JPH0250157B2 - - Google Patents
Info
- Publication number
- JPH0250157B2 JPH0250157B2 JP16413785A JP16413785A JPH0250157B2 JP H0250157 B2 JPH0250157 B2 JP H0250157B2 JP 16413785 A JP16413785 A JP 16413785A JP 16413785 A JP16413785 A JP 16413785A JP H0250157 B2 JPH0250157 B2 JP H0250157B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- distribution chamber
- pulverized coal
- swirling
- distributor
- 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
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- 239000003245 coal Substances 0.000 claims description 60
- 238000009826 distribution Methods 0.000 claims description 48
- 230000005514 two-phase flow Effects 0.000 claims description 14
- 239000007789 gas Substances 0.000 description 41
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 26
- 229910052757 nitrogen Inorganic materials 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000012159 carrier gas Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000002309 gasification Methods 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000003570 air Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Description
〔発明の利用分野〕
本発明は微粉炭の気流輸送に係り、特に微粉炭
が高濃度である場合に、微粉炭と輸送気体の固気
二相流を均等分配するのに好適な石炭分配器に関
する。
〔発明の背景〕
現在、噴流層ガス化装置において微粉炭とガス
化剤を複数のバーナからガス化炉内に旋回流を形
成するように供給する方式が開発されている。
これは、ガス化炉内に旋回流を形成することに
より微粉炭粒子を炉内に滞留させ反応時間を長く
してガス化効率を高めることを目的としている。
この旋回流のバランスが崩れた場合、ガス化効
率が悪くなることはもとより、1800℃におよぶバ
ーナ火炎による炉壁の侵食、過負荷によるバーナ
自体の破損等のトラブルが考えられ、各バーナに
均等に微粉炭を分配する技術が強く望まれてい
た。
バーナまでの微粉炭輸送の代表的方法として気
流輸送がある。搬送気体には酸素、空気、窒素、
生成ガス等があげられるが、安全性の面から反応
性の小さいガスが望ましい。このようなガスを大
量に用いると炉内を冷却してしまう。また生成ガ
ス発熱量を小さくし効率がおちる。さらに、生成
ガスからこのガスを分離するガス精製装置を煩雑
にする難点もある。また、水蒸気、空気、生成ガ
ス等を輸送気体として用いるにしても炉内温度の
抵下を抑えることを考えるとガス量は少ない方が
好ましい。
即ち、できるたけ少ない搬送気体を使つて均等
分配を得ることのできる分配器の開発が必要であ
る。
それに応えたものとしては米国特許第3204942
号が挙げられる。
この方法は単に微粉炭と輸送気体の固気二相流
を導入管と相対する分配室の上壁にぶつけ、分配
器内部の微粉炭を循環させ、それぞれの排出管入
口付近の微粉炭濃度を均一にして均等な分配を得
る方法であるが、それぞれの排出管の圧損差によ
り分配室内の流れが偏流する可能性がある。
また高圧系の場合に輸送管や分配器の径が小さ
くなり相対的に輸送気体量が増大しやすい等の考
慮がなされていない。
また、その問題を解決するため分配器内部に旋
回流を生じさせ各排出管の圧損に対して排出管入
口の差圧を高めてやり少量の輸送気体で均等な分
配を得ようとするものがあるが分室底部に微粉炭
が堆積して排出管入口をふさぐ欠点があつた。
〔発明の目的〕
本発明の目的は微粉炭を高濃度で気流輸送する
場合、その固気二相流を複数の場所へ分配する分
配器において、分配室内に粒子が堆積しないよう
な分配器を提供することにある。
〔発明の概要〕
管内を流れる固気二相流は輸送気体に対する固
体の量が多いほど管内の流動状態は均一性を欠
き、水平管の場合、管の底を流れたり曲管の場
合、管の外周を流れるようになる。そのため固気
二相流を単にＹ字管で分岐するような方法では均
等な分配は得られない。
そこで本発明では以下の構成により高濃度の固
気二相流を均等に分配する。
微粉炭の導入管を、分配室の下部に配置し、微
粉炭と輸送気体を垂直下方から上方へ向つて分配
室内に導入する。旋回ノズルを分配室の導入管入
口よりも上部に配置し分配室の中に旋回流を形成
できるようにする。排出管入口を分配室の軸に対
して放射状かつ同一水平面上に配置する。分配室
を前記導入管と分配室の接合部から上方へ向つ
て、その断面積が軸対称にゆるやかに広がるよう
な形状とする。
本発明によれば微粉炭の導入管を分配室の下部
に配置しているので、導入された微粉炭は浮遊状
態を保つ。このとき分配室下方から導入しても導
入管と分配室の接合部にエツジがあると分配室内
の固気二相流に対する空間ができ微粉炭の堆積層
をつくる。この堆積層が排出管の入口をふさぎ閉
塞するもがあらわれる。本発明では分配室断面積
を導入管断面積からゆるやかに広げているので微
粉炭は常に上昇方向の力をうけ堆積しない。浮遊
している微粉炭を旋回ノズルから吹出す旋回ガス
で分配室の軸に対して旋回させる
そして微粉炭、輸送気体、旋回気体を分配室の
円周方向によく分散し、分配室の軸に対して放射
状かつ同一水平面状に配置した排出管入口から排
出する。
〔発明の実施例〕
以下本発明の一実施例を図面によつて説明す
る。
第４図は噴流層ガス化装置における微粉炭供給
系の概略フローである。微粉炭ホツパ１内の微粉
炭（200メツシユ以下80重量％）１５をフイーダ
２により定量し、エゼクタ３において、窒素供給
装置４から供給される輸送用窒素５と混合する。
この固気二相流を導入管６を通して分配器７まで
運び複数（本例では８本）の排出管８に分配し噴
流層石炭ガス化炉９の石炭バーナから排出する。
また分配器７には旋回ガス１０または空気１４
用配管１６を接続する。
第１，２，３図に本発明による分配器７の詳細
構造を示す。微粉炭１５を輸送用窒素５によつて
導入管６から分配室１１に導入する。分配室１１
の垂直方向の断面積は導入管６からゆるやかに広
げてあるので粒子は常に浮上する方向に力を受け
る。このため分配室７底部への微粉炭粒子の堆積
を防ぎ浮遊して状態を保つ。一方、第２図に示し
たように分配室１１上部に同一水平面上に旋回ノ
ズル１２を複数個（本例では８個）あけており、
旋回用気体供給管１６から供給する旋回気体１０
又は15分配室内１１に吹出し旋回流を形成させ
る。分配室内１１の微粉炭をこの旋回流により旋
回させ、第３図に示すように分配室１１の垂直方
向の軸に対して同一水平面上に放射状に配置し
た、それぞれの排出管入口１３付近の微粉炭濃度
で強制的に等しくする。このため、それぞれの排
出管８の出口では等量の微粉炭を得ることができ
る。
第１，２，３図に示す分配室７を第４図に示す
微粉炭供給系へ適用したときの性能を第５図に示
す。
各排出管８出口での微粉炭排出量を知るため排
出管出口にバグフイルタを設けここで分配後の重
量を計つた。
常圧下で微粉炭約60Kg／ｈを0.6Kg／ｈの窒素
を用いて導入管５を通して分配器７まで送り旋回
用窒素流量を変化させた場合に各排出管８からの
微粉炭排出量のばらつきが、どのように変化する
かを第５図六角形のプロツトに示す。
横軸に窒素総流量、縦軸には各排出管８の石炭
排出量のばらつきの評価因子として
標準偏差＝√Σ（各排出管の石炭排出量−排
出量平均値）2／総排出量
なる値を示す。
できるだけ少ない搬送気体で均等な分配を得る
という目的から、分配器７の特性が第５図グラフ
の左下へ移行するほど好ましい。
旋回用窒素の流量をふやすほど石炭排出量のば
らつきが小さくなる。
搬送用窒素全量を導入管６から入れた場合（第
５図白丸のプロツト）従来例１と比較して、その
性能が優れており旋回の効果が確認された。
また、分配室１１上部に導入管を設置した場合
と下部に設定した場合の分配性能を比較するた
め、第６図に示すような分配器７を用い微粉炭を
分配器７上部から導入してみた。その結果、第７
図三角のプロツトに示す従来例２のように堆積し
た石炭を分散させるためには強い旋回力を必要と
し、本発明と同程度の標準偏差を得るには大量の
窒素を必要としていることが判つた。
その他の実施例を第８，９図に示す。この分配
器７では排出管入口１３と導入管６の間に旋回ノ
ズルを配置したところに特徴がある。輸送気体に
よつて微粉炭を導入管６を通して分配室１１内に
導入する。分配室１１を鉛直方向に上に向つて、
ゆるやかにその断面積を広げる構造としたので、
導入された微粉炭を堆積することなく、分配室１
１内に浮遊した状態を保つことができる。旋回気
体供給管１６から供給する旋回気体を旋回ノズル
を介して分配室１１内に吹出す。浮遊している微
粉炭にこの旋回力を与え、分配室１１の同一水平
面上に同周方向の微粉炭濃度を強制的に等しくす
る。旋回力をうけ分散した微粉炭を旋回ノズルの
上方に配置した排出管８から排出させる。排出管
入口が旋回を受けた固気二相流の下流に位置する
ため旋回の効果をより有効に生かすことができ
る。
また本発明による分配器７を石炭ガス化炉に適
用した実施例において、旋回気体として酸素、空
気成ガス等を用いれば、炉温の低下が比較的小さ
く（酸素の場合は上昇する）旋回気体量を増せる
ため分散性が良い領域で運転可能である。
特に旋回気体に酸素を用いた場合の案全性も分
配器より上流は保障され有効である。
旋回気体に窒素、空気を用いた場合との比較を
下表に示す。
[Field of Application of the Invention] The present invention relates to pneumatic transportation of pulverized coal, and provides a coal distributor suitable for evenly distributing a solid-gas two-phase flow of pulverized coal and transport gas, particularly when pulverized coal is highly concentrated. Regarding. [Background of the Invention] Currently, a system has been developed in which pulverized coal and a gasifying agent are supplied from a plurality of burners to a gasifier to form a swirling flow in a spouted bed gasifier. The purpose of this is to form a swirling flow in the gasifier to retain pulverized coal particles in the furnace, lengthen the reaction time, and increase gasification efficiency. If the balance of this swirling flow is disrupted, not only will the gasification efficiency deteriorate, but there will also be problems such as erosion of the furnace wall due to the burner flame reaching 1800℃ and damage to the burner itself due to overload. There was a strong desire for technology to distribute pulverized coal to Air transport is a typical method for transporting pulverized coal to the burner. Carrier gases include oxygen, air, nitrogen,
Examples include generated gas, but from the viewpoint of safety, gases with low reactivity are desirable. If a large amount of such gas is used, the inside of the furnace will be cooled. In addition, the generated gas calorific value is reduced, resulting in a decrease in efficiency. Furthermore, there is also the drawback that the gas purification equipment that separates this gas from the produced gas is complicated. Further, even if water vapor, air, generated gas, etc. are used as the transport gas, it is preferable that the amount of gas be small in order to suppress a drop in the temperature inside the furnace. That is, there is a need to develop a distributor that can achieve even distribution using as little carrier gas as possible. In response to this, U.S. Patent No. 3204942
The number is mentioned. This method simply impinges a solid-gas two-phase flow of pulverized coal and transport gas against the upper wall of the distribution chamber facing the inlet pipe, circulates the pulverized coal inside the distributor, and reduces the pulverized coal concentration near the inlet of each discharge pipe. Although this method achieves uniform distribution, there is a possibility that the flow within the distribution chamber will be uneven due to the pressure drop difference between the respective discharge pipes. Furthermore, no consideration is given to the fact that in the case of a high-pressure system, the diameters of transport pipes and distributors become smaller and the amount of gas to be transported tends to increase relatively. In addition, in order to solve this problem, a swirling flow is generated inside the distributor to increase the differential pressure at the inlet of the discharge pipe to compensate for the pressure loss in each discharge pipe, thereby achieving even distribution with a small amount of transport gas. However, there was a drawback that pulverized coal accumulated at the bottom of the compartment and blocked the outlet of the discharge pipe. [Object of the Invention] The object of the present invention is to provide a distributor that prevents particles from accumulating in the distribution chamber in a distributor that distributes the solid-gas two-phase flow to a plurality of locations when pulverized coal is transported by air at a high concentration. It is about providing. [Summary of the Invention] In a solid-gas two-phase flow flowing inside a pipe, the larger the amount of solids relative to the transport gas, the less uniform the flow state inside the pipe. It begins to flow around the periphery of. Therefore, even distribution cannot be obtained by simply branching the solid-gas two-phase flow using a Y-shaped pipe. Therefore, in the present invention, a high concentration solid-gas two-phase flow is evenly distributed using the following configuration. A pulverized coal introduction pipe is arranged at the lower part of the distribution chamber, and the pulverized coal and transport gas are introduced into the distribution chamber from vertically downward to upward. The swirling nozzle is arranged above the inlet of the introduction pipe of the distribution chamber to form a swirling flow in the distribution chamber. The outlet pipe inlet is arranged radially and co-horizontally with respect to the axis of the distribution chamber. The distribution chamber is shaped such that its cross-sectional area gradually widens axially symmetrically upward from the joint between the introduction pipe and the distribution chamber. According to the present invention, since the pulverized coal introduction pipe is arranged at the lower part of the distribution chamber, the introduced pulverized coal remains in a floating state. At this time, even if the coal is introduced from below the distribution chamber, if there is an edge at the joint between the introduction pipe and the distribution chamber, a space will be created for the solid-gas two-phase flow in the distribution chamber, creating a deposited layer of pulverized coal. This deposited layer appears to block the entrance of the discharge pipe. In the present invention, since the cross-sectional area of the distribution chamber is gradually expanded from the cross-sectional area of the introduction pipe, the pulverized coal is always subjected to upward force and does not accumulate. The floating pulverized coal is swirled around the axis of the distribution chamber by the swirling gas blown out from the swirling nozzle.Then, the pulverized coal, transport gas, and swirling gas are well dispersed in the circumferential direction of the distribution chamber, and the pulverized coal is swirled around the axis of the distribution chamber. It is discharged from the discharge pipe inlets arranged radially and in the same horizontal plane. [Embodiment of the Invention] An embodiment of the present invention will be described below with reference to the drawings. FIG. 4 is a schematic flowchart of a pulverized coal supply system in a spouted bed gasifier. Pulverized coal (less than 200 mesh, 80% by weight) 15 in the pulverized coal hopper 1 is measured by the feeder 2, and mixed with nitrogen 5 for transportation supplied from the nitrogen supply device 4 in the ejector 3.
This solid-gas two-phase flow is carried through the inlet pipe 6 to the distributor 7, distributed to a plurality of (eight in this example) discharge pipes 8, and discharged from the coal burner of the spouted bed coal gasifier 9. In addition, the distributor 7 has swirling gas 10 or air 14.
Connect the pipe 16 for use. 1, 2 and 3 show the detailed structure of the distributor 7 according to the invention. Pulverized coal 15 is introduced into the distribution chamber 11 through the introduction pipe 6 by means of transporting nitrogen 5. Distribution room 11
Since the vertical cross-sectional area of is gradually expanded from the introduction tube 6, the particles are always subjected to a force in the direction of floating. This prevents the pulverized coal particles from accumulating on the bottom of the distribution chamber 7 and keeps them floating. On the other hand, as shown in FIG. 2, a plurality of (eight in this example) rotating nozzles 12 are provided on the same horizontal plane above the distribution chamber 11.
Swirling gas 10 supplied from swirling gas supply pipe 16
Alternatively, a blowout swirl flow is formed in the distribution chamber 11. The pulverized coal in the distribution chamber 11 is swirled by this swirling flow, and as shown in FIG. Force equalization by charcoal concentration. Therefore, the same amount of pulverized coal can be obtained at the outlet of each discharge pipe 8. FIG. 5 shows the performance when the distribution chamber 7 shown in FIGS. 1, 2, and 3 is applied to the pulverized coal supply system shown in FIG. 4. In order to know the amount of pulverized coal discharged at the outlet of each discharge pipe 8, a bag filter was installed at the discharge pipe outlet and the weight after distribution was measured here. About 60 kg/h of pulverized coal is sent to the distributor 7 through the inlet pipe 5 using 0.6 kg/h of nitrogen under normal pressure, and when the swirling nitrogen flow rate is varied, the amount of pulverized coal discharged from each discharge pipe 8 varies. The hexagonal plot in Figure 5 shows how this changes. The horizontal axis is the total nitrogen flow rate, and the vertical axis is the evaluation factor for the dispersion of the coal discharge amount of each discharge pipe 8. Standard deviation = √Σ (coal discharge amount of each discharge pipe - average value of discharge amount) 2 / total discharge amount Show value. For the purpose of achieving even distribution with as little carrier gas as possible, it is preferable that the characteristics of the distributor 7 shift toward the lower left of the graph in FIG. 5. As the swirling nitrogen flow rate increases, the variation in coal discharge becomes smaller. When the entire amount of nitrogen for transport was introduced from the inlet tube 6 (plot of white circles in FIG. 5), the performance was superior compared to Conventional Example 1, and the swirling effect was confirmed. In addition, in order to compare the distribution performance when the introduction pipe is installed at the upper part of the distribution chamber 11 and when it is set at the lower part, pulverized coal was introduced from the upper part of the distributor 7 using the distributor 7 shown in Fig. 6. saw. As a result, the seventh
It can be seen that, as in Conventional Example 2 shown in the triangular plot in the figure, a strong swirling force is required to disperse the accumulated coal, and a large amount of nitrogen is required to obtain the same standard deviation as in the present invention. Ivy. Other embodiments are shown in FIGS. 8 and 9. This distributor 7 is characterized in that a swirling nozzle is disposed between the discharge pipe inlet 13 and the introduction pipe 6. The pulverized coal is introduced into the distribution chamber 11 through the inlet pipe 6 by means of a transport gas. Directing the distribution chamber 11 vertically upward,
Because it has a structure that gently expands its cross-sectional area,
distribution chamber 1 without depositing the introduced pulverized coal.
1 can be maintained in a floating state. The swirling gas supplied from the swirling gas supply pipe 16 is blown out into the distribution chamber 11 through the swirling nozzle. This swirling force is applied to the floating pulverized coal to forcibly equalize the pulverized coal concentration in the same circumferential direction on the same horizontal plane of the distribution chamber 11. The pulverized coal dispersed by the swirling force is discharged from a discharge pipe 8 disposed above the swirling nozzle. Since the discharge pipe inlet is located downstream of the swirled solid-gas two-phase flow, the swirling effect can be utilized more effectively. Further, in an embodiment in which the distributor 7 according to the present invention is applied to a coal gasification furnace, if oxygen, aerobic gas, etc. are used as the swirling gas, the decrease in the furnace temperature is relatively small (in the case of oxygen, it increases). Since the amount can be increased, it is possible to operate in a region with good dispersibility. Particularly when oxygen is used as the swirling gas, integrity is ensured upstream of the distributor and is effective. A comparison between using nitrogen and air as the swirling gas is shown in the table below.
本発明によれば、分配室内に微粉炭の堆積層を
つくることなく、分配室内に分散させるので微粉
炭と搬送気体の固気二相流の分配において、より
少い気体を用いて微粉炭を同量ずつ複数の管に分
ける効果がある。
According to the present invention, since the pulverized coal is dispersed within the distribution chamber without creating a layer of pulverized coal in the distribution chamber, less gas is used to distribute the pulverized coal in the solid-gas two-phase flow of the pulverized coal and the carrier gas. It has the effect of dividing the same amount into multiple tubes.
第１図は本発明になる分配器の側断面、第２図
は第１図のＡ−Ａ断面図、第３図は第１図のＢ−
Ｂ断面図である。第４図は石炭ガス化装置におけ
る微粉炭供給系の概略フロー、第５図は第１，
２，３図に示した分配器の特性図、第６図は導入
管を分配器上部にもつ分配器の側断面図、第７図
はその特性図、第８図はその他の実施例の側断面
図、第９図はそのＣ−Ｃ断面図である。
５……輸送用窒素、６……導入管、８……排出
管、１０……旋回用窒素、１１……分配室、１２
……旋回ノズル、１３……排出管入口、１４……
旋回用空気、１５……微粉炭、１６……旋回気体
供給管。
FIG. 1 is a side sectional view of the distributor according to the present invention, FIG. 2 is a sectional view taken along line AA in FIG. 1, and FIG. 3 is a sectional view taken along line B--
It is a sectional view of B. Figure 4 shows the schematic flow of the pulverized coal supply system in the coal gasifier, and Figure 5 shows the flow of the pulverized coal supply system in the coal gasifier.
Characteristic diagrams of the distributor shown in Figures 2 and 3, Figure 6 is a side cross-sectional view of the distributor with an inlet pipe at the top of the distributor, Figure 7 is its characteristic diagram, and Figure 8 is a side view of another embodiment. A sectional view, FIG. 9 is a sectional view taken along line C-C. 5...Nitrogen for transportation, 6...Introduction pipe, 8...Discharge pipe, 10...Nitrogen for swirling, 11...Distribution chamber, 12
...Swivel nozzle, 13...Discharge pipe inlet, 14...
Swirling air, 15...pulverized coal, 16... swirling gas supply pipe.
Claims (1)
固気二相流の複数の排気管及び分配室を有する微
粉炭の固気二相流分配器において、導入管を分配
室の下部に有し、微粉炭と輸送気体の固気二相流
を鉛直下方から上方へ向つて流れこむように配置
し、旋回ノズルを分配室の導入管よりも上部に分
配室の軸方向に対して旋回流が形成されるような
方向に配置し、排出管入口を分配室の軸に対して
放射状かつ同一水平面上に配置し、分配室を前記
導入管と分配室の接合部から上方に向つて、その
断面積がゆるやかに広がるような形状としたとを
特徴とする石炭分配器。1. An introduction pipe for solid-gas two-phase flow of pulverized coal and transport gas,
In a pulverized coal solid-gas two-phase flow distributor having a plurality of exhaust pipes and distribution chambers for solid-gas two-phase flow, the inlet pipe is located at the bottom of the distribution chamber, and the solid-gas two-phase flow of pulverized coal and transport gas is The swirling nozzle is arranged so that the flow flows in from vertically downward to upward, the swirling nozzle is arranged above the introduction pipe of the distribution chamber in a direction that creates a swirling flow in the axial direction of the distribution chamber, and the discharge pipe inlet is The distribution chamber is arranged radially and on the same horizontal plane with respect to the axis of the distribution chamber, and the distribution chamber is shaped so that its cross-sectional area gradually expands upward from the joint between the introduction pipe and the distribution chamber. coal distributor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16413785A JPS6225166A (en) | 1985-07-26 | 1985-07-26 | Coal distributor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16413785A JPS6225166A (en) | 1985-07-26 | 1985-07-26 | Coal distributor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6225166A JPS6225166A (en) | 1987-02-03 |
| JPH0250157B2 true JPH0250157B2 (en) | 1990-11-01 |
Family
ID=15787449
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16413785A Granted JPS6225166A (en) | 1985-07-26 | 1985-07-26 | Coal distributor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6225166A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0631348B2 (en) * | 1987-07-17 | 1994-04-27 | 株式会社日立製作所 | Generator Charging Device for Gasification Plant |
| JP2010145071A (en) * | 2008-12-22 | 2010-07-01 | Electric Power Dev Co Ltd | Distributor for powder body conveyed by air flow and distribution method |
| CN103201202B (en) * | 2010-11-16 | 2016-04-20 | 日清制粉集团本社股份有限公司 | Powder distribution device |
-
1985
- 1985-07-26 JP JP16413785A patent/JPS6225166A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6225166A (en) | 1987-02-03 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |