JPS594476B2 - Method and apparatus for high-pressure vaporization of powdered fuel - Google Patents

Method and apparatus for high-pressure vaporization of powdered fuel

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Publication number
JPS594476B2
JPS594476B2 JP11418278A JP11418278A JPS594476B2 JP S594476 B2 JPS594476 B2 JP S594476B2 JP 11418278 A JP11418278 A JP 11418278A JP 11418278 A JP11418278 A JP 11418278A JP S594476 B2 JPS594476 B2 JP S594476B2
Authority
JP
Japan
Prior art keywords
tank
pressure
distribution tank
carrier gas
powder
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
Application number
JP11418278A
Other languages
Japanese (ja)
Other versions
JPS5499103A (en
Inventor
シングニツツ・マンフレ−ト
クレ−チユマア・ホルスト
ゲ−レル・ピ−タ−
シユビアイゲル・ハンスヨアチム
テイエツツエ・ギユンタ−
バルヒマン・ルツツ
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.)
Brennstoffinstitut Freiberg
Original Assignee
Brennstoffinstitut Freiberg
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 Brennstoffinstitut Freiberg filed Critical Brennstoffinstitut Freiberg
Publication of JPS5499103A publication Critical patent/JPS5499103A/en
Publication of JPS594476B2 publication Critical patent/JPS594476B2/en
Expired legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Industrial Gases (AREA)
  • Cosmetics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Drying Of Solid Materials (AREA)

Description

【発明の詳細な説明】 本発明は直接に、または再処理の後に燃料ガス、合成用
ガス、還元ガスまたは都市ガスの混合成分その他として
使用することができるＣＯおよびＨ２含有ガスの製造の
ための粉末状燃料の高圧気化の方法および装置に関する
。DETAILED DESCRIPTION OF THE INVENTION The present invention provides a method for producing CO- and H2-containing gases which can be used directly or after reprocessing as fuel gas, synthesis gas, reducing gas or mixture component of city gas, etc. The present invention relates to a method and apparatus for high-pressure vaporization of powdered fuel.

粉末状燃料とは粉末状に粉砕された褐炭および石炭並び
に粉末状に粉砕された選炭および石油精製の含炭素固体
残滓および他の出所の適当な粉末度の含炭素固体有機材
料（例えば木材屑、古タイヤ、プラスチック屑）をいう
。Powdered fuels are pulverized lignite and coal as well as pulverized carbon-containing solid organic materials of suitable fineness from coal preparation and petroleum refining and other sources (e.g. wood chips, old tires, plastic waste).

広汎な各種燃料が可能であるので、遊離酸素を含む酸化
剤で炭焼反応の形で粉末状燃料を気化するのが特に好適
であることが判明した。Since a wide variety of fuels are possible, it has been found to be particularly suitable to vaporize the powdered fuel in the form of a charcoal reaction with an oxidizing agent containing free oxygen.

高圧でこのような技術を実施する時は、高圧系統への粉
末状燃料の確実な供給と均等な配給が特に技術上の問題
である。Reliable supply and uniform distribution of powdered fuel to the high pressure system is a particular technical problem when implementing such techniques at high pressures.

粉末状燃料と液体を混練してポンプで圧送できるペース
ト状にし、ポンプで高圧系統に送入し、配給することが
提案された。It was proposed that powdered fuel and liquid be mixed into a paste that could be pumped into a high-pressure system for distribution.

液体として液体炭化水素、例えば重油またはタールを使
用し、これと粉末状燃料を同時に気化する。A liquid hydrocarbon, such as heavy oil or tar, is used as the liquid, and this and the powdered fuel are simultaneously vaporized.

ところがこの解決法ではポンプ圧送を保証するために必
要な最大固体対液体比を考慮すると、燃料によって供給
される総エネルギーの内、粉末状固体燃料が充足するの
は、粉末状固体燃料の組織と熱量に従って通常３０ない
し４０％に過ぎず、大部分のエネルギは混練に使用され
る液体炭化水素のものとなっている。However, in this solution, considering the maximum solid-to-liquid ratio required to guarantee pumping, the powdered solid fuel suffices only a fraction of the total energy provided by the fuel due to the structure of the powdered solid fuel. The majority of the energy is in the liquid hydrocarbons used for kneading, usually only 30 to 40% depending on the calorific value.

混線に水を使用することもでき、適当なポンプで気化系
統の圧力に加圧された粉体・水混合物が加熱器を通過し
、そこで水が蒸発し、過熱され、本来の気化反応器に粉
体・蒸気混合物が送られるという解決法が公知である。Water can also be used in the crosstalk; a suitable pump pressurizes the powder/water mixture to the pressure of the vaporization system and passes through a heater, where the water evaporates, becomes superheated, and returns to the original vaporization reactor. Solutions are known in which powder/steam mixtures are fed.

特に多孔質の吸湿性の燃料、例えば軟褐炭の場合は、確
実なポンプ圧送のために必要な水分がすこぶる高いので
、水分の蒸発の過熱の後も水蒸気・粉体比は気化過程の
ために得ようとする最適値の数倍である。Particularly in the case of porous and hygroscopic fuels, such as soft lignite, the moisture required for reliable pumping is so high that even after superheating for moisture evaporation, the water vapor/powder ratio remains low due to the vaporization process. It is several times the optimal value to be obtained.

従って高圧系統の内部で懸濁物の水蒸気または水の一部
の厄介な分離を行わなければなうず、あるいは多量の水
蒸気の過量にかかわらず粉体の反応に必要な気化反応器
内温度を保証するために、気化処理用の酸素のために多
額の支出増を我慢しなければならない。This ensures the necessary temperature in the vaporization reactor for the reaction of the powders, regardless of the need for a cumbersome separation of the water vapor or part of the water in the suspension inside the high-pressure system, or even in the case of a large excess of water vapor. In order to achieve this, a large increase in expenditure for oxygen for the vaporization process must be endured.

例えば西ドイツ国特許公開公報第２５３６２４９号に記
載されているように、粉体の一部を水で、他の一部を液
体炭化水素で混練する場合は、基本的に同様の欠陥が生
まれる。Basically similar defects arise when part of the powder is kneaded with water and another part with liquid hydrocarbons, as described for example in DE 25 36 249 A1.

粉体が間欠的に操作される圧力締切りタンクを介して、
気化圧下の中間タンクに送られる粉末状燃料の高圧気化
法が知られている。Through a pressure shut-off tank in which the powder is operated intermittently,
High-pressure vaporization methods are known in which powdered fuel is sent to an intermediate tank under vaporization pressure.

粉末状燃料はこの中間タンクから機械式計量装置、例え
ば回転数が調節されるスクリューによって気体流コンベ
ヤに送入され、該気体流コンベヤが粉末状燃料を反応器
のバーナへ搬送する。From this intermediate tank, the powdered fuel is fed by a mechanical metering device, for example a speed-adjusted screw, to a gas flow conveyor, which conveys the powdered fuel to the burner of the reactor.

ガス状輸送媒質として酸素、水蒸気およびまたはＣ０２
、窒素、可燃性ガスまたはこの工程自体で生成され、回
収、冷却および精製されたガスが提案される。Oxygen, water vapor and or C02 as gaseous transport medium
, nitrogen, combustible gas or gas produced in the process itself, recovered, cooled and purified.

バーナへの粉末状燃料の完全な送給を保証するために、
機械式計量装置からバーナへの輸送管内に比較的高い速
度が必要であり、とりわけ気化圧が高い場合には多量の
ガス状輸送媒体も必要である。To ensure complete delivery of powdered fuel to the burner,
Relatively high velocities are required in the transport line from the mechanical metering device to the burner, and also large quantities of gaseous transport medium, especially if the vaporization pressure is high.

その結果、輸送のために使用される気体の種類によって
酸素比消費の増加、生成ガス中の不活性ガス（Ｎ２）の
レベルの増加が生じ、あるいは大部分の生成ガスに高価
で損失の伴なう回収・再圧縮を行うことになる。As a result, depending on the type of gas used for transport, this may result in increased oxygen specific consumption, increased levels of inert gas (N2) in the product gas, or an expensive and loss-making addition to most product gases. This will require recovery and recompression.

標準圧による方法で定評な技術である。This is a well-established technique using standard pressure.

輸送媒体として工業用酸素使用の場合は、バーナへの供
給管とバーナに爆発生粉体・酸素混合物が発生する危険
およびバツクファイアの危険が増大するので、高圧気化
処理においてはこの方法を差控えなければならない。If industrial oxygen is used as a transport medium, this method should be avoided in high-pressure vaporization processes due to the increased risk of creating an explosive raw powder/oxygen mixture in the supply pipe to the burner and the burner, as well as the risk of backfire. There must be.

この種の方法のもう一つの欠点は、高圧系統に機械式計
量装置を使用することである。Another disadvantage of this type of method is the use of mechanical metering devices in the high pressure system.

なぜなら本発明のような高い配給精度は比較的煩繁な障
害発生または煩繁な保守対策を代償とせざるを得ないか
らである。This is because the high distribution accuracy of the present invention comes at the cost of relatively troublesome occurrence of failures or complicated maintenance measures.

圧力締切りタンクを使用しないで、高圧系統への粉体の
搬入を遠心力方式（例えば西ドイツ国特許公報第２６１
７４９０号による）才たは容積変位式（例えば西ドイツ
国特許公報第１２５２８３９号、第１２６２４９４号に
よる）の連続式または半連続式「粉体ポンプ」によって
行う種類の方法においても、基本的に同じ問題が生まれ
る。The powder can be transported into the high-pressure system by centrifugal force (for example, West German Patent Publication No. 261) without using a pressure shut-off tank.
7490) or volumetric displacement (e.g. according to German Patent Publications No. 1252839, No. 1262494), processes of the type carried out by continuous or semi-continuous "powder pumps", the problem is essentially the same. is born.

また気化反応室への粉炭の供給と配給のために流動層方
式も利用される。A fluidized bed system is also used for supplying and distributing pulverized coal to the vaporization reaction chamber.

この流動層方式は粉末状燃料が不活性ガスの導入によっ
て間欠的に気化系統の圧力に加圧される圧力締切りタン
クと、粉末状燃料が圧力締切りタンクから転送され、不
活性ガスの吹込みによって燃料が流動化される高圧タン
クとから成る。This fluidized bed system uses a pressure shut-off tank in which powdered fuel is intermittently pressurized to the pressure of the vaporization system by introducing an inert gas, and a pressure shut-off tank in which the powdered fuel is transferred from the pressure shut-off tank and is injected with inert gas. and a high-pressure tank in which the fuel is fluidized.

この高圧タンクから粉体流が流動化不活性ガスと共に気
化反応器のバーナに送られるのである。From this high pressure tank the powder stream is sent to the burner of the vaporization reactor together with the fluidizing inert gas.

その場合、流量は流動層の密度および上記の高圧タンク
と気化反応器の間の差圧によってきまる。In that case, the flow rate depends on the density of the fluidized bed and the pressure difference between the above-mentioned high-pressure tank and the vaporization reactor.

文献のデータによれば、上記の構成（ウルマンの工業化
学大辞典１０巻、石炭気化の項を参照）によってすこぶ
る大きな固体気化比が得られる（使用状態で計算してキ
ャリアガス１ｄ当り約３００′に９）ところが流動層の
保持は流動化不活性ガスの循環と高価な除塵・循環圧縮
装置を必要とするので、従来実験装置に適用された解決
法を工業設備へ転用することの可能性については、専門
文献、例えばモイニール著［燃料の気化および酸化転イ
■（ワインハイム１９６２年刊）で批判されている。According to data in the literature, the configuration described above (see Ullmann's Encyclopedia of Industrial Chemistry, Volume 10, Coal Vaporization) provides a very high solids vaporization ratio (approximately 300'/d of carrier gas, calculated under operating conditions). (9) However, maintaining a fluidized bed requires the circulation of fluidized inert gas and expensive dust removal/circulation compression equipment, so the possibility of applying the solution conventionally applied to experimental equipment to industrial equipment is discussed. has been criticized in the specialized literature, for example in the book by Moinir [Fuel Vaporization and Oxidation Conversion] (Weinheim, 1962).

本発明の目的は気化反応器への粉体の送り込み、配給、
導入のために高い均一性、高い信頼性および小さなキャ
リアガス消費で作動する連続方式の粉末状燃料高圧気化
の方法および装置である。The purpose of the present invention is to feed powder into a vaporization reactor, distribute it,
The present invention is a method and apparatus for high-pressure vaporization of powdered fuel in a continuous mode, which operates with high uniformity, high reliability and low carrier gas consumption for introduction.

本発明の根底をなすのは、高圧系統への粉末状燃料の送
り込み、気化反応器のバーナへの配給と導入がキャリア
ガスによって行われ、固体対キャリアガスの高い充填比
（使用状態で＞３００に＆／キャリアガスぜ）とバーナ
への供給管の高い比輸送能力が得られ、バーナへの粉体
流の高い配給精度が達成され、流動層の保持のためにキ
ャリアガスの循環を全く廃止して、高い信頼性を保証す
ることができる、高圧下の、好ましくは圧力５ないし５
０ ｂａｒの粉末状燃料気化法を提案する問題である。The basis of the invention is that the feeding of the powdered fuel into the high-pressure system, the delivery and introduction to the burner of the vaporization reactor is carried out by means of a carrier gas, and a high solids-to-carrier gas filling ratio (in use >300 A high specific transport capacity of the supply pipe to the burner (with carrier gas) and a high specific transport capacity of the supply pipe to the burner is achieved, achieving high delivery accuracy of the powder flow to the burner and completely eliminating the circulation of carrier gas to maintain the fluidized bed. under high pressure, preferably at a pressure of 5 to 5
This problem proposes a method for vaporizing powdered fuel at 0 bar.

本発明によれば、上述の問題は次のようにして解決され
る。According to the present invention, the above-mentioned problem is solved as follows.

すなわち気化のための粉末状燃料は貯留バンカから大気
圧のもとて圧力締切りタンクに送られる。That is, the powdered fuel for vaporization is sent from the storage bunker to the pressure shut-off tank under atmospheric pressure.

圧縮不活性ガス例えば窒素または炭酸ガスや導入するこ
とによってこの圧力締切タンクの内容物は、気化反応器
の圧力より僅かに高い圧力に加圧される。By introducing a compressed inert gas, such as nitrogen or carbon dioxide, the contents of this pressure shut-off tank are pressurized to a pressure slightly higher than the pressure of the vaporization reactor.

加圧された粉末状燃料は別の高圧タンク（以下配給タン
クと称する）に送られる。The pressurized powdered fuel is sent to another high pressure tank (hereinafter referred to as distribution tank).

この配給タンクの下部でガス状媒質（以下キャリアガス
と称する）の吹込みによって粉体充填物が弛緩され、粉
末状燃料は吹込まれたキャリアガスと共に、配給タンク
の下部に始まり、該下部に突出する輸送管を経て後置の
気化反応器のバーナに流入する。In the lower part of this distribution tank, the powder charge is relaxed by blowing in a gaseous medium (hereinafter referred to as carrier gas), and the powdered fuel, together with the injected carrier gas, starts at the bottom of the distribution tank and projects into said lower part. It flows into the burner of the downstream vaporization reactor via a transport pipe.

本発明によれば輸送管の自由断面積と下部の自由断面積
の比は約１：５０ないし１：３００である。According to the invention, the ratio of the free cross-sectional area of the transport tube to the free cross-sectional area of the lower part is approximately 1:50 to 1:300.

配給タンク下部の粉末状燃料の上記の弛緩は、局部的な
（下部に限られた）流動層が問題になる所まで進行する
ことができる。The above-mentioned relaxation of the powdered fuel in the lower part of the distribution tank can progress to the point where a localized (limited to the lower part) fluidized bed becomes a problem.

配給タンクの下部の上方にある粉末状燃料充填層が静止
充填層の特徴を持ち、この静止充填層が気化反応器への
粉末状燃料の排出に応じて徐々に下へすべって行き、配
給タンクから排出される粉体量の固体容積に相当する（
比較的少い）ガス量が通常、この充填層を流通するに過
ぎない。The powdered fuel packed bed above the bottom of the distribution tank has the characteristics of a stationary packed bed, and this stationary packed bed gradually slides downward as the powdered fuel is discharged to the vaporization reactor, corresponds to the solid volume of the amount of powder discharged from (
Usually only a relatively small amount of gas flows through this packed bed.

本発明の方法によれば、粉体の正味密度が１．４ｇ／ｃ
ｒＡの場合、使用状態で例えばキャリアガスｍ゛当り粉
体５００ゆの粉末状燃料をキャリアガス流に負荷するこ
とができる。According to the method of the present invention, the net density of the powder is 1.4 g/c
In the case of rA, the carrier gas flow can be loaded with powdered fuel, for example, 500 yd powder per m of carrier gas in the operating condition.

配給タンクの下部に送られるキャリアガス量を変化する
ことによって、気化反応器に流入する粉体流（単位時間
当り粉末状材料ｋｇ）をすこぶる正確に調節することが
でき、その場合粉体対キャリアガスの充填が広い範囲で
一定を保つことが判明した。By varying the amount of carrier gas fed into the lower part of the distribution tank, the powder flow (kg of powdered material per unit time) entering the vaporization reactor can be adjusted very precisely, in which case the powder versus carrier It was found that the gas filling remained constant over a wide range.

そこで気化反応器への燃料供給の調節を配給タンク下部
へのキャリアガス流を適当に変化することによって行う
ことが、本発明による方法のもう一つの特徴である。It is therefore another feature of the process according to the invention that the fuel supply to the vaporization reactor is adjusted by suitably varying the carrier gas flow to the lower part of the distribution tank.

そのために例えばバーナへの供給管内の粉体流の直接測
定あるいは配給タンクの示填の示差測定または粉体供給
もしくは粉体・酸素比に依存する気化反応器の測定量（
例えば気化反応器の反応室内に現れる温度）を制御パル
スとして使用することができる。For this purpose, for example, a direct measurement of the powder flow in the feed pipe to the burner or a differential measurement of the filling of the distribution tank or a measured quantity (
For example, the temperature present in the reaction chamber of a vaporization reactor) can be used as a control pulse.

本発明による方法においては、粉体・キャリアガス流の
排出に使用される、配給タンク下部に突出する輸送管を
充填層の弛緩部分の中に水平に、または上からあるいは
下から垂直に導くことができる。In the method according to the invention, the transport pipes projecting from the bottom of the distribution tank, which are used for discharging the powder/carrier gas stream, are guided horizontally into the relaxed part of the packed bed or vertically from above or from below. Can be done.

十分に大きな曲率半径を選べば、バーナへの輸送管の方
向変換によって輸送の定常性が不都合な影響を受けるこ
とはない。If a sufficiently large radius of curvature is selected, the constancy of the transport is not adversely affected by the redirection of the transport pipe to the burner.

従って配給タンクと反応器の任意の幾何学的配列が可能
である。Any geometric arrangement of distribution tanks and reactors is thus possible.

なお公知のように、輸送の定常性を一層改善するために
輸送管の個々の点でごく少量のキャリアガスを補充導入
することができる。In addition, as is known, in order to further improve the constancy of the transport, it is possible to supplement the transport pipe with very small amounts of carrier gas at individual points.

配給タンク内の粉体充填層の高さに生じる変動が少い程
、粉末状燃料の配給精度すなわち平均粉体流量に対する
瞬時粉体流量の変動幅の逆数が高いことが判明した。It has been found that the smaller the variation in the height of the powder packed bed in the distribution tank, the higher the powdered fuel distribution accuracy, that is, the reciprocal of the variation width of the instantaneous powder flow rate with respect to the average powder flow rate.

従って配給タンクに１個の圧力締切りタンクが配属され
ている本発明の上述の実施態様においては、圧力締切り
タンクの充填、給圧、放出および減圧の各サイクルの間
に配給タンク内の充填層の高さの相対的変動を十分に小
さくするために、配給タンクを比較的太きくし、特に上
部に比較的大きな断面積を設けなければならない。Therefore, in the above-described embodiment of the invention in which the distribution tank is assigned one pressure cut-off tank, the filling bed in the distribution tank is In order to keep the relative variations in height sufficiently small, the distribution tank must be relatively thick and have a relatively large cross-sectional area, especially in the upper part.

そこで本発明の別の実施態様は並列的に使用される２個
以上の圧力締切りタンクを配設し、これを交互に充填し
て配給タンクに放出することとする。Another embodiment of the invention therefore provides for two or more pressure shut-off tanks to be used in parallel, which are alternately filled and discharged into a distribution tank.

本発明の好適な実施態様においては圧力締切りタンクの
配給タンクへの放出が配給タンクの上方に配設された調
節自在な粉体流絞り装置を介して重力流出によって行わ
れ、上記の絞り装置は配給タンク内の粉体充填状態の澗
宇によって制御することかできる。In a preferred embodiment of the invention, the discharge of the pressure cut-off tank into the distribution tank is carried out by gravity flow through an adjustable powder flow restriction device arranged above the distribution tank, said restriction device being It can be controlled by controlling the powder filling state in the distribution tank.

圧力締切りタンク内の公知の充填状態測定器によって第
１のロックの放出の後に第２のロックからの粉体の流入
および第１のロックの減圧、再充填、給圧を、あるいは
その逆を行うことができる。A well-known filling state measuring device in the pressure cut-off tank causes the discharge of the first lock to be followed by the inflow of powder from the second lock and the depressurization, refilling and replenishment of the first lock, or vice versa. be able to.

同様にこれを２個以上の圧力締切りタンクの使用に転用
することができる。This can likewise be adapted to the use of more than one pressure cut-off tank.

この場所で必要な配給精度はバーナへの粉体流の配給の
場合より遥かに低いから、配給タンクへの粉体流の上記
の調節自在な絞り装置の機能に対して、摩耗の少い、保
守を必要としない簡単な装置例えばスターフィーダまた
はすべり弁で十分である。Since the required dosing precision here is much lower than in the case of dispensing the powder stream to the burner, a low-wear Simple devices that do not require maintenance, such as star feeders or slip valves, are sufficient.

本発明により常時少くとも１個の圧力締切りタンクが放
出のために配給タンクと連結されているか、あるいは空
の圧力締切りタンクの遮断と充填および給圧され外圧力
締切りタンクの接続の間にごく短い切換期間（総時間の
約１０％以下）があるように、圧力締切りタンクの数と
大きさおよび圧力締切りタンクの減圧、充填、給圧、放
出のサイクル時間並びに個々の圧力締切りタンクの切換
周期を相互に調整するのが好都合であることが判明した
。According to the invention, at least one pressure cut-off tank is always connected to the distribution tank for discharge, or there is only a short period between the cut-off of an empty pressure cut-off tank and the connection of a filling and pressurized external pressure cut-off tank. The number and size of pressure cut-off tanks and the cycle times for depressurizing, filling, charging and discharging pressure cut-off tanks, as well as the switching period of individual pressure cut-off tanks, so that there is a changeover period (approximately 10% or less of the total time). It has been found expedient to mutually adjust.

また本発明の１つの実施態様は圧力締切りタンクが公知
の適当な充填高さ測定器を装備することとし、この測定
器が圧力締切りタンクの最少充填高さまたは空状態を通
報すると同時に、充填および給圧された圧力締切りタン
クへの切換を行わせる。It is also an embodiment of the invention that the pressure cut-off tank is equipped with a suitable known filling height measuring device, which measures the minimum fill height or empty condition of the pressure cut-off tank, and simultaneously indicates the filling and emptying of the pressure cut-off tank. Make the switchover to the pressurized pressure cut-off tank.

本発明による方法にとって必要不可決という訳でないが
、局部的流動層が保持される配給タンク下部は全配給タ
ンクの上部より小さな直径とするのが好都合であること
が判明した。Although not essential to the process according to the invention, it has been found advantageous if the lower part of the distribution tank, in which the localized fluidized bed is maintained, has a smaller diameter than the upper part of the entire distribution tank.

このために例えば円錐形中間部によって上部を下部の直
径に絞る。For this purpose, the upper part is constricted to the diameter of the lower part, for example by means of a conical intermediate part.

その場合、バラ精品バンカの寸法設計の原理により公知
のように、筒状空胴を形成せずに充填層の均一な降下が
得ら、れるように、粉末状燃料の流動挙動に従って上記
の絞りの寸法を定めなければならない。In that case, according to the flow behavior of the powdered fuel, the above-mentioned orifice should be adjusted so that a uniform descent of the packed bed without forming a cylindrical cavity is obtained, as is known from the principles of dimensional design of bulk bunkers. The dimensions shall be determined.

粉末状燃料とキャリアガスのすこぶる高い充填比（使用
状態で＞４００ｋｇ／ｍ″）および高い粉体流量を保証
するために、バーナへの輸送管の内径の最適比を守らな
ければならない。In order to ensure a very high filling ratio of powdered fuel and carrier gas (>400 kg/m'' in use) and a high powder flow rate, an optimum ratio of the internal diameters of the transport pipes to the burner must be observed.

輸送管の断面積と配給タンヤ下部の断面積の比は設備の
能力および粉体の流動特性に関係し、既に示したように
約１：５０ないし１：３００の範囲内である。The ratio of the cross-sectional area of the transport tube to the cross-sectional area of the lower part of the distribution tank depends on the capacity of the equipment and the flow characteristics of the powder and, as already indicated, is in the range of about 1:50 to 1:300.

配給タンク下部に吹込まれるキャリアガスを全断面にわ
たってほぼ均一に分配すれば、バーナへの供給管内の粉
体・キャリアガス懸濁物の均質性と粉体流の調節の精度
に良い影響を与えることができることが判明した。A nearly uniform distribution of the carrier gas blown into the lower part of the distribution tank over the entire cross section has a positive influence on the homogeneity of the powder/carrier gas suspension in the supply pipe to the burner and on the accuracy of the regulation of the powder flow. It turns out that it can be done.

そこで公知の物理的原理を利用して、多孔質材料から成
る流入床を介してキャリアガスを粉体充填層に導入する
。Using known physical principles, a carrier gas is then introduced into the powder packed bed via an inlet bed of porous material.

流入床は本発明により通常使用の場合、少くとも単位断
面積当り充填層重量に相些する圧力損失を有する。In normal use according to the invention, the inlet bed has a pressure loss at least equal to the packed bed weight per unit cross-sectional area.

この流入床の材料として例えば焼結金属板、フェルト板
等が考えられる。Possible materials for this inflow bed include, for example, sintered metal plates, felt plates, and the like.

気化反応器内のバーナによって得られる最適到達可能の
気化能力を考慮し、またはバーナの故障または損傷の際
の、気化反応器に後置された設備の常温度への酸素噴出
の危険に対する安全性の向上を考慮して、気化反応器に
２個以上の互いに独立のバーナを装備するのが適当であ
る。Taking into account the optimum achievable vaporization capacity obtained by the burner in the vaporization reactor, or the safety against the risk of oxygen eruption to ambient temperature in the equipment downstream of the vaporization reactor in the event of a burner failure or damage. In order to improve the performance, it is appropriate to equip the vaporization reactor with two or more independent burners.

このような場合は本発明により付属圧力締切りタンクそ
の他の装置を備えた複数個の同様の配給タンクに従って
、複数個のバーナを設置することができる。In such a case, the invention allows multiple burners to be installed in accordance with multiple similar distribution tanks with attached pressure cut-off tanks and other devices.

ただし本発明により１個の配給タンクが複数個の下部ま
たは互いに分離された複数個の区画に区分された下部を
具備することもできる。However, according to the invention it is also possible for a distribution tank to have a lower part or a lower part divided into several mutually separated compartments.

これらの下部のそれぞれ、または下部の分離された各部
分に別個のキャリアガス流を吹込むことによって、上述
のように局部的流動層を発生することができ、当該の下
部または当該の部分に入り込むそれぞれ１個の輸送管を
介して、別個のバーナの１つに粉体を導くことができる
。By blowing a separate carrier gas stream into each of these lower parts, or into each separated part of the lower part, a localized fluidized bed can be generated as described above, which enters the lower parts or parts in question. The powder can be led to one of the separate burners via a transport pipe in each case.

その場合、粉末状燃料は配給タンクの共同の上部から個
別の下部に、または下部の分離された部分にすべって行
く。In that case, the powdered fuel slides from the joint upper part of the distribution tank to a separate lower part or to a separate part of the lower part.

本発明のその他の特徴は上述の多重配列にも同様に適用
される。Other features of the invention apply equally to the multiplex arrangement described above.

本発明によれば単数側または複数個の圧力締切りタンク
の給圧のため、およびキャリアガスとして、同じガス状
媒質を使用することができる。According to the invention, the same gaseous medium can be used for pressurizing the pressure cut-off tank or tanks and as carrier gas.

そのために例えば窒素、炭酸ガス、回収され再圧縮され
た自家発生可燃性ガス、社外産の可燃性ガスまたはこれ
らのガスの混合物が考えられる。For this purpose, for example nitrogen, carbon dioxide, recovered and recompressed self-generated combustible gases, externally produced combustible gases or mixtures of these gases are conceivable.

不活性ガスを使用する時は若干の酸素が含まれているこ
とがある。When using an inert gas, it may contain some oxygen.

しかし圧力締切りタンク内の発火性、爆発性粉炭・不活
性ガス・酸素混合物の発生を回避するために、酸素含量
を粉末状燃料の前処理法に従って６％以下の値に制限し
なければならない。However, in order to avoid the formation of flammable and explosive pulverized coal-inert gas-oxygen mixtures in the pressure-limited tank, the oxygen content must be limited to a value below 6% in accordance with the method for pre-treatment of pulverized fuels.

原則として水蒸気の使用も可能であるが、その場合は水
蒸気が粉末状材料に凝縮することを防止するために、こ
の水蒸気を著しく過熱し、かつまたは粉末状燃料を予熱
することが必要である。In principle, it is also possible to use steam, but then it is necessary to significantly superheat this steam and/or to preheat the powdered fuel in order to prevent it from condensing on the powdered material.

従って通常、水蒸気の使用は問題外である。Therefore, the use of steam is usually out of the question.

本発明により単数側または複数個の圧力締切りタンクの
給圧のためとキャリアガスとしての使用のために、異な
るガスを使用することも可能である。According to the invention, it is also possible to use different gases for pressurizing the pressure cut-off tank or tanks and for use as carrier gas.

すなわち圧力締切りタンクの給圧には粉体の爆発の危険
を回避することを考慮して、上述のように限られた酸素
含量の不活性ガスを使用し、他方キャリアガスとして空
気または０２含量約２１％以下の不活性ガス・酸素混合
物を使用することができる。In other words, in order to avoid the risk of explosion of the powder, an inert gas with a limited oxygen content is used for the supply pressure of the pressure-shut-off tank, and on the other hand, as a carrier gas, air or an inert gas with a limited oxygen content is used. Inert gas/oxygen mixtures of up to 21% can be used.

なぜなら粉体・キャリアガス混合物の粉体濃度は圧力締
切りタンク内の条件と違って、各使用段階で爆発の上限
を超えているからである。This is because the powder concentration of the powder/carrier gas mixture exceeds the explosive limit at each stage of use, unlike the conditions in the pressure shut-off tank.

この解決法ではキャリアガスの０２含量は気化過程のた
めに利用されるから、気化酸素の消費が適宜に引下げら
れると共に、生成される生ガスの、キャリアガスに原因
する不活性ガス濃度が約２０％減少される。In this solution, the 02 content of the carrier gas is utilized for the vaporization process, so that the consumption of vaporized oxygen is accordingly reduced and the inert gas concentration due to the carrier gas in the raw gas produced is approximately 20 % will be reduced.

本発明によるこの種のもう一つの方式は圧力締切りタン
クの給圧のために不活性ガス、好ましくは窒素を使用し
、キャリアガスとして可燃性ガスを使用する。Another method of this type according to the invention uses an inert gas, preferably nitrogen, for the pressure of the pressure cut-off tank and uses a flammable gas as the carrier gas.

このような方式は、可燃性ガスが全部気化反応器に流入
するので、このガスに含まれる熱量が工程で利用される
一方、圧力締切りタンクの給圧ガスは低床な不活性ガス
であり、この不活性ガスは除塵の後、大気中に逃失して
も環境に対して重大な被害または障害がないという利点
がある。In this type of system, all the flammable gas flows into the vaporization reactor, so the heat contained in this gas is used in the process, while the supply pressure gas in the pressure cut-off tank is a low-floor inert gas. This inert gas has the advantage that after dust removal, even if it escapes into the atmosphere, there will be no significant damage or disturbance to the environment.

幾つかの実施例について本発明を詳述しよう。The invention will now be described in detail with reference to several embodiments.

第１図および第２図による本発明方法の実施態様では、
０．２朋フルイのフルイ上が約１．０％という粒度スペ
クトルの含水量的１０％の褐炭粉末が粉炭供給管１を径
て貯留バンカ２に送られる。In the embodiment of the method according to FIGS. 1 and 2,
Lignite powder having a particle size spectrum of about 1.0% on the sieve of a 0.2 mm sieve and a moisture content of 10% is sent to a storage bunker 2 through a pulverized coal supply pipe 1.

キャリアガスは褐炭粉体の分離の後、フィルタ３を径で
系統を退出する。After the separation of the lignite powder, the carrier gas exits the system through the filter 3.

その場合、貯留バンカ２への粉炭供給は充填高さ測定装
置１９によって監視される。In that case, the supply of pulverized coal to the storage bunker 2 is monitored by a filling height measuring device 19.

圧力締切りタンク５の減圧と遮断装置４の開放の後に、
褐炭粉末は貯留バンカ２から圧力締切りタンク５に流れ
る。After reducing the pressure in the pressure cut-off tank 5 and opening the shut-off device 4,
Lignite powder flows from the storage bunker 2 to the pressure cut-off tank 5.

その場合圧力締切りタンク内の充填高さが充填高さ測定
器１８によって点検される。The filling height in the pressure cut-off tank is then checked using a filling height measuring device 18.

後者は最大および最小充填高さで信号を送る。The latter signals the maximum and minimum filling height.

最大充填高さに到達すると遮断装置４が閉じ、圧力締切
りタンク５は供給管２８と制御弁１４を介して不活性ガ
スにより、配給タンク内の圧力（本例では３０ｂａｒ）
に等しい圧力まで給圧される。When the maximum filling height is reached, the shut-off device 4 closes and the pressure cut-off tank 5 is controlled by inert gas via the supply pipe 28 and the control valve 14 to reduce the pressure in the distribution tank (30 bar in this example).
Pressure is supplied to a pressure equal to .

充填高さ測定器１７によって、配給タンクγ内の褐炭粉
末の充填高さが監視される。A filling height measuring device 17 monitors the filling height of lignite powder in the distribution tank γ.

この充填高さが最少値に達すると、高圧締切りタンク５
の上にある遮断装置６が開放されるから、高圧締切りタ
ンクの内容物が一度に、または数段階で配給タンクＴに
流れる。When this filling height reaches the minimum value, the high pressure shut-off tank 5
Since the upper blocking device 6 is opened, the contents of the high-pressure shut-off tank can flow into the distribution tank T, either all at once or in several stages.

充填高さ測定器１８の最小信号によって、遮断装置６が
閉鎖される。A minimum signal of the filling height measuring device 18 causes the shut-off device 6 to be closed.

放出されたがまだ圧力下の圧力締切りタンクは制御弁１
５と減圧ガス排出管２９を介して大気圧まで減圧され、
それと共に新たな充填過程が準備される。The pressure cut-off tank, which has been released but is still under pressure, is controlled by control valve 1.
5 and the pressure is reduced to atmospheric pressure via the reduced pressure gas discharge pipe 29,
At the same time, a new filling process is prepared.

配給タンク７は充填高さ測定器１７を装備する円筒形断
面の直立筒状上部と、円錐形中間片を介して上部と連結
された、小さな直径の下部８から成る。The distribution tank 7 consists of an upright cylindrical upper part of cylindrical cross-section equipped with a filling height measuring device 17 and a lower part 8 of small diameter, which is connected to the upper part via a conical intermediate piece.

下部８の底は二重底式に構成され、内壁は多孔質流人床
として形成されている。The bottom of the lower part 8 is constructed in a double bottom type, and the inner wall is formed as a porous drift bed.

制御弁１０を介して底部の外壁および流入床として構成
された内壁の間の間隙にキャリアガス流が送られる。A flow of carrier gas is delivered via a control valve 10 into the gap between the outer wall of the bottom and the inner wall configured as an inlet bed.

第２図に示す実施態様ではキャリアガスとして圧力締切
りタンクの給圧と同様の、供給管２８を経て送られる不
活性ガスが使用される。In the embodiment shown in FIG. 2, an inert gas is used as carrier gas, which is similar to the supply pressure of the pressure cut-off tank and is conveyed via the supply line 28.

ところが第１図では導管３４および３５を経て圧力締切
りタンクと配給タンク下部に異種のガスを送り込むこと
ができることが示唆されている。However, FIG. 1 suggests that different gases can be introduced into the pressure cut-off tank and the lower portion of the distribution tank via conduits 34 and 35.

この実施例では気化に必要な酸素を製造する時に発生す
る工業用窒素が導管３４によって送られる。In this embodiment, the industrial nitrogen generated during the production of the oxygen required for vaporization is conveyed by conduit 34.

他方、導管３５と循環圧縮機３７を介して自家発生ガス
がキャリアガスとして送り込まれる。On the other hand, self-generated gas is fed in as carrier gas via conduit 35 and circulation compressor 37.

キャリアガスとして使用されるガス状媒質は流入床を通
って配給タンクの下部に入り、配給タンク下部にある褐
炭粉末を弛緩させ、場所的に限られた（局部的）流動層
を発生させる。The gaseous medium used as carrier gas enters the lower part of the distribution tank through the inlet bed, relaxing the brown coal powder in the lower part of the distribution tank and creating a locally confined (localized) fluidized bed.

弛緩された褐炭粉末は直近の段階でキャリアガスにより
、上から局部的流動層に入り込んだ輸送管９の中に運び
込まれ、この管を経て褐炭粉末とキャリアガスが気化反
応器３１のバーナ３０に導入される。In the most recent stage, the relaxed lignite powder is carried by a carrier gas into the transport pipe 9 which enters the local fluidized bed from above, and through this pipe the lignite powder and carrier gas are transferred to the burner 30 of the vaporization reactor 31. be introduced.

輸送管９内の褐炭粉末の流量はキャリアガスの流量に、
広い範囲で大体比例する。The flow rate of lignite powder in the transport pipe 9 is equal to the flow rate of the carrier gas,
Roughly proportional over a wide range.

バーナへの褐炭粉末流の調節は、制御弁１０によりキャ
リアガス流を調節することによって行われる。Regulation of the lignite powder flow to the burner is achieved by regulating the carrier gas flow by means of a control valve 10.

第２図の実施例では制御弁１０は輸送管９の粉体流測定
装置１６からパルスを受取る。In the embodiment of FIG. 2, the control valve 10 receives pulses from a powder flow measuring device 16 in the transport line 9. In the embodiment of FIG.

これに対して第１図には制御弁１０の制御パルスとして
気化反応器３１の反応帯に現れ、温度測定点１３によっ
て測定される温度を使用できることが示されている。In contrast, FIG. 1 shows that the temperature appearing in the reaction zone of the vaporization reactor 31 and measured by the temperature measuring point 13 can be used as the control pulse of the control valve 10.

その他の条件が同じならば、上記の温度はバーナへの褐
炭粉末流の関数である。Other things being equal, the above temperatures are a function of the lignite powder flow to the burner.

必要ならば弁１１および単数側または複数個の平行の供
給点１２を介して少量の補助キャリアガスを輸送管９に
導入することが可能である。If necessary, it is possible to introduce a small amount of auxiliary carrier gas into the transport pipe 9 via the valve 11 and the side or parallel feed points 12.

それによって特に始動状態の時や褐炭粉末の流動性が不
良の場合（例えば繊維性木材状成分の割合が高いために
起こる）に粉体・キャリアガス流を一層安定させ、輸送
管の彎曲部が詰まる可能性を抑制することができる。This makes the powder/carrier gas flow more stable, especially during start-up conditions or when the flowability of the lignite powder is poor (e.g. due to a high proportion of fibrous wood-like components), and bends in the transport pipe are avoided. The possibility of clogging can be suppressed.

褐炭粉末流は輸送管９を経て気化反応器３１のバーナ３
０に達する。The lignite powder stream passes through the transport pipe 9 to the burner 3 of the vaporization reactor 31.
reaches 0.

バーナによって褐炭粉末は導管３６からバーナに送られ
る工業用酸素および水蒸気の混合物と接触させられる。The burner brings the lignite powder into contact with a mixture of industrial oxygen and water vapor which is conveyed to the burner via conduit 36.

褐炭粉末および気化剤と呼ばれる工業用酸素と水蒸気の
混合物は気化反応器３１の反応室で１５００°Ｃ程度の
温度および配給タンク内より僅かに低い圧力（約２９．
５ｂａｒ）で炎の形で互いに反応し合う。Lignite powder and a mixture of industrial oxygen and water vapor, called a vaporizing agent, are heated in the reaction chamber of the vaporizing reactor 31 at a temperature of the order of 1500°C and a pressure slightly lower than in the distribution tank (approximately 29°C).
5 bar) and react with each other in the form of flame.

生じた生ガスは後置の冷却・凝縮・ガス精製装置３２を
通過し、その後の用途に送られる。The resulting raw gas passes through a downstream cooling, condensation, and gas purification device 32 and is sent to subsequent uses.

配給タンク７の下部８には、使用状態で送入褐炭粉末を
当り約２．３５ｍ”に相当する標準状態で６３ｍ３のキ
ャリアガス量が送られる。The lower part 8 of the distribution tank 7 is fed with a carrier gas volume of 63 m@3 in standard conditions, which in use corresponds to approximately 2.35 m'' per feed lignite powder.

その場合、配給タンク下部のキャリアガス速度０．０２
５ ｍ／ｓ （、標準負荷）で流入床に０．２ｂａｒの
圧力損失が生じるように、流入床の寸法を定める。In that case, the carrier gas velocity at the bottom of the distribution tank is 0.02
The inlet bed is dimensioned such that at 5 m/s (at standard load) there is a pressure drop of 0.2 bar across the inlet bed.

輸送管ではキャリアガスｍ゛当り（使用状態）褐炭粉末
５００ｇの褐炭粉末・キャリアガス混合物すなわち１５
．５ｋｇ／Ｎｍの混合物が輸送される。In the transport pipe, 500 g of lignite powder/carrier gas mixture (in use state) per m of carrier gas, i.e. 15
．． A mixture of 5 kg/Nm is transported.

輸送管は粉体・キャリアガス混合物速度３．４ ｍ ／
ｓに対して設計されている。The transport pipe has a powder/carrier gas mixture velocity of 3.4 m/
It is designed for s.

第１図および第３図の実施態様は配給タンク７の充填の
ために２個の圧力締切りタンク５および２１が使用され
、交互に操作される。The embodiment of FIGS. 1 and 3 uses two pressure shut-off tanks 5 and 21 for filling the distribution tank 7, which are operated alternately.

第１の実施例と同じ性状の褐炭粉末が、やはり第１実施
例に記載されているように貯留バンカ２に送られる。Lignite powder having the same properties as in the first embodiment is sent to the storage bunker 2 as also described in the first embodiment.

貯留バンカ２は一方の導管と遮断装置４を介して圧力締
切りタンク５と、他方の導管と遮断装置２０を介して圧
力締切りタンク２１と連絡する。The storage bunker 2 communicates with a pressure cutoff tank 5 via a line and a cutoff device 4 on the one hand, and with a pressure cutoff tank 21 via a line and cutoff device 20 on the other hand.

遮断装置２０が閉じている時、第１実施例で説明したの
と同様にまず圧力締切りタンク５が減圧され、貯留バン
カ２から褐炭粉末が供給され、制御弁１４を介して導管
２８からの不活性ガスによって配給タンク７内の圧力ま
で加圧される。When the shut-off device 20 is closed, the pressure shut-off tank 5 is first depressurized in the same manner as described in the first embodiment, lignite powder is supplied from the storage bunker 2, and waste from the conduit 28 is discharged via the control valve 14. The pressure in the distribution tank 7 is pressurized by the active gas.

これらの操作の間に他方の圧力締切りタンク２１が開放
された遮断装置２２と回転数を調節できる耐圧密封スタ
ーフィーダ型の粗計量装置２３とを介して配給タンク７
と連絡する。During these operations, the other pressure cut-off tank 21 is connected to the distribution tank 7 via an opened cut-off device 22 and a pressure-tight sealed star feeder type coarse metering device 23 whose rotation speed can be adjusted.
contact.

その場合、圧力締切りタンク２１の内容物は粗計量装置
２３を介して配給タンクに送られ、その際粗計量装置は
充填高さ測定器１７によって制御され、配給タンク７内
の充填高さが所定の範囲内で一定に保たれる。In that case, the contents of the pressure cut-off tank 21 are transferred via a rough metering device 23 to the distribution tank, the rough metering device being controlled by a filling height measuring device 17 so that the filling height in the distribution tank 7 is determined. is kept constant within the range of

圧力締切りタンク２１が放出されると、充填高さ測定器
２７が遮断装置６の開放と遮断装置２２の閉鎖を行わせ
る信号を送る。When the pressure cut-off tank 21 is discharged, the filling height measuring device 27 sends a signal that causes the isolation device 6 to open and the isolation device 22 to close.

次に圧力締切りタンク５から配給タンクへ褐炭粉末が送
られ、他方、圧力締切りタンク２１は制御弁２６によっ
て減圧され、遮断装置２０の開放の後に褐炭粉末を充填
され、充填高さ測定器２７が最大値信号を発信した後、
遮断装置２０が閉鎖され、制御弁２５を介して不活性ガ
スで配給タンク７内の圧力に加圧され、次に圧力締切り
タンク５の充填高さ測定器１８がその空状態を指示する
と、配給タンクＴへの新たな放出のために待機する。The lignite powder is then sent from the pressure cut-off tank 5 to the distribution tank, while the pressure cut-off tank 21 is depressurized by the control valve 26 and is filled with lignite powder after the opening of the shut-off device 20, and the filling height measuring device 27 is After sending the maximum value signal,
The shut-off device 20 is closed and the pressure in the distribution tank 7 is pressurized with inert gas via the control valve 25, and then when the filling height meter 18 of the pressure cut-off tank 5 indicates its empty state, the distribution is stopped. Wait for new discharge into tank T.

配給タンクの機能と気化反応器への粉体流の供給は第１
実施例と比較して変わらないから、改めて説明すること
はしない。The function of the distribution tank and the supply of powder flow to the vaporization reactor are
Since there is no difference compared to the embodiment, it will not be explained again.

２個の圧力締切りタンクを備えた実施態様は、配給タン
ク７内の充填高さの移動の範囲を厳密にすることができ
る。An embodiment with two pressure cut-off tanks allows a tighter range of filling height movement within the distribution tank 7.

それは配給精度を高め、特に配給タンクの寸法、特に直
径を縮少することを可能にする。It increases the accuracy of the distribution and in particular makes it possible to reduce the dimensions of the distribution tank, especially the diameter.

それ故この実施態様は特に設備能力が高い場合に有利で
ある。This embodiment is therefore particularly advantageous if the installation capacity is high.

第４図と第５図は唯１個の配給タンクを使用して、気化
反応器の複数個の図では別個の独立に調節できるバーナ
に粉末状燃料が供給される、本発明の実施態様を説明す
る。Figures 4 and 5 illustrate an embodiment of the invention in which only one distribution tank is used to supply powdered fuel to separate and independently adjustable burners in multiple views of the vaporization reactor. explain.

配給タンク７の下部は星形に配設された３個の隔壁３８
によって３個の同じ扇形区画に区分されている。The lower part of the distribution tank 7 has three bulkheads 38 arranged in a star shape.
It is divided into three identical fan-shaped sections.

これらの区画は配給タンク上部側が開放しているから、
粉末状燃料は上部から自由に進入することができる。These compartments are open at the top of the distribution tank, so
Powdered fuel can freely enter from the top.

また隔壁は流入床２４および該流入床と区画底部の外壁
との間の間隙をも区分する。The partition also delimits the inlet bed 24 and the gap between the inlet bed and the outer wall of the compartment bottom.

隔壁によって形成される下部の区画のそれぞれは流入床
の下側に別個に調節できるキャリアガス供給部のための
接続部を有する。Each of the lower compartments formed by the partition walls has a connection for a separately adjustable carrier gas supply below the inlet bed.

キャリアガスは流入床を貫いて下部のそれぞれの区画に
ある粉体充填層に進入し、これを弛緩させて局部的流動
層を形成する。The carrier gas passes through the inlet bed and enters the powder packed bed in each lower compartment, relaxing it and forming a localized fluidized bed.

気化反応器３１のそれぞれの所属のバーナ３０にキャリ
アガス・粉体流を排出するために上から垂直に導き出さ
れた輸送管９が、上記の各区画で終わっている。A transport pipe 9 leading out vertically from above for discharging the carrier gas/powder stream to the respective associated burner 30 of the vaporization reactor 31 terminates in each of the above-mentioned sections.

この実施態様では粉体流の調節は好ましくは個々の輸送
管９の粉体流測定点１６によって行われる。In this embodiment, the regulation of the powder flow is preferably carried out by means of powder flow measurement points 16 on the individual transport pipes 9.

これらの測定点１６はそれぞれのキャリアガス供給管の
調整弁１０に作用する。These measuring points 16 act on the regulating valve 10 of the respective carrier gas supply pipe.

配給タンクまでの粉体供給と気化反応器および後続の装
置での諸過程のその後の推移は、前途の実施例で述べた
説明と同様であるから、改めて説明することはしない。The powder supply to the distribution tank and the subsequent course of the processes in the vaporization reactor and subsequent equipment are similar to those given in the previous examples and will not be described again.

上記の実施例に相当する褐炭粉末気化設備で下記の操業
結果が得られる。The following operational results are obtained with the lignite powder vaporization equipment corresponding to the above example.

燃料 褐炭 粉末度 ０．２朋フルイ上１０％含水量
１０％灰分
１０％熱量 ４９５０ｋｃａ
ｌ ／に９燃料送入量 １０ ｔ
／ ｈ使用圧 ３０ ｂａｒ配給タ
ンク給圧用不活性ガスの消費量 準備圧 ３５ ｂａｒ量
７５ＯＮｍ／ｈキャリアガス消費量 準備圧 ３５ ｂａｒ量
６５ＯＮｍ”／ｈ気化用工業用酸素（９
６％０□）の消費量３６８ＯＮｍ”／ｈ 気化用蒸気の消費量 １．８５ｔ／ｈキヤリアガ
スの性質 窒 素 自家発生生ガス生ガスの組成（無水
） ＣＯ％ ５２．２ ５４．５ Ｈ２％ ３１．０ ３２．３ ＣＯ２％ １１．３ １１．８ ＣＨ４％ ０．４ ０．４ Ｎ２ ％ ５．１ １．０熱量 ｋｃａ
ｌ／Ｎｍ ２４００ ２５００生ガスの発生（正味
） Ｎｍ３／ｈ １４０００１３２００Fuel Lignite fineness 0.2 10% moisture content on sieve
10% ash content
10% calorific value 4950kca
9 fuel input per l/10 t
/ h Working pressure 30 bar Consumption of inert gas for supplying pressure in the distribution tank Preparation pressure 35 bar
75ONm/h Carrier gas consumption Preparation pressure 35 bar amount
65ONm”/h Industrial oxygen for vaporization (9
Consumption of 6%0□) 368ONm”/h Consumption of vaporizing steam 1.85t/h Properties of carrier gas Nitrogen Composition of self-generated raw gas (anhydrous) CO% 52.2 54.5 H2% 31 .0 32.3 CO2% 11.3 11.8 CH4% 0.4 0.4 N2% 5.1 1.0 Calorific value kca
l/Nm 2400 2500 Raw gas generation (net) Nm3/h 1400013200

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

第１図は粉末状燃料の高圧気化のための全方法の概略構
成図、第２図は１個の圧力締切りタンクを有する実施態
様の粉末状燃料の送り込みおよび配給系統の概略図、第
３図は２個の圧力締切りタンクを交互に使用する実施態
様の粉末状燃料の送り込みおよび配給系統の概略図、第
４図１は気化反応器の３個の別個のバーナに供給するた
めに下部を３つの別個の区画に仕切った配給タンクの概
略図、ロスはイ図Ａ−Ｂ線断面図、第５図は第４図によ
る配給タンクと３個の別個に調節できるバーナを備えた
実施態様の粉末状燃料の送り込みおよび配給系統の概略
図を示す。 １・・・・・・粉体供給管、２・・・・・・貯留バンカ
、３・・・・・・フィルタ、４，６・・・・・・遮断装
置、５・・・・・・圧力締切りタンク、７・・・・・・
配給タンク、９・・・・・・輸送管、１０．１４，１５
・・・・・・制御弁、１１・・・・・・遮断弁、１２・
・・・・・供給点、１３・・・・・・温度測定点、１６
・・・・・・粉体流測定装置、１７，１８，１９・・・
・・・充填高さ測定器、２０．２２・・・・・・遮断装
置、２１・・・・・・圧力締切りタンク、２３・・・・
・・粗計量装置、２４・・・・・・流入床、２５、２６
・・・・・・制御弁、２７・・・・・・充填高さ測定器
、２８・・・・・・供給管、２９・・・・・・減圧ガス
排出管、３０・・・・・・バーナ、３１・・・・・・気
化反応器、３２・・・・・・ガス冷却精製装置、３４・
・・・・・不活性ガス導管、３５・・・・・・キャリア
ガス導管、３６・・・・・・ガス状媒質導管、３７・・
・・・・循環圧縮機、３８・・・・・・隔壁。FIG. 1 is a schematic diagram of the overall method for high-pressure vaporization of powdered fuel; FIG. 2 is a schematic diagram of the feed and distribution system for powdered fuel in an embodiment with one pressure cut-off tank; FIG. 3 FIG. 4 is a schematic diagram of a powdered fuel feed and distribution system for an embodiment using two pressure shut-off tanks alternately; FIG. Schematic representation of a distribution tank divided into two separate compartments; Ross is a sectional view taken along the line A-B; FIG. 5 shows a powder embodiment of the distribution tank according to FIG. 1 shows a schematic diagram of a fuel pumping and distribution system. 1... Powder supply pipe, 2... Storage bunker, 3... Filter, 4, 6... Shutoff device, 5... Pressure cut-off tank, 7...
Distribution tank, 9...transport pipe, 10.14,15
... Control valve, 11 ... Shutoff valve, 12.
...Feeding point, 13...Temperature measurement point, 16
...Powder flow measuring device, 17, 18, 19...
... Filling height measuring device, 20.22 ... Shutoff device, 21 ... Pressure cut-off tank, 23 ...
...Rough metering device, 24...Inflow bed, 25, 26
... Control valve, 27 ... Filling height measuring device, 28 ... Supply pipe, 29 ... Decompression gas discharge pipe, 30 ...・Burner, 31... vaporization reactor, 32... gas cooling purification device, 34...
...Inert gas conduit, 35...Carrier gas conduit, 36...Gaseous medium conduit, 37...
... Circulating compressor, 38 ... Bulkhead.

Claims (1)

【特許請求の範囲】 １ 圧力締切りタンクを使ってガス状助剤で給圧するこ
とによって粉末状燃料を気化系統の圧力に加圧し、気化
反応器の単数側または複数個のバーすへの粉末状燃料の
供給をキャリアガス流によって行う、高圧で、酸素によ
り、または遊離酸素を含む流動粉体中の気化剤により部
分酸化する粉末状燃料の気化法において、高圧下の粉末
状燃料を単数側または複数個の圧力締切りタンク５から
配給タンク７に供給し、重力の作用で準静止充填物とし
て前記配給タンクの下部８に流入させ、次にこの配給タ
ンクの下部にキャリアガスとしてガス状媒質を吹込むこ
とによって充填物を局部的に限られた範囲で弛緩させ、
または局部的流動層に変換し、粉末状燃料が多量に負荷
されたキャリアガスを弛緩層または局部的流動層の中に
入り込む輸送管９を介して気化反応器３１のバーナ３０
に給送し、粉末状燃料と酸素、または遊離酸素を含む気
化剤とを反応させ、上記の輸送管９の自由断面積と充填
物の弛緩部分または局部的流動層の自由断面積の比を１
：５０ないし１：３００に選定し、気化反応器３１のバ
ーナに流れる粉体流の調節が。 弛緩または流動化のために配給タンク下部に吸込まれる
キャリアガス流の量を変化することによって行われ、か
つバーナに流れる粉体流の調節のためのパルスが公知の
ようにバーナに流れる粉体流の直接測定により、あるい
は粉体流に依存し、または粉体流と単位時間にバーナに
流れる酸素量との比に依存する気化反応器内に現れる量
の測定によって得られることを特徴とする方法。 ２ 配給タンク７に前置された複数個の圧力締切りタン
ク５が交互に使用され、常時または総時間の最大１０％
の短い切換時間を除いて少くとも一方の圧力締切りタン
ク５が放出のために配給タンク７と連結されることを特
徴とする特許請求の範囲第１項に記載に方法 ３ 単数側または複数個の圧力締切りタンク５の配給タ
ンク７への放出が粗計量装置２３または調節可能な粉体
流絞り装置を介して行われ、粗計量装置または調節可能
な絞り装置として公知のように例えば耐圧密封スターフ
ィーダ、粗計量スクリニーまたはすべり弁が使用され、
かつパルス発振法としての配給タンク７内の公知の充填
高さ測定法によって配給タンク７内の充填高さが所定の
範囲内で一定に保たれるように粗計量装置２３または絞
り装置の制御が行われることを特徴とする特許請求の範
囲第１項または第２項に記載の方法。 ４ 単数側または複数個の圧力締切りタンク５への給圧
のため、およびキャリアガスとして工業窒素または酸素
含量６％以下の窒素・空気混合物・工業用炭酸ガス・可
燃性ガス・この方法の内部で生成され回収される可燃性
ガスまたはその混合物を使用することを特徴とする特許
請求の範囲第１項乃至第３項のいずれか１項に記載の方
法。 ５ 不活性ガス例えば最大酸素含量６％の窒素およびま
たは工業用炭酸ガスで単数側または複数個の圧力締切り
タンク５の給圧を行い、かつキャリアガスとして可燃性
ガスを使用することを特徴とする特許請求の範囲第１項
乃至第３項のいずれか１項に記載の方法。 ６ 不活性ガス例えば最大酸素含量６％の窒素およびま
たは工業用炭酸ガスで単数側または複数個の圧力締切り
タンク５の給圧を行い、かつキャリアガスとして空気ま
たは最大酸素含量２１％以下の酸素・不活性ガス混合物
を使用することを特徴とする特許請求の範囲第１項乃至
第３項のいずれか１項に記載の方法。 ７ 粉末状燃料として好ましくは粒度０．５間以下に粉
砕した、好ましくは含水量１２％以下の乾燥褐炭を使用
し、かつ配給タンク下部８のキャリアガスの自由断面に
関する速度が０．００５〜０．０２５ｍ／ｓ、配給タン
ク下部８からバーナ３０への輸送管９内の粉体、キャリ
アガス混合物の速度が１．０〜７．０ ｍ ／ Ｓであ
ることを特徴とする特許請求の範囲第１項乃至第６項の
いずれか１項に記載の方法。 ８ 粉末状燃料貯留バンカ、単数側または複数個の圧力
締切りタンク・配給タンク・気化反応器の単数側または
複数個のバーナに至る単数側または複数個の粉体送給管
（輸送管）・気化反応器・ガス冷却および後処理装置並
びに必要な連結管、調整・制御装置および必要な媒質の
供給と生成された産物および廃物の排出のための装置に
おいて、配給タンク７が円形断面の直立筒状の上部と直
立筒状上部側が開放している単数側または複数個の下部
８あるいは直立筒状の上部の側が開放している複数個の
区画に分割された下部８から成り、該下部８または複数
個の下部８のそれぞれまたは下部８の各区画が二重底を
備え、二重底の内壁が通気性材料で作られ、流入床とし
て構成され、二重底の外壁がガス状媒質の流量調節自在
な導入のための少くとも１個の接続部を具備し、配給タ
ンク７の側壁または二重底または直立筒状の上部を貫い
て単数側または複数個の内室の中に輸送管の役割をする
１個の管９または各々１個の管９が突出し、該管が単数
側または複数個のバーナ３０と連結されていることを特
徴とする装置。 ９ 配給タンク７の下部８の断面積が直立筒状の上部よ
り小さく、かつ配給タンクの上部にある粉末状燃料充填
層が全断面に均一に、導路を形成せずに下方に向って、
配給タンク７の単数側または複数個の下部８もしくは下
部８の分割された各区画にすべって行くように上部から
単数側または複数個の下部８もしくは下部８の分割され
た各区画への断面収縮部が形成されていることを特徴と
する特許請求の範囲第８項に記載の装置。 １０キヤリアガスのために設定された温度・圧力条件の
もとで、底部の全断面に対して０．００５〜０、０２５
ｍ／ ｓのガス速度で流入床が、配給タンク７内の粉
末状燃料充填層のかさ比重と高さの積に等しいか、また
はそれより大きい圧力損失を有することを特徴とする特
許請求の範囲第８項または第９項に記載の装置。 １１ 配給タンク７への粉末状燃料の供給管に公知の粗
計量装置２３または調節自在な粉体流絞り装置が設計さ
れており、この粗計量装置または調節自在な絞り装置の
上方で供給管が分岐し、２個以上の圧力締切りタンク５
を交互に配給タンク７に放出することができ、該配給タ
ンク７の上部が公知の充填高さ測定装置１７を装備し、
該測定装置は適当な調節装置を介して粗計量装置２３ま
たは調節自在な絞り装置と連結されており、かつ常時ま
たは総時間の最大１０％の短い切換時間を除いて少くと
も１個の圧力締切りタンク５が放出のために粗計量装置
２３または調整自在な絞り装置を介して配給タンク７と
連結されていることを特徴とする特許請求の範囲第８項
乃至第１０項のいずれか１項に記載の方法。 １２圧力締切りタンク５が公知の適当な充填高さ測定器
１７を具備し、該測定器が圧力締切りタンク５の附属品
の制御装置に作用して、その時放出のために配給タンク
７と連結されている圧力締切りタンク５の最小充填高さ
または空状態が指示された時、給圧が行われ、粉末状燃
料が充填された別の圧力締切りタンク５への切換を保証
することを特徴とする特許請求の範囲第１１項に記載の
装置。 １３単数個または複数個の配給タンク７の下部８または
該下部８の分割された各区画から気化反応器３１の単数
側または複数個のバーナ３０に至る単数側または複数個
の輸送管９に、バーナ３０への粉体流に対する公知の測
定装置が設置されており、該測定装置が調整装置を介し
て、単数側または複数個の流入床への単数側または複数
個のキャリアガス供給管にある調整器１０に作用するこ
とを特徴とする特許請求の範囲第８項乃至第１２項のい
ずれか１項に記載の装置。 １４粉体流または粉体流と単位時間にバーナ３０に流れ
る酸素量との比に依存する気化反応器３１の測定量、例
えば気化反応器３１の反応室温度の測定量が調節装置を
介して単数側または複数個の流入床への単数側または複
数個のキャリアガス供給管の調整器具１０に作用するこ
とを特徴とする特許請求の範囲第８項乃至第１２項のい
ずれか１項に記載の装置。[Claims] 1. Pressurize the powdered fuel to the pressure of the vaporization system by pressurizing it with a gaseous auxiliary using a pressure cut-off tank, and transfer the powdered fuel to one or more bars of the vaporization reactor. In a method of vaporization of powdered fuels in which the fuel is partially oxidized at high pressure by oxygen or by a vaporizing agent in a flowing powder containing free oxygen, the supply of fuel is by a carrier gas stream, in which the powdered fuel under high pressure is A distribution tank 7 is fed from a plurality of pressure-shutoff tanks 5 and allowed to flow under the action of gravity as a quasi-static charge into the lower part 8 of said distribution tank, into which a gaseous medium is then blown as a carrier gas. The filling is loosened locally in a limited range by
Alternatively, the burner 30 of the vaporization reactor 31 is converted into a localized fluidized bed and the carrier gas loaded with a large amount of powdered fuel is passed through the transport pipe 9 into the relaxed bed or into the localized fluidized bed.
The powdered fuel is reacted with oxygen or a vaporizing agent containing free oxygen, and the ratio of the free cross-sectional area of the transport pipe 9 to the free cross-sectional area of the relaxed portion of the packing or the local fluidized bed is determined. 1
:50 to 1:300 to adjust the powder flow flowing to the burner of the vaporization reactor 31. This is done by varying the amount of carrier gas flow sucked into the lower part of the distribution tank for relaxation or fluidization, and pulses for regulation of the powder flow flowing to the burner as known in the art. characterized in that it is obtained by direct measurement of the flow or by measurement of the amount present in the vaporization reactor, which depends on the powder flow or on the ratio of the powder flow and the amount of oxygen flowing into the burner per unit time. Method. 2 A plurality of pressure cut-off tanks 5 placed in front of the distribution tank 7 are used alternately, all the time or at most 10% of the total time.
Method 3 according to claim 1, characterized in that at least one pressure cut-off tank 5 is connected with a distribution tank 7 for discharge, except for short switching times. The discharge of the pressure cut-off tank 5 into the distribution tank 7 takes place via a coarse metering device 23 or an adjustable powder flow throttling device, for example a pressure-tight sealed star feeder, known as a coarse metering device or adjustable powder flow throttling device. , coarse metering screenies or slip valves are used;
In addition, the coarse metering device 23 or the throttle device is controlled so that the filling height in the distribution tank 7 is kept constant within a predetermined range by a known method of measuring the filling height in the distribution tank 7 as a pulse oscillation method. A method according to claim 1 or 2, characterized in that the method is carried out. 4 For supplying pressure to one or more pressure-shutoff tanks 5 and as carrier gas technical nitrogen or nitrogen-air mixtures with an oxygen content of up to 6%, industrial carbon dioxide, flammable gases, etc. 4. A method according to claim 1, characterized in that a combustible gas or a mixture thereof is used which is produced and recovered. 5. The pressure cut-off tank or tanks 5 are pressurized with an inert gas, for example nitrogen with a maximum oxygen content of 6% and/or industrial carbon dioxide, and a flammable gas is used as carrier gas. A method according to any one of claims 1 to 3. 6 Pressurizing the pressure shut-off tank or tanks 5 with an inert gas, for example nitrogen with a maximum oxygen content of 6% and/or industrial carbon dioxide, and as carrier gas air or oxygen with a maximum oxygen content of up to 21%. 4. Process according to claim 1, characterized in that an inert gas mixture is used. 7. Dry lignite, preferably pulverized to a particle size of 0.5 or less, preferably with a moisture content of 12% or less, is used as the powdered fuel, and the velocity with respect to the free cross section of the carrier gas in the lower part 8 of the distribution tank is between 0.005 and 0. .025 m/s, the velocity of the powder, carrier gas mixture in the transport pipe 9 from the distribution tank lower part 8 to the burner 30 is between 1.0 and 7.0 m/s. The method according to any one of Items 1 to 6. 8. Powdered fuel storage bunker, one or more pressure cut-off tanks, distribution tanks, one or more powder feed pipes (transport pipes) to one or more burners of the vaporization reactor, vaporization In the reactor, gas cooling and work-up equipment as well as the necessary connecting pipes, regulation and control equipment and equipment for supplying the necessary media and discharging the products and waste produced, the distribution tank 7 is of the form of an upright cylinder with a circular cross section. and an upright cylindrical lower part 8 with one or more sides open on the upper side or a lower part 8 divided into a plurality of compartments with the upright cylindrical upper side open, said lower part 8 or Each of the lower parts 8 or each compartment of the lower part 8 has a double bottom, the inner wall of the double bottom is made of a breathable material and configured as an inlet bed, and the outer wall of the double bottom is for regulating the flow rate of the gaseous medium. with at least one connection for free introduction, acting as a transport pipe through the side wall or double bottom or upright cylindrical top of the distribution tank 7 into the side or interior chambers; A device characterized in that a tube 9 or each tube 9 protrudes and is connected to the burner or burners 30. 9. The cross-sectional area of the lower part 8 of the distribution tank 7 is smaller than the upright cylindrical upper part, and the powdered fuel filling layer in the upper part of the distribution tank is uniformly distributed over the entire cross section, without forming a conduit,
Cross-sectional contraction from the upper part to the side or parts of the lower part 8 or each of the divided parts of the lower part 8 so as to slide into the side or parts of the lower part 8 or each of the divided parts of the lower part 8 of the distribution tank 7 9. A device according to claim 8, characterized in that a portion is formed. 10 Under the temperature and pressure conditions set for the carrier gas, 0.005 to 0.025 for the entire bottom section
Claim characterized in that, at a gas velocity of m/s, the inlet bed has a pressure drop equal to or greater than the product of the bulk specific gravity and the height of the packed bed of powdered fuel in the distribution tank 7. Apparatus according to clause 8 or 9. 11 A known coarse metering device 23 or an adjustable powder flow throttling device is designed in the feed pipe for the powdered fuel to the distribution tank 7, above which the feed pipe is connected. Branch, two or more pressure cut-off tanks 5
can be discharged alternately into a distribution tank 7, the upper part of which is equipped with a known filling height measuring device 17,
The measuring device is connected via a suitable regulating device to a rough metering device 23 or to an adjustable throttling device, and at least one pressure cut-off is present at all times or except for short switching times of up to 10% of the total time. 10. Claims 8 to 10, characterized in that the tank 5 is connected to the distribution tank 7 for discharge via a coarse metering device 23 or an adjustable throttle device. Method described. 12 The pressure cut-off tank 5 is equipped with a known and suitable filling height measuring device 17, which acts on the control device of the accessories of the pressure cut-off tank 5, which are then connected to the distribution tank 7 for discharge. It is characterized in that when a minimum filling height or an empty state of a pressure cut-off tank 5 is indicated, pressure is applied and a switchover to another pressure cut-off tank 5 filled with powdered fuel is ensured. Apparatus according to claim 11. 13 to one or more transport pipes 9 from the lower part 8 of the distribution tank or tanks 7 or from each divided compartment of the lower part 8 to the side or burners 30 of the vaporization reactor 31; A known measuring device for the powder flow into the burner 30 is installed, which measuring device is located in the carrier gas supply line(s) to the side(s) inlet bed(s) via a regulating device. 13. Device according to any one of claims 8 to 12, characterized in that it acts on a regulator (10). 14 A measured variable of the vaporization reactor 31, for example a measured variable of the reaction chamber temperature of the vaporization reactor 31, which depends on the powder flow or the ratio of the powder flow and the amount of oxygen flowing into the burner 30 per unit time, is controlled via a regulating device. 13. According to any one of claims 8 to 12, it acts on a regulating device 10 of the carrier gas supply pipe(s) to the inflow bed(s). equipment.
JP11418278A 1977-09-19 1978-09-19 Method and apparatus for high-pressure vaporization of powdered fuel Expired JPS594476B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DD10J/201064 1977-09-19
DD20106477A DD147188A3 (en) 1977-09-19 1977-09-19 METHOD AND DEVICE FOR PRESSURE GASIFICATION OF DUST-SOUND FUELS

Publications (2)

Publication Number Publication Date
JPS5499103A JPS5499103A (en) 1979-08-04
JPS594476B2 true JPS594476B2 (en) 1984-01-30

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ID=5509765

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JP11418278A Expired JPS594476B2 (en) 1977-09-19 1978-09-19 Method and apparatus for high-pressure vaporization of powdered fuel

Country Status (15)

Country Link
JP (1) JPS594476B2 (en)
AT (1) AT378199B (en)
AU (1) AU520077B2 (en)
CS (1) CS222955B1 (en)
DD (1) DD147188A3 (en)
DE (1) DE2831208A1 (en)
FR (1) FR2403377A1 (en)
GB (1) GB2004993B (en)
GR (1) GR65885B (en)
HU (1) HU180684B (en)
IN (1) IN150296B (en)
PL (1) PL111707B1 (en)
SU (1) SU1167194A1 (en)
TR (1) TR20754A (en)
YU (2) YU220078A (en)

Families Citing this family (49)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2947222C2 (en) * 1979-11-23 1987-05-07 Carbon Gas Technologie GmbH, 4030 Ratingen Device for gasification of solid, dusty to lumpy carbonaceous fuels and their use
DD206309A3 (en) * 1981-07-17 1984-01-18 Kretschmer Horst METHOD FOR REGULATING MASS STRUCTURES
CA1208258A (en) * 1982-06-23 1986-07-22 Bernardus H. Mink Process for conveying a particulate solid fuel
JPH0633370B2 (en) * 1984-11-09 1994-05-02 株式会社日立製作所 Coal gasification power plant
JPS61254695A (en) * 1985-05-07 1986-11-12 Mitsubishi Heavy Ind Ltd Feeding of coal and char to oxygen blow coal gasification furnace
JPH047174Y2 (en) * 1985-08-09 1992-02-26
DE3701399A1 (en) * 1986-02-24 1987-08-27 Freiberg Brennstoffinst Method and device for determining rheological characteristic values of fine bulk goods
DE3809851A1 (en) * 1988-03-24 1989-10-05 Krupp Koppers Gmbh METHOD FOR CONVEYING A FINE-GRAINED TO DUST-SHAPED FUEL IN A GASIFICATION REACTOR UNDER INCREASED PRESSURE
DE3813357A1 (en) * 1988-04-21 1989-11-02 Krupp Koppers Gmbh DEVICE FOR THE GASIFICATION OF FINE-GRAIN TO DUST-SHAPED FUELS
DE4004874A1 (en) * 1990-02-16 1991-08-29 Krupp Koppers Gmbh METHOD FOR OPERATING A PLANT FOR GASIFYING SOLID FUELS
DE4037490A1 (en) * 1990-11-26 1991-05-29 Deutsches Brennstoffinst Disposal of plastic material made of phenol:formaldehyde condensate - by gasifying and/or carbonising, comminuting and then mixing with crude or dry coal
DE4109063C2 (en) * 1991-03-20 1993-12-23 Noell Dbi Energie Entsorgung Process for the simultaneous recycling of lumpy and flowable combustible waste materials and residues
DE4125520C2 (en) * 1991-08-01 1998-11-12 Schwarze Pumpe Energiewerke Ag Process for the gasification of solid and liquid waste
DE4420449C5 (en) * 1994-02-15 2004-02-05 Thermoselect Ag Process for storing heterogeneous waste
DE4435349C1 (en) * 1994-09-21 1996-05-02 Noell En Und Entsorgungstechni Destruction of pollutants and gasifying of waste in a fluidised bed
DE19536383C2 (en) * 1995-09-29 2001-09-13 Krc Umwelttechnik Gmbh Method and device for the gasification of low calorific value fuels
DE19609721C2 (en) * 1996-03-13 2002-09-12 Noell Krc Energie & Umwelt Process for the energetic utilization of residual and waste materials as well as low calorific fuels in a steam power plant
DE19642161C2 (en) * 1996-10-12 2001-10-11 Krc Umwelttechnik Gmbh Process for the environmentally friendly recycling of residual waste
CN1919980B (en) * 2005-08-24 2012-07-04 未来能源有限公司 Gasification method and device for producing synthesis gases by partial oxidation of fuels containing ash at elevated pressure and with quench-cooling of the crude gas
DE102005041931B4 (en) * 2005-09-03 2018-07-05 Siemens Aktiengesellschaft Apparatus for producing synthesis gases by partial oxidation of ash-containing fuels under elevated pressure with partial quenching of the raw gas and waste heat recovery
DE202005021661U1 (en) * 2005-09-09 2009-03-12 Siemens Aktiengesellschaft Apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels and full quenching of the raw gas
DE102005047583C5 (en) * 2005-10-04 2016-07-07 Siemens Aktiengesellschaft Method and device for the controlled supply of fuel dust into an entrained flow gasifier
DE102005048488C5 (en) * 2005-10-07 2020-07-02 Siemens Aktiengesellschaft Method and device for high power entrained flow gasifiers
US20070225382A1 (en) 2005-10-14 2007-09-27 Van Den Berg Robert E Method for producing synthesis gas or a hydrocarbon product
AU2006203439B2 (en) * 2006-08-09 2012-05-03 Siemens Energy Global GmbH & Co. KG Method and device for high-capacity entrained flow gasifier
US8303673B2 (en) * 2006-08-25 2012-11-06 Siemens Aktiengesellschaft Method and device for a high-capacity entrained flow gasifier
DE102008014475A1 (en) * 2008-03-17 2009-11-12 Uhde Gmbh Method and device for the metered removal of a fine to coarse-grained solid or solid mixture from a storage container
PL2257613T3 (en) * 2008-03-27 2017-06-30 Thyssenkrupp Industrial Solutions Ag Device for producing synthesis gas with a gasification reactor and connected to a quench chamber
DE202008016646U1 (en) * 2008-07-29 2009-07-02 Siemens Aktiengesellschaft Multi-stage dust dosing system for high pressures by means of locks
DE102009006384A1 (en) * 2009-01-28 2010-08-19 Uhde Gmbh Method for supplying an entrainment gasification reactor with fuel from a reservoir
DE102009048931B4 (en) 2009-10-10 2014-06-18 Linde Ag Dosing system, dense phase conveying system and method for feeding dusty bulk material
DE102009048961B4 (en) 2009-10-10 2014-04-24 Linde Ag Dosing device, dense phase conveying system and method for feeding dusty bulk material
JP5675297B2 (en) * 2010-11-22 2015-02-25 三菱重工業株式会社 Gasification facilities and coal gasification combined power generation facilities
DE102012217890B4 (en) 2012-10-01 2015-02-12 Siemens Aktiengesellschaft Combination of pressure charging and metering for continuous delivery of fuel dust into an entrainment gasification reactor over long distances
DE102013203739A1 (en) 2013-03-05 2014-09-11 Siemens Aktiengesellschaft Combination of pressure charging and metering for continuous delivery of fuel dust into an entrainment gasification reactor over long distances
DE102013216948B4 (en) 2013-08-26 2015-12-03 Siemens Aktiengesellschaft Device for measuring pressure and differential pressure in dust conveyor lines
DE102013224037A1 (en) 2013-11-25 2015-05-28 Siemens Aktiengesellschaft Preparation and conditioning of synthesis crude gases
DE102013224039A1 (en) 2013-11-25 2015-05-28 Clariant International Ltd. Treatment of synthesis gases from a gasification facility
DE102014202236A1 (en) 2014-02-07 2015-08-13 Siemens Aktiengesellschaft Auxiliary gas element for conveying dust streams
DE102014205823A1 (en) 2014-03-28 2015-10-01 Siemens Aktiengesellschaft Device for pneumatically conveying fuel dust into an air flow gasifier
DE202015106150U1 (en) 2015-11-13 2015-12-07 Choren Industrietechnik GmbH Pressure vessel with internals
DE102015119635B4 (en) 2015-11-13 2019-10-17 Choren Industrietechnik GmbH Pressure vessel with internals
DE102016201182A1 (en) 2016-01-27 2017-07-27 Siemens Aktiengesellschaft Diaphragm pump with dust suction from below
DE102016216016A1 (en) 2016-08-25 2018-03-15 Siemens Aktiengesellschaft Production of a porous aluminum filter for a membrane pump
DE102016216006A1 (en) 2016-08-25 2018-03-01 Siemens Aktiengesellschaft Double membrane for a dust pump
DE102016216012A1 (en) 2016-08-25 2018-03-01 Siemens Aktiengesellschaft Diaphragm pump with porous, curved aluminum filter
CN111690441B (en) * 2019-03-13 2021-02-26 中国石化工程建设有限公司 System for gasifier firing and method for gasifier firing
WO2021083715A1 (en) 2019-10-31 2021-05-06 Basf Se Method and system for operating a descending moving bed reactor with flowable granular material
JP2023085579A (en) * 2020-04-30 2023-06-21 株式会社ジャパンブルーエナジー Biomass gasification device

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1110897A (en) * 1953-08-27 1956-02-17 Union Carbide & Carbon Corp Pulverized coal pressure feeding and conveying apparatus
DE1189226B (en) * 1961-10-11 1965-03-18 Koppers Gmbh Heinrich Process for transferring a finely divided solid fuel from a room at normal pressure into a room under increased pressure
BE638732A (en) * 1962-10-24
JPS50136301A (en) * 1974-04-18 1975-10-29
DE2434526C2 (en) * 1974-07-18 1983-01-13 Shell Internationale Research Maatschappij B.V., 2501 's-Gravenhage Method and device for introducing finely divided solid fuel into a gasification chamber under increased pressure
NL7514128A (en) * 1975-12-04 1977-06-07 Shell Int Research METHOD AND EQUIPMENT FOR PARTIAL COMBUSTION OF CARBON POWDER.
US4057402A (en) * 1976-06-28 1977-11-08 Institute Of Gas Technology Coal pretreatment and gasification process

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PL111707B1 (en) 1980-09-30
YU220078A (en) 1982-08-31
AT378199B (en) 1985-06-25
IN150296B (en) 1982-09-04
YU111182A (en) 1984-02-29
JPS5499103A (en) 1979-08-04
FR2403377B1 (en) 1985-01-25
AU520077B2 (en) 1982-01-14
SU1167194A1 (en) 1985-07-15
PL209688A1 (en) 1979-06-18
DE2831208A1 (en) 1979-03-29
DE2831208C2 (en) 1988-01-14
HU180684B (en) 1983-04-29
GB2004993B (en) 1982-03-31
FR2403377A1 (en) 1979-04-13
CS222955B1 (en) 1983-08-26
YU42038B (en) 1988-04-30
AU3989778A (en) 1980-03-20
GR65885B (en) 1980-12-01
TR20754A (en) 1982-06-24
DD147188A3 (en) 1981-03-25
ATA524278A (en) 1984-11-15

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