JPS5910117Y2 - Polymer hydrocarbon gasification equipment - Google Patents
Polymer hydrocarbon gasification equipmentInfo
- Publication number
- JPS5910117Y2 JPS5910117Y2 JP13029779U JP13029779U JPS5910117Y2 JP S5910117 Y2 JPS5910117 Y2 JP S5910117Y2 JP 13029779 U JP13029779 U JP 13029779U JP 13029779 U JP13029779 U JP 13029779U JP S5910117 Y2 JPS5910117 Y2 JP S5910117Y2
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- Japan
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- main body
- gasification
- gasifier
- unburned carbon
- coal
- Prior art date
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Description
【考案の詳細な説明】
この考案は石炭その他の高分子炭化水素をガス化して、
可燃ガスを得るガス化装置の改良に関する。[Detailed explanation of the invention] This invention gasifies coal and other polymeric hydrocarbons,
This invention relates to improvements in gasifiers for obtaining combustible gas.
このようなガス化装置として従来より固定層ガス化炉、
流動層ガス化炉、噴流式ガス化炉、などが使用されてい
るが、しかしそれぞれ問題点を抱えている。Conventionally, fixed bed gasifiers,
Fluidized bed gasifiers, jet gasifiers, etc. are used, but each has its own problems.
石炭をガス化する場合を例にとって、以下に説明すると
、
(1)固定層ガス化炉
第1図に示す方法で石炭をガス化する。Taking the case of gasifying coal as an example, the following will explain: (1) Fixed bed gasifier Coal is gasified by the method shown in FIG. 1.
炉1上部から石炭を、炉底がら空気、水蒸気を供給する
。Coal is supplied from the top of the furnace 1, and air and steam are supplied from the bottom of the furnace.
石炭は予熱層2(〜450゜C)、乾留層3(450〜
800゜C)、還元層4 (800〜1000゜C)、
酸化層5 (1000〜1200’C)を経る過程でガ
ス化し、残りは灰となって炉底から取出される。Coal is heated in preheating layer 2 (~450°C) and carbonization layer 3 (450~
800°C), reduction layer 4 (800-1000°C),
It is gasified in the process of passing through the oxide layer 5 (1000-1200'C), and the remainder becomes ash and is taken out from the bottom of the furnace.
このガス化炉では、供給炭に対し通風を平らに均一に行
なわせることが、操作条件の根本である。In this gasifier, the fundamental operating condition is to uniformly ventilate the supplied coal.
したがって使用する炭種が制約を受ける点がまず指摘さ
れる。Therefore, the first point to be pointed out is that there are restrictions on the type of coal to be used.
つまり石炭としては微粒結性で灰分30%以下、水分2
5%以下のもの、しがも粒径6〜30 mmの粒状の形
で使用しなければならない。In other words, coal is fine-grained, has an ash content of 30% or less, and a moisture content of 2.
5% or less and must be used in granular form with a particle size of 6 to 30 mm.
粉炭を使ったのでは操業中に目詰りを起すし、粘着性の
石炭では乾留層にて通風に強い抵抗を与えるので、これ
もまずい。Powdered coal causes clogging during operation, and sticky coal provides strong resistance to ventilation in the carbonization layer, which is also undesirable.
非粘結炭も急熱されると粉化し易いがら、これまた不適
当である。Although non-caking coal is also easily pulverized when heated rapidly, it is also unsuitable.
つぎに指摘される欠点はガス化効率の小さな点である。The next drawback pointed out is the low gasification efficiency.
石炭の揮発分は乾留層3で乾留されるが、そこでは45
0〜800゜Cと温度が低いために、大部分がタールと
なる。The volatile content of coal is carbonized in carbonization layer 3, where 45
Since the temperature is low (0 to 800°C), most of it becomes tar.
このタールはつづく還元層4、酸化層5において一部が
ガス化、燃焼するけれど、かなりの量が灰と共に炉外に
取出される。A portion of this tar is gasified and burned in the subsequent reduction layer 4 and oxidation layer 5, but a considerable amount is taken out of the furnace together with the ash.
したがってこのタールの有効利用を計らなければ、ガス
化効率はきわめて小さなものとなる。Therefore, unless this tar is used effectively, the gasification efficiency will be extremely low.
(2)流動層ガス化炉
石炭粒子を比重と粒径に応じた固有の流動速度で移動さ
せ、気相中にけん垂させることによって、連続的にガス
化反応を行わせる方式である。(2) Fluidized Bed Gasification Furnace This is a method in which coal particles are moved at a specific fluidization speed depending on their specific gravity and particle size, and suspended in the gas phase to perform a gasification reaction continuously.
これも次に述べる如く炭種に制約を受ける。タリン力障
害を避けるため、石炭灰分の軟化点より少くともl00
゜C以上も低い温度でガス化しなければならないので、
ガス化速度にほおのづと限界があって、これを改善する
には反応性の大きな炭種が必要である。This is also limited by the type of coal as described below. At least l00 below the softening point of coal ash to avoid talin power disturbance
Since it must be gasified at a temperature lower than °C,
There is a limit to the gasification rate, and to improve this, a highly reactive coal type is required.
粘着性の強い石炭も、タリンカ障害の原因となるので、
不適当である。Strongly sticky coal can also cause tarinka failure.
It's inappropriate.
もうひとつの制約はダス1へ損失の大きいことで、これ
はとくに粒度分布の広い石炭や高熱にあうと粉化し易い
石炭、などを使った場合に目立つ現象である。Another limitation is the large loss to dust 1, which is a phenomenon that is particularly noticeable when using coal with a wide particle size distribution or coal that easily pulverizes when exposed to high heat.
(3)噴流式ガス化炉
これは微粉炭をガス化剤の気流とともに炉内に噴射し、
高温下で反応させるので、前述した2つのガス化炉と違
って、炭種の制限を受けない利点がある。(3) Jet gasifier This injects pulverized coal into the furnace together with an air stream of gasifying agent.
Since the reaction is carried out at high temperatures, there is an advantage that unlike the two gasifiers mentioned above, there is no restriction on the type of coal.
しかし、ガス化速度が大きいため、炉が大型化し易い。However, since the gasification rate is high, the furnace tends to be large-sized.
炉の設計寸法を小さくすればガス化が不充分となって、
多量の未燃カーボン(炭素)が発生する。If the design dimensions of the furnace are made smaller, gasification will become insufficient.
A large amount of unburned carbon is generated.
この考案は、上述した従来の問題点を解決したガス化装
置を提供するものである。This invention provides a gasifier that solves the above-mentioned conventional problems.
とくに噴流式ガス化炉の長所を生かし、その欠点を改善
したもので、炭種に制約を受けないばかりか広く高分子
炭化水素に適用でき、ガス化効率は高くて、しかも炉寸
法を小さくできるようにしたものである。In particular, it takes advantage of the advantages of the jet gasifier and improves its disadvantages.It is not limited by coal types, can be applied to a wide range of polymer hydrocarbons, has high gasification efficiency, and can be made smaller in furnace size. This is how it was done.
この考案が提供するガス化装置は、ガス化炉本体と、同
炉本体上部に設けて高分子炭火水素の粒子とガス化剤と
ガス化反応にて発生する未燃カーボンと等モル以上の酸
化カルシウムの粒子を同炉本体内部に噴射する噴射口と
、同炉本体上部に設ける生戊ガス抽出口と、未燃カーボ
ン、灰及び酸化カルシウムの流動堆積層を炉下部の周壁
と回転ロス}・ル自体との間に形威せしめる水蒸気吹込
用回転ロストルと、同炉本体底部に設ける灰取出口とを
有し、上記流動堆積層で未燃カーボンと酸化カルシウム
と水蒸気を反応させて水素を発生させることを特徴とす
る高分子炭化水素のガス化装置である。The gasification device provided by this idea consists of a gasification furnace body, a gasification agent installed on the top of the gasification furnace body, and an oxidation device that contains more than the same mole of unburned carbon generated in the gasification reaction between polymeric hydrocarbon particles, gasification agent, and gasification reaction. An injection port that injects calcium particles into the inside of the reactor main body, a raw gas extraction port provided in the upper part of the reactor main body, a fluidized deposit layer of unburned carbon, ash, and calcium oxide, and a peripheral wall in the lower part of the reactor and rotation loss. The reactor has a rotating rotor for blowing steam between the reactor itself and an ash outlet provided at the bottom of the reactor main body, and hydrogen is generated by reacting unburned carbon, calcium oxide, and steam in the fluidized bed. This is a polymer hydrocarbon gasification device characterized by:
すなわち、ガス化炉本体内部において、高分子炭化水素
を浮遊状態で可燃ガスにガス化する際、不完全なガス化
によって生ずる未燃カーボンを灰分とともに炉底に一定
時間滞在せしめ、それをCaOと水蒸気と反応させて水
素(H2)ガスに転換させ、そしてこのガスを上記可燃
ガスとともに戸外に抽出せしめるようにした。In other words, when high-molecular hydrocarbons are gasified into combustible gas in a suspended state inside the gasifier main body, unburnt carbon produced by incomplete gasification is allowed to stay at the bottom of the furnace together with ash for a certain period of time, and is converted into CaO. It was reacted with water vapor to convert it into hydrogen (H2) gas, and this gas was extracted outdoors together with the combustible gas.
このH2転換反応は発熱反応であるから、ガス化炉内を
昇温させ、ガス化反応を促進する効果がある。Since this H2 conversion reaction is an exothermic reaction, it has the effect of raising the temperature inside the gasifier and promoting the gasification reaction.
その結果、従来の噴流式ガス化炉に比べ、より小型のガ
ス化炉でガス化を完結せしめることができ、経済的にみ
て著しく有利になる。As a result, gasification can be completed with a smaller gasifier than a conventional jet gasifier, which is extremely advantageous from an economical standpoint.
従来では高分子炭化水素をガス化すると、必らず未燃カ
ーボンが生じて熱損失の原因となっていたが、この考案
では上述したとおり炉底において未燃カーボンをH2に
転換させるので、未燃カーボンによる熱損失を殆ど零に
することができる。Conventionally, when high-molecular hydrocarbons were gasified, unburned carbon was inevitably generated, causing heat loss, but in this design, as mentioned above, unburned carbon is converted to H2 at the bottom of the furnace, so there is no unburned carbon. Heat loss due to burnt carbon can be reduced to almost zero.
したがってこの考案のガス化装置は、炭種の制約を受け
ないばかりか、重質油やプラスチックなど高分子炭化水
素のガス化に広く適用することができる。Therefore, the gasification device of this invention is not only not subject to restrictions on the type of coal, but also can be widely applied to the gasification of high-molecular hydrocarbons such as heavy oil and plastics.
つぎに、この考案の一実施例を、図面を参照しながら説
明する。Next, one embodiment of this invention will be described with reference to the drawings.
第2図において、7はサイクロン型のガス化炉本体を示
す。In FIG. 2, 7 indicates a cyclone type gasifier body.
同炉本体7の上部7aには、側面周縁に開口する複数個
の原料噴射口8と、上面を貫通してガス化炉7内に開口
する可燃ガスの抽出口9と、同抽出口9に寄って上記噴
射口8の前方に位置する点火バーナ10と、少なくとも
この三者が設けてある。In the upper part 7a of the furnace body 7, there are a plurality of raw material injection ports 8 that open on the side periphery, a combustible gas extraction port 9 that penetrates the top surface and opens into the gasifier 7, and At least these three are provided, including an ignition burner 10 located in front of the injection port 8.
なお11は点火バーナ10の燃料管。噴射口8から供給
する原料というのは、微粉炭に代表される高分子炭化水
素つまり被ガス化物質と、空気や酸素あるいは酸化剤な
どのガス化剤と、それにCaOと、この三種類を指すも
のであって、噴射する際は第3図に示すように、それら
の混合物もしくは単独をガス化炉内壁に沿って同一方向
に旋回できるように噴射する。Note that 11 is a fuel pipe of the ignition burner 10. The raw materials supplied from the injection port 8 refer to three types: polymeric hydrocarbons represented by pulverized coal, that is, substances to be gasified, gasifying agents such as air, oxygen, or oxidizing agents, and CaO. When injecting, as shown in FIG. 3, a mixture or a single one of them is injected so as to be able to swirl in the same direction along the inner wall of the gasifier.
いっぽうガス化炉本体7の下部は、壁面7bの傾斜した
ホッパに形威される。On the other hand, the lower part of the gasifier main body 7 is shaped like a hopper with an inclined wall surface 7b.
ホッパ出口12には、中央に外周壁13と同心でかつ小
径の円筒状内周壁14を形或することによって、外周壁
13と内周壁14の間を灰取出通路15にするとともに
、内周壁14内側に中空の回転軸17を挿通させ、同軸
前端部に固定した水蒸気吹込用回転ロストル16をホッ
パ出口12の入口に位置させる。The hopper outlet 12 is formed with a small-diameter cylindrical inner wall 14 that is concentric with the outer wall 13 at the center, thereby creating an ash removal passage 15 between the outer wall 13 and the inner wall 14, and making the inner wall 14 A hollow rotary shaft 17 is inserted inside, and a rotary steam blowing rotor 16 fixed to the front end of the same shaft is positioned at the entrance of the hopper outlet 12.
回転軸17の他端近傍は、回転伝達装置18を介して電
動機19に連結する。The vicinity of the other end of the rotating shaft 17 is connected to an electric motor 19 via a rotation transmission device 18 .
したがって、炉壁7bを切断して回転ロストル16上方
から炉内をふかんすれば、ホッパ出口12は第4図に示
すようになり、ロストルのすぐ下からふかんすれば第5
図に示すようになる。Therefore, if the furnace wall 7b is cut and the inside of the furnace is blown from above the rotating rooster 16, the hopper outlet 12 will be as shown in FIG.
The result will be as shown in the figure.
この回転ロストル16は、炉下部の周壁と回転ロストル
16自体との間に流動堆積層24を形威しており、ここ
に高分子炭化水素とガス化剤との反応にて発生する未燃
カーボンや灰及び噴射口8から噴出した酸化カルシウム
(Cab)が堆積するようになっている。This rotary roaster 16 forms a fluidized deposit layer 24 between the peripheral wall of the lower part of the furnace and the rotary roaster 16 itself, and there is unburned carbon generated by the reaction between the high molecular weight hydrocarbon and the gasifying agent. Calcium oxide (Cab) ejected from the injection port 8 is deposited.
さらに上記回転ロストル16および同回転軸17は水蒸
気供給機構を形戒するもので、第6図に示すとおり、水
蒸気を炉底に供給できるようになっている。Furthermore, the rotary roaster 16 and the rotary shaft 17 function as a steam supply mechanism, and as shown in FIG. 6, steam can be supplied to the bottom of the furnace.
すなわち、いずれも中空構造体で、その中空部16a,
17 aは互に連通しており、回転ロストル16には複
数個の蒸気噴出孔20がうがたれている。That is, both are hollow structures, and the hollow parts 16a,
17a are in communication with each other, and a plurality of steam ejection holes 20 are provided in the rotary roaster 16.
回転軸17下端部は回転カップリングの雄部21に形威
して、回転カップリングの雌部22と嵌合もしくは接合
する仕組みとし、さらに後者雌部22は蒸気供給管23
の先端に連結するか、あるいはそれと一体に形或する。The lower end of the rotary shaft 17 is shaped like the male part 21 of the rotary coupling and is fitted or joined with the female part 22 of the rotary coupling, and the latter female part 22 is connected to the steam supply pipe 23.
Connected to the tip of or formed integrally with it.
したがって蒸気供給管23の水蒸気は、回転軸中空部1
7 a、回転ロストル中空部16 aを経て、噴射口2
0から炉内に噴出され、この水蒸気と未燃カーボンと酸
化カルシウムとが反応して水素を発生するようになって
いる。Therefore, the water vapor in the steam supply pipe 23 is transferred to the rotating shaft hollow part 1.
7a, through the rotary rostol hollow part 16a, the injection port 2
The water vapor is ejected into the furnace from zero, and this water vapor reacts with unburned carbon and calcium oxide to generate hydrogen.
なお、回転カップリング雄部21近傍の回転軸17上に
は、前述した回転伝達装置18の一部を構戊する歯車1
8aが固定されている。Incidentally, on the rotating shaft 17 near the male part 21 of the rotating coupling, there is a gear 1 that constitutes a part of the rotation transmitting device 18 described above.
8a is fixed.
つぎにこのように構威されたガス化装置の作用を説明す
る。Next, the operation of the gasifier configured in this manner will be explained.
噴射口8から、被ガス化物質である高分子炭化水素の微
粒子、ガス化剤、CaO粒子をガス化炉本体7内に高速
で噴射供給し、同炉内上部7aで旋回運動を起させる。Fine particles of polymeric hydrocarbon, gasifying agent, and CaO particles, which are substances to be gasified, are injected and supplied from the injection port 8 into the gasifier main body 7 at high speed, causing a swirling motion in the upper part 7a of the reactor.
噴射に際しては必らずしも同一の噴射口を使う必要はな
い。It is not necessarily necessary to use the same injection port for injection.
たとえばCaO粒子は、被ガス化物質、ガス化剤とは別
個の噴射口8を介して噴射してもよい。For example, the CaO particles may be injected through a separate injection port 8 from the substance to be gasified and the gasifying agent.
噴射された被ガス化物質は点火バーナ10による点火に
よって燃焼を開始する。The injected substance to be gasified is ignited by the ignition burner 10 and starts to burn.
なおCaOの必要量はガス化反応にて発生する未然カー
ボンと等モル以上で、通常被ガス化物質の約70%(重
量)となり、空気などのガス化剤の供給量は、被ガス化
物質の完全燃焼に必要な理論量の約50%以下である。The required amount of CaO is equal to or more than the mole of unresolved carbon generated in the gasification reaction, which is usually about 70% (by weight) of the material to be gasified, and the amount of gasifying agent such as air supplied is This amount is about 50% or less of the theoretical amount required for complete combustion.
被ガス化物質の部分燃焼によって高温燃焼ガスが発生す
る。High-temperature combustion gas is generated by partial combustion of the gasified substance.
このガスと未然の被ガス化物質とCaO粒子が、互に接
触して、下記の反応を起しながらガス化炉本体7内を下
降する。This gas, the previously gasified substance, and the CaO particles come into contact with each other and move down inside the gasifier main body 7 while causing the following reaction.
すなわち、被ガス化物質中の揮発分は高温燃焼ガスと接
触して蒸発し、高温燃焼ガス中の残留酸素およびH20
と次のように反応してCOとH2に変化する。That is, the volatile content in the gasified substance comes into contact with the high-temperature combustion gas and evaporates, leaving residual oxygen and H20 in the high-temperature combustion gas.
reacts with and changes into CO and H2 as follows.
2m+n
CmHn+mH20−+mCO十一丁一H2CmHn+
”02→mCO+ H2
また、被ガス化物質中の炭素は高温燃焼ガス中のCO2
、H20,H2および微量の02と次のように反応して
CO.H2およびメタンCH4になる。2m+n CmHn+mH20-+mCO11-1H2CmHn+
”02→mCO+ H2 In addition, carbon in the gasified substance is CO2 in the high-temperature combustion gas.
, H20, H2 and a trace amount of 02 to produce CO. becomes H2 and methane CH4.
C+.+02→CO
C+CO2→2CO
C+H20−+CO+H2
C+2H20→CO + 2 H2
C+2H2→CH4
生或したCO,H2、CH4は反応残の燃焼ガスと共に
ホッパ壁面7bに達し、そこで反転して随伴している粒
状固形分を分離したのち、再びガス化炉上部7aに向い
、可燃ガス抽出口9に流入する。C+. +02→CO C+CO2→2CO C+H20−+CO+H2 C+2H20→CO + 2 H2 C+2H2→CH4 The raw CO, H2, and CH4 reach the hopper wall surface 7b together with the combustion gas remaining from the reaction, where they are turned around and become part of the accompanying granular solids. After separating, the gas flows toward the upper part 7a of the gasifier and flows into the combustible gas extraction port 9.
分離された固形分はホッパ壁面7bを伝わって流動堆積
層24表面に落下する。The separated solid content travels along the hopper wall surface 7b and falls onto the surface of the fluidized sediment layer 24.
この粒状固形分の或分は、被ガス化物質の未反応炭素、
灰、CaOからなるもので、被ガス化物質中に硫黄Sが
存在すると、Sの燃焼反応で発生したSO2がCaOと
反応してCaSO3さらにはCaSO4となる。A portion of this granular solid content contains unreacted carbon of the substance to be gasified,
It consists of ash and CaO, and if sulfur S is present in the substance to be gasified, SO2 generated by the combustion reaction of S reacts with CaO to form CaSO3 and further CaSO4.
流動滞積層24の中央部には回転ロストル16が回転し
ながら、蒸気噴出孔20を介して水蒸気を流動滞積層2
4内に噴射している。A rotating rotor 16 is placed in the center of the fluidized accumulation layer 24 while rotating, and supplies water vapor to the fluidized accumulation layer 2 through the steam jet hole 20.
It is injected within 4.
ホッパ壁面7bと回転ロスI・ル16上面に堆積する粒
状の固形分は、ホッパ出口12の間隙、ホッパ壁面7b
の傾度、粒状固形分の沈降量、以上三者の相関関係によ
り互につながって、流動滞積層24を形或する。The granular solids deposited on the hopper wall surface 7b and the upper surface of the rotation loss I/L 16 are
The gradient of the granular solid content, the amount of sedimentation of the granular solids, and the correlation between these three factors interconnect to form a fluidized stagnation layer 24.
ホッパ壁面7bの傾きが急であると、壁面上の粒状固形
分は薄層をなして急速にホッパ出口12を通過する。When the slope of the hopper wall surface 7b is steep, the granular solids on the wall surface form a thin layer and rapidly pass through the hopper outlet 12.
逆に、ホッパ壁面7bの傾きがゆるい場合は、壁面上の
粒状固形分は厚層をなしてゆっくり降下する。On the contrary, when the slope of the hopper wall surface 7b is gentle, the granular solids on the wall surface form a thick layer and slowly descend.
その際、ホッパ出口12の間隙が粒状固形分の厚層より
小さな場合は、すなわち同層の表層部が回転ロス}・ル
16外縁に接触する場合は、同ロストル16上面の粒状
固形分と上記厚層とがつながって流動滞積層24を形或
し、そして該滞積層24下部から固形分が仄取出通路1
5に流れ込み、ガス化炉系外に取出される。At that time, if the gap between the hopper outlet 12 is smaller than the thick layer of granular solids, that is, if the surface layer of the same layer comes into contact with the outer edge of the rotation loss lever 16, the granular solids on the upper surface of the rotor 16 and the above The thick layers are connected to form a fluidized accumulation layer 24, and the solid content is removed from the lower part of the accumulation layer 24 through the extraction passage 1.
5 and is taken out of the gasifier system.
流動滞積層24における物質挙動は次のとおりである。The material behavior in the fluidized stagnation layer 24 is as follows.
その表層部には未燃カーボンとCaOが混在しているが
、それらが回転ロストル16から噴射された水蒸気と接
触し、かつ炉内の高温燃焼ガスの輻射熱を受けて約70
0’ C以上の高温に熱せられると、次の反応を起して
未燃カーボンはH2に、CaOはCaCO3にそれぞれ
転換する。Unburned carbon and CaO are mixed in the surface layer, and when they come into contact with the steam injected from the rotary rooster 16 and receive the radiant heat of the high-temperature combustion gas in the furnace, the
When heated to a high temperature of 0'C or higher, the following reactions occur, converting unburned carbon into H2 and CaO into CaCO3.
c+2 H20 + CaO −+CaCO3+ .2
H2↑生或物のうち、H2は流動滞積層24を抜け出
て炉内を上昇し、燃焼ガスと一緒に可燃ガス抽出口9内
に流入して、図示しない可燃ガス貯蔵タンク、あるいは
ガス焚ボイラに燃料として供給される。c+2 H20 + CaO −+CaCO3+ . 2
Of the H2↑ products, H2 escapes from the fluidized stagnation layer 24 and rises in the furnace, flows into the combustible gas extraction port 9 together with the combustion gas, and flows into a combustible gas storage tank (not shown) or a gas-fired boiler. is supplied as fuel.
CaCO3の方は固形分中の他の戊分、たとえば灰やC
aSO4等とともに流動滞積層24内を沈降し、前述し
たとおりホッパ出口12を経て、ガス化炉外部に取出さ
れる。CaCO3 contains other components in the solid content, such as ash and C.
It settles in the fluidized stagnation layer 24 together with aSO4 and the like, and is taken out to the outside of the gasifier via the hopper outlet 12 as described above.
炉外に取り出した粒状固形分は、粉砕したのち各戒分の
比重の差を利用してCaCO3を分別する。After pulverizing the granular solids taken out of the furnace, CaCO3 is separated using the difference in specific gravity of each precept.
CaCO3は図示しない加熱炉に送って、CaOとCO
2に分解処理し、うちCaOは再びガス化炉本体7内に
供給して、噴射口8より炉内に噴射する。CaCO3 is sent to a heating furnace (not shown), and CaO and CO are
2, CaO is again supplied into the gasifier main body 7 and injected into the furnace through the injection port 8.
以上で、この考案のガス化装置によれば、未燃カーボン
による熱損失を殆ど零に近づけることができ、装置自体
もコンパクトなものにすることが可能である。As described above, according to the gasification apparatus of this invention, the heat loss due to unburned carbon can be brought close to zero, and the apparatus itself can be made compact.
しかも被ガス化物質中にSが含まれていても、ガス化の
過程で脱硫されるので、無公害のきれいな可燃ガスを製
造することができる。Furthermore, even if the substance to be gasified contains S, it is desulfurized during the gasification process, so it is possible to produce clean, pollution-free combustible gas.
なおこの考案は要旨を逸脱しない範囲で種々変形して実
施できるもので前述した実施例に限定されるものではな
い。Note that this invention can be implemented with various modifications without departing from the gist, and is not limited to the embodiments described above.
ガス化炉としてサイクロン型を挙げたが、それに限らず
これまで噴流式ガス化炉で使われている型を使用できる
。Although the cyclone type gasifier is mentioned above, the present invention is not limited to this type, and any type that has been used in jet gasifiers can be used.
またガス化炉底部の回転ロストル及びその水蒸気供給機
構も、流動滞積層24内に水蒸気を均一に送り込めるも
のであれば、実施例に挙げたものに限らない。Further, the rotary rooster at the bottom of the gasifier and its steam supply mechanism are not limited to those described in the embodiments, as long as they can uniformly feed the steam into the fluidized stagnation layer 24.
たとえば回転ロストル16、回転軸17は回転運動に代
えて揺動運動できる方式としてもよい。For example, the rotary rotor 16 and the rotating shaft 17 may be of a type capable of swinging motion instead of rotating motion.
第1図は従来の固定層ガス化炉の概略構或図。
第2図はこの発明の一実施例の縦断面図で、そのIII
一■■I線、IV−IV線、■−V線に沿う横断面図を
、第3図、第4図、第5図に示す。
第6図は第2図に示すガス化装置の回転ロストル及びそ
の水蒸気供給機構の一例を示す拡大縦断面図。
7・・・ガス化炉本体、8・・・噴射口、9・・・可燃
ガス抽出口、10・・・点火バーナ、12・・・ホッパ
出口、15・・・灰取出通路、16・・・水蒸気吹込用
回転ロストル、17・・・回転軸、18・・・回転伝達
装置、19・・・電動機、20・・・蒸気噴射口、24
・・・流動滞積層。FIG. 1 is a schematic diagram of a conventional fixed bed gasifier. FIG. 2 is a vertical sectional view of one embodiment of the present invention, and its III
3, 4, and 5 show cross-sectional views taken along lines 1--I, IV--IV, and --V. FIG. 6 is an enlarged longitudinal cross-sectional view showing an example of the rotary roistle and its steam supply mechanism of the gasifier shown in FIG. 2. 7... Gasifier body, 8... Injection port, 9... Combustible gas extraction port, 10... Ignition burner, 12... Hopper outlet, 15... Ash removal passage, 16... - Rotating rotor for steam blowing, 17... Rotating shaft, 18... Rotation transmission device, 19... Electric motor, 20... Steam injection port, 24
...Fluid stagnation layer.
Claims (1)
の粒子とガス化剤とガス化反応にて発生する未燃カーボ
ンと等モル以上の酸化カルシウムの粒子を同炉本体内部
に噴射する噴射口と、同炉本体上部に設ける生或ガス抽
出口と、未燃カーボン、灰及び酸化カルシウムの流動堆
積層を炉下部の周壁と回転ロストル自体との間に形威せ
しめる水蒸気吹込用回転ロストルと、同炉本体底部に設
ける灰取出口とを有し、上記流動堆積層で未燃カーボン
と酸化カルシウムと水蒸気を反応させて水素を発生させ
ることを特徴とする高分子炭化水素のガス化装置。A system is installed in the gasifier main body and the upper part of the reactor main body, and injects into the reactor main body particles of polymeric hydrocarbon, gasifying agent, and calcium oxide particles in an amount equal to or more than the mole of unburned carbon generated in the gasification reaction. a raw gas extraction port provided in the upper part of the reactor main body, and a rotating steam injection port that forms a fluidized layer of unburned carbon, ash, and calcium oxide between the peripheral wall of the lower part of the reactor and the rotary rotor itself. The gasification of polymer hydrocarbons is characterized by having a rostol and an ash outlet provided at the bottom of the reactor main body, and generating hydrogen by reacting unburned carbon, calcium oxide, and water vapor in the fluidized bed. Device.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP13029779U JPS5910117Y2 (en) | 1979-09-20 | 1979-09-20 | Polymer hydrocarbon gasification equipment |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP13029779U JPS5910117Y2 (en) | 1979-09-20 | 1979-09-20 | Polymer hydrocarbon gasification equipment |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS5554336U JPS5554336U (en) | 1980-04-12 |
JPS5910117Y2 true JPS5910117Y2 (en) | 1984-03-30 |
Family
ID=29095783
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP13029779U Expired JPS5910117Y2 (en) | 1979-09-20 | 1979-09-20 | Polymer hydrocarbon gasification equipment |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS5910117Y2 (en) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH047773Y2 (en) * | 1985-05-28 | 1992-02-28 |
-
1979
- 1979-09-20 JP JP13029779U patent/JPS5910117Y2/en not_active Expired
Also Published As
Publication number | Publication date |
---|---|
JPS5554336U (en) | 1980-04-12 |
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