JPH0643589B2 - Coal gasifier - Google Patents
Coal gasifierInfo
- Publication number
- JPH0643589B2 JPH0643589B2 JP60170747A JP17074785A JPH0643589B2 JP H0643589 B2 JPH0643589 B2 JP H0643589B2 JP 60170747 A JP60170747 A JP 60170747A JP 17074785 A JP17074785 A JP 17074785A JP H0643589 B2 JPH0643589 B2 JP H0643589B2
- Authority
- JP
- Japan
- Prior art keywords
- burner
- coal
- nozzle
- oxidant
- oxidizer
- 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 - Fee Related
Links
- 239000003245 coal Substances 0.000 title claims description 57
- 239000007800 oxidant agent Substances 0.000 claims description 44
- 238000002309 gasification Methods 0.000 claims description 37
- 238000006243 chemical reaction Methods 0.000 claims description 26
- 230000001590 oxidative effect Effects 0.000 claims description 22
- 239000002893 slag Substances 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 15
- 229910002091 carbon monoxide Inorganic materials 0.000 description 14
- 239000007789 gas Substances 0.000 description 14
- 238000000034 method Methods 0.000 description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- 230000000149 penetrating effect Effects 0.000 description 7
- 238000002156 mixing Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000010883 coal ash Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000013016 damping Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- -1 steam Chemical compound 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は石炭ガス化炉に係り、特に反応速度が大きく、
短時間で高ガス化効率を達成しうる噴流層石炭ガス化炉
に関する。Description: TECHNICAL FIELD The present invention relates to a coal gasification furnace, and in particular, has a large reaction rate,
The present invention relates to a spouted bed coal gasification furnace that can achieve high gasification efficiency in a short time.
（従来の技術） 従来、石炭のガス化炉には、固定層、流動層、噴流層等
の装置がある。この中で噴流層、石炭灰の融点以上
（１．３００℃〜１．６００℃）に温度を高めるので、
他の方式に比較し、カーボンのガス化率や、水素
（Ｈ２）及び一酸化炭素（ＣＯ）の収量等を高めやす
く、また、公害性の副生物が少ないことから、合成ガス
及びガスタービン、スチームタービン複合発電用原料ガ
スの製造に好適である。(Prior Art) Conventionally, a coal gasification furnace includes devices such as a fixed bed, a fluidized bed, and a spouted bed. In this, because the temperature is raised above the melting point of the spouted bed and coal ash (1.300 ° C to 1.600 ° C),
Compared to other methods, it is easy to increase the gasification rate of carbon, the yield of hydrogen (H 2 ) and carbon monoxide (CO), etc., and there are few pollutant by-products. It is suitable for manufacturing a raw material gas for steam turbine combined cycle power generation.
噴流層には、微粉炭またはチャー（ガスと共に飛散する
カーボン粒子）とガス化剤（酸素、空気スチーム等）を
同じバーナより吹き込む１段方式の装置と、前記のバー
ナに加えて、微粉炭またはチャーだけを単独に吹き込む
バーナを設置する２段方式の装置がある。In the spouted bed, a pulverized coal or char (carbon particles that scatter with gas) and a gasifying agent (oxygen, air steam, etc.) are blown from the same burner in a one-stage system, and in addition to the burner, pulverized coal or There is a two-stage system that installs a burner that blows only char alone.
石炭ガス化反応は大別すると以下に示す方式で表され
る。The coal gasification reaction is roughly classified into the following methods.
石炭→チャー、Ｈ２、ＣＯ、ＣＯ２、ＣＨ４ …（１） チャー＋Ｏ２→ＣＯ２、ＣＯ、Ｈ２ …（２） 石炭 ＋Ｏ２→ＣＯ、ＣＯ２、Ｈ２ …（３） （１）式は熱分解反応であり、前記した２段方式におい
て微粉炭だけを単独に吹き込むバーナによって起こりや
すい。（１）式と（２）式の反応を明らかに区別して併
発させる方式の代表例としては公知の如く、米国のＢＩ
−ＧＡＳプロセスがある。また、石炭バーナから石炭と
ガス化剤を同時に供給し、意図的に（１）式と（２）式
とを区別しない（３）式の反応式によるプロセスがあ
り、代表例としてはＴｅｘａｃｏプロセス、、Ｓｈｅｌ
ｌ−Ｋｏｐｐｅｒｓプロセス等がある。Coal → Char, H 2 , CO, CO 2 , CH 4 (1) Char + O 2 → CO 2 , CO, H 2 (2) Coal + O 2 → CO, CO 2 , H 2 (3) (1) ) Is a thermal decomposition reaction, and is likely to occur by a burner in which only pulverized coal is blown into the two-stage system. As is well known as a representative example of a system in which the reactions of the formulas (1) and (2) are clearly distinguished and co-occurred, BI in the United States is known.
-There is a GAS process. Further, there is a process by a reaction formula of (3) in which coal and a gasifying agent are simultaneously supplied from a coal burner and the formulas (1) and (2) are not intentionally distinguished, and a typical example is a Texaco process, , Shel
1-Koppers process and the like.
いずれの場合も、カーボンのガス化率（ガスとして生成
するカーボン量の石炭中のカーボン量に対する比率）を
向上するための種々の試みがなされている。その最も代
表的な方法としては、ガスと共に飛散するチャーを回収
して再びガス化炉に戻してガス化する、所謂チャー再循
環方法があるが、この方法は、循環のためのポンプ、バ
ルブ、タンク等の機器類を必要とするため、ガス化プロ
セスを複雑にし、コスト高になる。また、チャーをガス
化炉に供給するためには搬送用ガスを必要とするが、こ
れに使用される窒素（Ｎ２）、スチーム、ＣＯ２、生成
ガス等の一部等はガス化反応に寄与せず、これらのガス
をガス化炉に必要以上に供給することは好ましくない。
さらに、循環するチャーの量が多くなるとガス化炉内や
ガス化炉出口から先の配管等の摩耗量が増大する。In any case, various attempts have been made to improve the gasification rate of carbon (the ratio of the amount of carbon produced as gas to the amount of carbon in coal). The most typical method is a so-called char recirculation method of collecting char scattered with gas and returning it to the gasifier again to gasify it. This method is a pump for circulation, a valve, Since equipment such as a tank is required, the gasification process is complicated and the cost becomes high. Further, in order to supply the char to the gasification furnace, a carrier gas is required, but nitrogen (N 2 ), steam, CO 2 , a part of the produced gas, etc. used for this are used in the gasification reaction. It is not preferable to supply these gases to the gasification furnace more than necessary without contributing.
Further, when the amount of circulating char is large, the amount of wear in the gasification furnace and the piping and the like from the gasification furnace outlet to the end increases.
そこで、本発明者等はチャーの再循環を省略するか、ま
たは循環量の著しい低減を図ることができる新しい石炭
ガス化法を提案した（例えば特願昭５８−４７１６２お
よび特願昭５８−５０４９６）。この方法は、第７図に
示すように、微粉炭１５と酸化剤１６を供給するバーナ
１７および１９を炉本体１３の上段および下段に設置
し、酸化剤１６を上段バーナ１７には少なく、下段バー
ナ１９には多く投入したり（特願昭５８−４７１６
２）、または下段バーナ１９の微粉炭を吹き込む仮想円
の径を上段バーナ１７の微粉炭を吹込で仮想円のそれよ
りも小さく設定するものである（特願昭５８−５０４９
６）。なお、図中、１１は生成ガス、１２は生成ガス排
出口、１４は断熱材、１８はガス化領域、２２および２
４は水入口および出口、２５は水である。Therefore, the present inventors have proposed a new coal gasification method capable of omitting char recirculation or significantly reducing the circulation amount (for example, Japanese Patent Application Nos. 58-47162 and 58-50496). ). In this method, as shown in FIG. 7, burners 17 and 19 for supplying pulverized coal 15 and an oxidizer 16 are installed in the upper and lower stages of the furnace body 13, and the oxidizer 16 is small in the upper burner 17 Many are put in the burner 19 (Japanese Patent Application No. 58-4716).
2), or the diameter of the virtual circle in which the pulverized coal of the lower burner 19 is blown is set to be smaller than that of the virtual circle by blowing the pulverized coal of the upper burner 17 (Japanese Patent Application No. 58-5049).
6). In the figure, 11 is a generated gas, 12 is a generated gas outlet, 14 is a heat insulating material, 18 is a gasification region, 22 and 2
4 is a water inlet and an outlet, and 25 is water.
酸化剤を上述のように上段および下段バーナに配分する
ことによって、下段バーナでは、特に 石炭＋Ｏ２→ＣＯ２、Ｈ２Ｏ、チャー …（４） 上段バーナでは、特に チャー＋ＣＯ２→２ＣＯ …（５） チャー＋Ｈ２Ｏ→Ｈ２＋ＣＯ …（６） の反応が起こり易くなる。この場合、（４）式に比較
し、（５）および（６）式の反応が遅いため、（５）お
よび（６）式の反応を如何に促進するかがガス化のポイ
ントとなる。下段バーナ１９では、（４）式の反応によ
って高温域が生成し、その結果、上段バーナ１７におけ
るチャーの反応速度が増大し、ガス化反応が促進され
る。また、この高温域によって、石炭灰（スラグ）２０
を溶融させ、スラグ排出口２１から路下部の水槽２３に
落下せしめる溶融温度を保持させる。さらに、（５）式
および（６）式の反応を促進させるために、バーナの微
粉炭を吹き込む仮想円の径を上述のように規定したこと
により、上段バーナから噴出する活性チャーを炉内に旋
回させながら下方に落下せしめ、チャーの滞留時間を著
しく増大させることができる。By distributing the oxidant to the upper and lower burners as described above, particularly in the lower burner, coal + O 2 → CO 2 , H 2 O, char ... (4) In the upper burner, especially char + CO 2 → 2CO ... ( 5) The reaction of char + H 2 O → H 2 + CO (6) easily occurs. In this case, the reactions of the equations (5) and (6) are slower than those of the equation (4), and the point of gasification is how to accelerate the reactions of the equations (5) and (6). In the lower burner 19, a high temperature region is generated by the reaction of the equation (4), and as a result, the reaction rate of char in the upper burner 17 increases and the gasification reaction is promoted. Also, due to this high temperature range, coal ash (slag) 20
Is melted and held at the melting temperature at which it is dropped from the slag discharge port 21 into the water tank 23 at the lower part of the passage. Further, in order to promote the reactions of the equations (5) and (6), the diameter of the virtual circle into which the pulverized coal of the burner is blown is defined as described above, so that the activated char ejected from the upper burner is introduced into the furnace. The whirlpool can be dropped while being swung to significantly increase the residence time of the char.
（発明が解決しようとする問題点） これらの方法は、従来技術に比較し、簡単な構造で石炭
のガス化効率を向上することができるが、さらにガス化
効率を高める方法が要望されていた。(Problems to be Solved by the Invention) These methods can improve the gasification efficiency of coal with a simple structure as compared with the prior art, but there has been a demand for a method of further increasing the gasification efficiency. .
本発明の目的は，微粉炭と酸化剤との混合を促進させ、
かつ活性化されたチャーの滞留時間を増大させることに
よりさらにガス化効率の高い多段方式の噴流層石炭ガス
化炉を提供することにある。The object of the present invention is to promote the mixing of pulverized coal and oxidant,
Another object of the present invention is to provide a multi-stage spouted bed coal gasification furnace with higher gasification efficiency by increasing the residence time of activated char.
（問題点を解決するための手段） 要するに本発明は、微粉炭と酸化剤の混合がよく、かつ
バーナより噴出される噴流の貫通力が小さいバーナを生
成ガスの流れに対して上流に設置し、その下流に微粉炭
と酸化剤の混合がよく、かつバーナより噴出される噴流
の貫通力が大きいバーナを設置することにより、活性の
あるチャーを形成させ、かつチャーの炉内滞留時間を増
大させ、ガス化効率を向上させるものである。すなわ
ち、本発明は、微粉炭ガス化反応領域と、この反応領域
の上端に生成ガス排出口と、前記反応領域の下端にスラ
グ排出口とを備え、かつ前記反応領域に酸化剤および微
粉炭をそれぞれ噴出する酸化剤ノズルおよび石炭ノズル
を有するバーナを２段以上備えた石炭ガス化炉におい
て、最下段以外のバーナは、酸化剤が石炭の噴流に向か
って噴出されるように酸化剤ノズルを配したバーナであ
ることを特徴とする。(Means for Solving Problems) In short, the present invention provides a burner in which pulverized coal and an oxidizer are well mixed and the penetrating force of the jet flow ejected from the burner is small, and the burner is installed upstream of the generated gas flow. By installing a burner that has good mixing of pulverized coal and oxidizer and large penetration of the jet flow ejected from the burner downstream of it, active char is formed and the residence time of char in the furnace is increased. And improve the gasification efficiency. That is, the present invention comprises a pulverized coal gasification reaction region, a generated gas outlet at the upper end of this reaction region, and a slag outlet at the lower end of the reaction region, and an oxidizer and pulverized coal in the reaction region. In a coal gasification furnace equipped with two or more stages of burners each having an ejecting oxidant nozzle and a coal nozzle, burners other than the lowest stage have oxidizer nozzles arranged so that the oxidant is ejected toward the coal jet. It is characterized by being a burner.
本発明において、最下段のバーナは、それ以外のバーナ
よりも貫通力が小さく、酸化剤が石炭ノズルの外周の接
線方向の速度成分をもって噴出されるように酸化剤ノズ
ルを配したバーナであることが好ましい。In the present invention, the lowermost burner has a smaller penetrating force than the other burners and is a burner in which an oxidant nozzle is arranged so that the oxidant is ejected with a tangential velocity component on the outer periphery of the coal nozzle. Is preferred.
また前記各段バーナは、それぞれ前記反応領域中に仮想
した仮想円の接線方向に吹き込むように設置され、かつ
最下段のバーナは、酸化剤が石炭ノズル外周の接線方向
に速度成分をもち、しかもその酸化剤の回転方向が炉内
壁に対し下向きとなるように酸化剤ノズルを配したバー
ナであることが好ましい。Further, each stage burner is installed so as to blow in the tangential direction of a virtual circle imaginary in the reaction region, and the bottom stage burner, the oxidizer has a velocity component in the tangential direction of the outer periphery of the coal nozzle, and It is preferable that the burner has an oxidant nozzle arranged such that the rotating direction of the oxidant is downward with respect to the inner wall of the furnace.
（実施例） 以下、添付図面によって本発明の実施例を説明する。第
１図は、本発明に用いるバーナの一例を示す断面図で、
バーナ本体７の中心には、石炭ノズル１が設置され、石
炭ノズル１から微粉炭および搬送用流体３が炉内に噴出
するようになっており、その外側には、酸素または、空
気のような酸化剤４が通る流路があり、その先端には、
酸化剤ノズル２が設置され、さらにその外側には、バー
ナを冷却するための流路があり、そこに冷却水５および
６が通るようになっている。第２図は、第１図に示すバ
ーナの平面図（II−II視図）、第３図は、第２図におけ
るIII−III断面の詳細図で、これは生成ガスの流れ方向
に対し、下流側に設置するバーナ、すなわち第７図にお
ける上段バーナ１７を記載したものである。このバーナ
には、中心の石炭ノズル１の中心軸に向かって酸化剤が
噴出するように、石炭ノズル１と酸化剤ノズル２Ａの軸
の成す角度（以下、衝突角と称する）が０゜＜α＜９０
゜になるように孔２Ａが穿設されている。すなわち、上
段バーナ１７は、酸化剤が石炭に衝突するように噴出さ
せるように構成されている。(Examples) Examples of the present invention will be described below with reference to the accompanying drawings. FIG. 1 is a sectional view showing an example of a burner used in the present invention.
A coal nozzle 1 is installed at the center of the burner body 7, and the pulverized coal and the transporting fluid 3 are ejected from the coal nozzle 1 into the furnace, and the outside thereof is exposed to oxygen or air. There is a flow path through which the oxidant 4 passes, and at the tip of it,
An oxidant nozzle 2 is installed, and further outside thereof, there is a flow path for cooling the burner, through which cooling water 5 and 6 pass. 2 is a plan view of the burner shown in FIG. 1 (view from II-II), and FIG. 3 is a detailed view of a III-III cross section in FIG. The burner installed on the downstream side, that is, the upper burner 17 in FIG. 7 is described. In this burner, the angle formed by the axes of the coal nozzle 1 and the oxidant nozzle 2A (hereinafter referred to as the collision angle) is 0 ° <α so that the oxidant is ejected toward the central axis of the central coal nozzle 1. <90
The hole 2A is formed so that the angle becomes 2 °. That is, the upper burner 17 is configured to eject the oxidizer so as to collide with the coal.
第４図は、本発明における下段バーナの一実施例を示す
第２図と同様な平面図であり、また第５図は酸化剤ノズ
ル２Ｂの軸に沿ったＶ−Ｖ断面の詳細図である。すなわ
ち、第４図に示すバーナは第２図に示す酸素ノズルをバ
ーナの中心軸との長さＬを石炭ノズルの径よりも大きく
した構造である。なお、Ｌが０のときは第２図に示す上
段バーナの構造になり、Ｌが０でない場合は本発明の下
段バーナに適するバーナの構造になる。石炭ノズル１の
外周の接線と同一平面上で交差するように酸化剤ノズル
２Ｂが穿設されている。酸化剤は、酸化剤ノズル２Ｂを
通り、炉内に旋回をしながら噴出される。なお、上記酸
化剤ノズル２Ｂの孔あきの角度は、第５図に示すように
旋回角β（０゜＜β＜９０゜）と定義され、上述した衝
突角と同じく、以後の説明に用いる。FIG. 4 is a plan view similar to FIG. 2 showing an embodiment of the lower burner of the present invention, and FIG. 5 is a detailed view of a VV cross section taken along the axis of the oxidizer nozzle 2B. . That is, the burner shown in FIG. 4 has a structure in which the length L of the oxygen nozzle shown in FIG. 2 with the central axis of the burner is larger than the diameter of the coal nozzle. When L is 0, the structure of the upper burner shown in FIG. 2 is obtained, and when L is not 0, the structure of the burner is suitable for the lower burner of the present invention. An oxidant nozzle 2B is provided so as to intersect with the tangent line of the outer periphery of the coal nozzle 1 on the same plane. The oxidant passes through the oxidant nozzle 2B and is jetted into the furnace while swirling. The angle of perforation of the oxidizer nozzle 2B is defined as a swirl angle β (0 ° <β <90 °) as shown in FIG. 5, and will be used in the following description, like the collision angle described above.
上述したように、第２図および第３図に示す上段バーナ
は、酸化剤が微粉炭の噴流に衝突するように構成したも
ので、微粉炭と酸化剤との混合は、非常に良好になる。
また石炭バーナの中心軸に交差して酸化剤が噴出される
ため、これらの混合流体は、速度の減衰は小さく、貫通
力が高いものとなる。このバーナをガス化炉の上段バー
ナとして使用すれば、石炭と酸化剤との混合がよいた
め、活性に富むチャーが生成されるのみならず、強い貫
通力を有するため、上述の活性チャーは、炉壁の周囲を
まわりながら落下し、また炉内の滞留時間が長いため、
前述の式（５）および（６）に示すガス化反応が十分行
われる。As described above, the upper burner shown in FIGS. 2 and 3 is configured so that the oxidizer collides with the jet flow of the pulverized coal, and the mixing of the pulverized coal and the oxidant becomes very good. .
Further, since the oxidizer is jetted across the central axis of the coal burner, the velocity of the mixed fluid is small and the penetrating power is high. If this burner is used as the upper burner of the gasification furnace, since the mixture of coal and the oxidizer is good, not only is char that is rich in activity is generated, but since it has a strong penetrating power, the above-mentioned activated char is Because it falls around the periphery of the furnace wall and the residence time in the furnace is long,
The gasification reaction represented by the above equations (5) and (6) is sufficiently performed.
一方、第４図および第５図に示す下段バーナは、酸化剤
がノズル２Ｂ出口で旋回をしながら噴出するため、バー
ナ出口近傍における微粉炭と酸化剤の場合は非常に良好
になり、さらに微粉炭と酸化剤の混合流体は旋回流であ
るため噴流は半径方向に拡がり、従って、軸方向の速度
の減衰は大きく、この混合された噴流の貫通力は著しく
小さくなる。このバーナを酸化剤の配分の多いガス火炉
の最下段のバーナに用いれば、まず、石炭と酸化剤の混
合がよいため活性したチャーが形成するばかりではな
く、貫通力が小さいため、上段バーナから噴出した活性
チャーの貫通力を低下することはなく、炉下部で高温域
を形成し、（４）式によって、多量のＣＯ２およびＨ２
Ｏを発生させることができる。On the other hand, in the lower burner shown in FIGS. 4 and 5, the oxidizer spouts while swirling at the outlet of the nozzle 2B, which is very good in the case of pulverized coal and oxidizer in the vicinity of the burner outlet. Since the mixed fluid of charcoal and oxidant is a swirl flow, the jet flow spreads in the radial direction, so that the velocity damping in the axial direction is large, and the penetrating force of this mixed jet becomes significantly small. If this burner is used for the bottom burner of a gas furnace with a large amount of oxidizer distribution, first, not only activated char is formed due to the good mixing of coal and oxidizer, but also the penetrating power is small, so the burner from the upper burner It does not reduce the penetrating power of the spouted activated char and forms a high temperature region in the lower part of the furnace, and a large amount of CO 2 and H 2
O can be generated.
次に、本発明によるバーナを用いたガス化実験の結果を
以下に示す。バーナについては、本発明のバーナと比較
するため、従来のバーナ構造として第６図に示すよう
に、衝突角α＝０度および旋回角β＝０度のものを用い
た。なお、円形断面のガス化炉において、特願昭５８−
５０４９６に記載のように石炭を炉内に仮想した仮想円
の接線方向に吹き込むようにした時、その仮想円の径
は、炉内径の１／２一定とした。また、旋回型のバーナ
（第４図及び第５図記載）については、炉内の旋回方向
との関連にいつても検討した。表１にその試験結果を示
す。Next, the result of the gasification experiment using the burner according to the present invention is shown below. Regarding the burner, in order to compare with the burner of the present invention, as a conventional burner structure, as shown in FIG. 6, a collision angle α = 0 degree and a turning angle β = 0 degree were used. In a gasification furnace with a circular cross section, Japanese Patent Application No. 58-
As described in 50496, when coal was blown into the furnace in a tangential direction of a virtual circle, the diameter of the virtual circle was set to 1/2 of the furnace inner diameter. Further, the swirl type burner (shown in FIGS. 4 and 5) was always examined in relation to the swirl direction in the furnace. Table 1 shows the test results.
表１からわかるように、まず、比較例１と実施例１を比
較すれば、本発明の第２図に示す酸化剤衝突型のバーナ
を上段バーナとして用いれば、冷ガス効率およびカーボ
ンガス化率共に約５％の向上が現れていることが判る。
また、比較例１と実施例２および３を比較すれば、上段
バーナに加えて本発明の第４図に示す旋回型のバーナを
下段に用いたときにも、従来のバーナを用いた時に比較
しそれぞれ効率が向上していることが判る。なお、仮想
円の回転方向と下段バーナの旋回方向については、炉壁
近傍の流れが下降流となる場合（実施例３）の方が、上
昇流となる場合（実施例２）よりも効率が高いことが判
る。これは、炉壁近傍が下向きとなることによって、上
段バーナで生じた活性チャーが、炉下部の高温域に引き
込まれるようになり、滞留時間の増加と共に、ガス化の
反応速度および反応時間が増加するためと考えられる。
さらに、実施例４では、上段および下段共に本発明のバ
ーナを設置したことにより、相乗効果を生じ、従来と比
較し、ガス化効率およびカーボンガス化率は格段に向上
させることができることが明らかである。 As can be seen from Table 1, first, comparing Comparative Example 1 with Example 1, if the oxidizer collision type burner shown in FIG. 2 of the present invention is used as the upper stage burner, the cold gas efficiency and the carbon gasification rate are increased. It can be seen that both of them show an improvement of about 5%.
Comparison between Comparative Example 1 and Examples 2 and 3 also shows that when the conventional type burner is used, the swirl type burner shown in FIG. 4 of the present invention is used in the lower stage in addition to the upper stage burner. It can be seen that the efficiency is improved in each case. Regarding the rotating direction of the virtual circle and the swirling direction of the lower burner, the efficiency in the case where the flow in the vicinity of the furnace wall is the downflow (Example 3) is higher than that in the case where the flow is the upflow (Example 2). It turns out to be expensive. This is because when the vicinity of the furnace wall faces downward, the activated char generated in the upper burner is drawn into the high temperature region in the lower part of the furnace, and the reaction rate of gasification and reaction time increase with the increase of residence time. It is thought to be to do.
Furthermore, in Example 4, by installing the burners of the present invention in both the upper and lower stages, a synergistic effect is produced, and it is clear that the gasification efficiency and the carbon gasification rate can be significantly improved as compared with the conventional case. is there.
（発明の効果） 本発明によれば、上段バーナより吹き込んだ微粉炭から
活性に富むチャーが形成され、そのチャーが、下段バー
ナより吹き飛んだ微粉炭から前記（４）式によって生成
したＨ２ＯおよびＣＯ２と炉底の高温部で接触し、前記
（５）式および（６）式の反応が、反応速度の大きい状
況でかつ長時間行なわれるので、チャーを完全にガス化
することができ、かつ、カロリーの高いガスを生成する
ことができる。According to the present invention (Effect of the Invention), char-rich active from pulverized coal was blown from the upper stage burner is formed, the char, H 2 O from a pulverized coal blew from the lower burner produced by the equation (4) and contacting with CO 2 and the furnace bottom of the hot section, the (5) the reaction of formula and (6), since carried out at for a long time greater availability of reaction rate, it can be completely gasified char And, it is possible to generate gas with high calories.
第１図はガス化に用いられるバーナの一実施例を示す断
面図、第２図は、第１図に示すバーナのII−II視図、第
３図は、第２図のバーナのIII−III断面を示す図、第４
図は、本発明に用いるバーナの一実施例を示す断面図、
第５図は、第４図のバーナのＶ−Ｖ視図、第６図は、従
来のバーナの平面図、第７図は、本発明に用いるガス化
炉の構造を示す断面図である。FIG. 1 is a sectional view showing an embodiment of a burner used for gasification, FIG. 2 is a view of the burner shown in FIG. 1 taken along line II-II, and FIG. 3 is a view of the burner shown in FIG. The figure which shows the III cross section, the 4th
FIG. 1 is a sectional view showing an embodiment of a burner used in the present invention,
FIG. 5 is a VV view of the burner of FIG. 4, FIG. 6 is a plan view of a conventional burner, and FIG. 7 is a sectional view showing the structure of the gasification furnace used in the present invention.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 古江 俊樹 広島県呉市宝町６番９号 バブコツク日立 株式会社呉工場内 (72)発明者 木田 栄次 広島県呉市宝町６番９号 バブコツク日立 株式会社呉工場内 (56)参考文献 特開 昭57−76087（ＪＰ，Ａ) 特開 昭59−176391（ＪＰ，Ａ) 特開 昭59−204686（ＪＰ，Ａ) 特開 昭58−194986（ＪＰ，Ａ) 特開 昭61−246287（ＪＰ，Ａ) 特開 昭61−12790（ＪＰ，Ａ) 実開 昭57−74949（ＪＰ，Ｕ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Toshiki Furu 6-9 Takaracho, Kure City, Hiroshima Prefecture Babkotuku Hitachi Co., Ltd. Kure Factory (72) Eiji Kida 6-9 Takaracho, Kure City, Hiroshima Prefecture Babkotuku Hitachi Co., Ltd. Kure Factory (56) Reference JP 57-76087 (JP, A) JP 59-176391 (JP, A) JP 59-204686 (JP, A) JP 58-194986 (JP, A) JP-A-61-246287 (JP, A) JP-A-61-12790 (JP, A) Actual development 57-74949 (JP, U)
Claims (3)
上端に生成ガス排出口と、前記反応領域の下端にスラグ
排出口とを備え、かつ前記反応領域に酸化剤および微粉
炭をそれぞれ噴出する酸化剤ノズルおよび石炭ノズルを
有するバーナを２段以上備えた石炭ガス化炉において、
最下段以外のバーナは、酸化剤が石炭の噴流に向かって
噴出されるように酸化剤ノズルを配したバーナであるこ
とを特徴とする石炭ガス化炉。1. A pulverized coal gasification reaction region, a produced gas discharge port at the upper end of the reaction region, and a slag discharge port at the lower end of the reaction region, and an oxidizer and a pulverized coal in the reaction region, respectively. In a coal gasifier equipped with two or more stages of burners each having an ejecting oxidant nozzle and a coal nozzle,
The burner other than the lowest stage is a burner in which an oxidant nozzle is arranged so that the oxidant is ejected toward the jet flow of coal.
バーナは、酸化剤が石炭ノズルの外周の接線方向の速度
成分をもって噴出されるように酸化剤ノズルを配したバ
ーナであることを特徴とする石炭ガス化炉。2. The burner according to claim 1, wherein the burner at the lowermost stage is a burner in which an oxidant nozzle is arranged so that the oxidant is ejected with a velocity component in the tangential direction of the outer circumference of the coal nozzle. Characteristic coal gasification furnace.
ナは、それぞれ前記反応領域中に仮想した仮想円の接線
方向に噴出流を抜き込むように設置され、かつ最下段の
バーナは、酸化剤が石炭ノズルの外周の接線方向に速度
成分をもち、しかもその酸化剤の回転方向が炉内壁に対
し下向きとなるように酸化剤ノズルを配したバーナであ
ることを特徴とする石炭ガス化炉。3. The claim 1 according to claim 1, wherein each stage burner is installed so as to extract the jet flow in the tangential direction of an imaginary circle imaginary in the reaction region, and the burner at the bottom stage is Coal gasification characterized in that the oxidizer has a velocity component in the tangential direction of the outer periphery of the coal nozzle, and is a burner in which the oxidizer nozzle is arranged so that the rotating direction of the oxidizer is downward with respect to the inner wall of the furnace. Furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60170747A JPH0643589B2 (en) | 1985-08-02 | 1985-08-02 | Coal gasifier |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60170747A JPH0643589B2 (en) | 1985-08-02 | 1985-08-02 | Coal gasifier |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6232185A JPS6232185A (en) | 1987-02-12 |
| JPH0643589B2 true JPH0643589B2 (en) | 1994-06-08 |
Family
ID=15910639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60170747A Expired - Fee Related JPH0643589B2 (en) | 1985-08-02 | 1985-08-02 | Coal gasifier |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0643589B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0627639Y2 (en) * | 1987-08-05 | 1994-07-27 | 三菱重工業株式会社 | Coal burning equipment |
| KR100241137B1 (en) * | 1997-11-24 | 2000-03-02 | 최수현 | Wet coal gasifier |
| CN107312570A (en) * | 2017-08-08 | 2017-11-03 | 龙志威 | Biomass gasifying furnace |
| KR102753330B1 (en) * | 2024-07-30 | 2025-01-14 | 주식회사 우석이엔씨 | Pyrolysis and gasification system and facilities for syngas generation |
| WO2026029575A1 (en) * | 2024-07-30 | 2026-02-05 | 주식회사 우석이엔씨 | Pyrolysis and gasification system and apparatus for producing synthesis gas |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5774949U (en) * | 1980-10-24 | 1982-05-08 | ||
| JPS5776087A (en) * | 1980-10-31 | 1982-05-12 | Nippon Kokan Kk <Nkk> | Jet flow type coal gasifiation using powdered coal and its device |
| JPS58194986A (en) * | 1982-05-10 | 1983-11-14 | Mitsubishi Heavy Ind Ltd | Multi-stage spouted bed gasification furnace |
| JPS59176391A (en) * | 1983-03-28 | 1984-10-05 | Hitachi Ltd | coal gasifier |
| JPS59204686A (en) * | 1983-05-10 | 1984-11-20 | Babcock Hitachi Kk | Coal gasification furnace |
| JPS6112790A (en) * | 1984-06-28 | 1986-01-21 | Babcock Hitachi Kk | Jet bed coal gasification furnace |
| JPS61246287A (en) * | 1985-04-24 | 1986-11-01 | Mitsubishi Heavy Ind Ltd | Spouted bed coal gasification oven |
-
1985
- 1985-08-02 JP JP60170747A patent/JPH0643589B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6232185A (en) | 1987-02-12 |
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