NO158066B - PROCEDURE FOR CARVING A CARBON-CONTAINING MATERIAL. - Google Patents
PROCEDURE FOR CARVING A CARBON-CONTAINING MATERIAL. Download PDFInfo
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- NO158066B NO158066B NO823341A NO823341A NO158066B NO 158066 B NO158066 B NO 158066B NO 823341 A NO823341 A NO 823341A NO 823341 A NO823341 A NO 823341A NO 158066 B NO158066 B NO 158066B
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- carbonaceous material
- level
- gas
- reactor
- heat energy
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
- F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/06—Continuous processes
- C10J3/08—Continuous processes with ash-removal in liquid state
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
-
- 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
- C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
- C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2204/00—Supplementary heating arrangements
- F23G2204/20—Supplementary heating arrangements using electric energy
- F23G2204/201—Plasma
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Processing Of Solid Wastes (AREA)
- Carbon And Carbon Compounds (AREA)
- Ceramic Products (AREA)
- Crystals, And After-Treatments Of Crystals (AREA)
Abstract
Et stykkeformet karbonholdig materiale forgasses til en gassblanding i det vesentlige bestående av CO og Hved at materialet via en sluseanordning (6) tilføres oveni-fra til en reaktor (1) til et bestemt fyllingsnivfi.Den genererte gass føres ut av reaktoren (1) ved et nivå som er lavere enn det karbonholdige materialets overflate (10). Oksydasjonsmiddel og/eller varmeenergi tilføres delvis ved et nivå som ligger over materialets overflate (10) og delvis til et nivå som ligger under nivået for en rørledning (4) for utføring av generert gass.En anordning for utførelse av fremgangsmåten omfatter en reaktor (1) med en øvre sluseanordning (61 for gasstett innmatnlng av det karbonholdige materialet, en slaggavtapningsanordning (13, 14)., samt en rørledning (5) for utførsel av generert gass, samt hensiktsmessig plasserte plasmageneratorer (3, 7) for tilførsel av varmeenergi og rørledninger (2, 8, 9) for innføring av et oksydasjonsmiddel.A piece of carbonaceous material is gasified to a gas mixture consisting essentially of CO and a level lower than the surface of the carbonaceous material (10). Oxidizing agent and / or heat energy are supplied partly at a level above the surface of the material (10) and partly at a level below the level of a pipeline (4) for carrying out generated gas. A device for carrying out the process comprises a reactor (1 ) with an upper sluice device (61 for gas-tight feed of the carbonaceous material, a slag discharge device (13, 14), and a pipeline (5) for the export of generated gas, as well as suitably placed plasma generators (3, 7) for supplying heat energy and pipelines (2, 8, 9) for the introduction of an oxidizing agent.
Description
Foreliggende oppfinnelse vedrører en fremgangsmåte avden art som er angitt i krav l's ingress. The present invention relates to a method of the type specified in claim 1's preamble.
Man har i lang tid forgasset karbon i sjaktovner og retor-tere samt også utført partiell forgasning i forbindelse med forkoksning. Ulempen ved disse kjente metoder er dels at forholdet mellom CO og H2 i den genererte gass ikke kan regu-leres, men først og fremst at gassen også inneholder en rekke uønskede stoffer såsom hydrokarbon, alkoholer, fenoler og tjære. Sistnevnte skyldes hovedsakelig at forgasningen delvis skjer under lav temperatur, dvs. ved temperaturer under 1000°C og under reduserende forhold. For a long time, carbon has been gasified in shaft furnaces and retorts, as well as partial gasification in connection with coking. The disadvantage of these known methods is partly that the ratio between CO and H2 in the generated gas cannot be regulated, but primarily that the gas also contains a number of undesirable substances such as hydrocarbons, alcohols, phenols and tar. The latter is mainly due to the fact that the gasification partly takes place at a low temperature, i.e. at temperatures below 1000°C and under reducing conditions.
For å avhjelpe disse svakheter har man i den senere tid ut-viklet andre karbonforgasningsmetoder hvor forgasningen skjer under høy temperatur og oksyderende forhold, slik som eksempelvis Koppers-Totzek^metoden. Denne metoden har imidlertid den ulempe a:t H20-innholdet på grunn av den termodynamiske likevekt blir relativt høy, hvilket innebærer at den på In order to remedy these weaknesses, other carbon gasification methods have recently been developed where the gasification takes place under high temperature and oxidizing conditions, such as, for example, the Koppers-Totzek method. However, this method has the disadvantage that, due to the thermodynamic equilibrium, the H20 content becomes relatively high, which means that the
denne måte fremstilte gassen for å kunne anvendes f.eks. this way produced the gas to be used e.g.
til reduksjon av jernmalm først må avkjøles, vaskes og siden gjenoppvarmes. Videre er muligheten ifølge denne kjente metode til å påvirke forholdet mellom CO og H2 fra forgasser-en utgående gass meget liten. for the reduction of iron ore must first be cooled, washed and then reheated. Furthermore, according to this known method, the possibility of influencing the ratio between CO and H2 from the gas leaving the carburettor is very small.
Det har nå overraskende vist seg at det er mulig å unngå ovennevnte ulemper og vanskeligheter ved de hittil kjente metoder ved å benytte fremgangsmåten ifølge foreliggende oppfinnelse som er særpreget ved det som er angitt i krav l's karakteriserende del, nemlig at oksydasjonsmiddel og varmeenergi tilføres delvis over det stykkformige karbonholdige materialets overflate og delvis fra et lavere nivå som ligger under gassuttagningsnivået i reaktoren. It has now surprisingly turned out that it is possible to avoid the above-mentioned disadvantages and difficulties of the hitherto known methods by using the method according to the present invention, which is characterized by what is stated in the characterizing part of claim 1, namely that oxidizing agent and heat energy are supplied partially over the lumpy carbonaceous material's surface and partly from a lower level that lies below the gas withdrawal level in the reactor.
rfølge oppfinnelsen skjer forgasningen ved høy temperatur og under oksyderende forhold og samtidig vil den primært dannede gass passere et varmt sjikt av koks eller kokslignende materiale, hvoretter gassens innhold av H20 reagerer med karbon til H2 eller CO. Videre har den ifølge oppfinnelsen foreslåtte metode mulighet til regulering av C0/H2~forholdet når varmeenergi tilføres via plasmageneratorer, hvoretter forholdet mellom H20, C02 og 02 i den oksyderende gassen kan variere innenfor vide grenser. According to the invention, the gasification takes place at a high temperature and under oxidizing conditions and at the same time the primarily formed gas will pass a hot layer of coke or coke-like material, after which the gas's content of H20 reacts with carbon to form H2 or CO. Furthermore, the method proposed according to the invention has the possibility of regulating the C0/H2 ratio when heat energy is supplied via plasma generators, after which the ratio between H20, C02 and 02 in the oxidizing gas can vary within wide limits.
Øvrige særtrekk ved oppfinnelsen fremgår av kravene 2-7. Other special features of the invention appear from claims 2-7.
Oppfinnelsen skal i det følgende forklares nærmere under henvisning til de to vedlagte tegninger, hvor: fig. 1 er en skisse av en egnet anordning for utførelse av The invention will be explained in more detail below with reference to the two attached drawings, where: fig. 1 is a sketch of a suitable device for carrying out
fremgangsmåten, og the procedure, and
fig. 2 viser en alternativ utførelse av den i fig. 1 viste fig. 2 shows an alternative embodiment of that in fig. 1 showed
anordning når det gjelder reaktorens nedre del. device as regards the lower part of the reactor.
Den i fig. 1 og alternativt fig. 2 viste anordningen består av en sjaktovn 1, som nederst er forsynt med rør 2 og plasmageneratorer 3, hensiktsmessig plassert symmetrisk rundt sjakten 1, hvis rør 2 er forsynt med innmatningsan-ordninger for oksydasjonsmiddel, eksempelvis ; o ■, H20 eller C02, samt eventuelt pulverformig karbonholdig materiale. The one in fig. 1 and alternatively fig. The device shown in 2 consists of a shaft furnace 1, which is provided at the bottom with pipes 2 and plasma generators 3, suitably placed symmetrically around the shaft 1, whose pipes 2 are provided with feeding devices for oxidizing agent, for example; o ■, H20 or C02, as well as any powdered carbonaceous material.
På et høyere nivå er sjakten 1 forsynt med en rørledning ,4 med gassuttak 5 for å avlede den i sjakten genererte gassen. Øverst er sjakten 1 forsynt dels med en gasstett sluseanordning 6 for tilførsel av stykkeformig karbonholdig materiale dels et rør for tilslutning til en plasmagenerator 7 og matnin-gsledninger 8, 9 for oksydasjonsmiddel. På et nivå mellom det faste materialets overflate 10 i sjakten 1 og rørledningen 4 munner ut i sjakten 1 tilførselsanordninger 11, 12 for eventuell tilførsel av ekstra oksydasjonsmiddel. Dersom prosessen ønskes drevet med flytende slagg eller fast aske, er sjaktens 1 bunn forsynt med enten et tapperør 13 (fig. 1) for slagg eller et roterende utmatningsorgan 14 At a higher level, the shaft 1 is provided with a pipeline ,4 with gas outlet 5 to divert the gas generated in the shaft. At the top, the shaft 1 is provided partly with a gas-tight sluice device 6 for the supply of piece-shaped carbonaceous material and partly with a pipe for connection to a plasma generator 7 and supply lines 8, 9 for oxidizing agent. At a level between the surface 10 of the solid material in the shaft 1 and the pipeline 4, supply devices 11, 12 open into the shaft 1 for any supply of additional oxidizing agent. If the process is to be operated with liquid slag or solid ash, the bottom of the shaft 1 is provided with either a drain pipe 13 (fig. 1) for slag or a rotating discharge device 14
(fig. 2) . (fig. 2) .
Den på tegningen viste anordning virker på følgende måte: Under og før forgasningen innmates det stykkeformige karbonholdige materialet eventuelt sammen med et svovelbindende middel eksempelvis dolomit via sluseanordningen 6 inn i sjakten 1 til et forutbestemt nivå. Varmeenergi tilføres ved hjelp av en eller flere plasmageneratorer 3 resp. 7 samtidig som oksydasjonsmiddel, så som eksempelvis 02, C02 eller YL^ O til-føres via tilførselsanordningene 2, resp. 8, 9. Det stykkeformige karbonholdige materialet som kan være stenkull, The device shown in the drawing works in the following way: During and before the gasification, the piece-shaped carbonaceous material is fed, possibly together with a sulphur-binding agent, for example dolomite, via the sluice device 6 into the shaft 1 to a predetermined level. Heat energy is supplied by means of one or more plasma generators 3 or 7 at the same time as oxidizing agent, such as for example O2, CO2 or YL^O is supplied via the supply devices 2, resp. 8, 9. The lumpy carbonaceous material which may be coal,
koks, lignitt, trekull eller partielt trekull mm. utsettes for en høy temperatur under oksyderende forhold, hvoretter de flyktige bestanddelene utskilles og reagerer med oksydasjonsmidlet til hovedsakelig CO og H2, mens den ikke flyktige delen forkokses og danner et fast stykkeformig kokslignende produkt. Det er viktig at oksydasjonsmidlet tilsettes i overskudd slik at sotdannelse unngås. Oksydasjonsmidlet som ikke har reagert med det karbonholdige materialets flyktige bestanddeler vil lengre ned i sjakten 1 reagere med den dannede koksen under ytterligere dannelse av CO og eventuelt H20. De produkter som dannes i sjaktens øvre del ovenfor rørledningens 4 nivå er således et kokslignende produkt som går videre ned gjennom sjakten og et gassformig produkt hovedsakelig bestående av CO og U^, som forlater sjakten 1 gjennom rørledningen 4. Temperaturen på overflaten av det kornete materialet i sjakten kan komme opp i ca. 2000°C, mens den gass som forlater sjakten via rørledningen 4 har en temperatur ikke høyere enn 1500°C. Det er også mulig å til-føre nødvendig varmeenergi ved partiell forbrenning av det karbonholdige materialet med oksygen istedet for å anvende en plasmagenerator. Omkring bunndelen av sjakten 1 finnes et antall Våt? 2 plasert forsynt enten med plasmagenera- coke, lignite, charcoal or partial charcoal etc. is exposed to a high temperature under oxidizing conditions, after which the volatile components are separated and react with the oxidizing agent to mainly CO and H2, while the non-volatile part is coked and forms a solid piece-like coke-like product. It is important that the oxidizer is added in excess so that soot formation is avoided. The oxidising agent which has not reacted with the volatile constituents of the carbonaceous material will further down the shaft 1 react with the formed coke with further formation of CO and possibly H20. The products that are formed in the upper part of the shaft above the level of the pipeline 4 are thus a coke-like product which continues down through the shaft and a gaseous product mainly consisting of CO and U^, which leaves the shaft 1 through the pipeline 4. The temperature on the surface of the granular material in the shaft can reach approx. 2000°C, while the gas leaving the shaft via pipeline 4 has a temperature no higher than 1500°C. It is also possible to supply the necessary heat energy by partial combustion of the carbonaceous material with oxygen instead of using a plasma generator. Around the bottom of shaft 1 there are a number of Wet? 2 placed supplied either with plasma genera-
torer eller med tilførselsanordninger for oksygen samt tilførselsanordninger for oksydasjonsmiddel og eventuelt pulveraktig karbonholdig materiale. På dette trinn skjer en fullstendig forgasning av såvel det gjennom sjakten nedrennende kokslignende materialet som det eventuelt innblåste pulveraktige karbonholdige materialet. Den CO2 og U^ O som eventuelt forlater reaksjonssonen umiddelbart før massen reagerer lengre oppe i sjakten med det nedrennende stykkeformige materialet til hovedsakelig CO eller H2. tors or with supply devices for oxygen as well as supply devices for oxidizing agent and possibly powdery carbonaceous material. At this stage, a complete gasification of both the coke-like material flowing down through the shaft and the possibly blown-in powdery carbonaceous material takes place. The CO2 and U^O which possibly leave the reaction zone immediately before the mass reacts further up the shaft with the flowing down lumpy material to mainly CO or H2.
Den genererte gass som hovedsakelig består av CO og H2 forlater sjakten gjennom rørledningen 4. The generated gas, which mainly consists of CO and H2, leaves the shaft through pipeline 4.
Det kan være hensiktsmessig på dette trinn gjennom material-rørene 2 å tilføre slaggdannere samt regulere slaggets vis-kositet og smeltepunkt og/eller svovelopptagende stoffer som inneholder Ca og/eller Mg, slik som eksempelvis dolomit-pulver. Det er også på dette trinn mulig å tilsette varme via plasmabrennere med partiell forbrenning av det karbonholdige materialet ved hjelp av oksygen. It may be appropriate at this stage to add slag formers through the material pipes 2 and to regulate the viscosity and melting point of the slag and/or sulfur-absorbing substances containing Ca and/or Mg, such as dolomite powder, for example. It is also possible at this stage to add heat via plasma burners with partial combustion of the carbonaceous material using oxygen.
Hvis man ønsker å danne flytende slagg, bør temperaturen i reaksjonssonen fremfor rørene 2 i sjaktens nedre del holdes over 1600°C. Under bruk av faste asker bør denne temperatur holdes under 1400°C. If one wishes to form liquid slag, the temperature in the reaction zone in front of the pipes 2 in the lower part of the shaft should be kept above 1600°C. When using solid ashes, this temperature should be kept below 1400°C.
Den heri.beskrevne fremgangsmåten ved å forgasse karbonholdig materiale gir store muligheter til å regulere H2/CO-forholdet i den genererte gass dels ved å regulere CO/H20-forholdet i oksydasjonsmidlet og dels ved at man regulerer varmetilførselen mellom partiell forbrenning og via plasma generatorene. The method described herein by gasifying carbonaceous material offers great opportunities to regulate the H2/CO ratio in the generated gas partly by regulating the CO/H20 ratio in the oxidizer and partly by regulating the heat supply between partial combustion and via the plasma generators .
Claims (7)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| SE8201263A SE8201263L (en) | 1982-03-01 | 1982-03-01 | INSTALLATION AND INSTALLATION FOR GASATION OF CARBONIC MATERIAL |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| NO823341L NO823341L (en) | 1983-09-02 |
| NO158066B true NO158066B (en) | 1988-03-28 |
| NO158066C NO158066C (en) | 1988-07-06 |
Family
ID=20346138
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO823341A NO158066C (en) | 1982-03-01 | 1982-10-04 | PROCEDURE FOR CARVING A CARBON-CONTAINING MATERIAL. |
Country Status (25)
| Country | Link |
|---|---|
| JP (1) | JPS58152091A (en) |
| KR (1) | KR880000353B1 (en) |
| AT (1) | AT389887B (en) |
| AU (1) | AU546482B2 (en) |
| BE (1) | BE894675A (en) |
| BR (1) | BR8206416A (en) |
| CA (1) | CA1208021A (en) |
| CS (1) | CS235097B2 (en) |
| DD (1) | DD208986A5 (en) |
| DE (1) | DE3233774C2 (en) |
| ES (1) | ES8400477A1 (en) |
| FI (1) | FI823440L (en) |
| FR (1) | FR2522333B1 (en) |
| GB (1) | GB2116201B (en) |
| IN (1) | IN156382B (en) |
| IT (1) | IT1153274B (en) |
| MX (1) | MX161612A (en) |
| NL (1) | NL8203909A (en) |
| NO (1) | NO158066C (en) |
| NZ (1) | NZ202333A (en) |
| PH (1) | PH18531A (en) |
| PL (1) | PL135926B1 (en) |
| SE (1) | SE8201263L (en) |
| YU (1) | YU235382A (en) |
| ZA (1) | ZA827876B (en) |
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| SE453750B (en) * | 1984-06-14 | 1988-02-29 | Skf Steel Eng Ab | KIT FOR GASING OF FINE DISTRIBUTED COAL CONTENTS |
| SE446101B (en) * | 1984-12-28 | 1986-08-11 | Skf Steel Eng Ab | SET AND DEVICE FOR GENERATING GAS |
| DE3611429A1 (en) * | 1985-02-15 | 1986-11-06 | SKF Steel Engineering AB, Hofors | WASTE DECOMPOSITION METHOD |
| GB2183249A (en) * | 1985-11-04 | 1987-06-03 | James Willis Associates Ltd | Thermal reactor |
| IT1236318B (en) * | 1989-11-29 | 1993-02-09 | Tomadini Gino & C | SOLID FUEL GASIFICATION EQUIPMENT |
| GB2259521A (en) * | 1991-09-12 | 1993-03-17 | Us Energy | Moving bed coal gasifier |
| US5435940A (en) * | 1993-11-12 | 1995-07-25 | Shell Oil Company | Gasification process |
| EP1148295B1 (en) * | 1999-01-27 | 2011-03-23 | Sumitomo Metal Industries, Ltd. | Gasification melting furnace for wastes and gasification melting method |
| JP2002226877A (en) * | 2001-01-29 | 2002-08-14 | Takeshi Hatanaka | Method and equipment for producing alternative natural gas equipment |
| JP2002226201A (en) * | 2001-01-29 | 2002-08-14 | Takeshi Hatanaka | Production method for hydrogen and apparatus therefor |
| JP2002227657A (en) * | 2001-02-02 | 2002-08-14 | Takeshi Hatanaka | Hydrogen engine, power generation system and vehicle driven thereby |
| DE10158463B4 (en) * | 2001-11-28 | 2004-02-12 | Hans Ulrich Feustel | Process for the combined recycling of waste materials of different types, consistency and composition in a shaft-melting gasifier |
| DE102006007457B4 (en) * | 2006-02-17 | 2007-12-27 | Native Power Solutions Gmbh & Co. Kg | Method and apparatus for producing gas from carbonaceous material |
| DE102006007458B4 (en) * | 2006-02-17 | 2010-07-08 | Native Power Solutions Gmbh & Co. Kg | Method and apparatus for gasifying carbonaceous material and apparatus for generating electrical energy |
| US9206364B2 (en) | 2006-05-12 | 2015-12-08 | Inentec Inc. | Gasification system |
| US7854775B2 (en) | 2006-05-12 | 2010-12-21 | InEn Tec, LLC | Combined gasification and vitrification system |
| MX2007008317A (en) * | 2007-07-06 | 2009-02-26 | Aba Res Sa De Cv | Microwave gasification device. |
| US9222039B2 (en) | 2008-01-14 | 2015-12-29 | Inentec Inc. | Grate for high temperature gasification systems |
| US8197566B2 (en) | 2008-12-08 | 2012-06-12 | General Electric Company | Gasifier additives for improved refractory life |
| US20120061618A1 (en) | 2010-09-11 | 2012-03-15 | James Santoianni | Plasma gasification reactors with modified carbon beds and reduced coke requirements |
| KR101387324B1 (en) * | 2011-12-22 | 2014-04-24 | 재단법인 포항산업과학연구원 | Method for amplifying coke-oven gas by using oxidation agents |
| CN104479743B (en) * | 2014-12-09 | 2017-05-31 | 中国东方电气集团有限公司 | A kind of rubbish plasma gasification stove with vapor as gasifying medium |
| KR101879095B1 (en) * | 2016-12-23 | 2018-07-16 | 주식회사 포스코 | Apparatus and method for recoveryng energy of coke oven ascension pipe |
| KR102501597B1 (en) | 2019-09-25 | 2023-02-20 | 주식회사 엘지화학 | System and Method for Manufacturing Diester-based Composition |
| CN111520722A (en) * | 2020-04-26 | 2020-08-11 | 攀枝花市蓝鼎环保科技有限公司 | A high temperature plasma incineration pyrolysis furnace for industrial solid waste treatment |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1195934A (en) * | 1916-08-22 | Assigi ios osi cub-hals to | ||
| AT9904B (en) * | 1901-09-06 | 1902-11-25 | Karl Dr Kostersitz | Marking device for the lawn tennis game. |
| DE170050C (en) * | 1903-12-11 | |||
| GB191111344A (en) * | 1911-05-10 | 1912-02-29 | John Lee Scott | Improvements in Apparatus for the Production of Gas. |
| GB292408A (en) * | 1927-11-10 | 1928-06-21 | Herbert Story Moore | Improvements in or relating to gas generators |
| AT128796B (en) * | 1928-10-24 | 1932-06-25 | Ig Farbenindustrie Ag | Process for the preparation of carbon monoxide. |
| FR674061A (en) * | 1928-11-27 | 1930-01-23 | Ashy fuel gasification process | |
| DE620392C (en) * | 1932-10-08 | 1935-10-21 | Rudolf Drawe Dr Ing | Process for generating a low-carbonic strong gas |
| DE664524C (en) * | 1935-04-12 | 1938-08-29 | Humboldt Deutzmotoren Akt Ges | Double fire gas generators, especially for fuels containing tar |
| GB470275A (en) * | 1936-02-14 | 1937-08-12 | Didier Werke Ag Fa | Improvements in the production of gas from carbonaceous fuels |
| DE710724C (en) * | 1937-10-11 | 1941-09-19 | Vergasungs Ind Akt Ges | Process for producing a hydrocarbon-poor hydrocarbon gas in alternating operation |
| DE895362C (en) * | 1949-12-10 | 1953-11-02 | Basf Ag | Process for the production of fuel gas by gasifying a bituminous fuel |
| AT172631B (en) * | 1950-06-16 | 1952-09-25 | Karl Dipl Ing Dr Techn Pilz | Plant for generating electricity and gas from bituminous fuels |
| DE976435C (en) * | 1950-09-02 | 1963-09-05 | Basf Ag | Process for the production of carbon oxide-hydrogen mixtures in tapping gas generators |
| DE1042817B (en) * | 1952-10-23 | 1958-11-06 | Koppers Co Inc | Process for producing a gas containing carbon monoxide and hydrogen |
| DE1020435B (en) * | 1953-11-13 | 1957-12-05 | Basf Ag | Process for producing a fuel gas with a high calorific value and a low-methane synthesis gas |
| BE845682A (en) * | 1976-08-26 | 1976-12-16 | PROCESS AND APPARATUS FOR REPRODUCING A HOT COMBUSTIBLE GAS FREE OF SULFUR AND OTHER CONTAMINANTS | |
| DD133816A1 (en) * | 1977-04-19 | 1979-01-24 | Bodo Wolf | PROCESS FOR PRODUCING HYDROGEN-BASED GASES FROM SOLID FUELS |
| US4153426A (en) * | 1977-07-18 | 1979-05-08 | Arthur G. Mckee & Company | Synthetic gas production |
| EP0051482A1 (en) * | 1980-11-04 | 1982-05-12 | Douglas Cochrane Sons And Company (Proprietary) Limited | Production of producer gas |
-
1982
- 1982-03-01 SE SE8201263A patent/SE8201263L/en unknown
- 1982-09-11 DE DE3233774A patent/DE3233774C2/en not_active Expired
- 1982-10-01 AT AT0364182A patent/AT389887B/en not_active IP Right Cessation
- 1982-10-04 NO NO823341A patent/NO158066C/en unknown
- 1982-10-05 GB GB08228345A patent/GB2116201B/en not_active Expired
- 1982-10-08 NL NL8203909A patent/NL8203909A/en not_active Application Discontinuation
- 1982-10-08 FI FI823440A patent/FI823440L/en not_active Application Discontinuation
- 1982-10-12 BE BE0/209218A patent/BE894675A/en not_active IP Right Cessation
- 1982-10-14 ES ES516495A patent/ES8400477A1/en not_active Expired
- 1982-10-19 YU YU02353/82A patent/YU235382A/en unknown
- 1982-10-21 IT IT23851/82A patent/IT1153274B/en active
- 1982-10-21 CS CS827485A patent/CS235097B2/en unknown
- 1982-10-21 DD DD82244193A patent/DD208986A5/en not_active IP Right Cessation
- 1982-10-26 FR FR8217897A patent/FR2522333B1/en not_active Expired
- 1982-10-26 KR KR8204799A patent/KR880000353B1/en not_active Expired
- 1982-10-28 ZA ZA827876A patent/ZA827876B/en unknown
- 1982-10-29 CA CA000414473A patent/CA1208021A/en not_active Expired
- 1982-10-29 IN IN1277/CAL/82A patent/IN156382B/en unknown
- 1982-10-29 AU AU90026/82A patent/AU546482B2/en not_active Ceased
- 1982-11-01 NZ NZ202333A patent/NZ202333A/en unknown
- 1982-11-05 BR BR8206416A patent/BR8206416A/en not_active IP Right Cessation
- 1982-11-08 JP JP57194802A patent/JPS58152091A/en active Pending
- 1982-11-17 PL PL1982239081A patent/PL135926B1/en unknown
- 1982-11-23 PH PH28183A patent/PH18531A/en unknown
- 1982-12-06 MX MX195463A patent/MX161612A/en unknown
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