JPH01119351A - Method for manufacturing fine powder - Google Patents
Method for manufacturing fine powderInfo
- Publication number
- JPH01119351A JPH01119351A JP62275054A JP27505487A JPH01119351A JP H01119351 A JPH01119351 A JP H01119351A JP 62275054 A JP62275054 A JP 62275054A JP 27505487 A JP27505487 A JP 27505487A JP H01119351 A JPH01119351 A JP H01119351A
- Authority
- JP
- Japan
- Prior art keywords
- fine powder
- specific surface
- surface area
- classified
- raw material
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000000843 powder Substances 0.000 title claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 title claims description 11
- 238000000034 method Methods 0.000 title description 20
- 238000010298 pulverizing process Methods 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims description 44
- 238000000227 grinding Methods 0.000 claims description 23
- 239000002893 slag Substances 0.000 claims description 21
- 239000000428 dust Substances 0.000 claims description 8
- 239000011802 pulverized particle Substances 0.000 claims description 4
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 9
- 239000002245 particle Substances 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 238000012360 testing method Methods 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000004568 cement Substances 0.000 description 5
- 239000000523 sample Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000049 pigment Substances 0.000 description 2
- 229920003023 plastic Polymers 0.000 description 2
- 239000004033 plastic Substances 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009837 dry grinding Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
Landscapes
- Disintegrating Or Milling (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
この発明は、例えばセメント原料としてのガラス質高炉
スラグ、セメント混和材、シリカ、アルミナ等のセラミ
ックス類、サンド、ガラス、プラスチック、顔料等、各
種の原料を乾式で粉砕し、その微粉を製造するための、
微粉の製造方法に関するものである。[Detailed Description of the Invention] [Field of Industrial Application] This invention is applicable to various materials such as vitreous blast furnace slag as a raw material for cement, cement admixtures, ceramics such as silica and alumina, sand, glass, plastics, pigments, etc. Dry grinding of raw materials to produce fine powder.
This invention relates to a method for producing fine powder.
例えば、高炉水砕スラグ等のガラス質高炉スラグ（以下
、スラグと略称する）を原料として製造されるスラグ系
セメントには、初期材令における水利硬化が遅い問題が
ある。この問題を解決するためには、スラグを細かく粉
砕して水利硬化を促進させることが必要である。For example, slag-based cement manufactured using vitreous blast furnace slag (hereinafter abbreviated as slag) such as granulated blast furnace slag as a raw material has a problem in that water hardening is slow at the initial stage of the material. To solve this problem, it is necessary to finely crush the slag to promote water hardening.
しかしながら、スラグの粉砕は、従来ボールミル、ロー
ラミル等の粉砕機により行なわれているため、粉砕機の
経済的な粉砕能力、粉砕に要するエネルギー及び時間等
から、その粉砕粒度は、３５００〜４５００ ｃｊ／
ｆ 程度である。従って、上述した水利硬化の促進効果
は低い。However, since slag is conventionally pulverized by a pulverizer such as a ball mill or a roller mill, the pulverized particle size is 3,500 to 4,500 cj/cm due to the economical pulverizing capacity of the pulverizer, the energy and time required for pulverization, etc.
It is about f. Therefore, the above-mentioned effect of promoting water hardening is low.
上述した問題を解決するために、特開昭６１−１４１６
４７号公報により１．スラグを粉砕する粉砕工程と、粉
砕工程によって得られた粉砕スラグを分級する分級工程
と、分級工程によって分級された分級微粉を捕集する捕
集工程とからなり、これによって、ブレーン比表面積で
６，０００〜１２゜０００ ｃｙｌ／ ｆ のスラグ
粉末を製造する、水硬性材料の製造方法が提案されてい
る。In order to solve the above-mentioned problem, Japanese Patent Application Laid-Open No. 61-1416
According to Publication No. 47, 1. It consists of a crushing process to crush slag, a classification process to classify the crushed slag obtained in the crushing process, and a collection process to collect the classified fine powder classified in the classification process. ,000 to 12°,000 cyl/f of slag powder has been proposed.
上述した方法によれば、粉砕したスラグを分級すること
によって、プレーン比表面積６，０００〜１２、 ＯＯ
Ｏｃｄ／ ｆ の微粉スラグが得られる。According to the above-mentioned method, by classifying the crushed slag, the plain specific surface area is 6,000 to 12, OO
A fine powder slag of Ocd/f is obtained.
しかしながら、近時、スラグ系セメントの水和硬化特性
を一段と高めるために、従来よシも一層微粉化された、
ブレーン比表面積が１２，０ＯＯｉ／ｆ超の超微粉スラ
グも要求されており、上述した方法では、このような超
微粉スラブを収率高く製造することができない。更に、
上述した方法では微粉スラグの収率が低く、分級工程に
おいて発生した分級粗粉に対する再粉砕処理等のために
製造効率が悪い等の問題がある。However, in recent years, in order to further improve the hydration hardening properties of slag-based cement, the conventional method has been made even more finely powdered.
Ultrafine slag with a Blaine specific surface area of more than 12,0 OOi/f is also required, and the method described above cannot produce such an ultrafine slag with high yield. Furthermore,
The above-mentioned method has problems such as a low yield of fine slag and poor production efficiency due to the re-pulverization treatment of the classified coarse powder generated in the classification process.
従って、この発明の目的は、ブレーン比表面積が６．
ＯＯＯｄｉ／ ９以上、特に１２，０００ ｄｌｆ
超の微粉を、高い収率で且つ効率的に製造するための、
微粉の製造方法を提供することにある。Therefore, the object of this invention is to have a Blaine specific surface area of 6.
OOOdi/ 9 or more, especially 12,000 dlf
In order to efficiently produce ultra-fine powder with high yield,
An object of the present invention is to provide a method for producing fine powder.
本発明者等は、上述した問題を解決すべく鋭意研究を重
ねた。その結果、粉砕工程における原料の粉砕粒度が、
分級工程における分級効率および分級微粉の粒度に大き
な影響を及ぼすことを知見した。The present inventors have conducted extensive research in order to solve the above-mentioned problems. As a result, the grinding particle size of the raw material in the grinding process is
It was found that the classification efficiency in the classification process and the particle size of the classified fine powder were greatly affected.
この発明は、上記知見に基きなされたものであって、原
料を粉砕する粉砕工程と、前記粉砕工程によって得られ
た粉砕原料を分級する分級工程と、前記分級工程によっ
て分級された分級微粉を捕集する捕集工程とからなる微
粉の製造方法において、前記粉砕工程における前記原料
の粉砕粒度を、ブレーン比表面積で４，３００〜８．
ＯＯＯｄｉ／ ｆ の範囲内とし、前記分級工程におい
て、前記ブレーン比表面積で４，３００〜８．０００
ｃｓｌ／ ｆ の粉砕原料を分級し、次いで、得られ
た分級微粉を前記捕集工程において捕集することによシ
、ブレーン比表面積で６． ｏ ｏ ｏ ｃｙｌ／ ｆ
以上の微粉を製造することに特徴を有するものであ
る。This invention was made based on the above knowledge, and includes a pulverizing step of pulverizing the raw material, a categorizing step of classifying the pulverized raw material obtained by the pulverizing step, and a classification step of capturing the classified fine powder classified by the categorizing step. In the method for producing fine powder, the particle size of the raw material in the pulverization step is set to 4,300 to 8.0 in Blaine specific surface area.
OOOdi/f is within the range of 4,300 to 8.000 in the Blaine specific surface area in the classification step.
By classifying the pulverized raw material of csl/f and then collecting the obtained classified fine powder in the collection step, the Blaine specific surface area is 6. o o o cyl/ f
This method is characterized by producing the above-mentioned fine powder.
この発明において、粉砕工程における原料の粉砕は、一
般に使用されているボールミル、ローラミル、振動ミル
等の粉砕機によって行なう。In this invention, the raw material in the pulverization step is pulverized by a commonly used pulverizer such as a ball mill, roller mill, or vibration mill.
粉砕工程における原料の粉砕粒度を、ブレーン比表面積
で４，３００〜Ｂ、 ＯＯＯａ／ｉ／ ｆ の範囲内
に限定した理由は、次の通りである。即ち、原料の粉砕
粒度がブレーン比表面積で４．３００ ｄｌ ？ 未満
では、粉砕により発生する微粉の量が少危ぐ、従って分
級微粉の収率が著しく低くなり、また、分級工程におい
て多量の分級粗粉が発生するので、分級粗粉の再粉砕等
のために多大の処理工程が必要となシ、製造効率が低下
する等の問題が生ずる。The reason why the pulverized particle size of the raw material in the pulverization step was limited to a Blaine specific surface area of 4,300 to B, OOOa/i/f is as follows. That is, the pulverized particle size of the raw material is 4.300 dl in Blaine specific surface area? If the amount is less, the amount of fine powder generated by pulverization will be small, and the yield of classified fine powder will be extremely low.Also, since a large amount of classified coarse powder will be generated in the classification process, it will be necessary to re-grind the classified coarse powder. Problems arise, such as requiring a large number of processing steps and reducing manufacturing efficiency.
一方、原料の粉砕粒度がブレーン比表面積で８、 ＯＯ
Ｏａｄ／ ｆ を超えると、粉砕工程における原料の
粉砕効率が極端に低下し、粉砕コストが増大する上、長
時間の粉砕によって生ずるメカノケミカル作用により、
粉砕原料の表面の活性度が低下する等の問題が生ずる。On the other hand, the grinding particle size of the raw material is 8 in Blaine specific surface area, OO
If Oad/f is exceeded, the grinding efficiency of the raw material in the grinding process will be extremely reduced, the grinding cost will increase, and due to mechanochemical effects caused by long-term grinding,
Problems such as a decrease in the surface activity of the pulverized raw material arise.
粉砕工程における原料の粉砕時に、例えば、メタノール
、エタノール、ジエチレングリコール等のアルコール類
、トリエタノールアミン等のアミン類からなる粉砕助剤
を、原料中に添加することが好ましい。When pulverizing the raw material in the pulverizing step, it is preferable to add a crushing aid to the raw material, for example, consisting of alcohols such as methanol, ethanol, diethylene glycol, and amines such as triethanolamine.
即ち、上述の粉砕助剤は、粒子の凝集を防止する作用を
有するから、粉砕助剤の添加によって原料の粉砕が効率
的に行なわれるので、ブレーン比表面積が５． ＯＯＯ
ａＡ／ ｆ 以上の微粉に経済的に粉砕することができ
る。That is, since the above-mentioned grinding aid has the effect of preventing particle agglomeration, the addition of the grinding aid enables efficient grinding of the raw material, so that the Blaine specific surface area is 5. OOO
It can be economically ground to a fine powder of aA/f or higher.
上述した粉砕助剤を添加した場合と添加しない場合の原
料の粉砕試験を行なった。粉砕試験は、原料として、第
１表に示す化学成分組成のスラグを使用し、これを乾燥
し次いで含有鉄分を除去した後、内容積が３８５ｔのボ
ールミル中に５０Ｋｇを投入してこれを粉砕し、粉砕経
過時間毎に粉砕した試料を採取し、そのブレーン比表面
積を測定することにより行なった。Grinding tests were conducted on raw materials with and without the addition of the above-mentioned grinding aid. In the pulverization test, slag with the chemical composition shown in Table 1 was used as a raw material, and after drying it and removing the iron content, 50 kg was put into a ball mill with an internal volume of 385 tons and pulverized. The results were obtained by collecting a pulverized sample every time the pulverization elapsed and measuring its Blaine specific surface area.
粉砕助剤としてジエチレングリコールを使用し、これを
原料の総量に対しｏ、１ｖｔ、％ 添加した。Diethylene glycol was used as a grinding aid, and was added in an amount of 1vt% based on the total amount of raw materials.
第２図はその試験結果を示すグラフである。第２図にお
いて、白丸印は粉砕助剤を添加しない場合でちり、黒丸
印は粉砕助剤を添加した場合である。第２図かられかる
ように、粉砕助剤を添加しない場合には、原料の粉砕粒
度は、ブレーン比表面積で約５． ＯＯＯｄ／ ｆ
が限界であるが、粉砕助剤を添加した場合には、ブレー
ン比表面積ｓ、ｏｏ。FIG. 2 is a graph showing the test results. In FIG. 2, white circles indicate dust when no grinding aid is added, and black circles indicate dust when a grinding aid is added. As can be seen from FIG. 2, when no grinding aid is added, the grinding particle size of the raw material is approximately 5.5 mm in Blaine specific surface area. OOOd/f
is the limit, but when a grinding aid is added, Blaine specific surface area s, oo.
−／ｆ まで粉砕が可能になる。It becomes possible to crush up to -/f.
分級工程における°粉砕原料の粗粒と微粉との分級は、
分級効率の高い気流分級機を使用することが望ましい。In the classification process, the classification of the crushed raw material into coarse particles and fine particles is as follows:
It is desirable to use an air classifier with high classification efficiency.
捕集工程における分級微粉の捕集は、例えばサイクロン
とバグフィルタ−とを直列に配置し、サイクロンによっ
て１次捕集した後、ノ（グツイルターによって２次捕集
を行なう２段階で行なうことが望ましい。即ち、上述の
ような２段階で捕集を行なうことにより、分級微粉を更
に２次分級することができ、１段捕集では困難な、ブレ
ーン比表面積が１２． ＯＯＯｃｄ／ｌ 以上の超微粉
の捕集が可能となる。It is desirable to collect the classified fine powder in the collection process in two stages, for example by arranging a cyclone and a bag filter in series, and performing primary collection by the cyclone and then secondary collection by a filter. In other words, by performing the two-stage collection as described above, the classified fine powder can be further classified into a second stage, and ultra-fine powder with a Blaine specific surface area of 12.00 cd/l or more can be obtained, which is difficult with one-stage collection. can be collected.
１次捕集のための集塵機は、サイクロンのような遠心力
集塵機のほかルーバーのような慣性力集塵機を使用して
もよく、２次捕集のだめの集塵機は、バグフィルタ−の
よりなｆ過式集塵機のほか電気集塵機を使用してもよい
。The dust collector for primary collection may be a centrifugal dust collector such as a cyclone, or an inertial dust collector such as a louver. In addition to type dust collectors, electric dust collectors may be used.
この発明により製造される微粉の粒度を、ブレーン比表
面積で６． ｏ ｏ ｏ ａｄ／ ｆ 以上に限定し
た理由は、次の通りである。即ち、６． ＯＯＯ６４／
ｆ 未満の微粉は、一般の粉砕機のみでも製造するこ
とができるので、分級工程を設けるメリットが小さい。The particle size of the fine powder produced by this invention is 6. o o o ad/f The reason for the above limitation is as follows. That is, 6. OOO64/
Fine powder of less than f can be produced using only a general pulverizer, so there is little merit in providing a classification step.
第１図は、この発明の方法の一実施態様を示す系統図で
ある。第１図に示すように、下部に原料排出用のスクリ
ューフィーダ２を有するホツノく１の下方には、強制渦
遠心分級式の分級機３が設けられ、分級機３には導管１
２によってサイクロン５およびバグフィルターマが直列
に接続されている。バグフィルタ−７の出側には、導管
１２２介して自動ダンパ９、ファン１．０および定風量
コントローラ１１が接続されている。FIG. 1 is a system diagram showing one embodiment of the method of the present invention. As shown in FIG. 1, a forced vortex centrifugal classifier 3 is installed below the hot spring 1 which has a screw feeder 2 for discharging raw materials at the bottom, and the classifier 3 has a conduit 1.
2 connects the cyclone 5 and the bag filter polymer in series. An automatic damper 9, a fan 1.0, and a constant air volume controller 11 are connected to the outlet side of the bag filter 7 via a conduit 122.
分級機の粗粉排出管１３にはロータリーノ（ルプ４が、
サイクロン５の下部にはロータリーノくルブ６がそして
バグフィルタ−７の下部にはロータリーパルプ８が各々
設けられている。１４は分級機３０ロ一タ回転用のモー
タである。The coarse powder discharge pipe 13 of the classifier is equipped with a rotorino (loop 4).
A rotary nozzle 6 is provided at the bottom of the cyclone 5, and a rotary pulp 8 is provided at the bottom of the bag filter 7. 14 is a motor for rotating the rotor of the classifier 30.
図示しない粉砕機によりブレーン比表面積で４．３００
〜８，０００ ＣＩ＋！／ｙ の粒度に粉砕された粉
砕原料は、ホッパ１内に供給され、ホツノ（１のスクリ
ューフィーダ２により所定量が分級機３に装入される。Blaine specific surface area is 4.300 by a crusher (not shown).
~8,000 CI+! The pulverized raw material pulverized to a particle size of /y is supplied into a hopper 1, and a predetermined amount is charged into a classifier 3 by a screw feeder 2 of 1.
分級機３は、モータ１４によって回転するロータを有す
る強制渦遠心分級式の気流分級機で、分級機３によって
分級された分級機゛粉は、導管１２によりサイクロン５
に導かれ、サイクロン５によってプレーン比表面積的６
，０００〜１２，０００（−ｄ／９の微粉が１次捕集さ
れる。１次捕集された前記微粉は、ロータリーパルプ６
を開くことによりサイクロン５から排出され回収される
。一方、分級機３によって分級された分級粗粉は、ロー
タリーパルプ４を開くことにより粗粉排出管１３を通っ
て排出される。The classifier 3 is a forced vortex centrifugal classifier air flow classifier having a rotor rotated by a motor 14.
guided by the plane specific surface area 6 by the cyclone 5
,000 to 12,000 (-d/9) is primarily collected.The primary collected fine powder is
By opening it, it is discharged from the cyclone 5 and collected. On the other hand, the classified coarse powder classified by the classifier 3 is discharged through the coarse powder discharge pipe 13 by opening the rotary pulp 4.
サイクロン５によって捕集されなかった分級微粉は、導
管１２によってバグフィルタ−７に導かれ、バグフィル
タ−７によってブレーン比表面積が約１２． ＯＯＯｃ
ｊ／ ｆ 以上の微粉が２次捕集される。２次捕集され
た前記微粉は、ロータリーパルプ８を開くことによりバ
グフィルターマから排出され回収される。The classified fine powder not collected by the cyclone 5 is guided to the bag filter 7 through the conduit 12, and the bag filter 7 has a Blaine specific surface area of about 12. OOOc
Fine particles of j/f or more are collected secondary. The secondarily collected fine powder is discharged from the bag filter machine and recovered by opening the rotary pulp 8.
次に、この発明を実施例により説明する。 Next, the present invention will be explained using examples.
原料として、第１表に示した化学成分組成のスラグを使
用し、内容積３８５ｔのボールミルによってこれを粉砕
し、本発明の範囲内のブレーン比表面積を有する粉砕原
料（以下、「本発明供試原料」という）Ｎｌｌｌ−５と
、比較のための本発明の範囲外のブレーン比表面積を有
する粉砕原料（以下、「比較用供試原料」という）Ｎａ
ｌとを調製したざ使用した原料の量は、本発明供試原料
および比較用供試原料共、各々５ｏＫｆであり、粉砕に
当っては、原料の総量に対しｏ、１ｗｔ、％ のジエチ
レングリコールを粉砕助剤として添加した。As a raw material, slag having the chemical composition shown in Table 1 was used, and this was pulverized by a ball mill with an internal volume of 385 tons. N11-5 (hereinafter referred to as "raw material") and pulverized raw material having a Blaine specific surface area outside the range of the present invention for comparison (hereinafter referred to as "comparative sample raw material") Na
The amount of raw materials used for preparing 1 and 1 was 5oKf for both the present invention test material and comparative test material, and during pulverization, 1wt% diethylene glycol was added to the total amount of raw materials. Added as a grinding aid.
上述した本発明供試原料および比較用供試原料の谷々を
、強制渦遠心分級式の気流分級機（日清エンジニアリン
グ製、機名：ターポクラシファイアＴＣ−４０型）を使
用し、下記条件によって分級した。The above-mentioned test materials of the present invention and comparative test materials were separated using a forced vortex centrifugal classification type air classifier (manufactured by Nisshin Engineering, model name: Tarpo Classifier TC-40) under the following conditions. Classified.
供試原料の供給速度 ＝ ６０匂／Ｈ分級機のロータ
回転数： ３，００ Ｏｒ、ｐ、ｍ分級機の風量
： ｌ ５ ｒｒ？／ ｍｉｎ目標分級点
３μｍ
（注） 目標分級点は、部分分級効率曲線の５０チ分離
径を示す。Feeding rate of sample raw material = 60 odor/H Classifier rotor rotation speed: 3,00 Or, p, m classifier air volume
: l 5 rr? / min target classification point
3 μm (Note) The target classification point indicates the 50-chip separation diameter of the partial classification efficiency curve.
このようにして分級された分級微粉を、サイクロンによ
って１次捕集し、次いで、バグフィルタ−によって２次
捕集した。かくして得られた１次捕集微粉および２次捕
集微粉の捕集率並びにブレーン比表面積を第２表に示す
。The thus classified fine powder was first collected by a cyclone, and then secondarily collected by a bag filter. Table 2 shows the collection efficiency and Blaine specific surface area of the primary collected fine powder and secondary collected fine powder thus obtained.
第 ２ 表
第２表から明らかなように、粉砕原料として本発明の範
囲内のブレーン比表面積を有する本発明供試原料部１〜
５を使用し、これを分級し次いで２段捕集した場合には
、１次捕集でブレーン比表面積１０． ＯＯＯｃｗｌ／
ｆ クラスの微粉を８．７〜１９，４ｗＬ％、そして
、２次捕集でブレーン比表面積２０、 ＯＯＯｃｊ／
ｆ クラスの微粉を７．２〜１０．２ｗｔ。Table 2 As is clear from Table 2, the sample raw materials 1 to 1 of the present invention having Blaine specific surface areas within the range of the present invention as pulverized raw materials.
5, and when it is classified and then collected in two stages, the Blaine specific surface area in the first collection is 10. OOOcwl/
f class fine powder of 8.7 to 19.4 wL%, and secondary collection with Blaine specific surface area of 20, OOOcj/
7.2 to 10.2 wt of f class fine powder.
−の高い収率で捕集することができた。- could be collected with a high yield.
これに対し、粉砕原料としてブレーン比表面積が本発明
の範囲の下限未満である比較用供試原料ＮＩＬＬを使用
した場合には、１次捕集でブレーン比表面積１０，００
０ ｃｄ／ｆ クラスの微粉を４．７ ｗｔ、％、２
次捕集でブレーン比表面積２０，０００ ｉ／ｆ ク
ラスの微粉を僅か２．８ｖｔ、％ しか捕集することが
できなかった。On the other hand, when the comparative sample material NILL whose Blaine specific surface area is less than the lower limit of the range of the present invention is used as the pulverized raw material, the Blaine specific surface area is 10,000 in the primary collection.
0 cd/f class fine powder at 4.7 wt, %, 2
In the subsequent collection, only 2.8vt, % of Blaine specific surface area 20,000 i/f class fine powder could be collected.
上述した実施例は、原料としてスラグを使用したが、本
発明はこのようなスラグに限られるものではなく、例え
ばフライアッシュ、シリカ質原料、°石灰石等のセメン
ト混和材、シリカやアルミナ等のセラミックス類、サン
ド、ガラス、プラスチック、顔料等、各種原料および材
料の微粉化に広く適用することができる。Although the above embodiments used slag as a raw material, the present invention is not limited to such slag, and can be used, for example, with fly ash, siliceous raw materials, cement admixtures such as limestone, and ceramics such as silica and alumina. It can be widely applied to the pulverization of various raw materials and materials such as sand, glass, plastics, pigments, etc.
以上述べたように、この発明によれば、ブレーン比表面
積がａ、ｏｏｏ以上、特に１２．０００４今超の微粉を
、高い収率で且つ効率的に製造することができる工業上
優れた効果がもたらされる。As described above, the present invention has an industrially excellent effect of being able to efficiently produce fine powder with a Blaine specific surface area of a, ooo or more, particularly more than 12.0004, in a high yield. brought about.
第１図はこの発明の方法の一実施態様を示す系統図、第
２図は粉砕工程における原料の粉砕時間とプレーン比表
面積との関係を示すグラフである。
図面において、FIG. 1 is a system diagram showing one embodiment of the method of the present invention, and FIG. 2 is a graph showing the relationship between the grinding time of the raw material and the plain specific surface area in the grinding process. In the drawing,
Claims (4)
て得られた粉砕原料を分級する分級工程と、前記分級工
程によつて分級された分級微粉を捕集する捕集工程とか
らなる微粉の製造方法において、前記粉砕工程における
前記原料の粉砕粒度を、プレーン比表面積で４，３００
〜８，０００ｃｍ＾２／ｇの範囲内とし、前記分級工程
において、前記プレーン比表面積で４，３００〜８，０
００ｃｍ＾２／ｇの粉砕原料を分級し、次いで、得られ
た分級微粉を前記捕集工程において捕集することにより
、プレーン比表面積で６，０００ｃｍ＾２／ｇ以上の微
粉を製造することを特徴とする微粉の製造方法。(1) Consisting of a pulverizing step of pulverizing the raw material, a categorizing step of classifying the pulverized raw material obtained in the pulverizing step, and a collecting step of collecting the classified fine powder classified in the categorizing step. In the method for producing fine powder, the pulverized particle size of the raw material in the pulverizing step is set to 4,300 in plane specific surface area.
~8,000cm^2/g, and in the classification step, the plane specific surface area is 4,300~8,0
It is possible to produce fine powder with a plain specific surface area of 6,000 cm^2/g or more by classifying the pulverized raw material of 00 cm^2/g and then collecting the obtained classified fine powder in the collection step. Characteristic method for producing fine powder.
添加する、特許請求の範囲第（１）項に記載の微粉の製
造方法。(2) The method for producing fine powder according to claim (1), wherein a grinding aid is added to the raw material in the grinding step.
列に配置された２基の集塵機により２段階で行なう、特
許請求の範囲第（１）項に記載の微粉の製造方法。(3) The method for producing fine powder according to claim (1), wherein the collection of the classified fine powder in the collection step is performed in two stages using two dust collectors arranged in series.
の範囲第（１）項〜第（３）項の何れか１つに記載の微
粉の製造方法。(4) The method for producing fine powder according to any one of claims (1) to (3), wherein the raw material is vitreous blast furnace slag.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62275054A JPH0653234B2 (en) | 1987-10-30 | 1987-10-30 | Method for producing fine powder |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62275054A JPH0653234B2 (en) | 1987-10-30 | 1987-10-30 | Method for producing fine powder |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01119351A true JPH01119351A (en) | 1989-05-11 |
| JPH0653234B2 JPH0653234B2 (en) | 1994-07-20 |
Family
ID=17550202
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62275054A Expired - Fee Related JPH0653234B2 (en) | 1987-10-30 | 1987-10-30 | Method for producing fine powder |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0653234B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02107542A (en) * | 1988-01-11 | 1990-04-19 | Geochem Corp | Liquid additive composition |
| JP2003002706A (en) * | 2001-06-20 | 2003-01-08 | Mitsubishi Materials Corp | Method of treating industrial waste water |
| JP2004002165A (en) * | 2002-03-28 | 2004-01-08 | Kansai Electric Power Co Inc:The | Cement admixture and its production method |
| CN104689898A (en) * | 2015-03-13 | 2015-06-10 | 浙江拓翔建材有限公司 | Improved-structured slag powder grinding control system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5767051A (en) * | 1980-10-06 | 1982-04-23 | Onoda Cement Co Ltd | Hydraulic composition |
| JPS61141647A (en) * | 1984-12-11 | 1986-06-28 | 日本鋼管株式会社 | Hydraulic material and manufacture |
-
1987
- 1987-10-30 JP JP62275054A patent/JPH0653234B2/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5767051A (en) * | 1980-10-06 | 1982-04-23 | Onoda Cement Co Ltd | Hydraulic composition |
| JPS61141647A (en) * | 1984-12-11 | 1986-06-28 | 日本鋼管株式会社 | Hydraulic material and manufacture |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02107542A (en) * | 1988-01-11 | 1990-04-19 | Geochem Corp | Liquid additive composition |
| JP2003002706A (en) * | 2001-06-20 | 2003-01-08 | Mitsubishi Materials Corp | Method of treating industrial waste water |
| JP2004002165A (en) * | 2002-03-28 | 2004-01-08 | Kansai Electric Power Co Inc:The | Cement admixture and its production method |
| CN104689898A (en) * | 2015-03-13 | 2015-06-10 | 浙江拓翔建材有限公司 | Improved-structured slag powder grinding control system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0653234B2 (en) | 1994-07-20 |
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