DE2530600C2 - Process for the catalytic pressure gasification of fossil fuels with water vapor - Google Patents
Process for the catalytic pressure gasification of fossil fuels with water vaporInfo
- Publication number
- DE2530600C2 DE2530600C2 DE19752530600 DE2530600A DE2530600C2 DE 2530600 C2 DE2530600 C2 DE 2530600C2 DE 19752530600 DE19752530600 DE 19752530600 DE 2530600 A DE2530600 A DE 2530600A DE 2530600 C2 DE2530600 C2 DE 2530600C2
- Authority
- DE
- Germany
- Prior art keywords
- reaction
- water vapor
- gasification
- fossil fuels
- catalyst
- 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
- 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
- C10J3/78—High-pressure apparatus
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
-
- 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
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
-
- 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
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
-
- 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
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
-
- 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
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
- C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1853—Steam reforming, i.e. injection of steam only
Description
IiIi
Die Erfindung bezieht sich aul ein Verfahren zur Vergasung fossiler Brennstoffe in einem Vergaser in Gegenwart eines Katalysators oder eines Gemisches von Katalysatoren mit Wasserdampf bei erhöhten Drücken und Temperaturen.The invention relates to a method for gasifying fossil fuels in a gasifier in Presence of a catalyst or a mixture of catalysts with water vapor at increased Pressures and temperatures.
Bei d>rr Vergasung fossiler Brennstoffe werden als Vergasungsmittel meist Gemische aus Sauerstoff und Wasserdampf, gelegentlich auch Gemische aus Wasserdampf und Luft verwendet, die den Brennstoff meist im Gegenstrom durchsetzen. Dabei erzeugt der zugesetzte Sauerstoff durch teilweise Verbrennung der Kohle die Reaktionstemperatur und die Reaktionswärme, die für die endotherme Reaktion zwischen Kohle und Wasserdampf benötigt wird.During the gasification of fossil fuels, as Gasification agents mostly mixtures of oxygen and water vapor, occasionally also mixtures of water vapor and air are used, which usually pass through the fuel in countercurrent. The added Oxygen by partially burning the coal the reaction temperature and the heat of reaction necessary for the endothermic reaction between coal and water vapor is required.
Die dabei erzeugten Rohgase enthalten je nach Verfahren in unterschiedlichen Anteilen Kohlenmonoxid. Wasserstoff. Methan, Kohlendioxid und nicht umgesetzten Wasserdampf sowie je nach Vergasungsmittel teilweise auch höhere Anteile an Stickstoff. Der im Einsatzbrennsioff enthaltene Schwefel befindet sich zum größeren Teil im Gas als Schwefelwasserstoff und in geringen Mengen als Kohlenoxidsulfid und muß aus dem Rohgas durch Gaswäsche entfernt werden. Gemeinsam mit den gasförmigen Schwefelverbindungen wird auch das vorhandene Kohlendioxid ausgewaschen. The raw gases generated in this process contain carbon monoxide in different proportions, depending on the process. Hydrogen. Methane, carbon dioxide and unreacted water vapor as well as depending on the gasification agent sometimes also higher proportions of nitrogen. The sulfur contained in the fuel used is located for the most part in the gas as hydrogen sulfide and in small amounts as carbon oxide sulfide and must be taken out the raw gas can be removed by gas scrubbing. Together with the gaseous sulfur compounds the existing carbon dioxide is also washed out.
Allgemein sind für die Vergasung folgende Reaktionen wichtig:In general, the following reactions are important for gasification:
Die genannten Reakiionsemhalpien beziehen sich auf Kokskohlcnstoff und weichen etwa um 3 kcal/mol von ·>> den auf Graphit bezogenen Standardenihalpicn ab.The reaction emhalpies mentioned relate to coke carbon and vary by about 3 kcal / mol from · >> the standard graphite related to graphite.
Die Haupireaktion der Vergasung, nämlich die UmsetzungThe main reaction of the gassing, namely the implementation
C +ΙΙ,Ο-CO+H,. .n C + ΙΙ, Ο-CO + H ,. . n
ist siark endotherm und läuft mit technisch nutzbarer Geschwindigkeit erst oberhalb 750 bis 800"C ab. Die für die Reaktion benötigte Wärmemenge kann durch folgende Maßnahmen zugeführt werden:is siark endothermic and runs with technically usable Speed only decreases above 750 to 800 "C. The for The amount of heat required for the reaction can be supplied by the following measures:
VyVy
a) Verbrennung eines Teils des fossilen Brennstoffes mittels Sauerstoff oder Luft (autothcrmc Vergasung). a) Burning part of the fossil fuel by means of oxygen or air (autothermal gasification).
b) Beheizung des Reaktors von außen mit Wärmefluß durch die Wand des Reaktors oder mittels bo besonderer Heizelemente.b) heating of the reactor from the outside with heat flow through the wall of the reactor or by means of bo special heating elements.
c) im Kreislauf geführte fossile, flüssige oder gasförmige Wärmeträger.c) fossil, liquid or gaseous in a cycle Heat transfer medium.
Alle diese Möglichkeiten wurden bereits untersucht v> und in tier Praxis erprobt. Weitgehend durchgesetzt hat sich die autotherme Vergasung mit Sauerstoff und Dampf. In !-!ntwicklung befindet sieh die Zufuhr von Hochtemperatur-Kcrnwärmc mittels Außenbeheizung. Besonderes Augenmerk wird aber auch der Erhöhung des Vergascrdurchsatzcs geschenkt. Während die im Betrieb befindlichen Lurgi-Druck-Vcrgaser bei Drükken von 30 bar und Temperaturen von 700 bis 10000C arbeiten, ist es Ziel der neuen amerikanischen Arbeiten, die Vergasung unter dem für die Einspeisung in ein Ferngasnetz benötigten Druck durchzuführen, d. h. bei 70 bar und darüber. Die Durchführung des Vergasiingsprozesscs bei höheren Wasserdampfdrücken führte jedoch im allgemeinen zur Herabsetzung der Reaktionsgeschwindigkeit. Die Verminderung der Reaktionsgeschwindigkeit bei höheren Wasserdampfdrükkcn ließ bisher das Arbeiten bei höheren Drücken uninteressant erscheinen.All of these possibilities have already been investigated and tested in practice. Autothermal gasification with oxygen and steam has become widely accepted. The supply of high-temperature core heat by means of external heating is currently in development. Special attention is also paid to increasing the gas throughput. While the Lurgi pressure gasifiers in operation work at pressures of 30 bar and temperatures of 700 to 1000 0 C, the aim of the new American work is to carry out the gasification under the pressure required for feeding into a long-distance gas network, ie at 70 bar and above. Carrying out the gasification process at higher water vapor pressures, however, generally led to a reduction in the rate of the reaction. The reduction in the rate of reaction at higher water vapor pressures has hitherto made working at higher pressures appear uninteresting.
In der DE-PS 5 76 134 ist bereits ein Verfahren zur Erzeugung von Starkgas beschrieben worden, bei dem bitumöse Brennstoffe oder Entgasungsrückstände bei hohem Druck mittels Wasserdampf zur Reaktion gebracht werden. Es wird insbesondere Methan und Kohlendioxid erzeugt. Zur Beschleunigung des Rcaktionsablaufcs sind bei diesem Verfahren bereits katalytisch wirkende Zuschlüge, wie Eisenoxid oder Alkalien dem Brennstoff beigemischt worden.In DE-PS 5 76 134 is already a method for Production of strong gas has been described, with the bitumous fuels or degassing residues can be reacted at high pressure by means of steam. It is particularly methane and Generates carbon dioxide. To accelerate the reaction process are in this process already catalytically active additives, such as iron oxide or Alkalis have been added to the fuel.
In der US-PS 37 75 072 wird ein Verfahren bcschric-In US-PS 37 75 072 a method is bcschric-
ben. mil dem man .his organischem Material ein Gas mit hohem Heizwert erzeugen kann. Dabei wird das organische Material, das zuvor mit einem Katalysator getränkt worden ist. bei Temperaturen von 550 bis 1000 C und in einem Druckbereieh von 4 bis HO bar mit Wasserdampf zur Reaktion gebracht. Als Katalysatoren werden Alkalicarbonate, -hydroxide, -acetale, -formiate, -sulfate und -chloride vorgeschlagen.ben. with which one .his organic material a gas with can generate high calorific value. It uses the organic material previously with a catalyst has been soaked. at temperatures from 550 to 1000 C and in a pressure range from 4 to HO bar Reacting steam. As catalysts are alkali carbonates, hydroxides, acetals, formates, sulfates and chlorides suggested.
Die GB-I1S 5 14 302 offenbart ein Verfahren, bei dem durch Hydrierung von kohlenstoffhaltigem Material Kohlenwasserstoffgas erzeugt werden kann. Dieser Patentschrift ist zu entnehmen, wie man die zur Beschleunigung des Rcaklionsablaufs vorgeschlagenen Katalysatoren zuvor dem kohlenstoffhaltigen Material beigeben kann. IZs sind hier sowohl die mechanische Zumischung des Katalysators zum kohlenstoffhaltigen Material, die Imprägnierung des kohlenstoffhaltigen Materials mit einer Lösung des Katalysaiornietalls als auch das Einblasen von fcinverteiltem Katalysator vermittels des zum I lydriercn gebrauchten Gases in den Reaktionskessel erwähnt.GB-I 1 S 5 14 302 discloses a process in which hydrocarbon gas can be generated by hydrogenating carbonaceous material. This patent specification shows how the catalysts proposed to accelerate the reaction can be added to the carbonaceous material beforehand. The mechanical admixture of the catalyst with the carbonaceous material, the impregnation of the carbonaceous material with a solution of the catalyst metal and the blowing of dispersed catalyst into the reaction vessel by means of the gas used for the hydrogenation are mentioned here.
Weiterhin ist es bekannt, zur Vergasung von fossilen Brennstoffen den Brennstoffen in größeren Mengen Calciumoxid ziizumischen. Dadurch gelingt es. die Dampf-Kohlenstoff reaktion ihcrmoneuiral zu führen (IJS-KS 26 82 455).It is also known for the gasification of fossil fuels to use the fuels in larger quantities Mix in calcium oxide. That's how it works. to carry out the steam-carbon reaction in a mononuiral manner (IJS-KS 26 82 455).
Schließlich hat man bereits vorgeschlagen, zur Herstellung von Synthesegas aus einem kohlcnwasserstoffhaltigen Brennstoff den Brennstoff mit einer freien Sauerstoff enthaltenden Gasmenge in Anwesenheit oincs Temperaturmoderators einer Pariialoxidation zu unterwerfen. Dabei kann als Tcmpcraturmodcrator Wasserdampf verwendet werden, der Alkaliverbindungen gelöst enthält (DIi-PS 25 16 908).Finally, it has already been proposed, for the production of synthesis gas from a fuel containing hydrocarbons, to subject the fuel to a partial oxidation with an amount of gas containing free oxygen in the presence of a temperature moderator. It can be used as Tcmpcraturmodcrator steam, de r alkali compounds containing dissolved (DII-PS 25 16 908).
Ausgehend von einem Verfahren mit den Merkmalen des Oberbegriffes des Anspruchs 1 liegt der Erfindung die Aufgabe zugrunde, feste Brennstoffe mit Wasserdampf bei einem Druck von 70 ba·· und mehr zu vergasen, um eine direkte Einspeisung des Produktgases in ein Ferngasnet/, zu ermöglichen. Zugleicn sollen möglichst hohe Reaktionsgeschwindigkeiten angestrebt werden. Auch soll der Anteil an Wasserstoff und Kohlendioxid zu Lasten des Anteils an Kohlenmonoxid gesteigert werden.The invention is based on a method with the features of the preamble of claim 1 the task is to use solid fuels with water vapor at a pressure of 70 ba ·· and more gasify in order to enable the product gas to be fed directly into a remote gas network /. At the same time The aim is to achieve the highest possible reaction rates. Also should the proportion of hydrogen and Carbon dioxide can be increased at the expense of the proportion of carbon monoxide.
Zur Lösung dieser Aufgabe ist gemäß der Erfindung vorgesehen, daß der Katalysator oder das Katalysatorgemisch
in Form von Alkalisalzen als Lösung in dem auf wenigstens 70 bar hochgespannten Wasserdampf der
Reaktion zugeführt wird.
Bei einem derart ausgebildeten Verfahren werdenTo achieve this object, it is provided according to the invention that the catalyst or the catalyst mixture is fed to the reaction in the form of alkali salts as a solution in the steam pressurized to at least 70 bar.
With such a trained method
Reaktionsgeschwindigkeiten erreicht, die sogar höher sind als die Reaktionsgeschwindigkeiten bei niederen Drücken und gleicher Temperatur. Dabei kann die Katalysatormenge im Wasserdampf der Sättigungskon-. zentralicn entsprechen oder an diese nahezu herankommen. Der Katalysator wird zuvor in der gewünschten Menge in dem zu verdampfenden Wasser gelöst. Dabei ist es recht vorteilhaft, daß bei den weiter unten angegebenen Dampfdrücken die Löslichkeit in der Dampfphase ebenso groß ist wie in der flüssigen Phase. Als Stoffe, die sowohl im hochgespannten Wasserdampfgut löslich sind als auch bezogen auf die Reaktion zwischen Kohle und Wasserdampf gute katalytische Eigenschaften haben, kommen gemäß der Erfindung die Salze der Alkalien zum Einsatz. In erster Linie eignen sich deren Hydroxide, Borate, einschließlich Kaliumtetraborat, und Carbonate, einschließlich Bicarbonate. Gewisse Reaktionsbeschleunigungen zeigen auch die Alkali-Chloride. Von diesen wiederum haben die Carbonate und Hydroxide des Kaliums besonders interessante Eigenschaften. Beispielsweise werden in Wasserdampf \on 825'-C und 150 bar 0,007 g Kaliumhydroxid auf 1000 g Wasser gelöst. Obwohl die unter diesen Bedingungen im Wasserdampf gelöste Salzmenge sehr gering ist, wird gegenüber einer Vergasung bei 30 bar Wasserdampfdruck eine Umsatzbeschleunigung um den Faktor vier erhalten. Die durch den Zusatz von Katalysatoren bewirkte Erhöhung der Reaktionsgeschwindigkeit entspricht einer Gcschwindigkeilserhöhung, die durch eine Temperaturerhöhung von ca. 150 bis 2000C erreicht wird. Die in der Kohlenasche befindlichen Alkaliverbindungen, hauptsächlich Silicate, zeigen eher eine Inhibicrung der Reaktion.Reached reaction rates that are even higher than the reaction rates at low pressures and the same temperature. The amount of catalyst in the water vapor of the saturation con-. centrally correspond to or almost approach them. The catalyst is previously dissolved in the desired amount in the water to be evaporated. It is very advantageous that at the vapor pressures given below, the solubility in the vapor phase is just as great as in the liquid phase. According to the invention, the salts of alkalis are used as substances which are soluble in high-tension water vapor and which have good catalytic properties in relation to the reaction between coal and water vapor. Primarily their hydroxides, borates, including potassium tetraborate, and carbonates, including bicarbonates, are suitable. The alkali chlorides also show certain acceleration of the reaction. Of these, in turn, the carbonates and hydroxides of potassium have particularly interesting properties. For example, 0.007 g of potassium hydroxide is dissolved in 1000 g of water in steam at 825 ° C. and 150 bar. Although the amount of salt dissolved in the water vapor under these conditions is very small, a conversion acceleration by a factor of four is obtained compared to gasification at 30 bar water vapor pressure. The effected by the addition of catalysts enhance the reaction rate corresponds to a Gcschwindigkeilserhöhung, which is achieved by a temperature increase of about 150 to 200 0 C. The alkali compounds in the coal ash, mainly silicates, tend to inhibit the reaction.
Überraschenderweise zeigt sich weiterhin, daß nach dem Verfahren dieser Erfindung die Zusammensetzung des Rohgases sich in der Weise ändert, daß mehr Wasserstoff und Kohlendioxid und weniger Kohlenmonoxid entsteht. Der Gehalt des Rohgases an Kohlenmonoxid gehl juf Werte von weniger als 2 Vol.-% zurück. Damit würde das Rohgas besonders für die Herstellung von synthetischem Erdgas nach dem thermodynamisch günstigeren, durch die Gleichungen 3. 4 und 8 repräsentierten Weg geeignet sein. Abgesehen davon ist es nach dem Verfahren dieser Erfindung möglich, ohne Einbuße an Vergasungskapazität Vergasungsdrükke in der Höhe anzuwenden, wie sie für die Weiterverwendung des Fertigproduktes wünschenswert sind. Außerdem wird die Wärmebilanz des Vergasers infolge Bevorzugung von Reaktion 7 gegenüber Reaktion 3 verbessert.Surprisingly, it is also found that, according to the method of this invention, the composition of the raw gas changes in such a way that more hydrogen and carbon dioxide and less carbon monoxide arises. The carbon monoxide content of the raw gas falls back to values of less than 2% by volume. This would make the raw gas especially for the production of synthetic natural gas after the thermodynamic cheaper way represented by equations 3.4 and 8 may be suitable. Apart from this it is possible according to the method of this invention without sacrificing gasification capacity gasification pressures to be used in the amount that is desirable for the further use of the finished product are. In addition, as a result of the preference for reaction 7 improved over reaction 3.
Claims (2)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
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DE19752530600 DE2530600C2 (en) | 1975-07-09 | 1975-07-09 | Process for the catalytic pressure gasification of fossil fuels with water vapor |
Applications Claiming Priority (1)
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DE19752530600 DE2530600C2 (en) | 1975-07-09 | 1975-07-09 | Process for the catalytic pressure gasification of fossil fuels with water vapor |
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DE2530600A1 DE2530600A1 (en) | 1977-01-27 |
DE2530600C2 true DE2530600C2 (en) | 1984-02-02 |
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DE19752530600 Expired DE2530600C2 (en) | 1975-07-09 | 1975-07-09 | Process for the catalytic pressure gasification of fossil fuels with water vapor |
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Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3133670A1 (en) * | 1981-08-26 | 1983-03-17 | Kraftwerk Union AG, 4330 Mülheim | Process for gasifying carbonaceous raw materials |
US7763160B2 (en) | 2003-12-19 | 2010-07-27 | Shell Oil Company | Systems and methods of producing a crude product |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2411879A1 (en) * | 1977-12-19 | 1979-07-13 | Exxon Research Engineering Co | CATALYTIC PROCESS FOR THE PREPARATION OF COMBUSTIBLE GAS FROM COAL |
DE2817835C2 (en) * | 1978-04-24 | 1984-04-05 | Kraftwerk Union AG, 4330 Mülheim | Process for the catalytic pressure gasification of solid fuels with water vapor |
DE3133723C2 (en) * | 1981-08-26 | 1984-03-29 | Kraftwerk Union AG, 4330 Mülheim | Process for gasifying carbonaceous raw materials with superheated steam |
US5630854A (en) * | 1982-05-20 | 1997-05-20 | Battelle Memorial Institute | Method for catalytic destruction of organic materials |
DE3222653C1 (en) * | 1982-06-16 | 1983-04-21 | Kraftwerk Union AG, 4330 Mülheim | Process for converting carbonaceous fuel into a combustible product gas |
DE3228532A1 (en) * | 1982-07-30 | 1984-02-02 | BKMI Industrieanlagen GmbH, 8000 München | Process for carbonizing and gasifying carbonaceous solids |
US4597775A (en) * | 1984-04-20 | 1986-07-01 | Exxon Research And Engineering Co. | Coking and gasification process |
DE3508303A1 (en) * | 1985-03-08 | 1986-09-11 | Ruhrgas Ag | Process and equipment for the catalytic gasification of coal with steam |
JPS6395292A (en) * | 1986-10-09 | 1988-04-26 | Univ Tohoku | Catalytic gasification of coal using chloride |
US5019135A (en) * | 1987-10-13 | 1991-05-28 | Battelle Memorial Institute | Method for the catalytic conversion of lignocellulosic materials |
NZ253874A (en) * | 1992-06-05 | 1996-04-26 | Battelle Memorial Institute | Catalytic conversion of liquid organic materials into a product gas of methane, carbon dioxide and hydrogen |
BRPI0405935A (en) * | 2003-12-19 | 2005-10-04 | Shell Int Research | Methods of Producing a Transportable Petroleum and Crude Oil, Heating Fuel, Lubricants or Chemicals and Crude Oil Product |
DE102004038491B4 (en) * | 2004-08-07 | 2010-07-22 | Karlsruher Institut für Technologie | Process for converting biomass into gaseous products |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE576134C (en) * | 1931-03-22 | 1933-05-08 | Metallgesellschaft Ag | Process for the production of strong gas and by-products by gasifying bituminous fuels or degassing residues by means of steam under higher pressure |
GB574302A (en) * | 1944-01-29 | 1945-12-31 | Leonard Gordon Higham | New or improved apparatus for the development of photo-prints |
US2682455A (en) * | 1949-06-16 | 1954-06-29 | Consolidation Coal Co | Gasification of carbonaceous solid fuels |
US3775072A (en) * | 1970-12-14 | 1973-11-27 | Chevron Res | Gas production |
US3689240A (en) * | 1971-03-18 | 1972-09-05 | Exxon Research Engineering Co | Production of methane rich gases |
-
1975
- 1975-07-09 DE DE19752530600 patent/DE2530600C2/en not_active Expired
Cited By (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3133670A1 (en) * | 1981-08-26 | 1983-03-17 | Kraftwerk Union AG, 4330 Mülheim | Process for gasifying carbonaceous raw materials |
US7763160B2 (en) | 2003-12-19 | 2010-07-27 | Shell Oil Company | Systems and methods of producing a crude product |
US7811445B2 (en) | 2003-12-19 | 2010-10-12 | Shell Oil Company | Systems and methods of producing a crude product |
US7828958B2 (en) | 2003-12-19 | 2010-11-09 | Shell Oil Company | Systems and methods of producing a crude product |
US7854833B2 (en) | 2003-12-19 | 2010-12-21 | Shell Oil Company | Systems and methods of producing a crude product |
US7879223B2 (en) | 2003-12-19 | 2011-02-01 | Shell Oil Company | Systems and methods of producing a crude product |
US7959797B2 (en) | 2003-12-19 | 2011-06-14 | Shell Oil Company | Systems and methods of producing a crude product |
US8025791B2 (en) | 2003-12-19 | 2011-09-27 | Shell Oil Company | Systems and methods of producing a crude product |
US8070936B2 (en) | 2003-12-19 | 2011-12-06 | Shell Oil Company | Systems and methods of producing a crude product |
US8163166B2 (en) | 2003-12-19 | 2012-04-24 | Shell Oil Company | Systems and methods of producing a crude product |
US8268164B2 (en) | 2003-12-19 | 2012-09-18 | Shell Oil Company | Systems and methods of producing a crude product |
US8394254B2 (en) | 2003-12-19 | 2013-03-12 | Shell Oil Company | Crude product composition |
US8608938B2 (en) | 2003-12-19 | 2013-12-17 | Shell Oil Company | Crude product composition |
US8613851B2 (en) | 2003-12-19 | 2013-12-24 | Shell Oil Company | Crude product composition |
US8663453B2 (en) | 2003-12-19 | 2014-03-04 | Shell Oil Company | Crude product composition |
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