US2859258A - Process for the production of ethylene - Google Patents
Process for the production of ethylene Download PDFInfo
- Publication number
- US2859258A US2859258A US461294A US46129454A US2859258A US 2859258 A US2859258 A US 2859258A US 461294 A US461294 A US 461294A US 46129454 A US46129454 A US 46129454A US 2859258 A US2859258 A US 2859258A
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- US
- United States
- Prior art keywords
- ethylene
- gas
- methane
- recycle
- mixture
- 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.)
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims description 27
- 239000005977 Ethylene Substances 0.000 title claims description 27
- 238000000034 method Methods 0.000 title claims description 20
- 238000004519 manufacturing process Methods 0.000 title description 5
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 38
- 239000000203 mixture Substances 0.000 claims description 12
- 238000005336 cracking Methods 0.000 claims description 10
- 238000004227 thermal cracking Methods 0.000 claims description 6
- 229930195734 saturated hydrocarbon Natural products 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 229930195735 unsaturated hydrocarbon Natural products 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 15
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 7
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 6
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 6
- 150000002736 metal compounds Chemical class 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- SNAAJJQQZSMGQD-UHFFFAOYSA-N aluminum magnesium Chemical compound [Mg].[Al] SNAAJJQQZSMGQD-UHFFFAOYSA-N 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910052804 chromium Inorganic materials 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
Definitions
- Application Serial No. 432,016 is concerned primarily with the production of ethylene by the thermal cracking of hydrocarbons wherein the by-products of the process are recycled for additional treatment to produce additional quantities of ethylene.
- the process set forth in this prior patent application cannot be used with a raw material such as methane. The reason for this is that the thermal conversion of the methane molecule requires substantially higher temperatures than those necessary for the cracking of the hydrocarbons because of the far greater thermal stability of methane molecules.
- methane may be used as the raw material if, prior to the recycle in which the main formation of ethylene takes place, there is provided a recycle operating at substantially higher temperatures than the first mentioned recycle.
- the methane is partly converted to ethylene and partly to saturated and unsaturated hydrocarbons having two or more carbon atoms in the molecule. These hydrocarbons can then be cracked at lower temperatures.
- the unconverted methane is then returned to the primary recycle together with a fresh amount of methane "ice which takes the place of that consumed during the first reaction. That portion of the cracked gas which remains after the separation of the ethylene is introduced into the secondary recycle, at the lower temperatures, where conversion to ethylene takes place in accordance with the process as described in the above-mentioned copending application Serial No. 432,016.
- the saving of energy is efiected by the use of the heating gases, used in the primary recycle, to heat the apparatus used in the secondary recycle, the temperature of these gases having been lowered during their use for heating the primary recycle. It has been found that a temperature range of between about 800 C. and 1100 C. is
- the recovery of the ethylene from the primary cracking step preferably takes place by means of adsorption methods. This is necessary in this case because the yield is relatively small and results in a so-called lean gas. It has been determined that adsorption methods are the only economically feasible methods for recovering the ethylene.
- the primary cracking step provides the highest yields if the cracking is conducted in the presence of suitable catalysts.
- catalysts preferably take the form of oxygen-containing metal compounds wherein the metals are of the second, third and fourth groups of the periodic system.
- the catalysts which may be used are aluminum oxide, magnesium aluminum silicate, and magnesium aluminum molybdate.
- these oxygen-containing metal compounds are preferably activated by the addition of small amounts of heavy metals.
- the heavy metals which may be used are lead, copper, chromium, iron, nickel, cobalt, arsenic, antimony, gold, silver and mercury.
- the primary recycle may be conducted either at atmcspheric, sub-atmospheric or super-atmospheric pressures. More particularly, the primary recycle is preferably conducted at pressures ranging between one and five kg./cm. It is preferable, however, to employ a certain amount of superatmospheric pressure, that is,
- the secondary recycle may be conducted under the same pressure conditions as the primary recycle; however, in the secondary recycle the application of a super-atmospheric pressure and the employment of catalysts are not necessary.
- the apparatus for conducting the secondary recycle therefore, may be relatively simple and inexpensive.
- Example Five cubic meters of methane per hour were introduced at a pressure of two kg./cm. into a reaction chamber which was maintained at 1050 C.
- the reaction chamber was filled with a catalyst consisting of magnesium aluminum silicate.
- the catalyst was activated by a small amount of chromium comprising about 3%.
- the exit gas had the following composition in percent by volume:
- a process for obtaining ethylene in high yields comprising the steps of thermally cracking a gas which is at least predominantly methane at a relatively high temperature ranging between about 800 C. and 1100 C. to partly convert said gas to a mixture of ethylene and saturated and unsaturated hydrocarbons, separating said mixture from the unconverted portions of the gas, removing the ethylene from the mixture, and subjecting the remainder ofsaid mixture to a second thermal-- cracking step at a relatively lower temperature ranging between about 600 C. and 800 C. to convertthe said remainder of said mixture at least partially to ethylene.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
United States Patent 2,859,258 PROCESS FOR THE PRODUCTION OF E'I'HYLENE Kurt Fischer, Altotling, Upper Bavaria, and Gunter Rummert, Burghausen (Salzach), Germany, assignors to Farbwerke Hoechst- Aktiengesellschaft vormals Meister Lucius & Bruning, Frankfurt am Main, Germany, a corporation of Germany No Drawing. Application October 8, 1954 Serial No. 461,294
Claims priority, application Germany October 10, 1953 6 Claims. (Cl. 260-683) This invention relates to the production of ethylene and particularly relates to the production of ethylene by the thermal cracking of methane or natural gases which predominately contain methane. This application is a continuation in part of co-pending U. S. patent application Serial No. 432,016, filed May 24, 1954.
Application Serial No. 432,016 is concerned primarily with the production of ethylene by the thermal cracking of hydrocarbons wherein the by-products of the process are recycled for additional treatment to produce additional quantities of ethylene. The process set forth in this prior patent application, however, cannot be used with a raw material such as methane. The reason for this is that the thermal conversion of the methane molecule requires substantially higher temperatures than those necessary for the cracking of the hydrocarbons because of the far greater thermal stability of methane molecules.
It has heretofore been known to convert methane to acetylene at extremely high temperatures, as, for example, by the use of an electric are. This conversion into acetylene involves a reaction which is unduly expensive and therefore commercially infeasible. The expense is incurred, in the first place, by the high amounts of energy which are consumed during the endothermic formation of the acetylene; in the second place this acetylene formation requires complex and expensive apparatus. Furthermore, since the energy must be removed in the form of hydrogenation heat which is developed during the hydrogenation of acetylene to ethylene; this exothermic reaction, following the previous endothermic reaction, involves a total waste of energy since the energy level at the completion of the process is substantially similar to the energy level at the beginning of the process, even though a great deal of energy has been used during the process. It is, therefore, highly desirable to effect the cracking between such temperature ranges that there is very little formation of acetylene but a substantially large formation of ethylene.
According to the process embodied in this invention, methane may be used as the raw material if, prior to the recycle in which the main formation of ethylene takes place, there is provided a recycle operating at substantially higher temperatures than the first mentioned recycle.
In the recycle at the higher temperatures the methane is partly converted to ethylene and partly to saturated and unsaturated hydrocarbons having two or more carbon atoms in the molecule. These hydrocarbons can then be cracked at lower temperatures.
The raw, cracked gas which is formed in the primary recycle; that is, the recycle operating at the higher temperatures, is separated from the unconverted portion of the methane and the ethylene is then removed therefrom. The unconverted methane is then returned to the primary recycle together with a fresh amount of methane "ice which takes the place of that consumed during the first reaction. That portion of the cracked gas which remains after the separation of the ethylene is introduced into the secondary recycle, at the lower temperatures, where conversion to ethylene takes place in accordance with the process as described in the above-mentioned copending application Serial No. 432,016.
The combination of a primary recycle operating at a relatively high temperature and a secondary recycle operating at a relatively lower temperature not only serves to simplify the entire process but also acts to save energy.
The saving of energy is efiected by the use of the heating gases, used in the primary recycle, to heat the apparatus used in the secondary recycle, the temperature of these gases having been lowered during their use for heating the primary recycle. It has been found that a temperature range of between about 800 C. and 1100 C. is
required for the primary recycle, while a temperature range of between about 600 C. and 800 C. is required for the secondary recycle. Optimum results have been achieved when the temperature of the primary recycle is between about 950 C. and 1050 C. and when the temperature of the secondary recycle is between about 700 C. and 750 C.
The recovery of the ethylene from the primary cracking step preferably takes place by means of adsorption methods. This is necessary in this case because the yield is relatively small and results in a so-called lean gas. It has been determined that adsorption methods are the only economically feasible methods for recovering the ethylene.
It has been found that the primary cracking step provides the highest yields if the cracking is conducted in the presence of suitable catalysts. Such catalysts preferably take the form of oxygen-containing metal compounds wherein the metals are of the second, third and fourth groups of the periodic system. Among the catalysts which may be used are aluminum oxide, magnesium aluminum silicate, and magnesium aluminum molybdate. In order to obtain optimum results, these oxygen-containing metal compounds are preferably activated by the addition of small amounts of heavy metals. Among the heavy metals which may be used are lead, copper, chromium, iron, nickel, cobalt, arsenic, antimony, gold, silver and mercury.
' The primary recycle may be conducted either at atmcspheric, sub-atmospheric or super-atmospheric pressures. More particularly, the primary recycle is preferably conducted at pressures ranging between one and five kg./cm. It is preferable, however, to employ a certain amount of superatmospheric pressure, that is,
pressures ranging between one and five kg./cm. in order to simplify the adsorption separation process due to the formation of high molecular reaction products.
The secondary recycle may be conducted under the same pressure conditions as the primary recycle; however, in the secondary recycle the application of a super-atmospheric pressure and the employment of catalysts are not necessary. The apparatus for conducting the secondary recycle, therefore, may be relatively simple and inexpensive.
Example Five cubic meters of methane per hour were introduced at a pressure of two kg./cm. into a reaction chamber which was maintained at 1050 C. The reaction chamber was filled with a catalyst consisting of magnesium aluminum silicate.
The catalyst was activated by a small amount of chromium comprising about 3%. The exit gas had the following composition in percent by volume:
Percent Propylene and butylene 0.2 Propane and butane 2.1 Ethane 1.6 Hydrogen 24.3 Ethylene 2.4 Methane 69.4
From this gas mixture the methane and the ethylene were removed by means of adsorption on active carbon, and the methane was returned to the reaction chamber together with 30.6%. of fresh methane. The entire remaining gas, after separation of the ethylene and methane, was again subjected to cracking in a coiled tube heated externally to 800 C. andyielded a cracked gas having the following composition:
Percent Propylene and butylene 25.0 Saturated hydrocarbons and hydrogen 54.3 Ethylene 20.7
Introduced, 13.33 kg. Obtained, 5.25 kg. Fresh rnethane=100% Ethylene=39.4%
As many apparently widely diflferent embodiments of this invention may be made without departing from the spirit and scope hereof, it is to be understood that the invention is not limited to the specific embodiments hereof, except as defined in the appended claims.
What is claimed in this invention is:
1. A process for obtaining ethylene in high yields comprising the steps of thermally cracking a gas which is at least predominantly methane at a relatively high temperature ranging between about 800 C. and 1100 C. to partly convert said gas to a mixture of ethylene and saturated and unsaturated hydrocarbons, separating said mixture from the unconverted portions of the gas, removing the ethylene from the mixture, and subjecting the remainder ofsaid mixture to a second thermal-- cracking step at a relatively lower temperature ranging between about 600 C. and 800 C. to convertthe said remainder of said mixture at least partially to ethylene.
2. The process of claim 1 wherein the unconverted portion of said gas is again subjected to the thermal cracking at the relatively high temperature.
3. The process of claim lswherein said relativelyhigh temperature comprises a temperature ranging between about 950 C. and 1050" C. and wherein said relatively lower temperature comprises a temperature ranging between 700 C. and '750" C.
4. The process of claim 1 wherein the thermal crack ing of the gas at the relatively high temperature takes place in the presence of a catalyst comprising an oxygen containing metal compound wherein the metal is selected from the group consisting of the metals of the second, third and fourth groups of the. PeriodicSystem.
5. The process of claim 4 wherein said oxygen-con taining metal compound is activated by the addition of 1 a relativelysmalliamount of a heavy metal.
6. The process of claim 1 wherein the heat for the second cracking .step is at least partially provided bythe cooled heating gas from the first cracking step.
References Cited in the; file of this patent UNITED STATES PATENTS 1,524,355 'Haynes et al. Jan. 27, 1925 1,677,363 Olivier July 17, 1928 2,014,724 Eastman Sept. 17, 1935 2,498,806 Hachmuth Feb. 28, 1950-.
2,597,346 Lefier May 20, 1952 FOREIGN PATENTS 749,916 France Aug. 1, 1933 OTHER REFERENCES Frolich et al.: Ind. and Engr. Chem., vol. 27 (1935), pp. 10 -9.
Claims (1)
1. A PROCESS FOR OBTAINING ETHYLENE IN HIGH YIELDS COMPRISING THE STEPS OF THERMALLY CRACKING A GAS WHICH IS AT LEAST PREDOMINANTLY METHANE AT A RELATIVELY HIGH TEMPERATURE RANGING BETWEEN ABOUT 800*C. AND 1100* C. TO PARTLY CONVERT SAID GAS TO A MIIXTURE OF ETHYLENE AND SATURATED AND UNSATURATED HYDROCARBONS, SEPARATING SAID MIXTURE FROM THE UNCONVERTED PROTIONS OF THE GAS, REMOVING THE ETHYLENE FROM THE MIXTURE, AND SUBJECTING THE REMAINDER OF SAID MIXTURE TO A SECOND THERMAL CRACKING STEP AT A RELATIVELY LOWER TEMPERATURE RANGING BETWEEN ABOUT 600*C. AND 800C. TO CONVERT THE SAID REMAINDER OF SAID MIXTURE AT LEAST PARTIALLY TO ETHYLENE.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE2859258X | 1953-10-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2859258A true US2859258A (en) | 1958-11-04 |
Family
ID=7999852
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US461294A Expired - Lifetime US2859258A (en) | 1953-10-10 | 1954-10-08 | Process for the production of ethylene |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2859258A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3268615A (en) * | 1961-12-28 | 1966-08-23 | Union Carbide Corp | High pressure cracking |
| US4205194A (en) * | 1978-05-08 | 1980-05-27 | 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 |
| US4567311A (en) * | 1983-10-31 | 1986-01-28 | Chevron Research Company | Conversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a silicon compound-containing catalyst |
| US4574038A (en) * | 1985-08-01 | 1986-03-04 | Alberta Oil Sands Technology And Research Authority | Microwave induced catalytic conversion of methane to ethylene and hydrogen |
| US4695668A (en) * | 1986-03-24 | 1987-09-22 | The Standard Oil Company | Molybdenum-tungsten-containing catalyst and methane conversion process using same |
| US4808563A (en) * | 1986-03-24 | 1989-02-28 | The Standard Oil Company | Molybdenum-tungsten-containing catalyst for methane conversion process |
| US4822944A (en) * | 1986-07-11 | 1989-04-18 | The Standard Oil Company | Energy efficient process for upgrading light hydrocarbons and novel oxidative coupling catalysts |
| US4929789A (en) * | 1988-01-15 | 1990-05-29 | The Standard Oil Company | Process for pyrolyzing or thermal cracking a gaseous or vaporized hydrocarbon feedstock using a novel gas-solids contacting device and an oxidation catalyst |
| US5012028A (en) * | 1986-07-11 | 1991-04-30 | The Standard Oil Company | Process for upgrading light hydrocarbons using oxidative coupling and pyrolysis |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1524355A (en) * | 1920-03-08 | 1925-01-27 | Carbide & Carbon Chem Corp | Process of making olefines |
| US1677363A (en) * | 1926-02-03 | 1928-07-17 | Le Petrole Synthetique Sa | Process of treating methane gas |
| FR749916A (en) * | 1932-02-26 | 1933-08-01 | Improvements in the conversion of methane to other hydrocarbons | |
| US2014724A (en) * | 1934-03-20 | 1935-09-17 | Texas Co | Manufacture of olefines |
| US2498806A (en) * | 1946-07-16 | 1950-02-28 | Phillips Petroleum Co | Production of ethylene |
| US2597346A (en) * | 1948-10-29 | 1952-05-20 | Universal Oil Prod Co | Method for effecting the conversion of organic reactant streams |
-
1954
- 1954-10-08 US US461294A patent/US2859258A/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1524355A (en) * | 1920-03-08 | 1925-01-27 | Carbide & Carbon Chem Corp | Process of making olefines |
| US1677363A (en) * | 1926-02-03 | 1928-07-17 | Le Petrole Synthetique Sa | Process of treating methane gas |
| FR749916A (en) * | 1932-02-26 | 1933-08-01 | Improvements in the conversion of methane to other hydrocarbons | |
| US2014724A (en) * | 1934-03-20 | 1935-09-17 | Texas Co | Manufacture of olefines |
| US2498806A (en) * | 1946-07-16 | 1950-02-28 | Phillips Petroleum Co | Production of ethylene |
| US2597346A (en) * | 1948-10-29 | 1952-05-20 | Universal Oil Prod Co | Method for effecting the conversion of organic reactant streams |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3268615A (en) * | 1961-12-28 | 1966-08-23 | Union Carbide Corp | High pressure cracking |
| US4205194A (en) * | 1978-05-08 | 1980-05-27 | 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 |
| US4567311A (en) * | 1983-10-31 | 1986-01-28 | Chevron Research Company | Conversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a silicon compound-containing catalyst |
| US4574038A (en) * | 1985-08-01 | 1986-03-04 | Alberta Oil Sands Technology And Research Authority | Microwave induced catalytic conversion of methane to ethylene and hydrogen |
| US4695668A (en) * | 1986-03-24 | 1987-09-22 | The Standard Oil Company | Molybdenum-tungsten-containing catalyst and methane conversion process using same |
| US4808563A (en) * | 1986-03-24 | 1989-02-28 | The Standard Oil Company | Molybdenum-tungsten-containing catalyst for methane conversion process |
| US4822944A (en) * | 1986-07-11 | 1989-04-18 | The Standard Oil Company | Energy efficient process for upgrading light hydrocarbons and novel oxidative coupling catalysts |
| US5012028A (en) * | 1986-07-11 | 1991-04-30 | The Standard Oil Company | Process for upgrading light hydrocarbons using oxidative coupling and pyrolysis |
| US4929789A (en) * | 1988-01-15 | 1990-05-29 | The Standard Oil Company | Process for pyrolyzing or thermal cracking a gaseous or vaporized hydrocarbon feedstock using a novel gas-solids contacting device and an oxidation catalyst |
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