JPS6310695A - Moving bed gasifier - Google Patents

Moving bed gasifier

Info

Publication number
JPS6310695A
JPS6310695A JP61153471A JP15347186A JPS6310695A JP S6310695 A JPS6310695 A JP S6310695A JP 61153471 A JP61153471 A JP 61153471A JP 15347186 A JP15347186 A JP 15347186A JP S6310695 A JPS6310695 A JP S6310695A
Authority
JP
Japan
Prior art keywords
coal
air
combustion
fed
gas
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.)
Pending
Application number
JP61153471A
Other languages
Japanese (ja)
Inventor
Takao Ishihara
崇夫 石原
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Heavy Industries Ltd
Original Assignee
Mitsubishi Heavy Industries Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mitsubishi Heavy Industries Ltd filed Critical Mitsubishi Heavy Industries Ltd
Priority to JP61153471A priority Critical patent/JPS6310695A/en
Publication of JPS6310695A publication Critical patent/JPS6310695A/en
Pending legal-status Critical Current

Links

Classifications

    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency
    • Y02P20/129Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

PURPOSE:To greatly reduce the cost of coal gasification through a remarkable lowering in the contents of NOx and SOx in the formed gas and efficient removal of dust, by forming a coal layer having a suitable thickness by coal mass fed from the top portion of a furnace and introducing a suitable amt. of air. CONSTITUTION:Coal and limestone and fed from a coal feeder 4 provided under a coal banker 3 through a coal charging port 5 into a moving bed gasifier 6. On the other hand, combustion air is passed from a forced-draft device 17 through an air preheater 16 and an air preheater outlet air line 14. Then, part of the combustion air is fed as an air for coal gasification, while the remaining combustion gas is fed as a secondary air 15 for a burner into a boiler 18. The air 7 is reacted with coal in a coal gasification reaction zone 8 comprising a coal layer to gasify combustible substances contained in the coal. The amount of NOx can be minimized by reducing the flow rate of the air 7 below the theoretical combustion air and suitably adjusting the position and the proportion of the blowing. SOx is reacted with the finely divided limestone which has been fed simultaneously with the coal for desulfurization. The feeding portion and feeding amount of the air are adjusted so that the gas temperature of the reaction zone is 800-900 deg.C.

Description

【発明の詳細な説明】 〔産業上の利用分野〕 本発明は石炭焚きボイラ等の各種燃焼炉に適用される石
炭ガス化炉に関する。
DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a coal gasifier that is applied to various combustion furnaces such as coal-fired boilers.

〔従来の技術〕[Conventional technology]

石炭ガス化炉としては、流動床ガス化炉、噴流床ガス化
炉、固定床ガス化炉等があり、各々テスト炉又は一部実
用化されているが、各々一長一短があり、低公害炉(低
NOX 、低Box 、低パイウ゛°ン)としては、い
ずれも完全ではない。
Coal gasifiers include fluidized bed gasifiers, entrained bed gasifiers, and fixed bed gasifiers, each of which has been tested or partially put into practical use, but each has its own advantages and disadvantages. None of them are perfect in terms of low NOx, low box, and low piston.

〔発明が解決しようとする問題点〕[Problem that the invention seeks to solve]

本発明による本移動床石炭ガス化炉は、脱硝。 This moving bed coal gasifier according to the present invention is capable of denitrification.

脱硫、脱じんを同時に達成し、低公害ガス燃料を、ボイ
ラ等燃焼設備へ連続的に供給する装置である。
This is a device that simultaneously achieves desulfurization and dust removal and continuously supplies low-pollution gas fuel to combustion equipment such as boilers.

〔問題点を解決するための手段〕[Means for solving problems]

すなわち本発明は、原炭を貯蔵する原炭バンカと2石炭
の原炭塊を上部より投入する投入口と2この原炭を充填
する燃焼炉及び原炭の燃焼て必要な燃焼用空気を該燃焼
炉の上部および側部より供給する複数の空気投入口と発
生し之ガスを排出するガス排出口と、燃焼の完結した石
炭ガラを取り出す石炭ガラ取り出しホッパーより成る石
炭ガス化炉において、前記原炭バンカへ微粉状又は粒状
の石灰石を適当均等に散布混合し、ガス化ゾーンでの空
気比を燃焼用理論空気量以下に保ち、かつガス温度f 
800 ℃〜9θ0゛・つとiる礒、空気の投入場所及
び1共に適宜コントロールし、ま九原、突の燃焼及びガ
ス化1応完了後の石炭ガラの形成する石炭ガラ層を発生
ガスの排出口までの間に適当fx厚さで形成する事を特
徴とする移動床ガス化炉を提供するものである。
In other words, the present invention consists of a raw coal bunker for storing raw coal, 2 input ports for charging raw coal lumps from above, 2 combustion furnaces for charging the raw coal, and a combustion air necessary for combustion of the raw coal. In a coal gasification furnace, the raw material is Finely powdered or granular limestone is dispersed and mixed appropriately and evenly into the coal bunker, and the air ratio in the gasification zone is kept below the theoretical combustion air amount, and the gas temperature f
800°C to 9θ0゛・To control the air injection location and 1 as appropriate, the coal debris layer formed by the coal debris after the initial combustion and gasification is completed, and the generated gas is discharged. The purpose of the present invention is to provide a moving bed gasifier characterized in that it is formed with an appropriate fx thickness up to the outlet.

〔作用〕[Effect]

上部より投入される石炭塊により適正な厚さの石炭層を
形成し、適量の工室を投入することにより、還元雰囲気
の状態で、ガス化反応を起こし、 NOXの発生を、抑
制すると共【9石炭と同時に投入した石灰石により1発
生ガス中のSOxは、脱硫さnる。連続的な石炭の投入
に伴って、ガス化贋応の完了した石炭ガラは、順次。
By forming a coal seam of appropriate thickness with the coal lumps introduced from the top and introducing an appropriate amount of processing chambers, a gasification reaction occurs in a reducing atmosphere, suppressing the generation of NOx and [ 9 SOx in the generated gas is desulfurized by the limestone added at the same time as the coal. With the continuous input of coal, the coal waste that has undergone gasification is processed one by one.

下部ホッパーより排出され9石炭層のレベルは。The level of 9 coal seams discharged from the lower hopper is.

一定に保たれる。remains constant.

又2発生したガスの取り出しは、下部の石炭ガラの適正
厚さ以下のレベルで行われる為1発生ガスに含まれるパ
、/ 、、、ンは、はとんど2石炭ガラの間全通過する
途中で、物理的抵抗で1石炭ガラ層【捕促され、ガスは
、クリーンガスとして、取り出される。
In addition, since the gas generated in 2 is taken out at a level below the appropriate thickness of the lower coal shell, the gas contained in the gas generated in 1 must pass through the entire gap between the 2 coal shells. On the way, the gas is trapped by a layer of coal due to physical resistance, and the gas is extracted as clean gas.

〔実施例〕〔Example〕

賜について実施例を説明する。 An example will be explained regarding the gift.

■原炭投入口より2石炭及び■石灰石投入口より1石灰
石を、適量、  (a/s :1,5〜5.0 ) 微
粉状にて、■石炭バンカ内で2石炭(原炭)と石灰石が
均等に混合される様、供給され、一旦■石炭バンカ内に
貯蔵される。
■Two coals from the raw coal input port and ■One limestone from the limestone input port, in fine powder (a/s: 1.5~5.0), ■Two coals (raw coal) in the coal bunker. The limestone is supplied so that it is evenly mixed and temporarily stored in the coal bunker.

これらの石炭及び石灰石は、■石炭バンカの下に設けら
れた■給炭機より■石炭投入口をへて、■移動床ガス化
炉に投入される。一方、燃焼用エアは、0押込通風機よ
りりΦ空気予熱器。
These coal and limestone are fed into the moving bed gasifier through the coal feeder located below the coal bunker and through the coal inlet. On the other hand, combustion air is supplied by a Φ air preheater rather than a forced draft fan.

■空気予熱器量ロエア系統を経て一部は、■石炭ガス化
用エアとして、供給され、他は、0バ一ナー用2次エア
として0ボイラ(火炉)へ。
■Amount of air preheater After passing through the air system, some of the air is supplied as ■air for coal gasification, and the rest goes to the 0 boiler (furnace) as secondary air for the 0 burner.

投入される。投入された■石炭ガス化用エアは。Injected. ■The air for coal gasification that was input.

石炭層によ多構成された■石炭ガス化反応域にと おいて1石炭を反応し2石炭中の可燃分(炭化水素2等
)を、ガス化する。この時、 0H4(メタン、 Co
、 CmHmの可燃性ガスが9発生し、同時に微量のB
ox 、 NOxも発生する。
1) Coal is reacted in the coal gasification reaction zone, which is composed of multiple coal seams, and 2) the combustible content (hydrocarbons, etc.) in the coal is gasified. At this time, 0H4 (methane, Co
, CmHm combustible gas was generated, and at the same time a trace amount of B was generated.
Ox and NOx are also generated.

NOxについては、■石炭ガス化用エアの流量(空気比
)を、理論燃焼空気量以下とし、かつ。
Regarding NOx, ■ the flow rate (air ratio) of air for coal gasification should be below the theoretical combustion air amount, and.

吹き込み位置1割合等を、適切に、調整することで、 
NOxを、最少に抑制できる。又、 SOxについては
1石炭と同時に投入した微粉石灰石と。
By appropriately adjusting the blowing position 1 ratio, etc.,
NOx can be suppressed to a minimum. Also, regarding SOx, pulverized limestone was added at the same time as coal.

反応し、  802−1− CaO−)−HO2= C
aSO4により脱硫されるが、この場合、友応域でのガ
ス温度は。
React, 802-1-CaO-)-HO2=C
It is desulfurized by aSO4, but in this case, the gas temperature in the friendly region is .

800〜900℃にコントロールされる方が望ましいの
で、■石炭ガス化用エアの吹込みは、この点も考慮して
調整される。■ガス化反応域で発生した2石炭ガスは、
■の下に構成される■石炭ガラ層(ガス化反応完了域)
を通り、[相]発生ガス取り出し口へ達するが、この時
発生ガス中に含まれるパイジン(フライアラシン等)は
■石炭ガラ層のフィルター効果により、はとんど。
Since it is preferable to control the temperature at 800 to 900°C, (1) blowing of air for coal gasification is adjusted taking this point into consideration. ■The two coal gases generated in the gasification reaction zone are
■Coal glass layer (gasification reaction completion area) formed under ■
[Phase] The generated gas reaches the outlet, but at this time, the pyridine (fly aracin, etc.) contained in the generated gas is almost completely eliminated due to the filtering effect of the coal glass layer.

除去され、クリーン時可燃ガスとなり、@石炭ガス配管
を9通りボイラ内に設けられた[相]ガヌバーナーへ、
導びかれる。
It is removed and becomes a combustible gas when clean, and goes through 9 ways of coal gas piping to the [phase] Gannu burner installed in the boiler.
be guided.

[相]ガスバーナーより、[相]ボイラへ投入された。The [phase] gas was fed into the [phase] boiler from the gas burner.

石炭ガスは、[相]バーナー用2次エアと9反応し。The coal gas reacts with the [phase] secondary air for the burner.

ボイラ火炉内で、燃焼を完結する。もちろんこの際、2
段燃焼等の方法により1発生NOxは最小に抑制される
Combustion is completed in the boiler furnace. Of course, at this time, 2
One NOx generation can be suppressed to a minimum by a method such as staged combustion.

燃焼が完了した後、燃焼排ガスは9通常の重油焚きボイ
ラと同様、■過熱器、@ボイラバンり、EC0(節炭器
)、■空気予熱器をへて、[相]煙突より大気へ排出さ
れる。
After combustion is completed, the combustion exhaust gas passes through the superheater, @boiler van, EC0 (coal economizer), and air preheater, and is discharged into the atmosphere from the [phase] chimney, just like in a normal heavy oil-fired boiler. Ru.

又、■石炭投入口より、供給された石炭は。Also, ■The coal supplied from the coal input port.

■石炭ガス化反応域で、ガス化反応により、可燃分が、
ガス状で抜け、天分を主体とした9石炭ガラとなり、■
石炭ガラ層を、形成し、順次■石炭ガラ排出フィーダー
より、排出される。
■In the coal gasification reaction zone, combustible matter is
It escapes in gaseous form and becomes 9 coal gala mainly composed of genius, ■
A layer of coal debris is formed and is sequentially discharged from a coal debris discharge feeder.

本発明により、りNOX≦100 ppm、 2)脱硫
率≧90%、3)パイジ′ン100mVNrr)1が達
成され1重油焚きボイラ等の燃料転換については、容量
減少(Derat、ing )がほとんどなく可能とな
る。又石炭焚きボイラとして、EP、バグフィルター等
を省略でき、大巾なコストダウンが計れる。
According to the present invention, NOx≦100 ppm, 2) desulfurization rate≧90%, 3) piston 100 mVNrr) 1) have been achieved, and there is almost no capacity reduction (Derat, ing) for fuel conversion of single-fuel oil-fired boilers, etc. It becomes possible. Also, as a coal-fired boiler, EP, bag filter, etc. can be omitted, resulting in significant cost reductions.

〔発明の効果〕〔Effect of the invention〕

本発明の移動床ガス化炉によれば生成ガス中のNOxお
よびBoxを大幅に低減できるとともにフライアッシュ
等のパイジンを効率的に取り除くことができEP、バグ
フィルター等を省略できるため、大幅なコストダウンを
計ることができる。
According to the moving bed gasifier of the present invention, it is possible to significantly reduce NOx and BOX in the produced gas, and it is also possible to efficiently remove particles such as fly ash, and to omit EP, bag filters, etc., thereby significantly reducing costs. You can measure the down.

【図面の簡単な説明】[Brief explanation of drawings]

第1図は2本発明てよる移動床ガス化炉弐石大ボイラ系
統図の1実施例の図。 ■・・・石、炭(原炭)投入口、■・・・石灰石投入口
。 ■・・・石炭バンカ、■・・・給炭機、■・・・石炭投
入口。 ■・・・移動床ガス化炉、■・・・石炭ガス化用エア。 ■・・・石炭ガス化反応域、■・・・石炭ガラ層(ガス
化又志完了域)、[相]・・・発生ガス取り出し口、@
・・・石炭ガラ排出フィーダー、′@・・・石炭ゴ、X
、配曹。 [相]・・・ガスバーナー、o・・・空気予熱器出口エ
ア系統、[相]・・・バーナー用2次エア、4Φ・・・
空気予熱器。 ■・・・押込通風機、[相]・・・ボイラ(火炉)、ζ
[相]・・・燃焼ガス系統、[相]・・・煙突、[相]
・・・過熱器、@・・・ボイラパンク、  ECO
FIG. 1 is a diagram showing one embodiment of a moving bed gasifier Nishiki large boiler system diagram according to the present invention. ■...Stone, charcoal (raw coal) input port, ■...Limestone input port. ■...Coal bunker, ■...Coal feeder, ■...Coal input port. ■...Moving bed gasifier, ■...Air for coal gasification. ■...Coal gasification reaction zone, ■...Coal glass layer (gasification completion area), [phase]...Generated gas outlet, @
...Coal waste discharge feeder,'@...Coal waste, X
, Staff Sgt. [Phase]...Gas burner, o...Air preheater outlet air system, [Phase]...Secondary air for burner, 4Φ...
Air preheater. ■... Forced draft fan, [phase]... Boiler (furnace), ζ
[Phase]... Combustion gas system, [Phase]... Chimney, [Phase]
...Superheater, @...Boiler puncture, ECO

Claims (1)

【特許請求の範囲】[Claims] 原炭を貯蔵する原炭バンカと、石炭の原炭塊を上部より
投入する投入口と、この原炭を充填する燃焼炉、及び原
炭の燃焼に必要な燃焼用空気を該燃焼炉の上部および側
部より供給する複数の空気投入口と、発生したガスを排
出するガス排出口と、燃焼の完結した石炭ガラを取り出
す石炭ガラ取り出しホッパーより成る石炭ガス化炉にお
いて、前記原炭バンカへ微粉状又は粒状の石灰石を適当
均等に散布混合し、ガス化ゾーンでの空気比を燃焼用理
論空気量以下に保ち、かつガス温度を800℃〜900
℃となる様、空気の投入場所及び量共に適宜コントロー
ルし、また、原炭の燃焼及びガス化反応完了後の石炭ガ
ラの形成する石炭ガラ層を、発生ガスの排出口までの間
に適当な厚さで形成する事を特徴とする移動床ガス化炉
A raw coal bunker that stores raw coal, an input port that inputs raw coal blocks from above, a combustion furnace that fills this raw coal, and a combustion air that is necessary for combustion of raw coal that is connected to the upper part of the combustion furnace. In a coal gasifier, the coal gasifier is composed of a plurality of air inlets supplied from the side, a gas outlet for discharging the generated gas, and a coal debris take-out hopper for taking out the coal debris that has been completely combusted. Sprinkle and mix limestone in the form of limestone or granules evenly, keep the air ratio in the gasification zone below the theoretical combustion air amount, and keep the gas temperature between 800℃ and 900℃.
℃, the location and amount of air input are appropriately controlled, and the layer of coal debris formed by coal debris after the combustion of raw coal and gasification reaction is A moving bed gasifier characterized by being formed with a thickness.
JP61153471A 1986-06-30 1986-06-30 Moving bed gasifier Pending JPS6310695A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP61153471A JPS6310695A (en) 1986-06-30 1986-06-30 Moving bed gasifier

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP61153471A JPS6310695A (en) 1986-06-30 1986-06-30 Moving bed gasifier

Publications (1)

Publication Number Publication Date
JPS6310695A true JPS6310695A (en) 1988-01-18

Family

ID=15563294

Family Applications (1)

Application Number Title Priority Date Filing Date
JP61153471A Pending JPS6310695A (en) 1986-06-30 1986-06-30 Moving bed gasifier

Country Status (1)

Country Link
JP (1) JPS6310695A (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2721690A1 (en) * 1994-06-23 1995-12-29 Envirotec Group Ltd Disposal of solid hospital wastes by incineration

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2721690A1 (en) * 1994-06-23 1995-12-29 Envirotec Group Ltd Disposal of solid hospital wastes by incineration
WO1996000266A1 (en) * 1994-06-23 1996-01-04 Envirotec Group Limited Method and device for thermally processing hospital waste and the like

Similar Documents

Publication Publication Date Title
CA1227970A (en) Method and apparatus for combustion of diverse materials and heat utilization
KR100325282B1 (en) Fuel and sorbent feed for circulating fluidized bed steam generator
NL7906187A (en) METHOD FOR DIRECT REDUCTION OF IRON OXIDE USING GAS FROM COAL
JP2967394B2 (en) Desulfurization of carbonaceous fuel
JPH0648791A (en) Production of cement
CN101495211A (en) Method and apparatus for oil shale pollutant sorption/nox reburning multi-pollutant control
JPH10504637A (en) Combustion method
CN1188425A (en) Process for dry desulphurisation of combustion gas
CN104403697B (en) A kind of coal-fired boiler in power plant smoke emissioning pollution thing controls device and control method
US4724777A (en) Apparatus for combustion of diverse materials and heat utilization
EP0021558A1 (en) Method and apparatus for removing sulfur dioxide from gas
JP6224903B2 (en) Method for removing sulfur in pulverized coal combustion equipment
JPS6140886B2 (en)
JP3384435B2 (en) Fluidized bed furnace exhaust gas desulfurization method
CN1024525C (en) Balanced phosphoric acid plant cogeneration route
JPS6310695A (en) Moving bed gasifier
EP0126619A2 (en) Improvements in and relating to a method and apparatus for combustion of materials
CN104531225B (en) Multielement duplex gas generating system
JPS62125891A (en) Treatment of fly ash
Castleman Thermal processing
JPS62200107A (en) Furnace desulfurizing method
CN107883779A (en) A kind of steel mill's sintering smoke gas comprehensive treatment system and method
JPS638361B2 (en)
JP4105864B2 (en) Recycling method of fly ash in fluidized bed boiler.
JPS6033201B2 (en) Coal combustion equipment