JPS6310695A - Moving bed gasifier - Google Patents
Moving bed gasifierInfo
- 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
Links
- 239000003245 coal Substances 0.000 claims abstract description 82
- 238000002485 combustion reaction Methods 0.000 claims abstract description 22
- 238000002309 gasification Methods 0.000 claims abstract description 21
- 235000019738 Limestone Nutrition 0.000 claims abstract description 12
- 239000006028 limestone Substances 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 238000007599 discharging Methods 0.000 claims 1
- 239000008187 granular material Substances 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 24
- 238000007664 blowing Methods 0.000 abstract description 3
- 238000006477 desulfuration reaction Methods 0.000 abstract description 3
- 230000023556 desulfurization Effects 0.000 abstract description 3
- 239000000567 combustion gas Substances 0.000 abstract description 2
- 239000000428 dust Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 239000003034 coal gas Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
Classifications
-
- Y—GENERAL 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
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.
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.
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.
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.
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.
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.
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.
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、 ＥＣＯFIG. 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)
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.
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)
| 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 |
-
1986
- 1986-06-30 JP JP61153471A patent/JPS6310695A/en active Pending
Cited By (2)
| 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 |