JPS623877B2 - - Google Patents
Info
- Publication number
- JPS623877B2 JPS623877B2 JP53066630A JP6663078A JPS623877B2 JP S623877 B2 JPS623877 B2 JP S623877B2 JP 53066630 A JP53066630 A JP 53066630A JP 6663078 A JP6663078 A JP 6663078A JP S623877 B2 JPS623877 B2 JP S623877B2
- Authority
- JP
- Japan
- Prior art keywords
- steam
- gasifier
- methane
- helium
- converted
- 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
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
-
- 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
-
- 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
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
-
- 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
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
- C10J2300/1662—Conversion of synthesis gas to chemicals to methane
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Engine Equipment That Uses Special Cycles (AREA)
Description
【発明の詳細な説明】
本発明は、原子核的に加熱された循環ヘリウム
を用いて炭素含有物質からメタン或は合成ガスを
製造する装置に関している。その場合、炭素の一
部分が水素と共に水素添加ガス化装置の中でメタ
ンに変換され、そして炭素の他の部分が水蒸気と
共に水蒸気ガス化装置の中で合成ガスに変換され
る。そして前記メタンの少くとも一部は水蒸気と
共に分解炉の中で水素に変換される。この装置は
メタン（CH4）、或は僅かな成分のCO2とCH4と
を含むH2とCOとの混合物としての合成ガスの何
れかを発生する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an apparatus for producing methane or synthesis gas from carbon-containing materials using nuclear-heated circulating helium. In that case, a part of the carbon is converted together with hydrogen into methane in a hydrogasifier, and another part of the carbon is converted with water vapor into synthesis gas in a steam gasifier. At least a portion of the methane is then converted into hydrogen together with water vapor in a cracking furnace. This device generates either methane (CH 4 ) or synthesis gas as a mixture of H 2 and CO with minor components of CO 2 and CH 4 .
雑誌「Chemie−Ingenieur−Technik」1974
年、第938頁、特に第１図および第941頁、特に第
２図に、石炭の水蒸気ガス化により行われるメタ
ンの製造方法がそれぞれ記載されている。その第
937頁には石炭のメタンへの水素添加ガス化の新
規方法が言及されている。しかし上記両方法とも
著しい欠点を免れない。水素添加のガス化におい
ては、石炭の滞溜時間が長いため、およびガス化
装置の寸法が制限を受けるために、石炭の完全な
変換は達成できない。水素添加ガス化の場合に生
ずる残留コークスは、灰分の外尚使用された炭素
の約30〜45％を含む。これに対し水蒸気ガス化に
おいては、使用された炭素が殆ど残りなくガス化
されるが、このプロセスは高温（石炭では790
℃、褐炭では630゜〜660℃）においてのみ進行す
るので、反応炉内で放出される熱の高温範囲に層
する部分だけがガス化に利用されるに過ぎない。
純然たる水蒸気ガス化プロセスにおいては残留熱
は殆ど蒸気発生従つて発電用にのみ利用される。
ながならこの蒸気のごくわずかな部分が前記プロ
セスで用いられるに過ぎないからである。 Magazine "Chemie-Ingenieur-Technik" 1974
, page 938, in particular FIG. 1, and page 941, especially FIG. 2, respectively, describe a process for the production of methane carried out by steam gasification of coal. The first
On page 937, a new method of hydrogen gasification of coal to methane is mentioned. However, both of the above methods suffer from significant drawbacks. In hydro-gasification, complete conversion of coal cannot be achieved due to the long residence time of the coal and the limited dimensions of the gasifier. The residual coke produced in the case of hydrogasification contains approximately 30-45% of the carbon used besides the ash. In contrast, in steam gasification, the used carbon is gasified with almost no residue, but this process is carried out at high temperatures (for coal, 790
Since the process proceeds only at temperatures between 630° and 660°C for lignite, only the portion that falls within the high temperature range of the heat released in the reactor is used for gasification.
In pure steam gasification processes, the residual heat is used almost exclusively for steam generation and thus for power generation.
This is because only a small portion of this steam is used in the process.
米国Oak Ridge National Laboratory1976年11
月の報告書「ORNL／TM−5242」第82頁に記載
されている装置においては、炭素が原子核の熱に
よつてメタンに変換されている。先づ石炭が乾燥
され、然る後水素添加されてガス化され、そして
残りのコークスが水蒸気ガス化装置の中で合成ガ
スに変換される。発生したメタンの一部はメタン
分解炉（この場合リフオーマと称される）の中で
熱い水蒸気添加のもとに合成ガスに変換される。
しかしこのような方法は尚次のような欠点があ
る。即ちこの場合、水蒸気ガス化装置に供給され
る蒸気の温度が経済的なガス化温度よりも著しく
低いということである。従つて高い温度範囲にお
いて取出された熱の一部が蒸気を加熱するだけに
利用され、ガス化には役立たない。従つて同一出
力の原子炉においても、この場合に処理される石
炭の量は少く、従つてガスの収量もより少くな
る。 Oak Ridge National Laboratory, USANovember 1976
In the device described on page 82 of the lunar report "ORNL/TM-5242," carbon is converted to methane by the heat of the atomic nucleus. The coal is first dried, then hydrogenated and gasified, and the remaining coke is converted to synthesis gas in a steam gasifier. A portion of the methane generated is converted into synthesis gas with the addition of hot steam in a methane cracking furnace (in this case referred to as a reformer).
However, this method still has the following drawbacks. This means that in this case the temperature of the steam fed to the steam gasifier is significantly lower than the economical gasification temperature. A portion of the heat extracted in the high temperature range is therefore used only to heat the steam and is not useful for gasification. Therefore, even in reactors with the same power, the amount of coal that is processed in this case is smaller and therefore the gas yield is also smaller.
本発明の目的は、上述の欠点が大幅に回避され
た原子核的に加熱される循環ヘリウムを用いて炭
素含有物質からメタン或は合成ガスを製造する装
置を得ることにある。 The object of the invention is to obtain a device for producing methane or synthesis gas from carbon-containing materials using nuclear-heated circulating helium, in which the above-mentioned disadvantages are largely avoided.
この目的は本発明によれば、ヘリウム循環路内
の水蒸気ガス化装置と分解炉との間にプロセス蒸
気の過熱装置が配置され、上記プロセス蒸気過熱
装置からの蒸気が水蒸気ガス化装置の中へ供給さ
れることにより達成される。この提案によつて配
置されたヘリウム循環路内の水蒸気ガス化装置と
分解炉との間にプロセス蒸気過熱装置は水蒸気ガ
ス化装置の効率を著しく高める。なぜならこのよ
うな仕方で上記水蒸気ガス化装置は、既にガス化
に必要な温度を有するプロセス蒸気を得るからで
ある。従つて、ガス化装置へ運び込まれる熱は殆
ど完全にガス化反応に利用されるので、原子炉出
力に関しては可能最大のガスを生産することがで
きる。その他の材料の使用量と比較してプロセス
蒸気量は著しく少ないので、本発明によるプロセ
ス蒸気過熱装置のための付加費用は極めて僅少で
ある。プロセス蒸気過熱装置に起因する循環ヘリ
ウムの分解炉への進入温度の低下は、ほんの僅か
に過ぎない。なぜならプロセス蒸気過熱装置が無
い場合でも、ヘリウムからプロセス蒸気へ与えら
れる熱量は水蒸気ガス化装置へ運び込まれる必要
があるからである。本発明による水素添加による
ガス化と水蒸気ガス化との組合せにおいては、分
解炉を通されるメタンの量が他の物質の流量と対
比して僅少であるので、本発明装置によつても分
解炉には何等著しい付加経費は見込まれない。 According to the invention, this object is achieved by disposing a process steam superheater between the steam gasifier and the cracking furnace in the helium circuit, the steam from the process steam superheater flowing into the steam gasifier. This is achieved by being supplied. A process steam superheater placed in accordance with this proposal between the steam gasifier and the cracking furnace in the helium circuit significantly increases the efficiency of the steam gasifier. This is because in this way the steam gasifier obtains process steam that already has the temperature required for gasification. The heat transferred to the gasifier is therefore almost completely utilized for the gasification reaction, so that the maximum possible gas can be produced in terms of reactor power. Since the amount of process steam is significantly lower compared to the amount of other materials used, the additional costs for the process steam superheating device according to the invention are very low. There is only a slight reduction in the temperature of circulating helium entering the cracking furnace due to the process steam superheater. This is because even in the absence of a process steam superheater, the amount of heat imparted from the helium to the process steam needs to be conveyed to the steam gasifier. In the combination of gasification by hydrogen addition and steam gasification according to the present invention, the amount of methane passed through the cracking furnace is small compared to the flow rate of other substances, so the apparatus of the present invention can also be used for decomposition. No significant additional costs are expected for the furnace.
本発明の実施態様として、ヘリウム循環路にお
いて分解炉の後方にプロセス蒸気予備過熱装置
が、そしてその後方に蒸気発生装置が配置され、
この蒸気発生装置からの蒸気がタービンを駆動
し、この蒸気タービンより抽気された蒸気がプロ
セス蒸気として直接分解炉へ、そして前記プロセ
ス蒸気予備過熱装置を介して水蒸気ガス化装置へ
案内される。この場合の蒸気発生装置は、所定の
ヘリウム温度において約180バールの過熱蒸気を
発生する。このような高圧は後でプロセス蒸気と
して使用するために必要でないので、この場合熱
経済的見地からは、この蒸気を先づタービン内で
減圧させ、引続き少くとも部分的に再び過熱する
のが有利である。蒸気ガス化装置においてもメタ
ン分解炉においても、高温ではあつても低圧の、
例えば40バールのプロセス蒸気が入用である。従
つて熱経済的見地からは、プロセス蒸気をこの装
置へ進入する前に、できるだけ過熱するのが有利
である。 As an embodiment of the present invention, a process steam presuperheater is arranged behind the cracking furnace in the helium circulation path, and a steam generator is arranged behind it,
Steam from the steam generator drives a turbine, and steam extracted from the steam turbine is guided as process steam directly to the cracking furnace and then to the steam gasifier via the process steam presuperheater. The steam generator in this case generates superheated steam of approximately 180 bar at a given helium temperature. Since such high pressures are not required for later use as process steam, it is advantageous from a thermoeconomic point of view in this case to first depressurize this steam in the turbine and then at least partially resuperheat it. It is. In both steam gasifiers and methane cracking furnaces, high temperature but low pressure
For example, 40 bar of process steam is required. From a thermoeconomic point of view, it is therefore advantageous to superheat the process steam as much as possible before it enters the apparatus.
次に、本発明により主としてメタンを製造する
装置を略示する図面を参照して、本発明を更に具
体的に説明する。 Next, the present invention will be explained in more detail with reference to the drawings, which schematically show mainly an apparatus for producing methane according to the present invention.
ヘリウム１次回路２を有する原子炉１は熱交換
器３を介してヘリウム２次回路４に熱を与える
が、この２次回路には順次水蒸気ガス化装置５、
プロセス蒸気過熱装置６、メタン分解炉７、プロ
セス蒸気予備過熱装置８、蒸気発生装置９および
ヘリウム圧縮機１０が配置されている。原料炭
は、先づ水素を添加されて大部分が水素添加ガス
化装置１１内で小量の水素、一酸化炭素および二
酸化炭素を含むメタンの混合物に変換される。引
続き、水素添加ガス化装置１１より排出されたコ
ークスは、水蒸気ガス化装置５の中で過熱水蒸気
の添加のもとで殆ど残らずガス化され、この場合
二酸化炭素、水素および少量の一酸化炭素とメタ
ンより成る混合物が生ずる。これまでの評価によ
れば、水素添加ガス化装置１１において、ルール
炭では使用された原料炭の60％、ドイツ褐炭では
その65乃至70％までがガス化される。原料炭の60
％がガス化される場合、分解炉７の中で約８％の
発生メタンが水素に分解される。上述の回路は、
石炭の種類が異る場合にも、ほぼ自動的にプロセ
ス全体を安定化する。水素添加ガス化装置１１内
でより多くガス化が行われる場合、そこに残るコ
ークスがそれだけ少くなる。水蒸気ガス化装置５
の中ではそれに応じてより少ない水素が作られ、
それに応じてヘリウム２次回路４によりより多く
の熱が分解炉７に与えられ、この分解炉はそれに
応じてより多くのメタンを分解することが可能と
なり、従つて水蒸気ガス化装置５より流出時にな
くなる水蒸気の量が補充される。水素添加ガス化
装置１１から出てくる製品は１２において再生的
に冷却され、１３において更に冷却され、１４に
おいて洗滌され、１５において二酸化炭素と硫化
水素が除去され、そして低温ガス分離装置１６へ
供給される。水蒸気ガス化装置５から出てくる製
品は１７において冷却され、分解炉７から出てく
る製品と一緒に変換装置１８に供給され、その中
に存在する一酸化炭素が水と共に二酸化炭素およ
び水素に変換される。その後製品は１９において
冷却され、２０において二酸化炭素および硫化水
素が除去され、２１において圧縮され、１２にお
いて再生的に予熱され、そして水素添加ガス化装
置１１へ供給される。既に上で述べた低温ガス分
離装置１６は所望の最終製品としてメタンを発生
するが、その他に水素も発生し、これは圧縮機２
２および上に述べた再生予熱装置１２を介して再
び前記水素添加ガス化装置１１へ供給される。同
様に１６において分離された一酸化炭素は２３に
おいて圧縮され、そして上に述べた変換装置１８
へ供給される。 A nuclear reactor 1 having a helium primary circuit 2 supplies heat to a helium secondary circuit 4 via a heat exchanger 3, which is sequentially connected to a steam gasifier 5,
A process steam superheater 6, a methane decomposition furnace 7, a process steam presuperheater 8, a steam generator 9, and a helium compressor 10 are arranged. The coking coal is first doped with hydrogen and converted into a mixture of mostly methane with small amounts of hydrogen, carbon monoxide and carbon dioxide in the hydrogasifier 11 . Subsequently, the coke discharged from the hydrogen gasifier 11 is gasified to almost no residue in the steam gasifier 5 with the addition of superheated steam, in this case carbon dioxide, hydrogen and a small amount of carbon monoxide. A mixture of methane and methane is formed. According to past evaluations, in the hydrogenation gasifier 11, 60% of the coking coal used for Ruhr coal and 65 to 70% of German brown coal are gasified. 60 of coking coal
% of the generated methane is decomposed into hydrogen in the cracking furnace 7. The above circuit is
It almost automatically stabilizes the entire process, even with different types of coal. The more gasification takes place in the hydrogen gasifier 11, the less coke will remain there. Steam gasifier 5
Correspondingly less hydrogen is produced in
Correspondingly, more heat is given by the helium secondary circuit 4 to the cracking furnace 7, which is able to decompose correspondingly more methane and thus more heat on exit from the steam gasifier 5. The amount of water vapor that is lost is replenished. The product emerging from the hydrogen gasifier 11 is regeneratively cooled at 12, further cooled at 13, washed at 14, carbon dioxide and hydrogen sulfide removed at 15, and fed to a cryogenic gas separation unit 16. be done. The product coming out of the steam gasifier 5 is cooled in 17 and fed together with the product coming out of the cracking furnace 7 to a converter 18 in which the carbon monoxide present is converted together with water into carbon dioxide and hydrogen. converted. The product is then cooled at 19, stripped of carbon dioxide and hydrogen sulfide at 20, compressed at 21, regeneratively preheated at 12, and fed to the hydrogasifier 11. The cold gas separation unit 16 already mentioned above produces methane as the desired end product, but also hydrogen, which is fed to the compressor 2.
2 and the above-mentioned regeneration preheating device 12, it is again supplied to the hydrogenation gasification device 11. Similarly, the carbon monoxide separated at 16 is compressed at 23 and the above-mentioned converter 18
supplied to
ヘリウム２次回路４によつて加熱される蒸気発
生装置９は、発電のためタービン２４へ蒸気を供
給し、タービンからの約40バールの圧力を有する
抽出蒸気の一部は分解炉７へ、そして一部はプロ
セス蒸気予備過熱装置８へ、そしてこれよりプロ
セス蒸気過熱装置６を経て水蒸気ガス化装置５へ
供給される。図示の導管の下方或は右側に指示さ
れた℃で現わされた温度は、この装置の正常運転
時の温度の一例を示している。 A steam generator 9 heated by a helium secondary circuit 4 supplies steam to a turbine 24 for power generation, a part of the extracted steam from the turbine having a pressure of about 40 bar is sent to a cracking furnace 7 and A portion is supplied to the process steam presuperheater 8 and from there via the process steam superheater 6 to the steam gasifier 5 . The temperature indicated in degrees Celsius below or to the right of the illustrated conduit represents an example of the temperature during normal operation of the device.
上述の装置は、3000MWのガス冷却形高温原子
炉を用い、38％の揮発成分を含有する炎性ガス炭
を使用した場合、毎時約575000Nm3のメタンの製
造が見込まれる。水蒸気ガス化装置５、プロセス
蒸気過熱装置６および分解炉７を直列に接続する
ことにより、既知の方法に比較してガス化に利用
し得る核エネルギーが増大され、従つて原子炉の
同一出力におけるガスの生産が高められる。上述
の炎性ガス炭を用いた場合、毎時985tの流量が算
出される。本発明装置の起動は、既知の装置に対
比して特に簡単である。なぜなら水素添加ガス化
装置１１を運転するための水素は、分解炉７の中
で該ガス系統内に存在するメタンより製造できる
からである。 The above-mentioned device is expected to produce approximately 575,000 Nm 3 of methane per hour using a 3000 MW gas-cooled high-temperature reactor and flaming gas coal containing 38% volatile components. By connecting the steam gasifier 5, the process steam superheater 6 and the cracking furnace 7 in series, the nuclear energy available for gasification is increased compared to known methods, and thus for the same power of the reactor. Gas production is increased. When using the above-mentioned flaming gas charcoal, a flow rate of 985 tons per hour is calculated. The activation of the device according to the invention is particularly simple compared to known devices. This is because the hydrogen for operating the hydrogen gasifier 11 can be produced in the cracking furnace 7 from the methane present in the gas system.
図面は本発明装置の一実施例を示す系統図であ
る。
１……原子炉、２……ヘリウム１次回路、３…
…熱交換器、４……ヘリウム２次回路、５……水
蒸気ガス化装置、６……プロセス蒸気過熱装置、
７……メタン分解炉、８……プロセス蒸気予備過
熱装置、９……蒸気発生装置、１０……ヘリウム
圧縮機、１１……水素添加ガス化装置、１２……
再生冷却（又は予熱）装置、１３……冷却装置、
１４……浄化装置、１５……CO2、H2S除去装
置、１６……低温ガス分離装置、１７……冷却装
置、１８……変換装置、１９……冷却装置、２０
……CO2、H2S除去装置、２１……圧縮機、２２
……圧縮機、２３……圧縮機、２４……タービ
ン。
The drawing is a system diagram showing one embodiment of the device of the present invention. 1... Nuclear reactor, 2... Helium primary circuit, 3...
... heat exchanger, 4 ... helium secondary circuit, 5 ... steam gasifier, 6 ... process steam superheater,
7...Methane decomposition furnace, 8...Process steam pre-superheater, 9...Steam generator, 10...Helium compressor, 11...Hydrogenation gasifier, 12...
Regenerative cooling (or preheating) device, 13... cooling device,
14...Purification device, 15... CO2 , H2S removal device, 16...Low temperature gas separation device, 17...Cooling device, 18...Conversion device, 19...Cooling device, 20
...CO 2 , H 2 S removal device, 21 ... Compressor, 22
...Compressor, 23...Compressor, 24...Turbine.
Claims (1)
置の中でメタンに変換され、炭素の他の部分が水
蒸気と共に水蒸気ガス化装置の中で合成ガスに変
換され、前記メタンの少くとも一部が水蒸気と共
に分解炉の中で水素に変換されるようにした原子
核的に加熱された循環ヘリウムにより炭素含有物
質からメタン或は合成ガスを製造する装置におい
て、 (a) ヘリウム循環路内の水蒸気ガス化装置と分解
炉との間にプロセス蒸気過熱装置が配置されて
いること、 (b) 上記プロセス蒸気過熱装置からの蒸気が水蒸
気ガス化装置へ供給されること、 を特徴とする核エネルギーによる石炭のガス化装
置。 ２ (a) ヘリウム循環路内の分解炉の後方にプロ
セス蒸気予備過熱装置が、その後方に蒸気発生
装置が配置されていること、 (b) 前記蒸気発生装置からの蒸気がタービンを駆
動すること、 (c) 前記蒸気タービンより抽気された蒸気がプロ
セス蒸気として直接分解炉へ、および前記プロ
セス蒸気予備過熱装置を経て水蒸気ガス化装置
へ案内されること、 を特徴とする特許請求の範囲第１項記載の装置。[Claims] 1. A part of the carbon is converted into methane together with hydrogen in a hydrogasifier, and another part of the carbon is converted into synthesis gas together with water vapor in a steam gasifier, and the methane is converted into synthesis gas in a steam gasifier. In an apparatus for producing methane or synthesis gas from carbon-containing materials by means of nuclear-heated circulating helium, at least a portion of which is converted together with water vapor into hydrogen in a cracking furnace, comprising: (a) a helium circuit; (b) steam from the process steam superheater is supplied to the steam gasifier; and (b) steam from the process steam superheater is supplied to the steam gasifier. Coal gasification equipment using nuclear energy. 2 (a) A process steam presuperheater is located behind the cracking furnace in the helium circulation path, and a steam generator is located behind it; (b) Steam from the steam generator drives a turbine. (c) steam extracted from the steam turbine is guided as process steam directly to a cracking furnace, and via the process steam pre-superheater to a steam gasifier. Apparatus described in section.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE2724802A DE2724802C2 (en) | 1977-06-02 | 1977-06-02 | Device with a nuclear-heated helium circuit for the production of methane or synthesis gas from coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS541305A JPS541305A (en) | 1979-01-08 |
| JPS623877B2 true JPS623877B2 (en) | 1987-01-27 |
Family
ID=6010445
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6663078A Granted JPS541305A (en) | 1977-06-02 | 1978-06-02 | Apparatus for gasifying coal with nuclear energy |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPS541305A (en) |
| DE (1) | DE2724802C2 (en) |
| FR (1) | FR2401217A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2908771C2 (en) * | 1979-03-06 | 1984-07-12 | Kraftwerk Union AG, 4330 Mülheim | Combined plant for the gasification of coal and the reduction of metal ores |
| GB2078251B (en) * | 1980-06-19 | 1984-02-15 | Gen Electric | System for gasifying coal and reforming gaseous products thereof |
| JPS59189191A (en) * | 1983-04-13 | 1984-10-26 | Tokyo Gas Co Ltd | Preparation of fuel gas with high calorific value |
| DE3335523A1 (en) * | 1983-09-30 | 1985-04-18 | Hochtemperatur-Reaktorbau GmbH, 4600 Dortmund | Plant and process for generating synthesis gas from coal, using thermal energy generated by nuclear means |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3854896A (en) * | 1973-01-29 | 1974-12-17 | Gilbert Associates | Method of converting coal to pipeline quality gas |
| DE2358372A1 (en) * | 1973-11-23 | 1975-05-28 | Rheinische Braunkohlenw Ag | METHOD OF USING THE THERMAL ENERGY OF A HIGH TEMPERATURE NUCLEAR REACTOR BY GASIFYING SOLID, CARBON-CONTAINING MATERIALS |
| DE2553506C2 (en) * | 1975-11-28 | 1984-04-26 | GHT Gesellschaft für Hochtemperaturreaktor-Technik mbH, 5060 Bergisch Gladbach | Device for the production of methane or synthesis gas from carbonaceous substances with the help of a nuclear reactor |
| DE2609320C3 (en) * | 1976-03-06 | 1978-08-17 | Kraftwerk Union Ag, 4330 Muelheim | Coal gasifier |
-
1977
- 1977-06-02 DE DE2724802A patent/DE2724802C2/en not_active Expired
-
1978
- 1978-05-31 FR FR7816331A patent/FR2401217A1/en active Granted
- 1978-06-02 JP JP6663078A patent/JPS541305A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS541305A (en) | 1979-01-08 |
| FR2401217A1 (en) | 1979-03-23 |
| FR2401217B1 (en) | 1983-11-10 |
| DE2724802C2 (en) | 1986-09-18 |
| DE2724802A1 (en) | 1978-12-07 |
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