DE1180481C2 - Process for generating methane-containing gases - Google Patents
Process for generating methane-containing gasesInfo
- Publication number
- DE1180481C2 DE1180481C2 DE1958G0024508 DEG0024508A DE1180481C2 DE 1180481 C2 DE1180481 C2 DE 1180481C2 DE 1958G0024508 DE1958G0024508 DE 1958G0024508 DE G0024508 A DEG0024508 A DE G0024508A DE 1180481 C2 DE1180481 C2 DE 1180481C2
- Authority
- DE
- Germany
- Prior art keywords
- hydrocarbons
- weight
- water vapor
- catalyst
- nickel
- 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
- 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
- C10K3/02—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 by catalytic treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
- B01J10/007—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
-
- 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
- C01B3/34—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 by reaction of hydrocarbons with gasifying agents
- C01B3/38—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 by reaction of hydrocarbons with gasifying agents using catalysts
- C01B3/382—Multi-step processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1052—Nickel or cobalt catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Hydrogen, Water And Hydrids (AREA)
Description
Die Erfindung bezieht sich auf die Erzeugung von methanhaltigen Gasen aus Mischungen von vorwiegend paraffinischen Kohlenwasserstoffen, die im Mittel 4 bis 10 Kohlenstoffatome enthalten, wie z. B. Erdöldestillaten, durch Umsetzung mit Wasserdampf in Gegenwart eines Katalysators.The invention relates to the generation of methane-containing gases from mixtures of predominantly paraffinic hydrocarbons containing an average of 4 to 10 carbon atoms, such as. B. Petroleum distillates, by reaction with steam in the presence of a catalyst.
Es ist bekannt, methanhaltige Gase aus Mischungen von niedrigsiedenden Kohlenwasserstoffen, die Schwefel als Verunreinigung enthalten, dadurch zu erzeugen, daß man den Dampf der Kohlenwasserstoffe mit Wasserdampf in Gegenwart eines Nickelkatalysators bei Temperaturen zwischen etwa 870 und 1040° C zur Bildung eines Gemisches, das im wesentlichen aus Wasserstoff und Kohlenmonoxyd besteht, umsetzt, das Gemisch durch einen Schwefeladsorber oder -wäscher führt und das gereinigte Gemisch zur Bildung von Methan bei Temperaturen zwischen 260 und 482° C mit einem Nickelkatalysator in Berührung bringt. Das bekannte Mehrstufenverfahren hat den Nachteil, daß in der ersten Stufe eine besondere Wärmezufuhr erforderlich ist, da die Umsetzung der Kohlenwasserstoffe mit Wasserdampf zur Bildung eines Gemisches von Wasserstoff und Kohlenmonoxyd endotherm ist. Zu diesem Zweck muß entweder Sauerstoff der ersten Stufe zugeführt werden, um Wärme durch Verbrennung in der Reaktionszone freizusetzen, oder es ist eine besondere Erhitzung des in einer Vielzahl von Rohren vorgesehenen Katalysators von außen erforderlich. Solche Arbeitsweisen unter Erzeugung von Wärme bzw. mit besonderer Wärmezufuhr sind sowohl hinsichtlich des Betriebes als· auch der erforderlichen Apparatur kostspielig und unwirtschaftlich.It is known to produce methane-containing gases from mixtures of low-boiling hydrocarbons which Contain sulfur as an impurity, produced by the fact that one produces the vapor of the hydrocarbons with steam in the presence of a nickel catalyst at temperatures between about 870 and 1040 ° C to form a mixture consisting essentially of hydrogen and carbon monoxide consists, converts, the mixture passes through a sulfur adsorber or scrubber and the purified Mixture for the formation of methane at temperatures between 260 and 482 ° C with a nickel catalyst brings in touch. The known multi-stage process has the disadvantage that in the first Stage a special supply of heat is required because the reaction of the hydrocarbons with water vapor is endothermic to form a mixture of hydrogen and carbon monoxide. To this Purpose must either be fed to the first stage oxygen to heat by combustion in to release the reaction zone, or it is a special heating of the in a variety of tubes provided catalyst required from the outside. Such working methods with the generation of heat or with a special supply of heat are required both in terms of operation and · Apparatus expensive and uneconomical.
Es ist ferner ein Verfahren bekannt, gemäß welchem aus Dieselöl und Kerosin Ölgas (hauptsächlich H2, CH4, C2H4 und CO) durch Erhitzen auf 700 bis 900° C unter Anwendung eines Nickelkatalysators und in Gegenwart von Wasserdampf hergestellt wird. Es werden bei dieser Arbeitsweise in Übereinstimmung mit dem bei hohen Reaktionstemperaturen herrschenden Reaktionsgleichgewicht nur sehr geringe Mengen von Methan und in der Hauptsache Kohlenmonoxyd und Wasserstoff er-A method is also known according to which oil gas (mainly H 2 , CH 4 , C 2 H 4 and CO) is produced from diesel oil and kerosene by heating to 700 to 900 ° C. using a nickel catalyst and in the presence of steam. In this procedure, in accordance with the reaction equilibrium that prevails at high reaction temperatures, only very small amounts of methane and mainly carbon monoxide and hydrogen are produced.
halten. . , ·keep. . , ·
Das erfindungsgemäße Verfahren zum Erzeugen von methanhaltigen Gasen aus Mischungen von vorwiegend paraffinischen Kohlenwasserstoffen, die im Mittel 4 bis 10 Kohlenstoff atome enthalten, durchThe inventive method for generating methane-containing gases from mixtures of predominantly paraffinic hydrocarbons that contain an average of 4 to 10 carbon atoms through
ίο Umsetzung mit Wasserdampf in Gegenwart eines Nickelkatalysators ist dadurch gekennzeichnet, daß man die dampfförmigen Kohlenwasserstoffe und Wasserdampf im Verhältnis von 2 bis 5 Gewichtsteilen Dampf auf 1 Gewichtsteil der Kohlenwasser- stoffe oder bei Verwendung von Kohlenwasserstoffen, die im Mittel 4 bis 7 Kohlenstoffatome enthalten, im Verhältnis von 1,5 bis 5 Gewichtsteilen Dampf auf 1 Gewichtsteil der Kohlenwasserstoffe durch ein katalytisches Bett von mit Tonerde aktiviertem redu-ίο reaction with steam in the presence of a Nickel catalyst is characterized in that the vaporous hydrocarbons and Water vapor in the ratio of 2 to 5 parts by weight of steam to 1 part by weight of the hydrocarbon substances or when using hydrocarbons that contain an average of 4 to 7 carbon atoms, in the ratio of 1.5 to 5 parts by weight of steam to 1 part by weight of the hydrocarbons through one catalytic bed of alumina activated reductive
ao ziertem Nickel bei Atmosphärendruck oder bei Uberatmosphärendruck führt und den Kohlenwasserstoffdampf und den Wasserdampf in das Katalysatorbett bei einer Temperatur über 350° C leitet, so daß das Bett durch die Reaktion auf einer Temperatur in dem Bereich von 400 bis 550° C gehalten wird.ao ed nickel at atmospheric pressure or at Uber atmospheric pressure leads and the hydrocarbon vapor and the water vapor in the catalyst bed at a temperature above 350 ° C, so that the Bed is maintained at a temperature in the range of 400 to 550 ° C by the reaction.
Die Erfindung gründet sich auf die Erkenntnis, daß die Umsetzung von vorwiegend aus den genannten paraffinischen Kohlenwasserstoffen bestehenden Mischungen mit Wasserdampf in zufriedenstellender Weise bei einer Temperatur in dem Bereich von 400 bis 550° C ohne die Notwendigkeit einer Wärmezufuhr von außen oder einer besonderen Wärmeerzeugung im Reaktionsraum ausgeführt werden kann, wenn die Kohlenwasserstoffe und der Wasserdampf auf einer Temperatur über 350° C vorerhitzt werden, und daß die auf diese Weise unmittelbar erhaltenen Gase vergleichsweise reich an Methan sind, da sie beispielsweise mehr als 50 Volumprozent Methan nach Entfernung von Kohlendioxyd und Wasserdampf aus dem erhaltenen Gasgemisch enthalten. The invention is based on the knowledge that the implementation of predominantly from the above paraffinic hydrocarbons existing mixtures with water vapor in a more satisfactory manner Way at a temperature in the range of 400 to 550 ° C without the need for heat from the outside or a special heat generation in the reaction chamber can if the hydrocarbons and the water vapor are preheated to a temperature above 350 ° C and that the gases obtained directly in this way are comparatively rich in methane are because they are, for example, more than 50 percent by volume after removal of carbon dioxide and methane Contain water vapor from the gas mixture obtained.
Bei Versuchen, die Kohlenwasserstoff-Wasserdampf-Reaktion bei Temperaturen unter 900 und über 550° C auszuführen, wurde festgestellt, daß sich auf dem Katalysator wesentliche Mengen an Kohlenstoff abscheiden, sofern nicht ein großer Überschuß von Wasserdampf verwendet wird. Die Abscheidung von Kohlenstoff verschlechtert die Wirkung des Katalysators und verstopft die Apparatur.When attempting the hydrocarbon-water vapor reaction at temperatures below 900 and Carry out above 550 ° C, it was found that there are significant amounts of on the catalyst Separate carbon unless a large excess of water vapor is used. the Deposition of carbon worsens the effectiveness of the catalyst and clogs the apparatus.
Wenn die Abscheidung von Kohlenstoff durch Wasserdampf verhindert werden soll, sind sehr große Mengen von Wasserdampf (etwa 100 Gewichtsteile Wasserdampf je 1 Gewichtsteil Kohlenwasserstoff) erforderlich, welche das Verfahren unwirtschaftlich und technisch unbrauchbar machen.If the deposition of carbon by water vapor is to be prevented, they are very large Amounts of water vapor (about 100 parts by weight of water vapor per 1 part by weight of hydrocarbon) required, which make the process uneconomical and technically unusable.
Bei dem Verfahren gemäß der Erfindung Wird die Ablagerung von Kohlenstoff durch Verwendung von Anteilen an Wasserdampf innerhalb der vorstehend angegebenen Bereiche vermieden, so daß kein großer Überschuß von Wasserdampf erforderlich ist.In the method according to the invention, the deposition of carbon is carried out by using Contents of water vapor avoided within the ranges given above, so that no large Excess of steam is required.
Die Temperatur, auf die der Kohlenwasserstoffdampf und der Wasserdampf vorerhitzt werden müssen, um das Katalysatorbett auf einer Temperatur in dem erfindungsgemäß anzuwendenden Bereich zu halten, hängt von den relativen Anteilen der Kohlenwasserstoffe und des Wasserdampfes und von dem Druck ab, bei dem das Verfahren ausgeführt wird. Die Vorerhitzungstemperatur soll je-The temperature to which the hydrocarbon vapor and water vapor are preheated have to keep the catalyst bed at a temperature in the range to be used according to the invention to keep depends on the relative proportions of hydrocarbons and water vapor and on the pressure at which the procedure is carried out. The preheating temperature should
doch immer über 350° C, um eine ausreichende Aktivität des Katalysators zu gewährleisten, und zweckmäßig unter 500° C liegen, um eine vorzeitige thermische Zerlegung der Kohlenwasserstoffe zu vermeiden. but always above 350 ° C to ensure sufficient activity of the catalyst, and expediently below 500 ° C in order to avoid premature thermal decomposition of the hydrocarbons.
Der Druck kann bis zu 50 at betragen, jedoch kann er gewünschtenfalls auch höher sein. Geeignete Drücke liegen in dem Bereich von 10 bis 25 at.The pressure can be up to 50 atm, but it can also be higher if desired. Suitable Pressures are in the range of 10 to 25 at.
Je niedriger die Temperatur des Katalysatorbettes ist, um so höher ist der Methangehalt in dem erzeugten Gas, und je höher der Druck ist, um so höher ist der Methangehalt. Das erzeugte Gas enthält nach der Entfernung von Kohlendioxyd und Wasserdampf aus ihm im allgemeinen wenigstens 50 Volumprozent Methan, und die Konzentration an Methan kann bei verhältnismäßig hohem Druck, wie z. B. 50 at, 80 Volumprozent übersteigen.The lower the temperature of the catalyst bed, the higher the methane content in the product Gas, and the higher the pressure, the higher the methane content. The generated gas contains after the removal of carbon dioxide and water vapor from it generally at least 50 percent by volume Methane, and the concentration of methane can be at relatively high pressure, such as. B. 50 at, Exceed 80 percent by volume.
Der bei der Kohlenwasserstoff-Wasserdampf-Reaktion benutzte Katalysator besteht aus mit Aluminiumoxyd (Tonerde) aktiviertem reduziertem Nickel und enthält beispielsweise 15% Nickel. Ein solcher Katalysator kann in bekannter Weise bereitet werden, indem man eine wäßrige Lösung von wasserlöslichen Salzen, wie den Nitraten, von Nickel und Aluminium mit einem Alkali, wie Natriumcarbonat, behandelt, um einen Niederschlag eines Gemisches von Nickel- und Aluminiumverbindungen zu erzeugen, den Niederschlag wäscht und trocknet, die Nickelverbindung zu metallischem Nickel reduziert und das sich ergebende Gemisch von reduziertem Nickel und Tonerde in Korn- oder Tablettenform bringt. Gegegebenenf alls kann man Körner von aktivierter Tonerde mit einer wäßrigen Lösung von Nickelnitrat imprägnieren und dann rösten und das Nickeloxyd zu metallischem Nickel reduzieren.The one in the hydrocarbon-water vapor reaction The catalyst used consists of reduced nickel and activated with aluminum oxide (alumina) for example contains 15% nickel. Such a catalyst can be prepared in a known manner by an aqueous solution of water-soluble salts, such as the nitrates, of nickel and aluminum treated with an alkali such as sodium carbonate to produce a precipitate of a mixture of nickel and to produce aluminum compounds, the precipitate washes and dries the nickel compound reduced to metallic nickel and the resulting mixture of reduced nickel and Brings clay in grain or tablet form. Given All activated alumina grains can be impregnated with an aqueous solution of nickel nitrate and then roast and reduce the nickel oxide to metallic nickel.
Die Erfindung wird nachstehend an zwei Beispielen näher erläutert.The invention is explained in more detail below using two examples.
Es wurde ein Erdölleichtdestillat verwendet, welches einen Siedebereich von 37 bis 72° C und eine Dichte von 0,649 bis 20° C hatte und 99,6 Volumprozent paraffinische Kohlenwasserstoffe und 0,4 Volumprozent aromatische Stoffe enthielt. Ein Gemisch von 1 Gewichtsteil des Dampfes des Destillats und 2 Gewichtsteilen Wasserdampf wurde auf etwa 420° C vorerhitzt und durch ein gut wärmeisoliertes Rohr geführt, welches ein Bett aus einem körnigen Nickel-Tonerde-Katalysator enthielt, der in der oben beschriebenen Weise bereitet war. Die bei verschiedenen Reaktionstemperaturen und unter verschiedenen Drücken erzielbaren Ergebnisse sind in der nachstehenden Tabelle angegeben:A light petroleum distillate was used which had a boiling range of 37 to 72 ° C and a Density from 0.649 to 20 ° C and 99.6 percent by volume paraffinic hydrocarbons and 0.4 percent by volume Contained aromatic substances. A mixture of 1 part by weight of the vapor of the distillate and 2 parts by weight of steam was preheated to about 420 ° C and through a well heat-insulated Pipe led, which contained a bed of a granular nickel-alumina catalyst, which in the above described way was prepared. Those at different reaction temperatures and under different Pressures achievable results are given in the table below:
Fortsetzungcontinuation
Zusammensetzung des
erzeugten Gases'in
VolumprozentComposition of
generated gases'in
Volume percentage
ίο CO2 ίο CO 2
CO CO
H2 H 2
CH4 CH 4
H2O H 2 O
Zusammensetzung des
Gases nach Entfernung von CO2 und
H2O in Volumprozent Composition of
Gas after removal of CO 2 and
H 2 O in percent by volume
so CO2 so CO 2
CO CO
H2 H 2
CH4 CH 4
Vorerhitzungstemperatur in ° C Preheating temperature in ° C
KatalysatortemperaturCatalyst temperature
Atmosphären
druckAtmospheres
pressure
427,5
420427.5
420
Druckpressure
10 at I 25 at10 at I 25 at
413,3
475413.3
475
25 at25 at
11,411.4
32,632.6
47,247.2
20,020.0
77,077.0
420
500420
500
Für dieses Beispiel wurde ein schwereres Erdöldestillat als im Beispiel 1 verwendet. Dieses schwerere Destillat bestand aus Kohlenwasserstoffen mit 8 bis 13 Kohlenstoffatomen, wobei die mittlere Anzahl von Kohlenstoffatomen 10 betrug. Das Destillat hatte einen Siedebereich von 100 bis 174° C und eine Dichte von 0,764 und enthielt 85,0 Volumprozent paraffinische Kohlenwasserstoffe und 15,0 Volumprozent aromatische Stoffe. Ein Gemisch von 1 Gewichtsteil des Dampfes des Destillats und 2 Gewichtsteileri Wasserdampf wurde auf 480° C vorerhitzt und über ein Bett aus einem körnigen Nickel-Tonerde-Katalysator bei 500° C unter einem Druck von 25 at geführt. Die Zusammensetzungen der erhaltenen Gase vor und nach der Entfernung von Kohlendioxyd und Wasserdampf waren die folgenden:For this example, a heavier petroleum distillate was used than used in example 1. This heavier distillate consisted of hydrocarbons with 8 to 13 carbon atoms, the average number of carbon atoms being 10. The distillate had a boiling range of 100 to 174 ° C and a density of 0.764 and contained 85.0 percent by volume paraffinic hydrocarbons and 15.0 percent by volume of aromatic substances. A mixture of 1 part by weight of the vapor of the distillate and 2 parts by weight of water vapor was preheated to 480 ° C and over a bed of granular nickel-alumina catalyst at 500 ° C under pressure run by 25 at. The compositions of the gases obtained before and after the removal of Carbon dioxide and water vapor were the following:
Zusammensetzung des erzeugten Gases in Volumprozent Composition of the gas generated in percent by volume
CO2 12,7CO 2 12.7
CO 0,5CO 0.5
H2 7,4H 2 7.4
CH4 31,1CH 4 31.1
H2O ·. 48,3H 2 O ·. 48.3
Zusammensetzung des Gases nach Entfernung von CO2 und H2O in VolumprozentComposition of the gas after removal of CO 2 and H 2 O in percent by volume
CO2 2,0CO 2 2.0
CO 1,3CO 1.3
H2 18,6H 2 18.6
CH4 78,1CH 4 78.1
Claims (2)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB731058A GB820257A (en) | 1958-03-06 | 1958-03-06 | Process for the production of gases containing methane from hydrocarbons |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| DE1180481B DE1180481B (en) | 1964-10-29 |
| DE1180481C2 true DE1180481C2 (en) | 1973-05-10 |
Family
ID=9830686
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DE1958G0024508 Expired DE1180481C2 (en) | 1958-03-06 | 1958-05-09 | Process for generating methane-containing gases |
Country Status (2)
| Country | Link |
|---|---|
| DE (1) | DE1180481C2 (en) |
| GB (1) | GB820257A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2359116A1 (en) | 1972-11-28 | 1974-05-30 | Japan Gasoline | PROCESS FOR PRODUCING A METHANE CONTAINING GAS IN THE CONTEXT OF LOW-TEMPERATURE STEAM REFORMING OR LOW-TEMPERATURE STEAM REFORMING PROCESS FOR HYDROCARBONS FOR THE PRODUCTION OF A METHANE-RICH GAS |
Families Citing this family (75)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB969637A (en) * | 1961-06-09 | 1964-09-16 | Gas Council | Process for the production of gases containing methane from hydrocarbons |
| GB1000309A (en) * | 1962-09-21 | 1965-08-04 | Gas Council | Improvements in or relating to the treatment of gases |
| GB994278A (en) * | 1962-10-25 | 1965-06-02 | Gas Council | Process for the production of gases containing methane from hydrocarbons |
| GB1018382A (en) * | 1963-04-02 | 1966-01-26 | Gas Council | Improvements in or relating to the production of gases containing methane from hydrocarbons |
| US3407149A (en) * | 1963-10-21 | 1968-10-22 | Exxon Research Engineering Co | Promoted catalyst for methane production |
| US3404100A (en) * | 1963-10-21 | 1968-10-01 | Exxon Research Engineering Co | Methane production using a promoted catalyst |
| US3320182A (en) * | 1963-10-21 | 1967-05-16 | Exxon Research Engineering Co | High activity nickel-alumina catalyst |
| GB1029711A (en) * | 1964-01-17 | 1966-05-18 | Gas Council | Process for the production of combustible gases |
| US3395004A (en) * | 1964-01-20 | 1968-07-30 | Exxon Research Engineering Co | Low-temperature, high-pressure, catalytic, partial conversion of naphtha hydrocarbons to hydrogen |
| US3450514A (en) * | 1964-01-20 | 1969-06-17 | Exxon Research Engineering Co | Controlled conversion of light naphtha to town gas |
| US3449099A (en) * | 1964-02-10 | 1969-06-10 | Exxon Research Engineering Co | Process for reacting hydrocarbons and steam using spent catalyst for pretreating |
| US3371050A (en) * | 1964-02-18 | 1968-02-27 | Exxon Research Engineering Co | Promoted catalyst for production of town gas at low temperatures |
| NL6402670A (en) * | 1964-03-13 | 1965-09-14 | ||
| GB1033765A (en) * | 1964-03-05 | 1966-06-22 | Gas Council | Process for the production of methane-containing gases |
| US3396124A (en) * | 1964-05-07 | 1968-08-06 | Exxon Research Engineering Co | Catalyst for low temperature conversion of hydrocarbons to hydrogen and methane |
| US3508889A (en) * | 1964-05-22 | 1970-04-28 | Exxon Research Engineering Co | Process for producing high quality town gas for delivery |
| GB1043377A (en) * | 1964-06-08 | 1966-09-21 | ||
| DE1470718A1 (en) * | 1964-08-05 | 1969-04-10 | Metallgesellschaft Ag | Process for the production of methane-rich gases by catalytic hydrogenative cleavage of hydrocarbons |
| US3446594A (en) * | 1965-08-03 | 1969-05-27 | United Aircraft Corp | Method for generating hydrogen from liquid hydrogen-containing feedstocks |
| GB1152009A (en) * | 1966-02-24 | 1969-05-14 | Gas Council | Process for Preparing Methane-Containing Gases |
| GB1271721A (en) * | 1968-05-03 | 1972-04-26 | Gas Council | A process for the production of methane-containing gases |
| NL151042B (en) * | 1970-02-26 | 1976-10-15 | Basf Ag | PROCEDURE FOR REFORMING HYDROCARBON GASES WITH STEAM, PROCEDURE FOR MANUFACTURING A CATALYST TO BE USED THEREIN, AND MOLDED CATALYST SO MADE. |
| US3778239A (en) * | 1971-03-10 | 1973-12-11 | Ford Bacon & Davis Inc | Production of gaseous and liquid fuels from crude oil |
| US3932147A (en) | 1971-06-28 | 1976-01-13 | Japan Gasoline Co., Ltd. | Method of reforming hydrocarbons |
| US3963642A (en) * | 1971-08-20 | 1976-06-15 | Metallgesellschaft Aktiengesellschaft | Process for producing a reducing gas |
| GB1447974A (en) * | 1972-11-13 | 1976-09-02 | British Gas Corp | Process for the production of gases containing methane from hydro carbons |
| JPS5550080B2 (en) * | 1972-11-28 | 1980-12-16 | ||
| US3828474A (en) * | 1973-02-01 | 1974-08-13 | Pullman Inc | Process for producing high strength reducing gas |
| US3942957A (en) * | 1973-05-14 | 1976-03-09 | British Gas Corporation | Production of combustible gases |
| GB2184367A (en) * | 1985-12-18 | 1987-06-24 | British Gas Plc | Methanation catalysts |
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|---|---|---|---|---|
| US2711419A (en) * | 1951-03-30 | 1955-06-21 | Surface Combustion Corp | Process and apparatus for making fuel gas |
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- 1958-03-06 GB GB731058A patent/GB820257A/en not_active Expired
- 1958-05-09 DE DE1958G0024508 patent/DE1180481C2/en not_active Expired
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2711419A (en) * | 1951-03-30 | 1955-06-21 | Surface Combustion Corp | Process and apparatus for making fuel gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2359116A1 (en) | 1972-11-28 | 1974-05-30 | Japan Gasoline | PROCESS FOR PRODUCING A METHANE CONTAINING GAS IN THE CONTEXT OF LOW-TEMPERATURE STEAM REFORMING OR LOW-TEMPERATURE STEAM REFORMING PROCESS FOR HYDROCARBONS FOR THE PRODUCTION OF A METHANE-RICH GAS |
Also Published As
| Publication number | Publication date |
|---|---|
| GB820257A (en) | 1959-09-16 |
| DE1180481B (en) | 1964-10-29 |
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