JPH0324195A - Coal gasification reactor - Google Patents

Coal gasification reactor

Info

Publication number
JPH0324195A
JPH0324195A JP2135525A JP13552590A JPH0324195A JP H0324195 A JPH0324195 A JP H0324195A JP 2135525 A JP2135525 A JP 2135525A JP 13552590 A JP13552590 A JP 13552590A JP H0324195 A JPH0324195 A JP H0324195A
Authority
JP
Japan
Prior art keywords
reactor
outlet
slag
diameter ratio
length
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.)
Granted
Application number
JP2135525A
Other languages
Japanese (ja)
Other versions
JP2932198B2 (en
Inventor
Hendrikus Johannes Antonius Hasenack
ヘンドリカス・ヨハネス・アントニウス・ハセナツク
Petrus H W M Daverveldt
ペトラス・ヘンリカス・ヴイルヘルムス・マリエ・ダーフエルヴエルト
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Publication of JPH0324195A publication Critical patent/JPH0324195A/en
Application granted granted Critical
Publication of JP2932198B2 publication Critical patent/JP2932198B2/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic 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
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

PURPOSE: To provide a coal gasification reactor which prevents ascending of slag and entrainment of slag drops and improves slagging efficiency by placing a vertical cylinder, having a predetermined length to diameter ratio, between the output of the reactor and the inlet of a rapid cooling section.
CONSTITUTION: In a reaction vessel 1 comprising a slag outlet 2 at the bottom, a plurality of burners 3 emitting a flame in the tangential direction on the side wall, and a gas outlet 4 at the top, a vertical cylinder 4a having a length to diameter ratio, Ls to Ds ratio, of 4 to 6 is provided between the gas outlet 4 and a rapid cooling section inlet 5a of a rapid cooling system 5.
COPYRIGHT: (C)1991,JPO

Description

【発明の詳細な説明】 本発明は微粉砕固体炭素含有燃料および酸化剤の部分酸
化法を実施するための反応器に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a reactor for carrying out a process for partial oxidation of pulverized solid carbon-containing fuels and oxidizers.

微粉砕固体炭素含有燃料は、微粉砕固体炭素含有燃料を
酸素含有ガスで反応器中で部分燃焼させることによる合
成ガスの製造法に適用され、そこで部分燃焼プロセス中
に生じた液体スラグは反応器の底の出口から取出されそ
して重力でスラグ排出手段を通って水浴またはスラグ鵞
，冷槽へ入り、そこで急冷により固化する。The pulverized solid carbon-containing fuel is applied in the process of producing synthesis gas by partial combustion of the pulverized solid carbon-containing fuel with oxygen-containing gas in a reactor, where the liquid slag produced during the partial combustion process is The slag is removed from the outlet at the bottom of the slag and passes by gravity through a slag discharge means into a water bath or slag tank, where it solidifies by rapid cooling.

微粉砕固体炭素含有燃料を酸素含有ガスとして実質的に
純粋の酸素で部分燃焼すると一酸化炭素と水素から主と
して或る合戒ガスを生ずる．酸素含有ガスが空気または
酸素富化空気である場合は生ずる合或ガスは勿論実質的
な量の窒素をも含有する．微粉砕固体炭素含有燃料は一
般に石炭または褐炭、泥炭、木材、コークス、すす等の
ような他の固体燃料を意味するが、液体またはガスと粒
状固体燃料の混合物も可能である。Partial combustion of pulverized solid carbon-containing fuel with substantially pure oxygen as an oxygen-containing gas produces a certain compound gas primarily from carbon monoxide and hydrogen. If the oxygen-containing gas is air or oxygen-enriched air, the resulting reaction gas will of course also contain substantial amounts of nitrogen. Finely ground solid carbon-containing fuel generally refers to coal or other solid fuels such as lignite, peat, wood, coke, soot, etc., but mixtures of granular solid fuels with liquids or gases are also possible.

有利には、調節剤も反応器中に導入される。調節剤の目
的は反応器の温度に低減効果を及ぼすことである．これ
は調節剤と合或ガス製造の反応体および／または生或物
との間の吸熱反応により確保される．適当な調節剤はス
チームおよび二酸化炭素である。Advantageously, a regulator is also introduced into the reactor. The purpose of the regulator is to have a reducing effect on the temperature of the reactor. This is ensured by an endothermic reaction between the regulator and the reactants and/or products of the gas production. Suitable moderators are steam and carbon dioxide.

ガス化は有利には１２００ないし１７００℃の範囲の温
度および１ないし２００バールの範囲の圧力で実施され
る． 合或ガスの製造を行なう反心器はいかなる適当な形状を
有してもよい． 微粉砕固体炭素含有燃料および酸素含有ガスの反応器へ
の供給は目的に適するいかなる方法でも行なうことがで
き、詳述はしない． 部分燃焼反応で生じる液体スラグは落下しそして反応器
底に配設された出口を通って排出される．例えば石炭ガ
ス化のような微粉砕固体炭素含有燃料の部分酸化法では
、燃料は供給装置からガス化器へ適当なキャリャ流体に
より送られる．熱い生戒物ガスは通常、粘着性粒子を含
有し、これは冷却すると粘着性を失う。Gasification is advantageously carried out at a temperature in the range 1200 to 1700°C and a pressure in the range 1 to 200 bar. The reactor for producing the gas may have any suitable shape. The feeding of the pulverized solid carbon-containing fuel and the oxygen-containing gas to the reactor can be carried out in any manner suitable for the purpose and will not be described in detail. The liquid slag resulting from the partial combustion reaction falls and is discharged through an outlet located at the bottom of the reactor. In partial oxidation processes of finely divided solid carbon-containing fuels, such as coal gasification, the fuel is conveyed from a feeder to a gasifier by a suitable carrier fluid. Hot biological gases usually contain sticky particles that lose their stickiness when cooled.

熱い生成物ガス中の粘着性粒子は生戒物ガスを更に処理
するプラントにおいて問題を起すであろう。何故ならば
、粒子の例えば壁、弁または出口への望ましくない沈着
はプロセスに悪影響を及ぼすであろうからである．更に
、そのような沈着物は除去が非常に困難である。粘着性
粒子は部分的にまたは完全に溶融状態にありうる；それ
らは金属、塩または灰からなり得、そして一般にこれら
粒子は約８００″Ｃ以下の温度で粘着性を失う。Sticky particles in the hot product gas may cause problems in plants that further process raw material gases. This is because undesired deposition of particles, for example on walls, valves or outlets, will adversely affect the process. Moreover, such deposits are very difficult to remove. Sticky particles can be partially or completely molten; they can be composed of metals, salts or ash, and generally these particles lose their stickiness at temperatures below about 800''C.

従って熱い生成物ガスは反応器の頂部の生或物出口の上
に位置する急冷域で急冷される。急冷域では生成物ガス
を冷却するために例えば水またはガスのような適当な急
冷媒が生成物ガス中に導入される． 微粉砕固体炭素含有燃料の部分酸化法において接線方向
に火を放つバーナを適用することは知られており、即ち
複数の接線方向に向けられたバーナが反応容器の壁の円
周方向の間隔をおいた点に同じ水平レベル上に配置され
そして反応器中に渦巻流を生じさせる。The hot product gas is therefore quenched in a quench zone located above the product outlet at the top of the reactor. In the quench zone, a suitable quenching medium, such as water or gas, is introduced into the product gas to cool it. It is known to apply tangentially firing burners in the partial oxidation process of finely ground solid carbon-containing fuels, i.e. a plurality of tangentially oriented burners are used to increase the circumferential spacing of the walls of the reaction vessel. at the same horizontal level and create a swirling flow in the reactor.

しかしこの反応器設計は未だ若干の欠点を有するようで
ある：スラグ化効率はかなり小さい（４０−５０％）；
反応器出口でスラグ上昇の起る可能性がありそして熱い
合威ガスの反応器から急冷部へ短絡が起りうる． 本発明の目的は９０−９５％のスラグ化効率を有する反
応器設計を提供することである．本発明の他の目的はス
ラグ上昇およびスラグ滴連行が防止される反応器設計を
提供することである， 本発明の更に他の目的は合或ガスの前記短絡が防止され
る反応器設計を提供することである．従って本発明は微
粉砕固体炭素含有燃料および酸化剤（ｏｘｉｄａｎｔ）
の部分酸化法を実施するための反応器であって、頂部に
生成物ガス用出口、底部にスラグ出口、側壁に複数のバ
ーナ開口、円周方向の間隔をおいた点に同じ水平レベル
上に小さな放火角で配置された複数の接線方向に向けら
れたバーナを有する反応器容器を含み、その出口の上に
急冷部を備えた前記反応器において、反応器出口と急冷
部入口の間に所定の長さ対直径の比を有する立て筒が配
置された反応器を提供する．用語放火角はバーナの対称
軸とバーナの中心および同じ水平レベルでの反応器の中
心を通る線の間の角度として定められる。However, this reactor design still appears to have some drawbacks: the slagging efficiency is quite low (40-50%);
Slag rise can occur at the reactor outlet and short circuiting of hot combined gas from the reactor to the quench zone can occur. It is an object of the present invention to provide a reactor design with a slagging efficiency of 90-95%. Another object of the invention is to provide a reactor design in which slag rise and slag droplet entrainment is prevented. Still another object of the invention is to provide a reactor design in which said shorting of the gas is prevented. It is to be. Accordingly, the present invention provides a finely divided solid carbon-containing fuel and an oxidant.
A reactor for carrying out a partial oxidation process with an outlet for the product gas at the top, a slag outlet at the bottom, a plurality of burner openings in the side walls, on the same horizontal level at circumferentially spaced points. In said reactor comprising a reactor vessel having a plurality of tangentially oriented burners arranged at a small firing angle and with a quench section above its outlet, a predetermined distance between the reactor outlet and the quench section inlet is provided. A reactor is provided in which a vertical tube having a length-to-diameter ratio of is arranged. The term firing angle is defined as the angle between the axis of symmetry of the burner and the line passing through the center of the burner and the center of the reactor at the same horizontal level.

本発明を添付図面を参照してより詳細に実施例により記
載する。The invention will be described in more detail by way of example with reference to the accompanying drawings, in which: FIG.

第１図を参照して、反応器容器（１）はその底部にスラ
グ出口（２）、複数の接線方向に火を放つバーナ（３）
、その頂部にガス出口（４）および反応器出口（４）の
上に急冷入口（５ａ）を含む急冷系（５）を備える．接
線方向に向けられたバーナ（３）は円周方向の間隔をお
いた点に同じ水平レベル上に配置されそして反応器容器
（１）中に渦巻流を起す。Referring to Figure 1, the reactor vessel (1) has a slag outlet (2) at its bottom and a plurality of tangentially firing burners (3).
, with a quenching system (5) comprising a gas outlet (4) at its top and a quenching inlet (5a) above the reactor outlet (4). The tangentially oriented burners (3) are arranged on the same horizontal level at circumferentially spaced points and create a swirling flow in the reactor vessel (1).

急冷系（５）はその出口（６）で合或ガスを更に処理す
る装置に連結される，。そのような装置は当該技術分野
の熟達者には知られており、詳述しない。第２図では第
１図と同じ参照番号が使用されている。The quenching system (5) is connected at its outlet (6) to a device for further processing the combined gas. Such devices are known to those skilled in the art and will not be described in detail. The same reference numerals are used in FIG. 2 as in FIG. 1.

第２図において反応器（１）はその出口（４）に延長管
または立て筒（４ａ）を備える。この延長部は反応器出
口（４）と急冷部入口（５ａ）の間に位置しそして所定
の長さ対直径の比Ｌ　ｓ　／　ＤＳを有する． 急冷系（５）は反応器出口から離れた位置におかれる．
有利にはＬ　ｓ　／　Ｄ　ｓは４ないし６であり、より
特にＬ　ｓ　／　Ｄ　ｓは５である（第２図に示すよう
に）． 更に、第２図において、急冷系（５）は長さ対直径の比
Ｌｑ／Ｄｑ＝３を有しそして反応器（１）は長さ対直径
の比Ｌ　ｒ　／　Ｄ　ｒ　＝　３を有する。In FIG. 2, the reactor (1) is equipped with an extension tube or stand (4a) at its outlet (4). This extension is located between the reactor outlet (4) and the quench section inlet (5a) and has a predetermined length-to-diameter ratio L s /DS. The quenching system (5) is located away from the reactor outlet.
Advantageously L s /D s is between 4 and 6, more particularly L s /D s is 5 (as shown in FIG. 2). Furthermore, in FIG. 2, the quenching system (5) has a length-to-diameter ratio Lq/Dq=3 and the reactor (1) has a length-to-diameter ratio L r /D r =3.

第３ａ図は４つのバーナＡ，Ｂ，Ｃ，Ｄを含む接線方向
バーナ配置を示す。バーナは水平に配置されそして中心
点已に向けられ、これは放火角が０度であることを意味
する． 第３ｂ図は４つのバーナＡ′、Ｂ′、Ｃ′、Ｄ′を含み
放火角が５度である本発明の接線方向バーナ配置を示す
。有利には、本発明による放火角は３ないし５度の範囲
である．バーナは所定面積を有する中心円Ｅ′に向けら
れる。Figure 3a shows a tangential burner arrangement comprising four burners A, B, C, D. The burner is placed horizontally and directed towards the center point, which means the firing angle is 0 degrees. FIG. 3b shows a tangential burner arrangement of the invention including four burners A', B', C', D' and a firing angle of 5 degrees. Advantageously, the firing angle according to the invention is in the range of 3 to 5 degrees. The burners are directed towards a central circle E' having a predetermined area.

本発明の反応器設計を使用すると、立て筒内の大きな遠
心力が大きな沈降速度および従って大きなスラグ化効率
を生ずるであろう。何故ならばスラグの大部分・は管延
長部の下部に沈積し、十字線の設立によるかまたは管の
更なる狭まりによる生或物ガスの渦を減少させることが
できるからである。これは冷たい合戒ガスが反応器に再
び入るのを防止するであろう。Using the reactor design of the present invention, large centrifugal forces within the vertical tube will result in large settling velocities and therefore large slagging efficiencies. This is because most of the slag is deposited at the bottom of the tube extension, reducing the vortex of the product gas due to the establishment of the crosshairs or due to further narrowing of the tube. This will prevent cold gas from re-entering the reactor.

立て筒は合戒ガスの乱流をも減少させるであろう．この
減少および急冷部入口直下の立て筒壁が垂直であり従っ
て第１図における反応器天井よりも非常に急勾配である
ことはスラグ上昇またはスラグ連行の防止に有利であろ
う。The vertical tube would also reduce the turbulence of the gas. This reduction and the fact that the vertical tube wall directly below the quench section inlet is vertical and therefore much steeper than the reactor ceiling in FIG. 1 may be advantageous in preventing slag rise or slag entrainment.

最後に、立て筒は流れ短絡を減少させるであろう。斯て
反応器出口への通り抜け時間は増大する。Finally, the vertical tube will reduce flow shorts. The transit time to the reactor outlet is thus increased.

従って転化率は高くなりそして出口温度は低下しうる． 本発明の種々の変形が当該技術分野の熟達者には上記記
載および添付図面から明らかとなるであろう。そのよう
な変形は特許請求の範囲内に入ることが意図される。Therefore, the conversion rate can be higher and the outlet temperature can be lowered. Various modifications of the invention will become apparent to those skilled in the art from the foregoing description and accompanying drawings. Such modifications are intended to fall within the scope of the claims.

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

第１図は従来の反応器および急冷域の概略縦断面図、 第２図は本発明の反応器設計の概略縦断面図、第３ａ図
は第１図の線１−１に沿った横断面図、第３ｂ図は第２
図の線■−Ｈに沿った横断面図である。 １・・・反応器容器、２・・・スラグ出口、３・・・バ
ーナ、４・・・ガス出口、４ａ・・・立て筒、５・・・
急冷系。 ＦＩＧ．３ｏ Ｄ ＦＩＧ．３ｂ Ｄ１FIG. 1 is a schematic longitudinal cross-sectional view of a conventional reactor and quench zone; FIG. 2 is a schematic longitudinal cross-sectional view of the reactor design of the present invention; FIG. 3a is a cross-sectional view taken along line 1--1 in FIG. Figure 3b is the second
FIG. DESCRIPTION OF SYMBOLS 1...Reactor container, 2...Slag outlet, 3...Burner, 4...Gas outlet, 4a...Vertical cylinder, 5...
Rapid cooling system. FIG. 3o D FIG. 3b D1

Claims (4)

【特許請求の範囲】[Claims] （１）微粉砕固体炭素含有燃料および酸化剤の部分酸化
法を実施するための反応器であって、頂部に生成物ガス
用出口、底部にスラグ出口、側壁に複数のバーナ開口、
円周方向の間隔をおいた点に同じ水平レベル上に小さな
放火角で配置された複数の接線方向に向けられたバーナ
を有する反応器容器を含み、その出口の上に急冷部を備
えた前記反応器において、反応器出口と急冷部入口の間
に所定の長さ対直径の比を有する立て筒が配置された前
記反応器。(1) A reactor for carrying out a process for partial oxidation of pulverized solid carbon-containing fuels and oxidizers, comprising an outlet for the product gas at the top, a slag outlet at the bottom, and a plurality of burner openings in the side walls;
said reactor vessel with a plurality of tangentially oriented burners arranged at circumferentially spaced points on the same horizontal level and at a small firing angle, and equipped with a quench section above its outlet. In the reactor, a vertical tube having a predetermined length-to-diameter ratio is disposed between the reactor outlet and the quenching section inlet. （２）立て筒が４ないし６の長さ対直径比を有する特許
請求の範囲第１項記載の反応器。(2) The reactor according to claim 1, wherein the vertical tube has a length-to-diameter ratio of 4 to 6. （３）立て筒が５の長さ対直径比を有する特許請求の範
囲第２項記載の反応器。(3) The reactor according to claim 2, wherein the vertical tube has a length-to-diameter ratio of 5. （４）放火角が３ないし５度である特許請求の範囲第１
−３項のいずれか記載の反応器。(4) Claim 1 in which the firing angle is 3 to 5 degrees.
- The reactor according to any of item 3.
JP2135525A 1989-05-30 1990-05-28 Coal gasification reactor Expired - Lifetime JP2932198B2 (en)

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GB898912316A GB8912316D0 (en) 1989-05-30 1989-05-30 Coal gasification reactor
GB8912316.0 1989-05-30

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DE (1) DE69011216T2 (en)
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JP2932198B2 (en) 1999-08-09
DK0400740T3 (en) 1994-08-29
DE69011216D1 (en) 1994-09-08
AU618195B2 (en) 1991-12-12
CN1025345C (en) 1994-07-06
DE69011216T2 (en) 1995-02-16
CN1047688A (en) 1990-12-12
ES2058754T3 (en) 1994-11-01
EP0400740B1 (en) 1994-08-03
AU5602290A (en) 1990-12-06
CA2017635A1 (en) 1990-11-30
EP0400740A1 (en) 1990-12-05
CA2017635C (en) 2000-05-09
ZA904064B (en) 1991-02-27

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