JP2509192B2 - Method for producing carbon monoxide and hydrogen containing gas - Google Patents

Method for producing carbon monoxide and hydrogen containing gas

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Publication number
JP2509192B2
JP2509192B2 JP61223929A JP22392986A JP2509192B2 JP 2509192 B2 JP2509192 B2 JP 2509192B2 JP 61223929 A JP61223929 A JP 61223929A JP 22392986 A JP22392986 A JP 22392986A JP 2509192 B2 JP2509192 B2 JP 2509192B2
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Prior art keywords
gas
reaction chamber
carbon monoxide
hydrocarbons
auxiliary reaction
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 - Lifetime
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JP61223929A
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Japanese (ja)
Other versions
JPS6274993A (en
Inventor
サンテン スベン
ベンテル ラルス
Original Assignee
エスケ−エフ ステイ−ル エンジニアリング アクテイエボラ−グ
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Industrial Gases (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Description

【発明の詳細な説明】 〔産業上の利用分野〕 本発明は、工業上公知の技術を使用すると並びに炭素
及び／又は炭化水素を含有するいかなる種類の出発原料
も利用することが可能な、一酸化炭素と水素とを含有す
るガスを製造する方法であって、それによれば、そのガ
スを還元ガス、燃焼用ガス、又は合成ガスとして使用す
る前に、エネルギーを消費し且つ費用のかかるスクラビ
ング工程にかけることを必要としない方法に関する。DETAILED DESCRIPTION OF THE INVENTION Industrial Field of the Invention The present invention uses industrially known techniques and can utilize any type of starting material containing carbon and / or hydrocarbons. A method of producing a gas containing carbon oxide and hydrogen according to which an energy consuming and costly scrubbing process is used before the gas is used as a reducing gas, a combustion gas or a synthesis gas. Regarding a method that does not require running.

〔従来の技術及び発明が解決しようとする問題点〕[Problems to be Solved by Prior Art and Invention]

燃焼を利用してエネルギーを供給する操作、並びに、
歴青炭、泥炭、その他同種類のもののような乾燥コーク
ス以外の出発原料を使用する操作においては、CO＋H2は
もちろんH2O及び炭化水素を含有するガスが得られる。Operation to supply energy using combustion, and
In operations using starting materials other than dry coke, such as bituminous coal, peat, and the like, a gas containing H 2 O and hydrocarbons as well as CO + H 2 is obtained.

標準的には、ガス中のCO2＋H2Oの最大含有量は約10％
を目標とされるが、一方それと同時に、重質炭化水素の
含有量はできる限り０％に近くあるべきである。As standard, the maximum content of CO 2 + H 2 O in gas is about 10%
, While at the same time the content of heavy hydrocarbons should be as close to 0% as possible.

酸素ガス（空気）と蒸気とを使用する、ガスと炭素質
原料とが向流に移動する旧来のガス化法においては、熱
をきわめてよく利用することが可能であるが、反応温度
が低いため、このガスは大量のタールを含有する。更
に、灰の形で残留生成物が得られ、これを環境に対して
無害な方法で処分するのは困難である。燃焼工程におけ
る反応温度を高くして灰を溶融させること及び操作圧力
を上げることによって、かなり有利にすることができ
る。抜き出した凝固スラグは浸出に対してきわめて耐性
があり、また、反応器の単位容積当りの生産量が増加す
る。更に、過剰酸素を還元操作にとって合理的な量に維
持することができる。すなわち、例えば、生じた一酸化
炭素のうちのある量は熱損失を補うために燃焼させてCO
2にする必要がある。しかしながら、タールの問題はま
だ残り、それゆえにガスは、例えば還元ガスとして直接
使用することができない。In the conventional gasification method using oxygen gas (air) and steam, in which gas and carbonaceous raw material move countercurrently, heat can be used very well, but the reaction temperature is low. , This gas contains large amounts of tar. Furthermore, a residual product is obtained in the form of ash, which is difficult to dispose of in a manner which is harmless to the environment. Significant advantages can be obtained by increasing the reaction temperature in the combustion process to melt the ash and increase the operating pressure. The extracted coagulated slag is very resistant to leaching and also increases the production volume per reactor volume. Furthermore, excess oxygen can be maintained in a reasonable amount for the reduction operation. That is, for example, some of the carbon monoxide produced is burned to compensate for heat loss and CO
Must be 2 . However, the tar problem still remains and therefore the gas cannot be used directly, eg as reducing gas.

従って、本発明の主目的は、炭素及び／又は炭化水素
を含有するいかなる種類の出発原料でもガスを発生させ
るために使用するのを可能にする一方、その上そのガス
を還元ガス、燃焼用ガス、又は合成ガスとして使用する
前に、エネルギーを消費し且つ費用のかかるスクラビン
グ工程にかけることを必要としない工業的に公知の技術
を使用する方法の確立を達成することである。Thus, the main object of the present invention is to allow any type of starting material containing carbon and / or hydrocarbons to be used for generating gas, while additionally using that gas as reducing gas, combustion gas. Or to establish a process using industrially known techniques that does not require energy consuming and expensive scrubbing steps before use as syngas.

〔問題点を解決するための手段及び作用効果〕[Means for solving the problems and effects]

上記の主目的は、炭素及び／又は炭化水素を含有する
原料と酸化体とから製造したガスを、そのガス中の炭化
水素を分解するため、プラズマ発生器により加熱したガ
スと同時に補助反応室に供給することを実質的に特徴と
する、本発明による方法で達成される。The main purpose of the above is to produce a gas produced from a raw material containing carbon and / or hydrocarbon and an oxidant into the auxiliary reaction chamber at the same time as the gas heated by the plasma generator in order to decompose the hydrocarbon in the gas. This is achieved with the method according to the invention, which is essentially characterized by feeding.

プラズマ発生器により加熱され、それゆえにきわめて
高いエネルギー密度を有する熱いガスを供給することに
よって、ガス中のH2O，O2及び／又はCO2との反応はもち
ろん、ガス化装置からのガス中の炭化水素の熱分解が果
されてH2とCOとを生ずる。供給するガスのエネルギー密
度が高いので、必要とするガスの体積は比較的小さく、
従って本方法が実行可能となる。By supplying a hot gas which is heated by the plasma generator and therefore has a very high energy density, it is possible to react with the H 2 O, O 2 and / or CO 2 in the gas as well as in the gas from the gasifier. The hydrocarbons are thermally decomposed to produce H 2 and CO. Since the energy density of the gas supplied is high, the volume of gas required is relatively small,
Therefore, the method becomes feasible.

ガスは泥炭、坑口炭、無煙炭、又は林業廃棄物（fore
st waste）のような、炭素及び／又は炭化水素を含有す
る原料の熱分解又は部分燃焼によって製造することがで
きる。坑口炭の熱分解から得られるコークス炉ガスを使
用する場合、炭化水素はもちろんその外の汚染物質が存
在する。本発明に伴う大きな利点は、補助反応室におい
てこれらも分解されるということである。Gas can be peat, wellhead coal, anthracite, or forestry waste (fore
It can be produced by thermal decomposition or partial combustion of a raw material containing carbon and / or hydrocarbons such as st waste). When using coke oven gas obtained from the pyrolysis of mine coal, hydrocarbons as well as other contaminants are present. A great advantage with the present invention is that they are also decomposed in the auxiliary reaction chamber.

本発明の一つの態様によれば、補助反応室を通過後、
ガスは石灰石又はドロマイトの充填物を通して処理さ
れ、硫黄を取除かれる。前述の硫黄浄化（sulphur puri
fication）に使用する石灰石又はドロマイトは、炭化水
素の分解及び酸化体との反応の触媒としても働く。これ
は、補助反応室における電気エネルギーの消費を相応じ
て低下させるのを可能にする。According to one aspect of the invention, after passing through the auxiliary reaction chamber,
The gas is processed through a filling of limestone or dolomite to remove sulfur. The sulfur purification mentioned above (sulfur puri
Limestone or dolomite used for fication) also acts as a catalyst for the decomposition of hydrocarbons and the reaction with oxidants. This makes it possible to correspondingly reduce the consumption of electrical energy in the auxiliary reaction chamber.

本発明のもう一つの態様によれば、補助反応室からの
ガス中のCO2＋H2Oの含有量は、５％以下に管理される。According to another embodiment of the present invention, the content of CO 2 + H 2 O in the gas from the auxiliary reaction chamber is controlled to 5% or less.

後続の還元工程につないだ、本発明によるガス製造法
についての流れ図を概略的に示す添付の図面を参照し
て、本発明の付加的な利点及び特徴を下記の詳細な説明
に示す。Additional advantages and features of the present invention are set forth in the following detailed description with reference to the accompanying drawings, which schematically show a flow chart for a gas production process according to the invention, followed by a subsequent reduction step.

粗製ガスは、１で示されるガス化装置あるいはコーク
ス炉で製造される。発生した粗製ガスは、補助反応室２
に供給される。エネルギー密度の高い熱ガスを供給する
ため、少なくとも１つのプラズマ発生器３を補助反応室
に接続して設置する。粗製ガス中の炭化水素は、補助反
応室で分解され、そして反応してCO＋H2Oを生ずる。細
かく分割したコークス又はH2Oを補助反応室の鋭尖窓（l
ances）４を通して入れ、水素／炭素比を調節すること
ができよう。The crude gas is produced in a gasifier or coke oven designated by 1. The generated crude gas is used in the auxiliary reaction chamber 2
Is supplied to. At least one plasma generator 3 is installed in connection with the auxiliary reaction chamber in order to supply hot gas with high energy density. Hydrocarbons in the crude gas is decomposed in the auxiliary reaction chamber, the reaction to produce CO + H 2 O. Finely divided coke or H 2 O was added to the sharp pointed window (l
lances 4) to adjust the hydrogen / carbon ratio.

この後、ガスは、気密の仕切装置（sluice arrangeme
nt）７を通して供給された石灰石又はドロマイトの充填
物６を含有するシャフト５において硫黄浄化にかけら
れ、また、使用済みの充填物は、気密の仕切り装置８を
通してシャフトの底部から取出される。ガス中に残留す
るいかなる炭化水素も、石灰石又はドロマイトの充填物
で触媒反応的に分解される。含有炭化水素を熱分解する
ために使用するプラズマ発生器３で消費される電気エネ
ルギーを減少させるのに、これを使用することができ
る。After this, the gas is sluice arranged.
nt) 7 is subjected to sulfur purification in the shaft 5 containing a limestone or dolomite filling 6 and the used filling is removed from the bottom of the shaft through an airtight partitioning device 8. Any hydrocarbons remaining in the gas are catalytically decomposed with a limestone or dolomite charge. It can be used to reduce the electrical energy consumed in the plasma generator 3 used to pyrolyze the contained hydrocarbons.

次に、このようにして精製されて実質的にH2＋COと少
量のH2O＋CO2のみを含有するガスは、酸化物質（exidic
material）を還元するためのシャフト炉（shaft furna
ce）10に入れる前に温度及び組成に関して調節する室９
に移送される。The gas purified in this way and containing substantially only H 2 + CO and a small amount of H 2 O + CO 2 is then oxidised (exidic
shaft furna for reducing material
ce) chamber 9 to adjust for temperature and composition before putting into
Be transferred to.

調製されたガスは、入口12を通してシャフト炉10の底
部に供給され、そして、金属酸化物を含有する物質に対
して向流に流される。不純物とダストとを含有する部分
的に消費されたガスは、出口13を通して取出され、そし
てスクラバー14で洗浄される。The prepared gas is fed to the bottom of the shaft furnace 10 through the inlet 12 and is flowed countercurrent to the metal oxide containing material. The partially consumed gas containing impurities and dust is withdrawn through the outlet 13 and washed with a scrubber 14.

洗浄した、部分的に消費されたガスは、その後、フィ
ルター15で示されるように、他の目的に使用することが
できる。必要ならば、ガスの一部を管16,16a,16bを経由
して本発明の工程に再循環することができ、また、例え
ば、シャフト炉に入れるガスの温度と組成とを調節する
混合室９で使用することができよう。再循環ガスの一部
は、補助反応室に接続したプラズマ発生器で使用するこ
ともできよう。The washed, partially consumed gas can then be used for other purposes, as shown by filter 15. If desired, part of the gas can be recycled to the process of the invention via tubes 16, 16a, 16b, and also, for example, a mixing chamber to control the temperature and composition of the gas entering the shaft furnace. 9 could be used. Some of the recycled gas could also be used in a plasma generator connected to the auxiliary reaction chamber.

下記の実施例により本発明を更に説明する。 The invention is further described by the following examples.

〔実施例〕〔Example〕

30％の水分を含有する、下記の組成（％）、すなわ
ち、 の林業廃棄物を時間当り10トン、向流式ガス化装置の上
部に供給し、それと同時に酸化体を、1000℃に加熱した
空気の形でガス化装置の底部に供給する。加えた空気は
3700Nm3である。上部のガスの組成（％）は、次のとお
りである。The following composition (%), which contains 30% water: 10 tons of forestry waste per hour is fed to the top of a countercurrent gasifier, while oxidant is simultaneously fed to the bottom of the gasifier in the form of air heated to 1000 ° C. The added air is
It is 3700 Nm 3 . The composition (%) of the upper gas is as follows.

同時に、タール分析用の試料を採取し、それは、ガスが
タールを3.2g/Nm3含有することを示す。 At the same time, a sample for tar analysis is taken, which shows that the gas contains 3.2 g / Nm 3 of tar.

出てくるガスの温度は550℃、またその体積はおよそ1
7200Nm3である。次に、ガスを補助反応室に供給し、そ
してプラズマ発生器で加熱した空気を使って加熱する。
必要とする空気量は、わずかに約2100Nm3に過ぎない。
プラズマ発生器の助けによって、流入するガスの温度は
1250℃に上昇し、電気エネルギーの消費量はおよそ8.7M
Whである。The temperature of the gas that emerges is 550 ° C, and its volume is approximately 1
It is 7200 Nm 3 . The gas is then fed to the auxiliary reaction chamber and heated with heated air in the plasma generator.
The air volume required is only about 2100 Nm 3 .
With the help of the plasma generator, the temperature of the incoming gas is
The temperature rises to 1250 ℃, and the consumption of electric energy is about 8.7M
Wh.

含有メタン及びタールは、加熱した熱分解ガスからこ
うして取除かれ、そして、補助反応室を出ていくガスの
組成は、次のとおりである。The contained methane and tar are thus removed from the heated pyrolysis gas, and the composition of the gas leaving the auxiliary reaction chamber is as follows:

出ていくガスの量は、およそ19900Nm3である。 The amount of gas leaving is approximately 19900 Nm 3 .

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

図面は、後続の還元工程につないだ、本発明によるガス
製造法を概略的に示す流れ図である。 図中、１はガス化装置、２は補助反応室、３はプラスマ
発生器、５はシャフト、６は充填物、９は混合室、10は
シャフト炉、14はスクラバーである。The drawing is a schematic flow diagram of a gas production process according to the present invention followed by a subsequent reduction step. In the figure, 1 is a gasifier, 2 is an auxiliary reaction chamber, 3 is a plasma generator, 5 is a shaft, 6 is a packing, 9 is a mixing chamber, 10 is a shaft furnace, and 14 is a scrubber.

Claims (4)

(57)【特許請求の範囲】(57) [Claims] 【請求項１】工業上公知の技術を使用すること並びに炭
素及び／又は炭化水素を含有するいかなる種類の出発原
料も利用することが可能な、そのガスを還元ガス、燃焼
用ガス、又は合成ガスとして使用する前に、エネルギー
を消費し且つ費用のかかるスクラビング工程にかける必
要のない、一酸化炭素と水素とを含有し且つメタンを実
質的に含有しないガスを製造する方法であって、炭素及
び／又は炭化水素を含有する原料と酸化体とから製造し
たガスを、そのガス中の炭化水素を分解するため、再循
環ガス又は空気をプラズマ発生器により加熱して得られ
たガスと同時に反応室に供給する、一酸化炭素及び水素
含有ガスの製造方法。1. A reducing gas, a combustion gas, or a synthesis gas, the gas of which can be used by any technique known in the industry and which can utilize any kind of starting material containing carbon and / or hydrocarbons. A process for producing a gas containing carbon monoxide and hydrogen and substantially free of methane, which requires no energy-consuming and expensive scrubbing step before use as / Or a gas produced from a raw material containing a hydrocarbon and an oxidant, in order to decompose the hydrocarbon in the gas, a recycle gas or a gas obtained by heating air with a plasma generator and a reaction chamber at the same time And a method for producing a carbon monoxide- and hydrogen-containing gas. 【請求項２】補助反応室を通過後、石灰石又はドロマイ
トの充填物を通してガスを処理して硫黄を取除き、いか
なる残留炭化水素も分解し、そして酸化体との反応を達
成する、特許請求の範囲第１項記載の方法。2. After passing through the auxiliary reaction chamber, the gas is treated through a packing of limestone or dolomite to remove sulfur, decompose any residual hydrocarbons and achieve a reaction with the oxidant. The method according to claim 1. 【請求項３】細かく分割したコークス及び／又はH2Oを
補助反応室に入れる、特許請求の範囲第１項又は第２項
記載の方法。3. The method according to claim 1 or 2, wherein finely divided coke and / or H 2 O is placed in the auxiliary reaction chamber. 【請求項４】補助反応室からのガス中のCO2＋H2Oの含有
量を５％以下に管理する、特許請求の範囲第１項から第
３項までのいずれか１項に記載の方法。4. The method according to any one of claims 1 to 3, wherein the content of CO 2 + H 2 O in the gas from the auxiliary reaction chamber is controlled to 5% or less. .
JP61223929A 1985-09-25 1986-09-24 Method for producing carbon monoxide and hydrogen containing gas Expired - Lifetime JP2509192B2 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8504439-4 1985-09-25
SE8504439A SE457355B (en) 1985-09-25 1985-09-25 MAKE SURE TO PREPARE A CLEAN, CARBON OXIDE AND GAS GAS INCLUDING GAS

Publications (2)

Publication Number Publication Date
JPS6274993A JPS6274993A (en) 1987-04-06
JP2509192B2 true JP2509192B2 (en) 1996-06-19

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
JP61223929A Expired - Lifetime JP2509192B2 (en) 1985-09-25 1986-09-24 Method for producing carbon monoxide and hydrogen containing gas

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Country Link
JP (1) JP2509192B2 (en)
AT (1) AT396366B (en)
AU (1) AU589997B2 (en)
BE (1) BE905480A (en)
BR (1) BR8701328A (en)
CA (1) CA1309589C (en)
DE (1) DE3631015A1 (en)
FI (1) FI863726A (en)
FR (1) FR2587717B1 (en)
GB (1) GB2180849B (en)
IL (1) IL80027A0 (en)
IT (1) IT1213497B (en)
SE (1) SE457355B (en)

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FR2587717B1 (en) 1990-03-02
FI863726A0 (en) 1986-09-15
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AU589997B2 (en) 1989-10-26
JPS6274993A (en) 1987-04-06
FI863726A (en) 1987-03-26
FR2587717A1 (en) 1987-03-27
BE905480A (en) 1987-01-16
AU6258286A (en) 1987-03-26
SE8504439L (en) 1987-03-26
DE3631015C2 (en) 1988-10-06
GB2180849B (en) 1989-12-28
IL80027A0 (en) 1986-12-31
ATA256086A (en) 1992-12-15
CA1309589C (en) 1992-11-03
DE3631015A1 (en) 1987-04-16
AT396366B (en) 1993-08-25
BR8701328A (en) 1988-09-27
GB2180849A (en) 1987-04-08
SE8504439D0 (en) 1985-09-25
IT1213497B (en) 1989-12-20
SE457355B (en) 1988-12-19
IT8621793A0 (en) 1986-09-23

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