carried out using lipophilic granular solids in the same manner as the first stage deashing operation, and deashing with a relatively low ash removal rate is performed from deashing coal with a very low ash content. The gist of this paper is a step-by-step method for producing deashed coal, which is characterized by step-by-step acquisition of coal.
この発明の方法を、以下図面を参照しながらさ
らに詳しく説明する。 The method of the present invention will be explained in more detail below with reference to the drawings.
第１段階脱灰操作
(1) スラリー調製工程：灰分を含む天然の石炭
をたとえば湿式ボール・ミルにより粉砕し
て、粒径数百μｍから数十μｍの微粉炭をつ
くる。原炭中には通常７〜25重量％の灰分が
含まれているが、粉砕により灰分も細かく砕
かれる。つぎに、この灰分を含む微粉炭と水
とを混合して微粉炭の水スラリーをつくる。
場合によつては石炭を粒径数μｍのいわゆる
超微粉炭に粉砕することもある。石炭の粉砕
は水中で行なうのが好ましく、粉砕後はスラ
リーの濃度調整のためにさらに所要量の水を
添加する。 First stage deashing operation (1) Slurry preparation step: Natural coal containing ash is pulverized using, for example, a wet ball mill to produce pulverized coal with a particle size of several hundred μm to several tens of μm. Raw coal usually contains 7 to 25% by weight of ash, but the ash is also finely ground by pulverization. Next, this pulverized coal containing ash is mixed with water to create a pulverized coal-water slurry.
In some cases, coal may be pulverized into so-called ultra-fine coal with a particle size of several μm. The coal is preferably pulverized in water, and after pulverization, a required amount of water is added to adjust the concentration of the slurry.
(2) 造粒工程：つぎにこの微粉炭の水スラリー
に、すべての微粉炭を造粒するには少ない所
要量の液低沸点油、および造粒核となる親油
性粒状固形物を混合して造粒する。ここで、
低沸点油としては、蒸発潜熱が低く、かつ粘
性が低いものであつて、これは一般に知られ
ているように、初留温度30℃以上および留出
温度360℃で95％以上分留する軽質油よりな
るものである。低沸点油としては、具体的に
は灯油、軽油、ガソリン等を使用する。液状
低沸点油の使用量は、すべての微粉炭を造粒
するには少ない量であつてたとえば微粉炭に
対して約５〜10重量％である。また油の分散
が容易なるように界面活性剤を少量添加する
こともある。造粒核となる親油性粒状固形物
は、親油性を有していて、しかもあとの回収
が容易であるようなものであることが必要で
あり、また、比重は石炭の比重、すなわち
1.4に近似していることが望ましい。このよ
うな親油性粒状固形物としては、粒径約１mm
〜数mmの硬質ポリ塩化ビニル等の合成樹脂製
粒状物を使用する。親油性粒状固形物は微粉
炭に対して通常１：１の割合で混合するのが
好ましいが、親油性粒状固形物と微粉炭の総
量は水スラリー中において30重量％以下であ
り、この値を越えない範囲において微粉炭に
対する親油性粒状固形物の使用割合を増減し
ても勿論よい。 (2) Granulation process: Next, this water slurry of pulverized coal is mixed with liquid low-boiling oil, which is required in a small amount to granulate all of the pulverized coal, and lipophilic granular solids that will become granulation nuclei. and granulate. here,
Low boiling point oils have low latent heat of vaporization and low viscosity, and as is generally known, they are light oils that are fractionated by 95% or more at an initial distillation temperature of 30°C or higher and a distillation temperature of 360°C. It is made of oil. Specifically, kerosene, light oil, gasoline, etc. are used as the low boiling point oil. The amount of liquid low-boiling oil used is small enough to granulate all of the pulverized coal, for example, about 5 to 10% by weight based on the pulverized coal. A small amount of surfactant may also be added to facilitate oil dispersion. The lipophilic granular solids that serve as granulation nuclei must be lipophilic and easy to recover later, and the specific gravity must be the same as that of coal, i.e.
Ideally, it should be close to 1.4. Such lipophilic granular solids have a particle size of approximately 1 mm.
Use granules made of synthetic resin such as hard polyvinyl chloride with a diameter of several mm. It is usually preferable to mix the lipophilic granular solids with the pulverized coal at a ratio of 1:1, but the total amount of the lipophilic granular solids and pulverized coal in the water slurry is 30% by weight or less, and this value is Of course, the ratio of the lipophilic granular solids to the pulverized coal may be increased or decreased within a range not exceeding the above range.
微粉炭の水スラリーと、液状低沸点油と、
造粒核となる親油性粒状固形物を混合するに
はつぎの３つの方法がある。 A water slurry of pulverized coal, a liquid low boiling point oil,
There are the following three methods for mixing lipophilic granular solids that will become granulation nuclei.
(i) 微粉炭の水スラリーに親油性粒状固形物
を混合し、ついでこの水スラリー中に油を
混合する。 (i) Mixing lipophilic granular solids into a water slurry of pulverized coal and then mixing oil into the water slurry.
(ii) 親油性粒状固形物に予め油を添加して、
親油性粒状固形物の表面に油を付着させて
おき、ついでこの油付き親油性粒状固形物
を微粉炭の水スラリー中に混合する。 (ii) adding oil to the lipophilic granular solid in advance;
Oil is attached to the surface of the lipophilic granular solid, and then the oil-attached lipophilic granular solid is mixed into a water slurry of pulverized coal.
(iii) 微粉炭の水スラリーに油を混合し、つい
でこの水スラリーに親油性粒状固形物を混
合する。 (iii) mixing oil into a water slurry of pulverized coal and then mixing lipophilic granular solids into the water slurry;
上記のような混合物を撹拌して造粒するに
は、本出願人が先に提案した金網製撹拌翼を
備えた造粒装置（特開昭57−87823号公報参
照）あるいはその他の既知の造粒装置を使用
する。この造粒の過程においては、親油性粒
状固形物の表面に液状低沸点油が薄い膜状に
付着せられ、この油付き親油性粒状固形物を
核としてこれの表面の油に純度の高い微粉炭
が順次付着してゆき、いわゆる転動造粒によ
つて微粉炭が加速度的にきわめて迅速に造粒
せられる。 In order to stir and granulate the above-mentioned mixture, a granulating device equipped with a wire-mesh stirring blade proposed earlier by the present applicant (see Japanese Patent Application Laid-Open No. 1987-87823) or other known granulating devices can be used. Use grain equipment. In this granulation process, a thin film of liquid low-boiling oil is attached to the surface of the lipophilic granular solid, and highly pure fine powder is formed on the oil on the surface of the oil, using the oil-attached lipophilic granular solid as a core. The coal is deposited one after another, and the pulverized coal is granulated very quickly at an accelerated rate by so-called rolling granulation.
第１段階としては液状低沸点油の少量を少
なくしているので、微粉炭の全量は造粒され
ず、この段階では純度の高い微粉炭が油付き
親油性粒状固形物の表面に付着し、残りの未
造粒微粉炭と灰分は水スラリー中に残留す
る。 In the first stage, since the small amount of liquid low-boiling oil is reduced, the entire amount of pulverized coal is not granulated, and in this stage, highly pure pulverized coal adheres to the surface of the oily lipophilic granular solids. The remaining ungranulated pulverized coal and ash remain in the water slurry.
なお、原炭中の灰分の含有量がたとえば20
重量％程度と非常に多いような場合には、造
粒を行なう前に一次脱灰処理を行なつてもよ
い。すなわち、微粉炭の水スラリーと親油性
粒状固形物と液状低沸点油を混合すると、微
粉炭と親油性粒状固形物と油を含む液相と、
灰分を含む水よりなるスラリーとに分れる。
この灰分を含む水スラリーを、微粉炭を含む
液相から分離し、ついでこの微粉炭を含む液
相を清水で洗浄する。これによつて灰分のか
なりの量が除かれる。 In addition, if the ash content in the raw coal is, for example, 20
If the amount is very large, such as approximately % by weight, a primary deashing treatment may be performed before granulation. That is, when a water slurry of pulverized coal, lipophilic granular solids, and liquid low-boiling oil are mixed, a liquid phase containing pulverized coal, lipophilic granular solids, and oil is formed;
It is separated into a slurry consisting of water containing ash.
The water slurry containing ash is separated from the liquid phase containing pulverized coal, and the liquid phase containing pulverized coal is then washed with fresh water. This removes a significant amount of ash.
(3) 分離工程：つぎに水スラリー中より微粉炭
と液状低沸点油と親油性粒状固形物とよりな
る造粒物を分離して洗浄することにより、造
粒物を得るとともに、未造粒微粉炭と灰分を
含む水スラリーを取り出す。この処理は造粒
物を含む水スラリーをたとえばフイルターの
上に流して、洗浄水を上から噴霧することに
より行なう。場合によつては分離後の造粒物
を遠心分離機にかけてさらに水分を除去する
こともある。未造粒微粉炭と灰分を含む水ス
ラリーは、その後シツクナーおよび濾過機等
を備えた水処理装置において洗浄水分を除去
し、濃縮して、濃度調整を行なつたのち、つ
ぎの第２段階の脱灰操作の造粒槽へ導く。 (3) Separation step: Next, the granules consisting of pulverized coal, liquid low-boiling oil, and lipophilic granular solids are separated from the water slurry and washed to obtain granules and ungranulated A water slurry containing pulverized coal and ash is taken out. This treatment is carried out by, for example, pouring a water slurry containing the granules onto a filter and spraying washing water onto it. In some cases, the separated granules may be centrifuged to further remove moisture. The water slurry containing ungranulated pulverized coal and ash is then sent to a water treatment device equipped with a thickener and a filter to remove washing water, concentrate it, and adjust its concentration before proceeding to the second stage. Lead to the granulation tank for demineralization.
(4) 蒸発工程：つぎに高純度微粉炭と液状低沸
点油と親油性粒状固形物とよりなる洗浄後の
造粒物を加熱して、液状低沸点油と水分とを
蒸発せしめる。ここで、熱源としてはスチー
ムあるいは電熱を使用する。 (4) Evaporation step: Next, the washed granulated material consisting of high-purity pulverized coal, liquid low-boiling oil, and lipophilic granular solids is heated to evaporate the liquid low-boiling oil and water. Here, steam or electric heat is used as the heat source.
(5) 親油性粒状固形物回収工程：つぎに低沸点
油を除いた造粒物をたとえば振動を与えるこ
とにより分解して、高純度の脱灰炭と親油性
粒状固形物とに分離し、高純度の脱灰炭を得
るとともに、親油性粒状固形物を回収して上
記第２番目の造粒工程に返送する。この場合
親油性粒状固形物に液状低沸点油を添加した
のち造粒工程に返送してもよいし、また油を
添加することなくそのまま返送してもよい。 (5) Lipophilic granular solids recovery step: Next, the granules from which the low-boiling point oil has been removed are decomposed, for example by applying vibration, and separated into high-purity deashing coal and lipophilic granular solids. High-purity demineralized coal is obtained, and lipophilic granular solids are recovered and returned to the second granulation step. In this case, the lipophilic granular solid material may be returned to the granulation process after adding a liquid low boiling point oil, or may be returned as is without adding oil.
(6) 低沸点油回収工程：ガス状低沸点油と水分
とを含む蒸発ガスを凝縮したのち、液状低沸
点油と水とに分離し、液状低沸点油を上記造
粒工程に返送する。 (6) Low-boiling oil recovery process: After condensing the evaporated gas containing gaseous low-boiling oil and water, it is separated into liquid low-boiling oil and water, and the liquid low-boiling oil is returned to the granulation process.
このようにして製造された脱灰炭は、充分に
灰分が除去せられた高純度のものであり、これ
は高純度石炭を燃料とする燃焼装置において有
効に使用せられるものである。 The deashed coal produced in this manner has a high purity from which ash has been sufficiently removed, and can be effectively used in combustion equipment that uses high-purity coal as fuel.
第２段階脱灰操作
(7) 造粒工程：上記第１段階脱灰操作（）の
分離工程(3)から取り出した未造粒微粉炭と灰
分を含む水スラリーを濃度調整したのち、第
２段階の造粒槽に導き、このスラリーにさら
に液状低沸点油および造粒核となる親油性粒
状固形物を混合して造粒する。液状低沸点油
の使用量は、未造粒微粉炭に付着したままの
液状低沸点油をも考慮して第１段階の場合と
同様、残留微粉炭に対し５〜10重量％であ
る。また、油の分散が容易になるように、界
面活性剤を少量添加する。親油性粒状固形物
は微粉炭に対して１：１の割合で混合するの
が好ましいが、親油性粒状固形物と微粉炭の
総量はスラリー中において30重量％以下であ
り、この値を越えない範囲において微粉炭に
対する親油性粒状固形物の割合を減じても勿
論良い。 Second stage deashing operation (7) Granulation process: After adjusting the concentration of the water slurry containing the ungranulated pulverized coal and ash taken out from the separation process (3) of the first stage deashing operation () above, This slurry is further mixed with a liquid low-boiling point oil and a lipophilic granular solid material serving as granulation nuclei for granulation. The amount of liquid low-boiling oil used is 5 to 10% by weight based on the residual pulverized coal, as in the first stage, taking into account the liquid low-boiling oil still attached to the ungranulated pulverized coal. Additionally, a small amount of surfactant is added to facilitate oil dispersion. It is preferable to mix the lipophilic granular solids with the pulverized coal in a ratio of 1:1, but the total amount of the lipophilic granular solids and pulverized coal in the slurry is 30% by weight or less, and does not exceed this value. Of course, the ratio of lipophilic granular solids to pulverized coal may be reduced within this range.
そして造粒工程を行なつたのちは、上記第
１段階の脱灰操作（）の場合と同様に、分
離工程(3)、蒸発工程(4)、親油性粒状固形物回
収工程(5)および低沸点油回収工程(6)を行なつ
て脱灰炭を得るものである。 After the granulation process, the separation process (3), evaporation process (4), lipophilic granular solid recovery process (5) and Deashed coal is obtained by performing a low boiling point oil recovery step (6).
このようにして第２段階の脱灰操作（）によ
り得られた脱灰炭は、第１段階の脱灰炭に比較す
ると灰分の除去率は若干低下するが、それでもな
お灰分含有量の少ないものであり、これは通常の
燃焼装置において有効に使用せられるものであ
る。さらに必要に応じて、上記第２段階の脱灰操
作（）の分離工程から取り出した未造粒微粉炭
と灰分を含む水スラリーを濃度調整したのち、こ
れに低沸点油と親油性粒状固形物を混合して微粉
炭の造粒を行なう第３段階以降の脱灰炭操作を実
施する。こうして灰分含有量の非常に少ない脱灰
炭から比較的灰分除去率の低い脱灰炭までを段階
的に取得するものである。 The deashed coal thus obtained through the second stage deashing operation () has a slightly lower ash removal rate than the first stage deashed coal, but still has a low ash content. This can be effectively used in ordinary combustion devices. Furthermore, if necessary, after adjusting the concentration of the water slurry containing ungranulated pulverized coal and ash taken out from the separation process of the second stage deashing operation (), low boiling point oil and lipophilic granular solids are added to this. Deashing coal operations are carried out from the third stage onwards, in which pulverized coal is granulated by mixing. In this way, deashed coal with a very low ash content to deashed coal with a relatively low ash removal rate is obtained in stages.
なお、この発明の方法においては、原炭につい
て脱灰操作を少なくとも２段階で実施するもので
ある。 In addition, in the method of this invention, the deashing operation is performed on raw coal in at least two stages.
実施例
つぎに、この発明の実施例を比較例および参考
例とともに説明する。Examples Next, examples of the present invention will be described together with comparative examples and reference examples.
実施例
第１段階脱灰操作
灰分含有量7.02重量％のブレアゾール炭（オ
ーストラリア産）を粉砕して、200メツシユ以
下、すなわち粒径74μｍ以下の微粉炭をつく
り、これに水を混合して微粉炭の水スラリーを
つくる。つぎにこの微粉炭の水スラリーに親油
性粒状固形物を混合した。親油性粒状固形物は
硬質ポリ塩化ビニル製で、直径３mmおよび高さ
1.5mmの短い円柱状を有しており、また比重は
1.4で石炭の比重と近似していた。スラリーの
配合量は、微粉炭５重量％および親油性粒状固
形物５重量％とした。Example 1st stage deashing operation Blairsol coal (produced in Australia) with an ash content of 7.02% by weight is pulverized to produce pulverized coal of 200 mesh or less, that is, a particle size of 74 μm or less, and water is mixed with this to produce pulverized coal. Make a water slurry. Next, lipophilic granular solids were mixed into this water slurry of pulverized coal. The lipophilic granular solids are made of hard PVC and have a diameter of 3 mm and a height of
It has a short cylindrical shape of 1.5 mm, and its specific gravity is
The specific gravity was 1.4, which approximated the specific gravity of coal. The content of the slurry was 5% by weight of pulverized coal and 5% by weight of lipophilic granular solids.
ついで、この水スラリー中に液状ガソリンを
微粉炭に対する量で10重量％混合し、このスラ
リーを造粒装置に導入した。造粒装置として
は、本出願人が先に提案した水平な３枚のステ
ンレス金網製撹拌翼（直径360mm、目開き５
mm、針金直径0.5mm）を有する80容量の造粒
装置を使用し、金網製撹拌翼を周速が６〜10
ｍ／secとなるように20分間撹拌して造粒を行
なつた。この結果、全微粉炭の約20％の造粒物
を得た。その後スラリー中より造粒物を分離し
て水で洗浄することにより、灰分を除去し、洗
浄後の造粒物を140℃で３時間加熱してガソリ
ンと水とを蒸発せしめ、ついでガソリンを含ま
ない造粒物に振動を与えて分解し、ペレツト状
の脱灰炭と親油性粒状固形物を得た。脱灰炭よ
り親油性粒状固形物を分離して、これを造粒工
程に返送して再使用した。一方、ガソリンと水
分とを含む蒸発ガスはこれを凝縮させたのち、
液状ガソリンと水とに分離し、液状ガソリンは
造粒工程に返送して再使用した。ここで、ガソ
リンの回収率は70％であつた。このようにして
製造された脱灰炭の灰分含有量を測定したとこ
ろ、1.40重量％の灰分が含まれているだけであ
つた。 Next, liquid gasoline was mixed in this water slurry in an amount of 10% by weight based on the pulverized coal, and this slurry was introduced into a granulator. The granulation device used was three horizontal stainless wire mesh stirring blades (diameter 360 mm, opening 5) that the applicant had proposed earlier.
An 80-capacity granulation device with wire diameter of 0.5 mm and wire diameter of 0.5 mm was used.
Pelletization was performed by stirring for 20 minutes at a speed of m/sec. As a result, granules containing about 20% of the total pulverized coal were obtained. After that, the granules were separated from the slurry and washed with water to remove the ash, and the washed granules were heated at 140°C for 3 hours to evaporate gasoline and water, and then the gasoline and water were removed. The granules were decomposed by vibration to obtain pellet-like deashed coal and lipophilic granular solids. Lipophilic granular solids were separated from the deashed coal and returned to the granulation process for reuse. On the other hand, the evaporated gas containing gasoline and water is condensed and then
Liquid gasoline and water were separated, and the liquid gasoline was returned to the granulation process for reuse. Here, the gasoline recovery rate was 70%. When the ash content of the deashed coal thus produced was measured, it was found to contain only 1.40% by weight of ash.
第２段階脱灰操作
つぎに、上記第１段階脱灰操作の分離工程か
ら取り出した残りの末造粒微粉炭と灰分を含む
水スラリーを静置して上澄み液を捨て、微粉炭
濃度４重量％に濃度調整した。ついでこの水ス
ラリー80スラリー中に、微粉炭と同量の親油
性粒状固形物と、微粉炭に対して10重量％のガ
ソリンとを混合し、この水スラリーを上記第１
段階の場合と同じ造粒装置に導入して全微粉炭
の40％の造粒物を得た。（したがつて第１段階
と第２段階で合計60％の微粉炭を回収した。）
なお、親油性粒状固形物は第１段階において使
用したものと同じ素材のものを使用した。そし
てつぎに、この造粒物より第１段階の場合と同
様にガソリンを除去し、脱灰炭を製造した。こ
の第２段階の脱灰操作により得られた脱灰炭の
灰分含有量を測定したところ、2.03重量％の灰
分が含まれているだけであつた。 Second stage deashing operation Next, the water slurry containing the remaining granulated pulverized coal and ash taken out from the separation process of the first stage deashing operation is left to stand, the supernatant liquid is discarded, and the pulverized coal concentration is 4 wt. The concentration was adjusted to %. Next, in this water slurry 80, the same amount of lipophilic granular solids as the pulverized coal and 10% by weight of gasoline based on the pulverized coal were mixed, and this water slurry was mixed with the above-mentioned first slurry.
It was introduced into the same granulation equipment as in the step to obtain 40% granulated material of the total pulverized coal. (Therefore, a total of 60% of pulverized coal was recovered in the first and second stages.)
Note that the lipophilic granular solid material was made of the same material as that used in the first stage. Next, gasoline was removed from the granules in the same manner as in the first stage to produce deashed coal. When the ash content of the deashed coal obtained by this second stage deashing operation was measured, it was found that it contained only 2.03% by weight of ash.
参考例
上記実施例の原炭よりつくつた微粉炭の水スラ
リーを上記実施例で用いたものと同じ造粒装置に
導入し、この水スラリーに、親油性粒状固形物
と、微粉炭に対して20重量％の液状ガソリンを混
合して、水スラリー中の微粉炭の全量を一度に造
粒し、脱灰操作を行なつた。得られた脱灰炭には
1.86重量％の灰分が含まれていた。なお、これ
は、本発明の第１段階の脱灰操作（）において
得られた脱灰炭よりも灰分除去率の低いものであ
る。Reference Example A water slurry of pulverized coal made from the raw coal of the above example was introduced into the same granulation device as used in the above example, and this water slurry was added with lipophilic granular solids and pulverized coal. By mixing 20% by weight of liquid gasoline, the entire amount of pulverized coal in the water slurry was granulated at once, and a deashing operation was performed. The obtained deashed coal has
It contained 1.86% ash by weight. Note that this has a lower ash removal rate than the deashed coal obtained in the first stage deashing operation () of the present invention.
比較例
ここで、比較のために、上記実施例の原炭より
つくつた微粉炭５重量％を含む水スラリーを同じ
造粒装置に導入し、この水スラリーに液状ガソリ
ンを微粉炭に対して20重量％混合し、親油性粒状
固形物を全く用いないで従来法により造粒脱灰操
作を行なつたところ、得られた脱灰炭には、3.9
重量％の灰分が含まれていた。Comparative Example Here, for comparison, a water slurry containing 5% by weight of pulverized coal made from the raw coal of the above example was introduced into the same granulation device, and liquid gasoline was added to the water slurry at a rate of 20% by weight relative to the pulverized coal. When granulation and deashing were carried out using the conventional method without using any lipophilic granular solids, the resulting deashed coal contained 3.9% by weight.
It contained ash content of % by weight.
発明の効果
この発明の方法は、上述の次第で、灰分を含む
石炭を非常に細かい微粉炭に粉砕して、微粉炭の
水スラリーをつくり、この水スラリーに液状低沸
点油を添加して微粉炭を造粒するさいに、第１段
階においてとくに造粒核となる合成樹脂製親油性
粒状固形物を使用するとともに、すべての微粉炭
を造粒するには少ない所要量の液状低沸点油を使
用して、微粉炭の一部を造粒するようにしたか
ら、この第１段階の脱灰操作において灰分の巻込
み量が非常に少ない純度の高い高品位の脱灰炭を
製造することができる。また低沸点油と親油性粒
状固形物とは循環使用するものであるから、非常
に経済的である。そしてこの場合、親油性粒状固
形物は合成樹脂によりつくられているから、非常
に強度が大きいものであり、何回も反復して使用
することができるし、それ自体には灰分が含まれ
ていないため、脱灰炭の灰分含有量を低下させる
ようなことは全くない。Effects of the Invention As described above, the method of the present invention involves pulverizing coal containing ash into very fine pulverized coal to create a water slurry of pulverized coal, and adding liquid low-boiling oil to this water slurry to pulverize the coal into pulverized coal. When granulating charcoal, in the first stage, lipophilic granular solids made of synthetic resin are used as granulation nuclei, and a small amount of liquid low-boiling oil is required to granulate all the pulverized coal. Since a part of the pulverized coal is granulated using the pulverized coal, it is possible to produce high-grade deashed coal of high purity with a very small amount of ash entrained in this first stage deashing operation. can. Furthermore, since the low boiling point oil and the lipophilic granular solids are recycled, it is very economical. In this case, the lipophilic granular solids are made of synthetic resin, so they are extremely strong and can be used repeatedly, and they do not contain ash. Therefore, there is no reduction in the ash content of the deashed coal.
またこの発明においては、水スラリー中の微粉
炭を親油性粒状固形物を用いて、第１段階、第２
段階と段階的に、したがつて順次部分的に造粒
し、脱灰炭を製造するものであるから、高品位の
脱灰炭から比較的低品位の脱灰炭まで幅広く取得
することができる。したがつてこれらを燃料とし
て使用する場合においては、たとえば石油系燃料
がガソリンから重油まで段階的にあるのと同様
に、対象とする燃焼装置によつて選択的に使用す
ることができ、非常に効果的である。 In addition, in this invention, the pulverized coal in the water slurry is treated with lipophilic granular solids in the first stage and the second stage.
Since deashed coal is produced by granulating it step by step and therefore sequentially, it is possible to obtain a wide range of deashed coal from high-grade deashed coal to relatively low-grade deashed coal. . Therefore, when using these as fuel, they can be used selectively depending on the target combustion equipment, just as petroleum-based fuels are graded from gasoline to heavy oil. Effective.
図面は、この発明の方法を実施する工程を順次
示すブロツク図である。
The drawings are block diagrams sequentially illustrating the steps of carrying out the method of the invention.
Claims (1)
この灰分を含む微粉炭の水スラリーに、すべての
微粉炭を造粒するには少ない所要量の液状低沸点
油、および造粒核となる合成樹脂製親油性粒状固
形物を混合して造粒する工程と、造粒物を水スラ
リー中より取出して水で洗浄することにより、造
粒物と、未造粒微粉炭および灰分を含む水スラリ
ーとを分離する分離工程と、造粒物を加熱して、
液状低沸点油と水分とを蒸発せしめる工程と、低
沸点油を含まない造粒物を分解してペレツト状の
脱灰炭と親油性粒状固形物とに分離し、脱灰炭を
得るとともに、親油性粒状固形物を回収して上記
造粒工程に返送する工程と、ガス状低沸点油と水
とを含む蒸発ガスを凝縮したのち、液状低沸点油
と水とに分離し、液状低沸点油を上記造粒工程に
返送する工程とよりなる第１段階の脱灰操作を実
施し、つぎに、この第１段階の脱灰操作の分離工
程から取り出した未造粒微粉炭と灰分とを含む水
スラリーについて濃度を調整したのち微粉炭の造
粒を行なう第２段階以降の脱灰操作を上記第１段
階の脱灰操作と同様に親油性粒状固形物を用いて
実施して、灰分含有量の非常に少ない脱灰炭から
比較的灰分除去率の低い脱灰炭までを段階的に取
得することを特徴とする脱灰炭の段階的製造方
法。1. Pulverized coal is created by pulverizing coal containing ash,
This water slurry of pulverized coal containing ash is mixed with a small amount of liquid low-boiling oil needed to granulate all of the pulverized coal, and a lipophilic granular solid made of synthetic resin that will serve as granulation nuclei for granulation. a separation step of separating the granules from a water slurry containing ungranulated pulverized coal and ash by taking out the granules from the water slurry and washing them with water; and heating the granules. do,
A process of evaporating liquid low-boiling point oil and water, and decomposing the granulated material that does not contain low-boiling point oil to separate it into pellet-like deashed coal and lipophilic granular solids to obtain deashed coal, A step of collecting the lipophilic granular solids and returning them to the granulation step, condensing the evaporated gas containing gaseous low-boiling point oil and water, and then separating it into liquid low-boiling point oil and water. A first stage deashing operation consisting of a step of returning the oil to the granulation step is carried out, and then the ungranulated pulverized coal and ash taken out from the separation step of this first stage deashing operation are separated. After adjusting the concentration of the water slurry contained, the second and subsequent deashing operations, in which pulverized coal is granulated, are carried out using lipophilic granular solids in the same manner as the first-stage deashing operation, to reduce the ash content. A method for stepwise production of deashed coal, characterized by stepwise obtaining deashed coal from a very small amount of deashed coal to a relatively low deashed coal with a relatively low ash removal rate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2473281A JPS57139188A (en) | 1981-02-20 | 1981-02-20 | Stepwise preparation of deashed coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2473281A JPS57139188A (en) | 1981-02-20 | 1981-02-20 | Stepwise preparation of deashed coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57139188A JPS57139188A (en) | 1982-08-27 |
| JPS6258398B2 true JPS6258398B2 (en) | 1987-12-05 |
Family
ID=12146318
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2473281A Granted JPS57139188A (en) | 1981-02-20 | 1981-02-20 | Stepwise preparation of deashed coal |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS57139188A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03240699A (en) * | 1990-02-15 | 1991-10-28 | Nippon Sutando Service Kk | Vapor recovering device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3665066A (en) * | 1969-11-28 | 1972-05-23 | Canadian Patents Dev | Beneficiation of coals |
| JPS5370076A (en) * | 1976-12-03 | 1978-06-22 | Shell Int Research | Method of aggregating coal powder |
| JPS564692A (en) * | 1979-06-19 | 1981-01-19 | Atlantic Richfield Co | Reduction of sulfur and ash of coal |
-
1981
- 1981-02-20 JP JP2473281A patent/JPS57139188A/en active Granted
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3665066A (en) * | 1969-11-28 | 1972-05-23 | Canadian Patents Dev | Beneficiation of coals |
| JPS5370076A (en) * | 1976-12-03 | 1978-06-22 | Shell Int Research | Method of aggregating coal powder |
| JPS564692A (en) * | 1979-06-19 | 1981-01-19 | Atlantic Richfield Co | Reduction of sulfur and ash of coal |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03240699A (en) * | 1990-02-15 | 1991-10-28 | Nippon Sutando Service Kk | Vapor recovering device |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57139188A (en) | 1982-08-27 |
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