JPS6059955B2 - Fluidized bed gasifier - Google Patents
Fluidized bed gasifierInfo
- Publication number
- JPS6059955B2 JPS6059955B2 JP11517177A JP11517177A JPS6059955B2 JP S6059955 B2 JPS6059955 B2 JP S6059955B2 JP 11517177 A JP11517177 A JP 11517177A JP 11517177 A JP11517177 A JP 11517177A JP S6059955 B2 JPS6059955 B2 JP S6059955B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- plate portion
- conical plate
- central passage
- passage hole
- 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
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/44—Fluidisation grids
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Description
【発明の詳細な説明】
本発明は流動層方式ガス化炉に係り、特に、流動層内
での凝集物（クリンカ）の発生を防止するに好適な流動
層方式ガス化炉の分散板に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a fluidized bed gasifier, and in particular to a dispersion plate for a fluidized bed gasifier suitable for preventing the generation of aggregates (clinker) in the fluidized bed. It is.
従来一般に、流動層方式ガス化炉の流動層下部には分
散板が設置されており、例えば、石炭ガス化炉に対する
従来のものは、平板多孔板のもの、あるいは漏斗状のも
ので分散板本体の円錐形板の頂角が１６００前後の比較
的緩やかな角度のものの中央に凝集物抜き出し用の口を
有するものであつた。Conventionally, a dispersion plate is generally installed at the bottom of the fluidized bed of a fluidized bed gasifier.For example, the conventional dispersion plate for coal gasifiers is a flat perforated plate or a funnel-shaped dispersion plate. The conical plate had a relatively gentle apex angle of about 1600 mm and had an opening for extracting aggregates in the center.
そして、これらの分散板においては、鉛直方向または分
散板面に直角方向に、反応ガスを流動層内へ吹き込むた
めの多数の小孔が板面上ほぼ均等に配置されていた。
ところが、このような従来の分散板にあつては、流動化
用のガス化剤の吹き込み用の多数の小孔が、鉛直方向ま
たは分散板面に直角方向に穿孔されているため、各小孔
間の板面上はガスの流れも緩やかで、被ガス化物てある
石炭粒子の動かない、よどみ部が発生し、反応が不均一
となる欠点があつた。In these distribution plates, a large number of small holes for blowing the reaction gas into the fluidized bed were arranged almost evenly on the plate surface in a vertical direction or in a direction perpendicular to the surface of the distribution plate.
However, in such conventional dispersion plates, a large number of small holes for injecting the gasifying agent for fluidization are perforated vertically or perpendicularly to the surface of the dispersion plate. The flow of gas is slow on the surface of the plates between the two, creating stagnation areas where the coal particles that are gasified do not move, resulting in non-uniform reactions.
更に、石炭のガス化温度は、１０００〜１１００℃の高
温であるので、このような高温下に灰分を放置すると凝
集物が生成し、一層反応が不均一になるものであつた。
また、このような欠点に加えて、生成した凝集物も、分
散板上を中央通路孔の方向に移動する際、このよどみ部
にさえぎられて凝集物を抜き出す中央通路孔に集中でき
す、中途で停滞する傾向があり、この停滞した凝集物は
次第に生長し、遂には流動層全体の流動を阻害・し、操
業不能に陥れる危険性のあるものであつた。 本発明の
目的は、上記した従来技術の欠点をなくし、流動層内で
の凝集物の生成防止、および、万一凝集物が生成した場
合には、生成した凝集物；を連続排出することを可能と
する流動層方式ガス化炉を提供するにある。Furthermore, since the gasification temperature of coal is a high temperature of 1,000 to 1,100°C, if the ash is left to stand at such a high temperature, aggregates will form, making the reaction even more uneven.
In addition to these drawbacks, when the generated aggregates move on the distribution plate in the direction of the central passage hole, they are blocked by this stagnation part and cannot concentrate at the central passage hole from which the aggregates are extracted. This stagnant agglomerate gradually grows and eventually obstructs the flow of the entire fluidized bed, posing the danger of making it impossible to operate. The purpose of the present invention is to eliminate the above-mentioned drawbacks of the prior art, to prevent the formation of aggregates in a fluidized bed, and to continuously discharge the generated aggregates in the event that they occur. The purpose of the present invention is to provide a fluidized bed gasifier that enables the use of fluidized bed gasifiers.
本発明の特徴とするところは、流動層方式ガス化炉にお
いて、漏斗状分散板の円錐板部における多数の小孔を、
円錐板部の水平断面円の半径方向に対し一定の角度に穿
孔し、円錐板部の先端に中央通路孔を設け、中央通路孔
を通過するガスの流速を、流動層内の最大粒子の終端速
度の１．５〜３倍にしてあることである。以下に実施例
により、図面を参照して、本発明を更に詳述する。The feature of the present invention is that in a fluidized bed gasifier, a large number of small holes in the conical plate part of the funnel-shaped distribution plate are
Holes are bored at a constant angle with respect to the radial direction of the horizontal cross section of the conical plate, and a central passage hole is provided at the tip of the conical plate, so that the flow velocity of the gas passing through the central passage hole is adjusted to the end of the largest particle in the fluidized bed. The speed is 1.5 to 3 times higher. The present invention will be explained in more detail below by way of Examples and with reference to the drawings.
第１図は本発明である流動層方式ガス化炉の一実施例に
なる流動層方式石炭ガス化炉の概念を示す炉の下部縦断
面図である。FIG. 1 is a vertical sectional view of the lower part of a furnace showing the concept of a fluidized bed coal gasifier which is an embodiment of the fluidized bed gasifier according to the present invention.
第１図において、被ガス化物である粒状石炭またはチヤ
ーは、石炭ガス化炉本体２における石炭送入口３より炉
内に供給され、空気（または酸素）、スチーム等のガス
化剤と反応後、灰分排出口４より灰分を排出する。In FIG. 1, granular coal or chir, which is a substance to be gasified, is supplied into the furnace from a coal inlet 3 in a coal gasifier main body 2, and after reacting with a gasifying agent such as air (or oxygen) or steam, Ash is discharged from the ash discharge port 4.
炉内で生成した凝集物は中央通路孔１０から通路導管７
を経て炉外へ排出される。一方、ガス化剤てある空気ま
たは酸素とスチームとの混合ガスは、その一部が漏斗状
分散板１の多数の小孔を経由して流動層内１２へ旋回す
るように、炉本体２の下方の旋回ガス送入口５より分散
板１の下方へ送入され、混合ガスの他の部分が分散板の
中央通路孔１０から流動層内へ噴流吹き込みするように
、通路導管７内へ噴流ガス送入口６より送入されるよう
になされる。The aggregates generated in the furnace are transferred from the central passage hole 10 to the passage conduit 7.
After that, it is discharged outside the furnace. On the other hand, the gasification agent, air or a mixed gas of oxygen and steam, is placed in the furnace body 2 in such a way that a part of it swirls into the fluidized bed 12 via the large number of small holes in the funnel-shaped distribution plate 1. A jet of gas is fed into the lower part of the distribution plate 1 from the lower swirling gas inlet 5 and into the passage conduit 7 such that the other part of the mixed gas is blown into the fluidized bed from the central passage hole 10 of the distribution plate. It is configured to be fed through the feeding port 6.
第２〜４図は、第１図の漏斗状分散板１の詳細図である
。2 to 4 are detailed views of the funnel-shaped dispersion plate 1 of FIG. 1.
この漏斗状分散板１は、第３図の縦断面図に明．示され
ているように、円錐板部９の円錐の頂角は６０〜１５０
よの範囲のものであり、円維板部の周縁にサポート８が
備えられ、先端に中央通路孔１０が設けられている。This funnel-shaped dispersion plate 1 is clearly shown in the longitudinal sectional view of FIG. As shown, the apex angle of the cone of the conical plate portion 9 is 60 to 150
A support 8 is provided on the periphery of the circular fiber plate portion, and a central passage hole 10 is provided at the tip.
中央通路孔１０からは、下方から送られたガス！化剤が
流動層内へ噴流ガスとして吹き込まれ、流動層の上下方
向の攪伴に寄与すると共に、中央通路孔１０における噴
流ガスの流速を、被ガス化物である供給石炭の最大粒子
に対する終端流速の１．５〜３倍程度にすることにより
噴流ガスの噴入ｚ口部での凝集物の分離にも寄与する。Gas is sent from below through the central passage hole 10! The agent is blown into the fluidized bed as a jet gas, contributing to vertical agitation of the fluidized bed, and the flow velocity of the jet gas in the central passage hole 10 is adjusted to the final flow velocity with respect to the largest particle of the coal to be gasified. By making it approximately 1.5 to 3 times as large as 1.5 to 3 times, it also contributes to the separation of aggregates at the z-injection port of the jet gas.
これにより、通常粒子の落下を防止する一方、流動層内
における凝集物により上記のガス流速では落下防止でき
なくなつた凝集物が生成した場合は、それらの凝集物の
みが中央通路孔１０から炉外へ連続的に抜き出されるこ
とが可能となる。分散板本体の円維板部９には、特に第
４図の横断面拡大図および第２図の平面図に明らかなよ
うに、多数の小孔１１，１１・・・・・・が一様の配置
に穿孔されている。While this usually prevents the particles from falling, if aggregates are generated in the fluidized bed that cannot be prevented from falling at the above gas flow rate, only those aggregates will be transported from the central passage hole 10 to the furnace. It becomes possible to be continuously extracted to the outside. In the circular fiber plate portion 9 of the dispersion plate main body, a large number of small holes 11, 11, . perforated in the arrangement of.
それぞれの小孔１１は直径が１〜５顛の範囲の実質的に
同一直径のもので、円錐板部９の全面にほぼ均一に配置
されて、各小孔１１は水平断面円の半径方向に対する角
度が４５〜６０置）の角度の範囲の実質的に同一の角度
になされたものであることが好ましい。分散板における
このような多数の小孔１１の配置、各小孔１１の寸法お
よび方向性により、分散板上にガスの旋回流を形成させ
、そのガス流によ・つて流動層内の粒子を激しく攪拌す
ることができるのである。The respective small holes 11 have substantially the same diameter in the range of 1 to 5 square meters, and are arranged almost uniformly over the entire surface of the conical plate portion 9, so that each small hole 11 has a diameter in the range of 1 to 5 square meters, and is arranged almost uniformly over the entire surface of the conical plate portion 9. Preferably, the angles are substantially the same in the range of 45 to 60 angles. Due to the arrangement of the large number of small holes 11 in the distribution plate, and the size and direction of each small hole 11, a swirling flow of gas is formed on the distribution plate, and the particles in the fluidized bed are dispersed by the gas flow. It can be stirred vigorously.
以上の説明に明らかなように、本発明によれば、分散板
に一定角度穿孔するのみで、層内に内装物を設けること
なく旋回流を与えることができるので、流動化の停滞部
を生じることなく層内粒子全体に旋回流を与えることが
可能となる。As is clear from the above description, according to the present invention, a swirling flow can be provided by simply drilling holes at a certain angle in the distribution plate without providing any internal material in the layer, which causes stagnation of fluidization. It becomes possible to give a swirling flow to the entire particles in the layer without causing any turbulence.
このため、分散板上の粒子のよぼみ部が排除できると共
に、円周方向の攪拌力により凝集物の生成の防止、生成
凝集物の破砕、更には破砕不能の凝集物の連続的抜き出
しが可能てあり、従つて流動層内に凝集物を存在させる
ことなく運転できるので、特に長期間連続運転を可能と
する点において著しく効果のあるものである。また、旋
回力を与えることで従来融点付近温度（１０００〜１１
００′Ｃ）で運転していたものが、５０〜１００℃層内
温度を上昇させることができるため、被ガス化物の未燃
分をなくして全体のガス化効率を上げることができる。Therefore, it is possible to eliminate the concave part of the particles on the dispersion plate, and the stirring force in the circumferential direction can prevent the formation of aggregates, crush the formed aggregates, and furthermore, it is possible to continuously extract unbreakable aggregates. Therefore, it is possible to operate without the presence of aggregates in the fluidized bed, which is particularly effective in enabling continuous operation for a long period of time. In addition, by applying a swirling force, the temperature near the conventional melting point (1000 to 11
Since the temperature inside the layer can be increased by 50 to 100°C, the overall gasification efficiency can be increased by eliminating unburned matter of the gasified material.
第１図は本発明の概念を説明するために、本発明の一実
施例になる流動層方式石炭ガス化炉における漏斗状分散
板部分の縦断面図、第２図はその漏斗状分散板の半裁平
面図、第３図はその漏斗状分散板の縦断面図、第４図は
第３図の線■−■による断面拡大図である。In order to explain the concept of the present invention, Fig. 1 is a longitudinal cross-sectional view of a funnel-shaped dispersion plate portion in a fluidized bed type coal gasifier that is an embodiment of the present invention, and Fig. 2 is a longitudinal sectional view of the funnel-shaped dispersion plate portion. FIG. 3 is a longitudinal cross-sectional view of the funnel-shaped dispersion plate, and FIG. 4 is an enlarged cross-sectional view taken along line ■--■ in FIG. 3.
Claims (1)
記円錐板部の水平断面円の半径方向に対して一定の角度
に穿孔し、前記円錐板部の先端に中央通路孔を設け、前
記中央通路孔を通過するガスの流速が、流動層内の最大
粒子の終端速度の１．５〜３倍になるようになされたこ
とを特徴とする流動層方式ガス化炉。 ２ 前記円錐板部の円錐の頂角は６０〜１５０°である
ことを特徴とする特許請求の範囲第１項記載の流動層方
式ガス化炉。 ３ 前記一定の角度は４５〜６０°であり、前記多数の
小孔の直径は１．０〜５．０ｍｍであることを特徴とす
る特許請求の範囲第１項、第２項記載の流動層方式ガス
化炉。[Scope of Claims] 1. A large number of small holes in the conical plate portion of the funnel-shaped dispersion plate are bored at a constant angle with respect to the radial direction of the horizontal cross-sectional circle of the conical plate portion, and the holes are formed at the tip of the conical plate portion. Fluidized bed gasification characterized in that a central passage hole is provided, and the flow rate of gas passing through the central passage hole is 1.5 to 3 times the terminal velocity of the largest particle in the fluidized bed. Furnace. 2. The fluidized bed gasifier according to claim 1, wherein the apex angle of the cone of the conical plate portion is 60 to 150°. 3. The fluidized bed according to claims 1 and 2, wherein the certain angle is 45 to 60 degrees, and the diameter of the large number of small holes is 1.0 to 5.0 mm. Method gasifier.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11517177A JPS6059955B2 (en) | 1977-09-27 | 1977-09-27 | Fluidized bed gasifier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11517177A JPS6059955B2 (en) | 1977-09-27 | 1977-09-27 | Fluidized bed gasifier |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5448809A JPS5448809A (en) | 1979-04-17 |
| JPS6059955B2 true JPS6059955B2 (en) | 1985-12-27 |
Family
ID=14656092
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11517177A Expired JPS6059955B2 (en) | 1977-09-27 | 1977-09-27 | Fluidized bed gasifier |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6059955B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103897745A (en) * | 2014-03-28 | 2014-07-02 | 新奥科技发展有限公司 | Fluidized bed distribution plate, fluidized bed reactor and gasification method thereof |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5818940U (en) * | 1981-07-28 | 1983-02-05 | バブコツク日立株式会社 | Low calorie coal gasifier |
| JPS5980439U (en) * | 1982-11-25 | 1984-05-31 | バブコツク日立株式会社 | Fluidized bed equipment |
| JPS61200197A (en) * | 1985-03-01 | 1986-09-04 | Nippon Kokan Kk <Nkk> | Blowing of gasifying agent into coal gasification furnace |
| TR201010131T1 (en) * | 2008-06-05 | 2011-10-21 | Synthesis Energy Systems, Inc. | Fluid bed gasifier with solids discharge and sorting device. |
| US20150064089A1 (en) * | 2013-08-29 | 2015-03-05 | Honeywell International Inc. | Fluidized bed reactors including conical gas distributors and related methods of fluorination |
| US9511339B2 (en) * | 2013-08-30 | 2016-12-06 | Honeywell International Inc. | Series coupled fluidized bed reactor units including cyclonic plenum assemblies and related methods of hydrofluorination |
| CN104178224B (en) * | 2014-08-07 | 2017-04-05 | 新奥科技发展有限公司 | A kind of gas distributor, gasification furnace and carbonaceous material gasification process |
-
1977
- 1977-09-27 JP JP11517177A patent/JPS6059955B2/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103897745A (en) * | 2014-03-28 | 2014-07-02 | 新奥科技发展有限公司 | Fluidized bed distribution plate, fluidized bed reactor and gasification method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5448809A (en) | 1979-04-17 |
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