AU4230185A – Methane conversion
– Google Patents
AU4230185A – Methane conversion
– Google Patents
Methane conversion
Info
Publication number
AU4230185A
AU4230185A
AU42301/85A
AU4230185A
AU4230185A
AU 4230185 A
AU4230185 A
AU 4230185A
AU 42301/85 A
AU42301/85 A
AU 42301/85A
AU 4230185 A
AU4230185 A
AU 4230185A
AU 4230185 A
AU4230185 A
AU 4230185A
Authority
AU
Australia
Prior art keywords
methane
solid
oxide
gas
metal
Prior art date
1984-04-16
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.)
Granted
Application number
AU42301/85A
Other versions
AU580303B2
(en
Inventor
Anne M. Gaffney
Howard P. Withers
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Atlantic Richfield Co
Original Assignee
Atlantic Richfield Co
Priority date (The priority date 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 date listed.)
1984-04-16
Filing date
1985-04-11
Publication date
1985-11-15
1984-04-16
Priority claimed from US06/600,917
external-priority
patent/US4499324A/en
1984-04-16
Priority claimed from US06/600,665
external-priority
patent/US4499323A/en
1984-04-16
Priority claimed from US06/600,669
external-priority
patent/US4489215A/en
1984-10-31
Priority claimed from US06/666,694
external-priority
patent/US4721828A/en
1984-11-05
Priority claimed from US06/668,299
external-priority
patent/US4603091A/en
1985-04-11
Application filed by Atlantic Richfield Co
filed
Critical
Atlantic Richfield Co
1985-11-15
Publication of AU4230185A
publication
Critical
patent/AU4230185A/en
1989-01-12
Application granted
granted
Critical
1989-01-12
Publication of AU580303B2
publication
Critical
patent/AU580303B2/en
2005-04-11
Anticipated expiration
legal-status
Critical
Status
Ceased
legal-status
Critical
Current
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Espacenet
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Classifications
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
B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J23/18—Arsenic, antimony or bismuth
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
B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
B01J23/08—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of gallium, indium or thallium
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
B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
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
B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
B01J23/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of germanium, tin or lead
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
B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
B01J23/32—Manganese, technetium or rhenium
B01J23/34—Manganese
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
B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
B01J27/14—Phosphorus; Compounds thereof
B01J27/16—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr
B01J27/18—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr with metals other than Al or Zr
C—CHEMISTRY; METALLURGY
C07—ORGANIC CHEMISTRY
C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
C07C2/82—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling
C07C2/84—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen oxidative coupling catalytic
C—CHEMISTRY; METALLURGY
C07—ORGANIC CHEMISTRY
C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
C07C2523/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of rare earths
C—CHEMISTRY; METALLURGY
C07—ORGANIC CHEMISTRY
C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
C07C2523/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals
C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
C07C2523/46—Ruthenium, rhodium, osmium or iridium
C—CHEMISTRY; METALLURGY
C07—ORGANIC CHEMISTRY
C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
C07C2523/74—Iron group metals
C07C2523/745—Iron
C—CHEMISTRY; METALLURGY
C07—ORGANIC CHEMISTRY
C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
C07C2527/14—Phosphorus; Compounds thereof
C07C2527/16—Phosphorus; Compounds thereof containing oxygen
C07C2527/18—Phosphorus; Compounds thereof containing oxygen with metals
Description
METHANE CONVERSION BACKGROUND OF THE INVENTION FIELD OF THE INVENTION
This invention relates to systhesis of hydrocarbons from a methane source. A particular application of this invention is a method for convert¬ ing natural gas to a more readily transportable material. DESCRIPTION OF THE PRIOR ART
A major source of methane is natural gas. Other sources of methane have been considered for fuel supply, e.g., the methane present in coal deposits or formed during mining operations. Relatively small amounts of methane are also produced in various petro¬ leum processes.
The composition of natural gas at the well¬ head varies but the major hydrocarbon present is meth¬ ane. For example, the methane content of natural gas may vary within the range from about 40 to about 95 volume percent. Other constituents of natural gas include ethane, propane, butanes, pentane (and heavier hydrocarbons), hydrogen sulfide, carbon dioxide, helium and nitrogen.
Natural gas is classified as dry or wet de¬ pending upon the amount of condensable hydrocarbons contained in it. Condensable hydrocarbons generally comprise C3+ hydrocarbons although some ethane may be included. Gas conditioning is required to alter the composition of wellhead gas, processing facilities usually being located in or near the production fields. Conventional processing of wellhead natural gas yields processed natural gas containing at least a major amount of methane.
Large-scale use of natural gas often requires a sophisticated and extensive pipeline system. Lique¬ faction has also been employed as a transportation means, but processes for liquefying, transporting, and
revaporizing natural gas are complex, energy-intensive and require extensive safety precautions. Transport of natural gas has been a continuing problem in the ex¬ ploitation of natural gas resources. It would be extremely valuable to be able to convert methane (e.g., natural gas) to more readily handleable or transport¬ able products. Moreover, direct conversion to olefins such as ethylene or propylene would be extremely valuable to the chemical industry.
Recently, it has been discovered that methane may be converted to higher hydrocarbons by a process which comprises contacting methane and an oxidative synthesizing agent at synthesizing conditions (e.g., at a temperature selected within the range from about 500° to about 1000°C). Oxidative synthesizing agents are compositions having as a principal component at least one oxide of at least one metal which compositions produce C2+ hydrocarbon products, co-product water, and a composition comprising a reduced metal oxide when contacted with methane at synthesizing conditions. Reducible oxides of several metals have been identified which are capable of converting methane to higher hydrocarbons. In particular, oxides of manganese, tin, indium, germanium, lead, antimony and bismuth are most useful. See U.S. Patent Numbers 4,443,649; 4,444,984; 4,443,648; 4,443,645; 4,443,647; 4,443,644; and 4,443,646.
Commonly-assigned U.S. Patent Application Serial Number 522,935, filed August 12, 1983, discloses and claims a process which comprises contacting methane with an oxidative synthesizing agent under elevated pressure (e.g., 2-100 atmospheres) to produce greater amounts of C3+ hydrocarbon products. The entire content of this application is incorporated herein by reference.
Commonly-assigned U.S. Patent Application Serial Number 522,938, filed August 12, 1983, discloses
and claims a process for the conversion of methane with particles comprising an oxidative synthesizing agent which particles continuously recirculate between two physically separate zones—a methane contact zone and an oxygen contact zone. The entire content of this application is incorporated herein by reference.
U.S. Patent 4,499,322 discloses and claims a process for the conversion of methane to higher hydro¬ carbons which comprises contacting methane with an oxidative synthesizing agent containing a promoting amount of alkali metal and/or compounds thereof. The entire content of this patent is incorporated herein by reference.
U.S. Patent 4,495,374 discloses and claims a process for the conversion of methane to higher hydro¬ carbons which comprises contacting methane with an oxidative synthesizing agent containing a promoting amount of alkaline earth metal and/or .compounds thereof. The entire content of this patent is incorporated herein by reference. SUMMARY OF THE INVENTION
It has now been found that methane may be converted to higher hydrocarbon products by contacting a methane-containing gas with a reducible oxide of a metal selected from the group consisting of praseo¬ dymium, terbium and ruthenium. Preferably, the con¬ tacting is conducted at a temperature within the range of about 700 to 900°C.
It has also been found that methane may be converted to higher hydrocarbon products by contacting a methane-containing gas with a solid comprising: (1) a reducible oxide of a metal selected from the group con¬ sisting of praseodymium, terbium, cerium, iron and ruthenium and (2) at least one member of the group consisting of alkali metals, alkaline earth metals, and compounds thereof. Alkali metals are selected from the group consisting of Li, Na, K, Rb and Cs. Alkaline
earth metals are selected from the group consisting of Mg, Ca, Sr and Ba.
Methane is desirably contacted with the solid at a temperature within the range of about 500 to 1000°C. The atomic ratio of the reducible metal oxide (expressed as the metal, e.g., Pr) to alkali or alka¬ line earth metal is desirably within the range of about 1-15:1. Hydrocarbons produced by the process may include lower alkanes, lower olefins and aromatics. The reducible metal oxide is reduced by contact with methane and is reoxidizable by contact with an oxygen- containing gas.
Incorporating an alkali or alkaline earth metal into the contact solid substantially reduces the formation of comubstion products and improves higher hydrocarbon product selectivity. DETAILED DESCRIPTION OF THE INVENTION
Reducible oxides of Pr can be supplied from a variety of known sources. The term «reducible» is used to identify those oxides which are reduced by contact with methane at temperatures within the range of about 500 to 1000°C. A preferred oxide is PrgOχχ.
The contact solid employed in the present process may also contain, in a preferred embodiment of the present invention, at least one alkali metal or alkaline earth metal. Alkali metals are preferred. Sodium and lithium are presently preferred alkali metals. The amount of alkali/alkaline earth metal incorporated into the contact solid is not narrowly critical. The preferred atomic ratio of the reducible praseodymium oxide component (expressed as the metal, Pr) to the alkali/alkaline earth metal component (ex¬ pressed as the metal, e.g., Na) is within the range of about 1-15:1, more preferably within the range of about 1-3:1.
Reducible oxides of Tb can be supplied from a variety of known sources. The term «reducible» is used
to identify those oxides which are reduced by contact with methane at temperatures within the range of about 500 to 1000°C. A preferred oxide is TD4O7.
The contact solid employed in the present process may contain, in addition to a reducible oxide of Tb, at least one alkali or alkaline earth metal. Alkali metals are preferred. Sodium and lithium are presently preferred alkali metals. The amount of alkali/alkaline earth metal incorporated into the contact solid is not narrowly critical. The preferred atomic ratio of the reducible terbium oxide component (expressed as the metal, Tb) to the alkali/alkaline earth metal component (expressed as the metal, e.g., Na) is within the range of about 1-15:1, more prefer¬ ably within the range of about 1-3:1.
Reducible oxides of Ce can be supplied from a variety of known sources. The term «reducible» is used to identify those oxides which are reduced by contact with methane at temperatures within the range of about 500 to 1000°. A preferred oxide is Ceθ2»
The contact solid employed in the present process contains, in addition to a reducible oxide of Ce, at least one alkali metal, or alkaline earth metal. Alkali metals are preferred. Sodium and lithium are presently preferred alkali metals. The amount of alkali/ alkaline earth metal incorporated into the contact solid is not narrowly critical. The preferred atomic ratio of the reducible cerium oxide component (expressed as the metal, Ce) to the alkali/alkaline earth metal component (expressed as the metal, e.g., Na) is within the range of about 1-15:1, more prefer¬ ably within the range of about 1-3:1.
Reducible oxides of Fe can be supplied from a variety of known sources. The term «reducible» is used to identify those oxides which are reduced by contact with a methane at temperatures within the range of about 500 to 1000°C. Preferred oxides are e2θ3 and
e3θ . The bulk iron oxide Fe3θ4 is particularly preferred.
The contact solid employed in the present process may contain, in addition to a reducible oxide of Fe, at least one alkali metal or alkaline earth metal. Alkali metals are preferred. Sodium is par¬ ticularly preferred. The amount of alkali/alkaline earth metal incorporated into the contact solid is not narrowly critical. The preferred atomic ratio of the reducible iron oxide component (expressed as the metal, Fe) to the alkali/alkaline earth metal com¬ ponent (expressed at the metal, e.g., Na) is within the range of about 1-500:1, more preferably within the range of about 2-100:1; still more preferably about 2-10:1.
Reducible oxides of Ru can be supplied from a variety of known sources. The term «reducible» is used to identify those oxides which are reduced by contact with methane at temperatures within the range of about 500 to 1000°C. A preferred oxide is ruthenium dioxide.
The contact solid employed in the present process may contain, in addition to a reducible oxide of Ru, at least one alkali metal or alkaline earth metal. Alkali metals are preferred. Sodium is par¬ ticularly preferred. The amount of alkali/alkaline earth metal incorporated into the contact solid is not narrowly critical. The preferred atomic ratio of the reducible ruthenium oxide component (expressed as the metal, Ru) to the alkali/alkaline earth metal component (expressed as the metal, e.g., Na) is within the range of about 1-500:1, more preferably within the range of about 2-100:1, still more preferably within the range of about 2-10:1.
The contact solid may also contain other com¬ ponents heretofore referred to as oxidative synthe¬ sizing agents. Oxidative synthesizing agents generally comprise at least one oxide of at least one metal,
which oxides when contacted with methane at synthe¬ sizing conditions (e.g., at a temperature selected within the range of about 500 to 1000°C) produce higher hydrocarbon products, co-product water, and a reduced metal oxide. The composition thus contains at least one reducible oxide of at least one metal. The term «reducible» is used to identify those oxides of metals which are reduced by contacting methane at syntehsizing conditions (e.g., at temperatures selected within the range of about 500 to 1000°C). The term «oxide (s) of metal(s)» includes: (1) one or more metal oxides (i.e., compounds described by the general formula MxOy wherein M is a metal and the subscripts x and v designate the relative atomic proportions of metal and oxygen in the composition) and/or (2) one or more oxygen-containing metal compounds, provided that such oxides and compounds have the capability of performing to produce higher hydrocarbon products as set forth herein. Oxidative synthesizing agents have previously been found to comprise reduicble oxides of metals selected from the group consisting of Mn, Sn, In, Ge, Sb, Pb, and Bi and mixtures thereof. Particularly effective oxidative synthesizing agents have been found to comprise a reducible oxide of manganese and mixtures of a reducible oxide of manganese with other oxidative synthesizing agents.
It is within the scope of the present inven¬ tion to include other effective oxidative synthesizing agent components with the reducible metal oxides of the present invention. Thus, reducible oxides of metals selected from the group consisting of Pr, Tb, Ce, Fe and Ru may be combined with a reducible oxide of metals selected from the group consisting of Mn, Sn, In, Ge, Sb, Pb, Bi and mixtures thereof.
It is also within the scope of the present in¬ vention to include at least one phosphorus component in the solid contacted with methane.
While the exact composition of the contact solids is more complex, a preferred group of solids em¬ ployed in the process of this invention may be des¬ cribed by the following empirical expression:
Aa Bb Cc Pd Oe wherein A is selected from the group consiting of Pr, Tb, Ce, Fe, Ru and mixtures thereof; B is selected from the group consisting of alkali and alkaline earth metals; C is selected from the group consisting of Mn, Sn, In, Ge, Pb, Sb, Bi and mixtures thereof; a, b, c, d and e indicate the atomic ratio of each component; and when a is 10, b is within the range of about 0.5-10, c is within the range of about 0-10, d is within the range of about 0-10, and e has a value which is deter¬ mined by the valences and proportions of other elements present.
These components may be associated with other support materials. However, in a presently preferred embodiment, a reducible oxide of metals selected from the group consisting of Pr, Tb, Ce, Fe and Ru is em¬ ployed as a support for the other components of the solids. While use of other supports is within the scope of this invention, it has been found that materials such as silica and alumina tend to deactivate the solids of this invention via the formation of silicates and aluminates.
One particularly preferred embodiment of the present invention comprises contacting methane at a temperature within the range of about 500 to 1000°C with a solid comprising a member of the group consist¬ ing of alkali metals and compounds thereof associated with a support comprising a reducible oxide of Pr. Preferably, the reducible oxide of Pr comprises PrgOj . Still more particularly, the presently preferred alkali metals associated with these supports are Na and Li.
Another particularly preferred embodiment of
the present invention comprises contacting methane at a temperature within the range of about 500 to 1000°C with a solid comprising a member of the group consist¬ ing of alkali metals and compounds thereof associated with a support comprising a reducible oxide of Tb. Preferably, the reducible oxide of Tb comprises ^407. Still more particularly, the presently preferred alkali metals associated with these supports are Na and Li.
A further particularly preferred embodiment of the present invention comprises contacting methane at a temperature within the range of about 500 to 1000°C with a solid comprising a member of the group consisting of alkali metals and compounds thereof assoicated with a support comprising a reducible oxide of Fe. Preferably, the reducible oxide of Fe comprises Fe3θ4. Still more particularly, the presently prefer¬ red alkali metal associated with these supports is Na.
A still further particulary preferred em¬ bodiment of the present invention comprises contacting methane at a temperature within the range of about 500 to 1000°C with a solid comprising a member of the group consisting of alkali metals and compounds thereof associated with a support comprising a reducible oxide of Ru. Preferably, the reducible oxide of Ru comprises ruthenium dioxide. Still more particularly, the pre¬ sently preferred alkali metal associated with these supports is Na.
The contact solids employed in this invention can be prepared by any suitable method. Conventional methods such as precipitation, co-precipitation, impreg¬ nation, or dry-mixing can be used. Supported solids may be prepared by methods such as adsorption, impreg¬ nation, precipitation, co-precipitation, and dry-mixing. When phosphorus is incorporated in the agent, it is desirable to provide it in theform of a phosphate of an alkali metal or an alkaline earth metal. Substantially any compound of these elements can be employed in the
preparation of the promoted synthesizing agent.
A suitable method of preparation is to im¬ pregnate a support with solutions of compounds of the desired metals. Suitable compounds useful for impreg¬ nation include the acetates, acetylacetonates, oxides, carbides, carbonates, hydroxides, formates, oxalates, nitrates, phosphates, sulfates, sulfides, tartrates, fluorides, chlorides, bromides, or iodides. After impregnation the preparation is dried to remove solvent and the dried solid is prepared for use by calcining, preferably in air at a temperature selected within the range of about 300 to 1200°C. Particular calcination temperatures will vary depending upon the particular metal compound of compounds employed.
If phosphorus is used, the alkali/alkaline earth metal and phosphorus are preferably added to the composition as compounds containing both P and alkali/ alkaline earth metals. Examples are the orthophos- phates, metaphosphates, and pyrophosphates of alkali/ alkaline earth metals. Pyrophosphates have been found to give desirable results. Sodium pyrophosphate is particularly preferred.
Regardless of how the components of the contact solid are combined, the resulting composite generally will be dried and calcined at elevated tem¬ peratures prior to use in the process of this invention.
The present process is distinguished from previously suggested methane conversion processes with rely primarily on interactions between methane and at least one of nickel and the noble metals, such as rhodium, palladium, silver, osmium, iridium, platinum and gold. An example of this type of process is dis¬ closed in U.S. Patent 4,205,194. The present process does not require that methane be contacted with one or more of nickel and such noble metals and compounds thereof.
Moreover, in a preferred embodiment, such con-
tacting is carried out in the substantial absence of catalytically effective nickel and the noble metals and compounds thereof to minimize the deleterious catalytic effects of such metals and compounds thereof. For example, at the conditions, e.g., temperatures, useful for the contacting step of the present inven¬ tion, these metals when contacted with methane tend to promote coke formation, and the metal oxides when contacted with methane tend to promote formation of combustion products (COx) rather than the desired hydrocarbons. The term «catalytically effective» is used herein to identify that quantity of one or more of nickel and the noble metals and compounds thereof which when present substantially changes the distribution of products obtained in the contacting step of this invention relative to such contacting in the absence of such metals and compounds thereof.
In addition to methane, the feedstock em¬ ployed in the method of this invention may contain other hydrocarbon or non-hydrocarbon components, although the methane content should typically be within the range of about 40 to 100 volume percent, preferably from about 80 to 100 volume percent, more preferably from about 90 to 100 volume percent.
Operating temperatures for the contacting of methane-containing gas and the reducible metal oxide are generally within the range of about 500 to 1000°C. If reducible oxides of metals such as In, Ge or Bi are present in the solid, the particular temperature selected may depend, in part, on the particular redu¬ cible metal oxide(s) employed. Thus, reducible oxides of certain metals may require operating temperatures bleow the upper part of the recited range to minimize sublimation or volatilization of the metals (or com¬ pounds thereof) during methane contact. Examples are (1) reducible oxides of indium, (operating temperatures will preferably not exceed about 850°C); (2) reducible
oxides of germanium (operating temperatures will preferably not exceed about 850°C); and (3) reducible oxides of bismuth (operating temperatures will prefer¬ ably not exceed about 850°C).
Operating pressure for the methane contacting step are not critical to the presently claimed inven¬ tion. However, both general system pressure and par¬ tial pressure of methane have been found to effect overall results. Preferred operating pressures are within the range of about 1 to 100 atmospheres, more preferably within the range of about 1 to 30 atmos¬ pheres.
Contacting methane and a reducible metal oxide to form higher hydrocarbons from methane also produces a reduced metal oxide and co-product water. The exact nature of the reduced metal oxides are un¬ known, and so are referred to herein as «reduced metal oxides.» Regeneration of a reducible metal oxide is readily accomplished by contacting such reduced materials with oxygen (e.g., ‘an oxygen-containing gas such as air) at elevated temperatures, preferably at a temperature selected within the range of about 300 to 1200°C, the particular temperature selected depending on the meetal(s) included in the solid.
In carrying out the present process, a single reactor apparatus containing a fixed bed of solids may be used with intermittent of pulsed flow of a first gas comprising methane and a second gas comprising oxygen (e.g., oxygen, oxygen diluted with an inert gas, or air, preferably air) . The methane contacting step and the oxygen contacting step may also be performed in physically separate zones with solids recirculating between the two zones.
Thus, a suitable method for synthesizing hydrocarbons from a methane source comprises: (a) contacting a gas comprising methane and particles comprising a reducible metal oxide to form higher
hydrocarbon products, coproduct water, and reduced metal oxide; (b) removing particles comprising reduced metal oxide from the first zone and contacting the reduced particles in a second zone with an oxygen- containing gas to form particles comprising a reducible metal oxide and (c) returning the particles produced in the second zone to the first zone. The steps are preferably repeated at least periodically, and more preferably the steps are continuous. In the more pre¬ ferred embodiment solids are continuously circulated between at least one methane-contact zone and at least one oxygen-contact zone.
Particles comprising reducible metal oxide which are contacted with methane may be maintained as fluidized, ebullating, or entrained beds of solids. Preferably methane is contacted with a fluidized bed of solids.
Similarly, particles comprising reduced metal oxide which are contacted with oxygen my be maintained
» as fluidized, ebullating or entrained beds of solids.
Preferably oxygen is contacted with a fluidized bed of solids.
In one more preferred embodiment of the pre¬ sent invention, methane feedstock and particles com¬ prising a promoted oxidative synthesizing agent are continuously introduced into a methane contact zone maintained at synthesizing conditions. Synthesizing conditions include the temperatures and pressures described above. Gaseous reaction products from the methane contact zone (separated from entrained solids) are further processed—e.g., they are passed through a fractionating system wherein the desired hydrocarbon products are separated from unconverted methane and combustion products. Unconverted methane may be re¬ covered and recycled to the methane contact zone.
Particles comprising reduced metal oxide are contacted with oxygen in an oxygen contact zone for a
time sufficient to oxidize at least a portion of the reduced oxide to produce a reducible metal oxide and to remove, i.e., combust, at least a portion of any car¬ bonaceous deposit which may form on the particles in the methane contact zone. The conditions of the oxygen contact zone will preferably include a temperature selected within the range of about 300 to 1200°C, pressures of up to about 30 atmospheres, and average particle contact time within the range of about 1 to 120 minutes. Sufficient oxygen is preferably provided to oxidize all reduced metal oxide to produce a redu¬ cible oxide and to completely combust any carbonaceous deposit material deposited on the particles. At least a portion of the particles comprising promoted oxida¬ tive synthesizing agent which are produced in the oxygen contact zone are returned to the methane contact zone.
The rate of solids withdrawal from the meth¬ ane contact zone is desirably balanced with the rate of solids passing from the oxygen contact zone to the methane contact zone so as to maintain a substantially constant inventory of particles in the methane contact zone, thereby enabling steady state operation of the synthesizing system.
In one alternative process employing the method of this invention, a gas comprising oxygen may be co-fed with a hydrocarbon gas comprising methane to the methane contact zone. See U.S. Patent Application Serial Number 06/600,656, the entire content of which is incorporated herein by reference.
In a further alternative process employing the method of this invention, the olefin content of the effluent produced by methane conversion as described h herein may be oligomerized to produce normally liquid higher hydrocarbon products. See U.S. Patent Applic¬ ation Serial Number 06/600,657, the entire content of which is incorporated herein by reference.
In a still further alternative process em¬ ploying the method of this invention, it has been found advantageous to recover C2+ alkanes from (1) the effluent produced by methane conversion as described herein and/or (2) streams derived from such effluent and to recycle such alkanes to the methane contact zone. See U.S. Patent Application Serial Number 06/600, 878, the entire content of which is incorporated herein by reference.
In a still further alternative process em¬ ploying the method of this invention, it has been found that halogen promoters enhance results obtained when methane is converted to higher hydrocarbons by contact with a reducible metal oxide. See U.S. Patent Applica¬ tion Serial Number 06/600,668, the entire content of which is incorporated herein by reference. Also see U.S. Patent Application Serial Numbers 06/600,659 (chalcogen promoters) and 06/600,658 ( Ox promoters), the entire contents of which are incorporated herein by reference.
The invention is further illustrated by refer¬ ence to the following examples.
Methane-contact runs were made at about atmos¬ pheric pressure in quartz tube reactors (18 mm. inside diameter) packed with 10 ml. of contact solid. The reactors were brought up to temperature under a flow of nitrogen which was switched to methane at the start of the run. Unless otherwise indicated, all methane- contact runs described in the following examples had a duration of 2 minutes. At the end of each methane- contact run, the reactor was flushed with nitrogen and the solids were regenerated under a flow of air (usually at 800°C for 30 minutes). The reactor was then again flushed with nitrogen and the cycle repeated. Most of the results reported below are based on the cumulative sample collected after the contact solid has been through at least one cycle of methane contact and
regeneration.
Experimental results reported below include conversions and selectivities calculated on a carbon mole basis. Carbonate selectivities were calculated from the C0 content of the N2 purge gas collected after the methane contact run.
Space velocities are reported as gas hourly space velocities (hr.~l) and are identified as «GHSV» in the Examples.
EXAMPLE 1 A contact solid comprising sodium/Pr oxide was prepared by impregnating PrgOn with the appro¬ priate amount of sodium (as sodium acetate) from water solutions. The impregnated solids were dried at 110°C for 2 hours and then calcined in air by raising the temperature from 200°C to 800°C at a rate of about 100°/hour and then holding the temperature at 800°C for 16 hours. The calcined solids contained 4 wt. % Na. Results reported below in Table I are based on analyse’s of cumulative samples collected during a two-minute methane-contact run.
TABLE I Temp. (°C) 825
GHSV (hr.-1) 2400
% CH4 Conv. 36.4
% C2 + Sel. 51.2
% C0X Sel. 45.0
% Coke Sel. 1.1
% Carbonate Sel. 2.7
EXAMPLE 2 The procedure described in Example 1 was re¬ peated except that calcined Prg0]_i[_ was contacted with methane in the absence of sodium. Results are shown in Table II below.
TABLE II
Temp. (°C) 825
GHSV (hr._1 ) 2400
% CH4 Cσnv. 39.5
% C2 + Sel. 1.0
% C0X Sel. 95.7
% Coke Sel. 1.5
% Carbonate Sel. 1.7
] 3XAMPLE 3
A number of methane contact runs over 4 wt.
(prepared as described in Example 1) were performed to demonstrate the effect of temperatures and space velocities on process results. Results are shown in Table III below.
TABLE III
Temp. (°C) 750 750 750 825 825
GHSV (hr.-1: ) 1200 2400 4800 4800 4800
% CH4 Conv. 28.0 20.5 12.7 27.6 23.3
% C2 + Sel. 64.3 76.0 84.1 62.6 69.4
% C0X Sel. 28.3 20.2 12.1 34.3 27.2
% Coke Sel. 1.2 0.8 1.0 0.9 1.2
% Carbonate Sel. 3.3 3.0 2.8 2.2 2.2
EXAMPLE 4
A contact solid comprising NaMn02/Pr oxide was prepared by impregnating Pr 0]_χ with the appro¬ priate amount of sodium permanganate from a water solution. The calcined solids contained the equivalent of 10 wt. % NaMn02. Results reported below in Table IV are based on analyses of cumulative samples collect¬ ed during two-minute methane runs at a temperature of 825°C and 600 hr.~l GHSV.
TABLE IV % CH Conv. 80.9
% C2 + Sel. 6.8
% C0X Sel. 89.9
% Coke Sel. 3.3
EXAMPLE 5 A lithium/praseodymium oxide solid was pre¬ pared by impregnating PrgOχχ with the appropriate amount of lithium (as lithium acetate) from water solutions. The dried, calcined solid contained 1.2 wt. % Li. When the solid was contacted with methane at 775°C and 2400 hr.-l GHSV, the following results were obtained: 21.7% methane conversion and 74.3% C2+ hydrocarbon selectivity. After 15 cycles of methane contact/air regeneration, the following results were obtained during the sixteenth methane contact run: 8.2% conversion and 89.4% C + hydrocarbon selectivity.
EXAMPLE 6 A potassium/praseodymium oxide solid was pre¬ pared by impregnating PrgO χ with the appropriate amount of potassium (as potassium acetate) from water solutions. The dried, calcined solid contained 6.6 wt. % K. When the solid was contacted with methane at 775°C and 2400 hr.»1 GHSV, the following results were obtained: 28.6% methane conversion and 50.9% C2+ hydrocarbon selectivity.
EXAMPLE 7 A contact solid comprising sodium/Tb oxide was prepared by impregnating Tb θ7 with the appropriate amount of sodium (as sodium acetate) from water solu¬ tions. The impregnated solids were dried at 110°C for 2 hours and then calcined in air by raising the temper¬ ature from 200°C to 800°C at a rate of about 100°C/hour and then holding the temperature at 800°C for 16 hours. The calcined solids contained 4 wt. % Na. Results reported below in Table V are based on analyses of cumulative samples collected during a two-minute methane-contact run.
TABLE V
Temp. ( °C) 825
GHSV (hr._1) 1200
% CH4 Conv. 30.0
% C2 + Sel. 43.0
% COx Sel. 53.6
% Coke Sel. 0.7
% Carbonate Sel. 2.8
EXAMPLE 8
The procedure described in Example 7 was re¬ peated except that calcined ^407 was contacted with methane in the absence of sodium. Results are shown in Table IV below:
TABLE VI Temp. (°C) 825
GHSV (hr.-1) 1200
% CH4 Conv. 20.0
% C + Sel. 1.8
% C0X Sel. 94.9
% Coke Sel. 3.2
% Carbonate Sel. 0.1
EXAMPLE 9 A number of methane contact runs over 4 wt. % a/Tb4θ7 (prepared as described in Example 7) were per¬ formed to demonstrate the effect of temperatures and space velocities on process results. Results are shown in Table VII below.
TABLE VI
Temp. (°C) 750 750 825 825 850 875
GHSV (hr.-l) 1200 3600 600 2400 600 600
% CH4 Conv. 23.7 8.5 44.9 14.3 48.0 53.3
% C2 + Sel. 56.7 71.5 30.3 46.3 18.8 21.8
% C0X Sel. 38.9 22.7 64.5 50.3 80.3 80.8
% Coke Sel. 0.8 0.8 1.1 0.7 0.4 2.3
% Carbonate Sel. 3.7 5.0 4.2 2.8 0.5 6.1
EXAMPLE 10 A contact solid comprising sodium/Ce oxide was prepared by impregnating Ce02 with the appropriate amount of sodium (as sodium acetate) from water solu¬ tions. The impregnated solids were dried at 110°C for 2 hours and then calcined in air by raising the temper¬ ature from 200°C to 800°C at a rate of about 100°C/hour and then holding the temperature at 800°C for 16 hours. The calcined solids contained 4 wt. % Na. Results reported below in Table VIII are based on analyses of cumulative samples collected during a two-minute methane-contact run.
TABLE VIII
Temp. (°C) 825
GHSV (hr.»1] 1 1200
% CH4 Conv. 4.6
% C + Sel. 28.3
% C0X Sel. 32.4
% Coke Sel. 14.6
% Carbonate Sel. 24.8
EXAMPLE 11
The procedure described in example 10 was re¬ peated except that calcined Ce0 was contacted with methane in the absence of sodium. Results are shown in Table IX below.
TABLE IX Temp. (°C) 825
GHSV (hr.»1) 1200
% CH4 Conv. 25.7
% C + Sel. 0
% COx Sel. 99.0
% Coke Sel. 1.0
% Carbonate Sel.
EXAMPLE 12 A contact solid comprising NaMn02/Ce oxide was prepared by impregnating Ce0 with the appropriate amount of sodium permanganate from a water solution.
The calcined solids contained the equivalent of 10 wt. % NaMn02. Results reported below in Table X are based on analyses of cumulative samples collected during two-minute methane runs at a temperature of 825°C and 600 hr.-1 GHSV.
TABLE X % CH4 Conv. 23.4
% C + Sel. 20.4
% COx Sel. 45.3
% Coke Sel. 34.0
% Carbonate Sel.
EXAMPLE 13 A silica-supported solid was prepared by sequential impregnation, drying and calcination of the following components on a silica support: Na (provided as sodium acetate), Mn (provided as manganese acetate), and Ce provided as Ce(OH)3. Drying and calcination steps were performed as described in Example 10. The finished, calcined solid contained 10 wt. % Ce/10 wt. % Mn/1.7 wt % Na/Si02. When contacted with methane at 825°C and 600 hr.-1 GHSV, the following results were obtained: 10.2% methane conversion and 86.1% C2+ hydrocarbon selectivity.
EXAMPLE 14 A contact solid was prepared by slurrying 25 grams (0.108 moles) of reagent grade Fe3θ4 with 25 ml. of an aqueous solution containing 12.6 grams (0.093 moles) of reagent grade Na(CH3COO) *3H20. The slurry was dried at room temperature for one hour and then at 120°C for two hours. It was then calcined at 850°C for 16 hours in static air. On a weight basis, the material was analyzed to be 7.6% sodium with an Fe:Na ratio of 3.5.
A quartz-tube reactor (described above) was packed with 5 ml. of 12-28 mesh particles of the solid. The results obtained over a series of methane contact runs are described in Table XI below.
TABLE XI
Temp. GHSV % Selectivity To:
Run# (°C) (hr»1) % Conv. ≤2±- CO CO-2 Coke
1 600 860 0.5 15.4 0 84.6 0
2 600 860 0.4 0 0 100 0
3 700 860 2.5 5.1 0 94.9 0
4 700 860 1.8 14.3 0 84.9 0.8
5 800 860 14.6 40.8 0 57.7 1.5
6 800 860 23.5 28.3 0 70.9 0.8
7 825 860 26.7 26.4 0 71.6 2.1
8 825 860 29.4 26.9 0 71.6 1.5
9 825 1200 21.2 33.9 TR 64.7 1.4
10 825 1200 25.5 29.0 TR 70.3 0.7
11 825 2400 10.7 42.9 0 55.6 1.6
12 825 2400 10.4 46.4 0 52.9 0.7
13 825 3600 6.4 47.4 0 51.4 1.2
14 825 3600 6.5 48.7 0 50.6 0.7
15 800 860 16.4 31.9 0 66.3 1.8
16 800 1200 11.0 38.2 0 60.2 1.6
17 800 1200 10.6 37.6 0 61.1 1.3
EXAMPLE 15
A solid containing 7.3 wt. % Na and having an Fe:Na ratio of 3.5 was prepared as described in Example 14 except that reagent grade Fe θ3 was substituted for Fe3θ4. Methane contact runs were performed as described above and results obtained are described in Table XII below. It is apparent from the data that the solid prepared from Fe θ3 does not perform as well as the solid prepared from Fβ3θ4.
TABLE XI I
Temp. GHSV % Selectivity To ;
Run* (°C) (hr’1) % Conv. ≤3±- CO co2 Coke 1 600 860 0.8 13.2 0 38.7 48.1
2 600 860 0.5 11.6 0 62.1 26.4
3 700 860 2.9 27.7 0 65.1 7.2
4 700 860 4.0 33.2 0 63.7 3.1
5 800 860 28.3 19.4 0 79.8 0.7
6 800 860 27.0 19.2 0 80.2 0.6
7 800 1200 20.3 25.2 0 73.2 1.6
8 800 1200 20.3 25.0 0 74.0 1.1
9 825 1200 26.4 21.0 0 78.2 0.8
10 825 1200 24.4 22.8 0 76.5 0.7
11 825 2400 13.5 28.4 0 69.2 1.9
12 825 2400 10.5 45.9 0 53.2 0.9
13 825 3600 7.1 38.5 0 60.1 1.4
14 825 3600 6.8 45.3 0 53.9 0.8
1.5 850 3600 9.5 29.9 0 69.9 0.2
16 850 3600 8.6 37.4 0 61.9 0.7 EXAMPLE 16
To demonstrate the promotional effect of materials such as sodium, methane contact runs were made using only Fe3θ4 as the contact solid. Results are described in Table XIII below. In the absence of promoter material, methane conversion is greater but the selectivity to higher hydrocarbons is lower.
TABLE XIII
Temp. GHSV % Selectivity To ••
Run# (°C) (hr»1) % Conv. Ci±_ CO co2 Coke
1 600 860 1.4 0 0 100 0
2 700 860 20.1 .4 » 0 98.3 1.3
3 700 860 18.0 .6 0 98.1 1.4
4 800 860 52.9 .3 0 98.8 1.0
5 800 860 25.3 5.4 0 92.4 1.7
6 825 860 36.6 4.1 0 95.4 0.5
7 825 1200 22.8 6.5 0 92.3 1.2
8 825 2400 13.9 6.1 0 92.7 1.2
9 825 3600 9.4 6.0 0 93.4 0.7 EXAMPLE 17
Three contact solids were prepared from Fe3θ4, each with a different promoter (Li, Na or K) . The iron to alkali metal ratio was 7 in each solid. Results obtained during methane contact runs over the Na- promoted solid are described in Table XIV. Results obtained during methane contact runs over the K- promoted solid are described in Table XV. Results obtained during methane contact runs over Li-promoted solids are described in Table XVI.
TABLE XIV
Temp. GHSV % Selectivity Tc >:
Run* (°C) (hr»1) % Conv. C2___ CO CO-2 Coke
1 600 860 0.8 41.3 0 22.6 36.1
2 700 860 0.3 0 0 100 TR
3 700 860 3.4 17.0 0 79.0 3.9
4 700 860 3.8 22.6 0 74.8 2.5
5 800 860 30.7 12.4 0 87.0 0.6
6 800 860 27.0 17.3 0 81.9 0.8
7 800 1200 20.4 22.7 0 76.4 0.9
8 800 1200 18.9 23.5 0 74.6 1.9
9 800 2400 12.7 28.6 0 70.6 0.9
10 800 2400 12.2 28.7 0 70.6 0.7
11 825 2400 17.5 23.3 0 76.4 0.3
12 825 2400 13.9 28.3 0 71.0 0.7
13 835 3600 10.0 29.0 0 69.7 1.3
14 825 3600 9.5 28.6 0 70.9 0.5
TABLE XV
Temp. GHSV % Selectivity To •
Run* CO (hr*1) % Conv. -Qi±- CO ∞~ Coke
1 600 860 11.1 0.5 0 94.7 4.8
2 700 860 12.8 1.0 0 95.0 4.0
3 700 860 36.1 0.3 0 98.6 1.1
4 800 860 46.3 0.3 0 98.1 1.6
5 800 860 45.5 0.4 0 97.8 1.8
6 800 4800 7.7 2.6 0 96.6 0.8
TABLE XVI
Temp. GHSV % Selectivity To •
Run* CO (hr-1) % Conv. £2±- CO co2 Coke
1 600 860 2.1 0 0 100 0
2 700 860 17.6 0.5 0 48.5 0.4
3 700 860 27.3 0.2 0 99.1 0.6
4 800 860 66.1 0.2 0 99.4 0.5
5 800 860 54.7 0.5 0 98.5 0.9
6 700 860 15.7 0.7 0 47.5 1.8
7 700 1200 15.5 0.5 0 98.8 0.7
700 4800 5.1 0.7 0 98.1 1.2
Claims (57)
WHAT IS CLAIMED IS:
1. A method for converting methane to higher hydrocarbon products which comprises contacting a gas comprising methane and a reducible oxide of at least one metal selected from the group consisting of Pr, Tb and Ru at a temperature within the range of about 700 to 900°C.
2. The method of claim 1 wherein methane is contacted with a reducible oxide of Pr.
3. The method of claim 1 wherein methane is contacted with a reducible oxide of Tb.
4. The method of claim 1 wherein the gas com¬ prising methane contains from about 40 to about 100 volume percent methane.
5. The method of claim 1 wherein the gas com¬ prising methane contains from about 80 to about 100 volume percent methane.
6. The method of claim ,1 wherein the gas com¬ prising methane contains from about 90 to about 100 volume percent methane.
7. The method of claim 1 wherein the gas com¬ prising methane is natural gas.
8. The method of claim 1 wherein the gas com¬ prising methane is processed natural gas.
9. A method for synthesizing hydrocarbons from a methane source which comprises:
(a) contacting at a temperature within the range of about 700 to 900°C a gas comprising methane and a solid com¬ prising at least one reducible oxide of at least one metal selected from the group consisting of Pr, Tb and Ru, said contacting producing C + hydrocarbons, coproduct water and solids comprising a reduced metal oxide, and said contacting being carried out in the substantial absence of catalytically effective Ni, Rh, Pd, Ag, Os, Ir, Pt, Au and compounds thereof;
(b) recovering C2+ hydrocarbons;
(c) at least periodically contacting the solids comprising reduced metal oxide with an oxygen-containing gas to pro¬ duce a solid comprising a reducible metal oxide; and
(d) contacting a gas comprising methane with the solids produced in step (c) as recited in step (a).
10. The method of claim 9 wherein the temper¬ ature of step (c) is within the range of about 300 to 1200°C.
11. The method of claim 9 wherein methane is contacted with a solid comprising a reducible oxide of Pr.
12. The method of claim 9 wherein methane is contacted with a solid comprising a reducible oxide of Tb.
13. A method for converting methane to higher hydrocarbon products which comprises contacting at a temperature within the range of about 500 to 1000°C a gas comprising methane and a solid comprising:
(a) at least one reducible oxide of at least one metal selected from the group consisting of Pr, Tb, Ce, Fe and Ru, and (b) at least one member of the group consisting of alkali metals, alkaline earth metals, and compounds thereof.
14. The method of claim 13 wherein the solid comprises a reducible oxide of Pr.
15. The method of claim 13 wherein the solid comprises a reducible oxide of Tb.
16. The method of claim 13 wherein the solid comprises a reducible oxide of Ce.
17. The method of claim 13 wherein the solid comprises a reducible oxide of Fe.
18. The method of claim 13 wherein the solid comprises a reducible oxide of Ru.
19. The method of claim 14 wherein the atomic ratio of Pr to alkali/alkaline earth metal in said solid is within the range of about 1-15:1.
20. The method of claim 15 wherein the atomic ratio of Tb to alkali/alkaline earth metal in said solid is within the range of about 1-15:1.
21. The method of claim 16 wherein the atomic ratio of Ce to alkali/alkaline earth metal in said solid is within the range of about 1-15:1.
22. The method of claim 17 wherein the atomic ratio of Fe to alkali/alkaline earth metal in said solid is within the range of about 2-10:1.
23. The method of claim 18 wherein the atomic ratio of Ru to alkali/alkaline earth metal in said solid is within the range of about 2-10:1.
24. The method of claim 13 wherein the solid is contacted with a gas comprising methane at a temper¬ ature within the range of about 700 to 900°C.
25. The method of claim 13 wherein the gas comprising methane contains from about 40 to about 100 volume percent methane.
26. The method of claim 13 wherein the gas comprising methane contains from about 80 to about 100 volume percent methane.
27. The method of claim 13 wherein the gas comprising methane contains from about 90 to about 100 volume percent methane.
28. The method of claim 13 wherein the gas comprising methane is natural gas.
29. The method of claim 13 wherein the gas comprising methane is processed natural gas.
30. The method of claim 13 wherein component (b) of said solid is selected from the group consisting of alkali metals and compounds thereof.
31. The method of claim 30 wherein the alkali metal is selected from the group consisting of Li, Na, K, Rb, Cs, and compounds thereof.
32. The method of claim 30 wherein the alkali metal is selected from the group consisting of sodium, sodium compounds and mixtures thereof.
33. The method of claim 30 wherein the alkali metal is selected from the group consisting of potassium, potassium compounds and mixtures thereof.
34. The method of claim 30 wherein the alkali metal is selected from the group consisting of lithium, lithium compounds and mixtures thereof.
35. The method of claim 13 wherein the said reducible oxide and the alkali/alkaline earth metal are associated with a support material.
36. The method of claim 35 wherein said reduc¬ ible oxide is provided as a support for at least one of the other components ,of said solid.
37. The method of claim 13 wherein the said solid is described by the empirical formula:
Aa Bb Cc Pd 0e wherein A is selected from the group consisting of Pr, Tb, Ce, Fe, Ru and mixtures thereof; B is selected from the group consisting of alkali metals, alkaline earth metals and mixtures thereof; C is selected from the group consisting of Mn, Sn, In, Ge, Pb, Sb, Bi and mixtures thereof; a, b, c, d, and e indicate the atomic ratio of each component; and when a is 10, b is within the range of about 0.5-10, c is within the range of about 0-10, d is within the range of about 0-10, and e has a value which is determined by the valences and proportions of the other elements present.
38. The method of claim 37 wherein the com¬ ponents are associated with a support metal.
39. The method of claim 38 wherein at least one oxide of at least one metal selected from the group consisting of Pr, Tb, Ce, Fe and Ru is provided as a support for the other components of said solid.
40. The method of claim 39 wherein the sup¬ port comprises a reducible oxide of Pr.
41. The method of claim 39 wherein the sup¬ port comprises a reducible oxide of Tb.
42. The method of claim 39 wherein the sup¬ port comprises a reducible oxide of Ce.
43. The method of claim 39 wherein the sup¬ port comprises a reducible oxide of Fe.
44. The method of claim 39 wherein the sup¬ port comprises a reducible oxide of Ru.
45. The method of claim 39 wherein C is Mn.
46. The method of claim 39 wherein B is Na.
47. The method of claim 39 wherein B is K.
48. The method of claim 39 wherein B is Li.
49. A method for synthesizing hydrocarbons from a methane source which comprises:
(a) contacting at a temperature within the range of about 500 to 1000°C a gas comprising methane and a solid comprising (1) at least one reducible oxide of at least one metal selected from the group consisting of Pr, Tb, Ce, Fe and Ru; and (2) at least one member of the group consisting of alkali metals, alkaline earth metals, and compounds thereof, said contact¬ ing producing C + hydrocarbons, co-product water and solids compris¬ ing a reduced metal oxide; (b) recovering C2+ hydrocarbons;
(c) at least periodically contacting the solids comprising reduced metal oxide with an oxygen-containing gas to produce a solid comprising a redu- cible metal oxide; and (d) contacting a gas comprising methane with the solids produced in step (c) as recited in step (a).
50. The method of claim 49 wherein the said solid of step (a) comprises an alkali metal or compound thereof.
51. The method of claim 49 wherein the solid of step (a) comprises an alkali metal or compound thereof on a support consisting essentially of a redu¬ cible oxide of Pr.
52. The method of claim 49 wherein the solid of step (a) comprises an alkali metal or compound thereof on a support consisting essentially of a redu¬ cible oxide of Tb.
53. The method of claim 49 wherein the solid of step (a) comprises an alkali metal or compound thereof on a support consisting essentially of a redu¬ cible oxide of Fe.
54. The method of claim 49 wherein the temper¬ ature of step (c) is within the range of about 300 to 1200°C.
55. A method for converting methane to higher hydrocarbon products which comprises contacting at a temperature within the range of about 500 to 1000°C a gas comprising methane and a solid comprising a redu- cibile oxide of Pr and at least one member of the group consisting of alkali metals and compounds thereof.
56. The method of claim 55 wherein the alkali metal component of said solid is selected from the group consisting of sodium, sodium compounds, and mixtures thereof.
57. The method of claim 55 wherein the alkali metal component of said solid is selected from the group consisting of lithium, lithium compounds, and mixtures thereof.
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1985-04-11
Methane conversion
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1984-04-16
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(en)
1984-04-16
1984-04-16
Methane conversion
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US600669
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US600917
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US06/600,665
US4499323A
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1984-04-16
1984-04-16
Methane conversion
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1984-04-16
Methane conversion
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1984-10-31
Methane conversion
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1984-10-31
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1984-10-31
Methane conversion
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1984-10-31
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1984-11-05
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1984-11-05
Methane conversion
US668299
1984-11-05
US06/668,299
US4603091A
(en)
1983-11-05
1984-11-05
Recording medium for perpendicular magnetization
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Methane conversion to higher hydrocarbons
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Inst Francais Du Petrole
PROCESS FOR THE CONVERSION OF METHANE INTO HIGHER HYDROCARBONS
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1987-10-17
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British Petroleum Co Plc
Chemical process
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1993-06-15
Phillips Petroleum Co
COMPOSITION AND PROCESSES FOR THE OXIDATIVE CONVERSION OF ORGANIC COMPOUNDS USING THE SAME.
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1990-01-10
1991-01-01
Union Carbide Chemicals And Plastics Company Inc.
Double perovskite catalysts for oxidative coupling
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工業技術院長
Hydrocarbon production method
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2018-08-16
Sabic Global Technologies, B.V.
A process for catalytic oxidative dehydrogenation of ethane to ethylene in the presence of chlorine intermediates
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1916-01-24
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Ордена Трудового Красного Знамени Институт Катализа Со Ан Ссср
Method of producing highest paraffinic c9-c12 hydrocarbons
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1978-05-08
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Exxon Research & Engineering Co.
Process for the conversion of relatively low molecular weight hydrocarbons, to higher molecular weight hydrocarbons, catalyst-reagents for such use in such process, and the regeneration thereof
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Exxon Research & Engineering Co.
Catalysts for the conversion of relatively low molecular weight hydrocarbons to higher molecular weight hydrocarbons and the regeneration of the catalysts
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1982-08-30
1984-04-17
Atlantic Richfield Company
Methane conversion
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(en)
*
1982-08-30
1984-04-17
Atlantic Richfield Company
Methane conversion
1985
1985-04-04
CA
CA000478486A
patent/CA1250316A/en
not_active
Expired
1985-04-11
JP
JP60501782A
patent/JPH068254B2/en
not_active
Expired – Lifetime
1985-04-11
GB
GB08529906A
patent/GB2167766B/en
not_active
Expired
1985-04-11
WO
PCT/US1985/000650
patent/WO1985004866A1/en
active
IP Right Grant
1985-04-11
BR
BR8506605A
patent/BR8506605A/en
not_active
IP Right Cessation
1985-04-11
DE
DE8585902267T
patent/DE3575292D1/en
not_active
Expired – Fee Related
1985-04-11
EP
EP85902267A
patent/EP0179131B1/en
not_active
Expired – Lifetime
1985-04-11
AU
AU42301/85A
patent/AU580303B2/en
not_active
Ceased
1985-12-13
NO
NO85855020A
patent/NO169887C/en
unknown
1985-12-16
DK
DK582885A
patent/DK165503C/en
not_active
IP Right Cessation
1987
1987-08-26
GB
GB08720106A
patent/GB2192894B/en
not_active
Expired
1988
1988-06-06
AU
AU17433/88A
patent/AU595713B2/en
not_active
Ceased
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Assignee
Title
AU581892B2
(en)
*
1984-04-16
1989-03-09
Atlantic Richfield Company
Methane conversion to higher hydrocarbons
Also Published As
Publication number
Publication date
JPH068254B2
(en)
1994-02-02
EP0179131B1
(en)
1990-01-10
CA1250316A
(en)
1989-02-21
GB8529906D0
(en)
1986-01-15
NO855020L
(en)
1986-02-14
NO169887C
(en)
1992-08-19
DK582885A
(en)
1985-12-16
AU1743388A
(en)
1988-09-01
DK165503B
(en)
1992-12-07
BR8506605A
(en)
1986-04-15
DE3575292D1
(en)
1990-02-15
WO1985004866A1
(en)
1985-11-07
GB8720106D0
(en)
1987-09-30
AU580303B2
(en)
1989-01-12
GB2167766B
(en)
1988-11-16
GB2192894B
(en)
1988-11-16
NO169887B
(en)
1992-05-11
GB2167766A
(en)
1986-06-04
AU595713B2
(en)
1990-04-05
GB2192894A
(en)
1988-01-27
EP0179131A4
(en)
1986-09-15
DK165503C
(en)
1993-04-19
DK582885D0
(en)
1985-12-16
JPS61501850A
(en)
1986-08-28
EP0179131A1
(en)
1986-04-30
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