AU2002258486A1 - Method for converting natural gas to liquid hydrocarbons - Google Patents
Method for converting natural gas to liquid hydrocarbonsInfo
- Publication number
- AU2002258486A1 AU2002258486A1 AU2002258486A AU2002258486A AU2002258486A1 AU 2002258486 A1 AU2002258486 A1 AU 2002258486A1 AU 2002258486 A AU2002258486 A AU 2002258486A AU 2002258486 A AU2002258486 A AU 2002258486A AU 2002258486 A1 AU2002258486 A1 AU 2002258486A1
- Authority
- AU
- Australia
- Prior art keywords
- natural gas
- hydrogen
- stream
- conveying
- reactor
- 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.)
- Granted
Links
Description
METHOD FOR CONVERTING NATURAL GAS TO LIQUID HYDROCARBONS
FIELD OF THE INVENTION
This invention pertains to conversion of natural gas to hydrocarbon liquids. More particularly, natural gas is converted to reactive hydrocarbons and the reactive hydrocarbons are reacted with additional natural gas to form hydrocarbon liquids.
BACKGROUND OF THE INVENTION
Natural gas often contains about 60-100 mole per cent methane, the balance being primarily heavier al anes. Alkanes of increasing carbon number are normally present in decreasing amounts. Carbon dioxide, nitrogen, and other gases may be present.
Conversion of natural gas into hydrocarbon liquids has been a technological goal for many years. The goal has become even more important in recent years as more natural gas has been found in remote locations, where gas pipelines may not be economically justified. A significant portion of the world reserves of natural gas occurs in such remote regions. While liquefied natural gas (LNG) and methanol projects have long attracted attention by making possible conversion of natural gas to a liquid, in recent years the advent of large scale projects based upon Fisher-Tropsch (F-T) technology have attracted more attention. A review of proposed and existing F-T projects along with a discussion of economics of the projects has recently been published (Oil and Gas J.. Sept. 21 and Sept 28, 1998). In this technology, natural gas is first converted to "syngas," which is a mixture of carbon monoxide and hydrogen, and the syngas is converted to liquid paraffinic and olefinic hydrocarbons of varying chain lengths. The F-T technology was developed for using coal as a feed stock, and only two plants now operate using natural gas as feedstock — in South Africa and in Malaysia. A study showed that for a plant producing 45,000 bbls/day (BPD) of liquids in a U.S. location in 1993, investment costs would have been about $38,000 per BPD production (Oil and Gas J„ Sept. 28, 1998, p. 99). Improved designs are said to lower investment cost to the range of $30,000 per BPD for a 20,000 BPD facility. Such a plant would use about 180 MMSCFD of natural gas, 10 million GPD
of raw water and 150 BPD of normal butane, and would produce excess steam, which could be used to produce 10 megawatts of electricity.
The conversion of natural gas to unsaturated hydrocarbons and hydrogen by subjecting the hydrocarbons in natural gas to high temperatures produced by electromagnetic radiation or electrical discharges has been extensively studied. U.S.
Patent 5,277,773 discloses a conversion process that subjects methane plus hydrocarbons to microwave radiation so as to produce an electric discharge in an electromagnetic field. U.S. Patent 5,131,993 discloses a method for cracking a hydrocarbon material in the presence of a microwave discharge plasma and a carrier gas, such as oxygen, hydrogen and nitrogen, and, generally, a catalyst. U.S. Patent
3,389,189 is an example of patents relating to production of acetylene by an electric arc.
Methane pyrolysis to acetylene and hydrogen by rapid heating in a reaction zone and subsequent rapid quenching has also been extensively investigated. Subatmospheric pressures and specific ranges of velocities of hydrocarbon gases through the reaction zone are disclosed in U.S. Patent 3,156,733. Heat is supplied by burning of hydrocarbons.
Although the prior art has disclosed a range of methods for forming acetylene or ethylene from natural gas, an energy-efficient process for converting natural gas to a liquid that can be transported efficiently from remote areas to market areas has not been available. What is needed is a process that does not require large capital and operating expenditures such as required by the prior art processes. Also, the process should be energy efficient.
DESCRIPTION OF THE FIGURES
Fig. 1 shows a process diagram for one embodiment of the process of this invention in which the natural gas is heated to reaction temperature by burning a portion of the natural gas in a furnace.
Fig. 2 shows a process diagram of another embodiment of the process of this invention in which the natural gas is heated to reaction temperature by electrical energy produced by hydrogen and acetylene is reacted to ethylene prior to liquefaction.
Fig. 3 shows a process diagram for one embodiment of the process of this invention in which the natural gas is heated to reaction temperature by burning of hydrogen in a furnace and acetylene is reacted to ethylene prior to liquefaction.
Fig. 4 shows a process diagram for one embodiment of the process of this invention in which the natural gas is heated to reaction temperature by burning some of the natural gas in a furnace and acetylene is reacted to ethylene prior to liquefaction.
Fig. 5 shows a process diagram for one embodiment of the process of this invention in which the natural gas is heated to reaction temperature by electrical energy produced by hydrogen and a portion of the natural gas.
Fig. 6 shows a process diagram for one embodiment of the process of this invention in which the natural gas is heated to reaction temperature by burning a portion of the natural gas in a furnace.
SUMMARY OF THE INVENTION
A process for conversion of natural gas to a hydrocarbon liquid for transport from remote locations is provided. In one embodiment, the natural gas is heated to a temperature at which a fraction of the natural gas is converted to hydrogen and a reactive hydrocarbon such as acetylene or ethylene. The stream is then quenched to stop any further reactions and then reacted in the presence of a catalyst to form the liquid to be transported, predominantly naphtha or gasoline. Hydrogen may be separated after quenching and before the catalytic reactor. Heat for raising the temperature of the natural gas stream is provided by burning of a portion of the natural gas feed stream. Hydrogen produced in the reaction is available for further refining or in generation of electricity by oxidation in a fuel cell or turbine. In another embodiment, heat produced from the fuel cell is used to generate additional electricity. In another embodiment, the acetylene portion of the reactive hydrocarbon is reacted with hydrogen to form ethylene prior to reacting to form the liquid to be transported. In another embodiment, hydrogen produced in the reaction is burned to raise the temperature of the natural gas stream and the acetylene portion of the reactive hydrocarbon is reacted with hydrogen to form ethylene prior to reacting to form the liquid to be transported. In still another embodiment, hydrogen produced in
the process is used to generate electrical power, the electrical power used to heat the natural gas stream, and the acetylene portion of the reactive hydrocarbon stream is reacted with hydrogen to form ethylene prior to reacting to form the liquid to be transported.
DESCRIPTION OF PREFERRED EMBODIMENTS
United States Patent 6,130,260 and application 09/574,510 filed May 19, 2000, are incorporated by reference herein. Fig. 1 shows one embodiment of the steps for producing a liquid product such as naphtha or gasoline from natural gas in the present invention. In this embodiment, a portion of the natural gas feed is diverted from the feed stream to the burners in the combustion furnace 10, where the diverted natural gas is burned, preferably with oxygen-enriched, air such that NOx production from combustion furnace 10 is decreased. As shown in Fig. 1, inlet gas stream 12 is separated into inlet gas feed stream 14 and inlet gas burn stream 16. Inlet gas feed stream 14 is conveyed to the reaction chamber of combustion furnace 10. Inlet gas burn stream 16 is conveyed to the combustion chamber of combustion furnace 10. Inlet gas feed stream 14 is preferably pre-heated in pre-heaters (not shown) before it is heated to the preferred reaction temperature by heat exchange with the hydrocarbon-combustion gas. The flame temperature of inlet gas burn stream 16 should be adequate to reach a desired reaction temperature preferably between 1000 and 1800 K without oxygen enrichment of air, but sufficient enrichment can be easily achieved with membrane units, which are well known in the art, and this will avoid the necessity of NOx control in emissions from combustion furnace 10. Addition of water to the combustion zone of combustion furnace 10 may be used to lower flame temperature to a desired range, preferably about 300 to 500 K above the preferred reaction temperature of natural gas passing through tubes of combustion furnace 10. Residence time of gas in the tubes of combustion furnace 10 should be long enough to convert inlet gas feed stream 14 to acetylene, ethylene, and other reactive compounds and not so long as to allow significant further reactions before the quenching step, which is discussed below. It is preferred to maintain the residence time to under 100 milliseconds, most preferably under 80 milliseconds to minimize coke formation.
Bringing the natural gas feed stream, for simplicity here considered methane only, to high temperature causes the following reaction to occur:
2CH4→C2H6 + H2→C2H4 + H2→C2H2+H2→2C+H2. The desired products from this series of reactions are ethylene and acetylene. Suppression of the last reaction or last two reactions may be required to achieve the desired products. This may be accomplished by such methods as adjusting the reaction temperature and pressure, and/or quenching after a desired residence time. The desired hydrocarbon products of the reactions are designated herein as "reactive products." It is preferred to maintain the pressure of the natural gas within the reaction chamber of combustion furnace 10 to between 1 and 20 bars to achieve the reactive products. The reactive products resulting from the reaction in combustion furnace 10 leave combustion furnace 10 through furnace outlet stream 18.
In an alternative embodiment, shown in Fig. 3, natural gas is heated in high-temperature reactor 110 by means of electrical power that is produced by use of hydrogen in electrical power generator 50. Inlet gas stream 12 becomes inlet gas feed stream 14 and is directed to the reaction chamber of high temperature reactor 110. The electrical power may be produced by, for example, fuel cells powered by hydrogen or by a combined cycle gas or hydrogen gas turbine driving electrical generators. Water is also produced. Investment costs for fuel cell production of electrical power are high at present, but may be reduced by improved technology in the future. Combined cycle gas turbines are well known and at present produce electrical power at significantly lower capital costs per kW (approximately $ 385 per kW) than the capital costs of fuel cells (estimated at $3,000 per kW). In either case, the electrical power is used to increase the temperature of the natural gas stream entering high-temperature reactor 110. The high temperature may be produced from the electrical power by an electric arc or silent discharge between electrodes, using methods well known in the art. Alternatively, the high temperature may be produced by resistance heating of electrodes. In another alternative embodiment, a plasma may be formed in the natural gas stream using a plasma reactor, such as the "Plasmatron" sold by Praxair, Thermal Spray Systems, N670 Communication Drive, Appleton, WI 54915. Plasma temperatures are higher than the preferred temperature range for the
gas reactions of this invention, so a more energy-efficient process may be achieved without bringing the natural gas to plasma temperature. The higher temperature produces extra components in the product stream that require a great deal more energy and would make the process not as energy efficient. In another alternative embodiment, shown in Fig. 4, hydrogen separated from the reactive products, as described below, is directed to hydrogen combustion furnace 210, where the hydrogen is burned, preferably with oxygen-enriched air such that NOx production from hydrogen combustion furnace 210 is decreased. As further shown in Fig. 4, inlet gas stream 12 becomes inlet gas feed stream 14 and is directed to reaction chamber of hydrogen combustion furnace 210. Flame temperature of hydrogen is adequate to reach a desired reaction temperature without oxygen enrichment of air, but sufficient enrichment can be easily achieved with membrane units, which are well known in the art, and this will avoid the necessity of NOx control in emissions from hydrogen combustion furnace 210. Addition of water to the combustion zone of hydrogen combustion furnace 210 may be used to lower flame temperature to a desired range, preferably about 300 to 500 K above the preferred reaction temperature of natural gas passing through tubes in hydrogen combustion furnace 210.
The materials of construction of combustion furnace 10, high temperature reactor 110, and hydrogen combustion furnace 210 are not standard. Specialty materials such as tungsten, tantalum or ceramics may be used. The temperature rise should occur in a short period of time. The furnaces may be of the double-radiant-section box-type as pictured in Fig. 19.5, p. 681, of D. Q. Kern, Process Heat Transfer, McGraw-Hill Book Co., New York (1950). The furnace may use tantalum (Ta) or silicon/carbide tubing. Steam pressures will be low, about 6 psig. Kinetic calculations indicate a suitable time for heating the natural gas to the reaction temperature is in the range from about 1 millisecond to about 100 milliseconds. To stop the reactions and prevent the reverse reactions or further reactions to form carbon and other hydrocarbon compounds, rapid cooling or "quenching" is essential, typically in 10 to 100 milliseconds. As shown in Fig. 1, furnace outlet stream 18 is directed to quench system 15. Quenched furnace outlet stream 18 exits quench system 15 through quench outlet stream 19. The quench in
quench system 15 may be achieved by spraying water, oil, or liquid product into furnace outlet stream 18; "dumped" into water, natural gas feed, or liquid products; or expanded in a kinetic energy quench such as a Joule-Thompson expander, choke nozzle or turbo expander. This quench occurs in a similar fashion in high-temperature reactor 110 in Fig. 3, and hydrogen combustion furnace 210 in Fig. 4.
Furnace outlet stream 18 is typically essentially one part alkene/ alkyne mixture to three parts methane. In particular, "lean" natural gas, i.e., gas with 95% or greater methane reacts to mostly acetylene as a reactive product. Where the natural gas is lean, it is desirable to operate the furnace in the upper end of the desired range to achieve a higher content of alkynes, in particular acetylene. In contrast, in a richer stream, it may be desirable to operate at a temperature lower in the desirable range to achieve a higher content of alkenes, primarily ethylene.
As shown in Fig. 1 while the gas in furnace outlet stream 18 is still at a temperature above 500 K, but after quenching in quench system 15, a portion of the hydrogen in quench outlet stream 19 may be separated from the reactive hydrocarbon in hydrogen separator 20. In an alternative embodiment, all of the hydrogen is directed to liquefaction reactor 30 without the separator step of hydrogen separator 20. This separation step may be performed by any of a variety of processes, including membrane or pressure swing processes, described for example in: A. Malek and S. Farooq, "Hydrogen Purification from Refinery Fuel Gas by Pressure Swing Adsorption", AIChE J. 44, 1985 (1998). The hydrogen is removed from hydrogen gas separator 20 through hydrogen separator hydrogen stream 22. Hydrogen separator hydrogen stream 22 is composed primarily of hydrogen, but may also contain trace amounts of the other components in furnace outlet stream 18. After removal of the a portion of the hydrogen in hydrogen gas separator 20, the remaining portion of quench outlet stream 19 is removed from hydrogen gas separator 20 through hydrogen separator outlet stream 26.
As shown in Fig. 1, a portion of hydrogen separator hydrogen stream 26 may be recycled and combined with inlet gas stream 12 through recycle stream 49. Hydrogen separator hydrogen stream 22 may be used in any number of processes. In one embodiment of the present invention, as shown in Fig. 1, hydrogen separated in hydrogen separator 20 may be used to generate water and electricity by combining it
with oxygen or by burning it with oxygen in a turbine in electrical generator 50. For fuel cells, any fuel cell design that uses a hydrogen stream and an oxygen stream may be used, for example polymer electrolyte, alkaline, phosphoric acid, molten carbonate, and solid oxide fuel cells. Heat generated by the fuel cell or turbine may be used to boil the water exiting the fuel cell, forming steam. This steam may be used to generate electricity, for instance in a steam turbine. This electricity may be sold, or as shown in Fig. 3, used to power high-temperature reactor 110. The heat generated by the fuel cell or turbine may also be used in heat exchangers to raise the temperatures of streams in the process, such as in the preheaters. In an alternate embodiment, shown in Fig. 2, hydrogen separator outlet stream 22 may be produced as a product. In still another alternative embodiment, shown in Fig. 4, hydrogen separator recycle stream 22 is burned directly in hydrogen combustion furnace 210. As shown in Fig. 5, a portion of inlet gas stream 12 may be separated from inlet gas stream 12 and routed through supplemental gas stream 16 to electrical generator 50. In this way, additional electrical power may be generated. As shown in Fig. 6, electrical generator 50 may be eliminated entirely so as to maximize hydrogen production.
As further shown in Fig. 1, hydrogen separator outlet stream 26, which includes the reactive products, is conveyed from hydrogen separator 20 to liquefaction reactor 30. Liquefaction reactor 30 is a catalytic reactor that may include recycle and is designed to convert the reactive products to hydrocarbon liquids such as naphtha or gasoline. The principal liquefaction reactions in liquefaction reactor 30 are as follows: For acetylene,
7.CH4+C2H 2 = naphtha/gasoline + H , and for ethylene, m H.4. + C2 H4 = naphtha gasoline + H .
This reaction must be catalyzed to suppress the reaction of acetylene to benzene and to enhance the conversion to hydrocarbon liquids such as naphtha or gasoline, which is preferred for the method of this invention. Liquefaction reactor 30 shown in Fig. 1, should produce predominantly naphtha or gasoline, but may also produce some aromatic and cyclic compounds. The
vapor pressure of naphtha or gasoline is about 1 bar at 40°C. Thus, it can be transported via truck or ship. Heavier hydrocarbons such as crude oil may be added to the produced liquid to reduce vapor pressure of a liquid to be transported.
The reaction to produce naphtha or gasoline is thermodynamically favorable. The equilibrium thermodynamics for the reactions of acetylene and ethylene with methane are more favorable at low to moderate temperatures (300 - 1000 K). It is well known in the chemical industry that alkanes of ethane and higher can be converted to higher molecular weight hydrocarbons using acid catalysts, such as the zeolites H-ZSM-5 or Ultrastable Y (USY). Applicants have discovered that the amount of Brόenstead Acid sites on the catalyst should be maximized in comparison to the Lewis acid sites. This may be accomplished by increasing the silica to alumina ratio in the catalyst (Y Zeolites typically have Si/Al ratios of 2-8 whereas ZSM-5 typically has an Si/Al ratio of 15-30,000). Other alkylation catalysts are known in the chemical industry. In the present invention, the reaction of acetylene and ethylene to benzene is suppressed and the reaction of these reactive hydrocarbons with methane is enhanced. Steam may be introduced into the reactor to achieve the desired conversion results. The preferred reactor conditions are temperatures in the range from about 300 to about 1000 K and pressure in the range from about 2 to about 30 bar. The products of the liquefaction reaction leave liquefaction reactor 30 through catalytic reactor outlet stream 32.
As shown in Fig. 1, catalytic reactor outlet stream 32 may be sent to product separator 40. The primary purpose of product separator 40 is to separate the desired hydrocarbon liquid products from any lighter, primarily gaseous components that may remain after liquefaction. It should be understood that a cooling step may be considered a part of product separator 40 of Fig. 1. Cooling of the stream after the reaction may be necessary, depending upon the method of final separation and the optimum conditions for that separation. If the product separator 40 is simply a gas-liquid or flash separation, cooling may be necessary. Distillation, adsorption or absorption separation processes, including pressure-swing adsorption and membrane separation, may be used for the final separation. Any known hydrocarbon liquid-gas separation processes may be used for product separator 40, which is considered a part
of the catalytic reactor. The liquid hydrocarbons separated in product separator 40 are sent to storage or transport facilities through product separation outlet stream 42. The primarily gaseous components separated in product separator 40, which may consist primarily of hydrogen may be sent through light gas recycle stream 44 to electrical generator 50 through recycle purge stream 46, combined with reactor outlet stream 18 through light gas to reactor outlet stream 48, or a portion of recycle purge stream 46 may be sent to each. Alternatively, as shown in Fig. 4, light gas recycle stream 44 may be conveyed to hydrogen combustion furnace 210 for combustion rather than to a fuel cell or turbine for conversion to electricity. Note that processing steps may be added after liquefaction and before product separator 40 or, alternatively, after product separator 40, to convert the hydrocarbon liquids such as naphtha or gasoline or to heavier compounds such as diesel.
In still another embodiment, as shown in Figs. 2, 3, and 6, quench outlet stream 19 may be directed to hydro genation reactor 310, where alkynes, primarily acetylene, may be converted into the preferred intermediate product, ethylene and other olefins, according to general reaction (wherein the alkyne is acetylene):
C2H2+H2→ C2H4
Traditional catalysts for conversion of alkynes to alkenes are used to convert acetylene to ethylene. These include nickel-boride, metallic palladium, and bimetallic catalysts such as palladium with a group lb metal (copper, silver or gold). Some natural gas feed streams contained trace amounts of sulfur compounds that may act as a poison for the hydrogenation catalyst. In addition, incoming sulfur compounds may react in the hydrogen combustion furnace to form catalyst poisons, such as COS and H2S. It is preferable to remove or reduce the concentration of these catalyst poisons by means well known by those in the art, such as activated carbon or amine.
The products of the reaction that occurs in hydrogenation reactor 310 are conveyed to hydrogen separator 20 through hydrogenation outlet stream 312.
Because the conversion from acetylene to ethylene is not complete, hydrogenation outlet stream 312 contains both acetylene and ethylene, as well as hydrogen and some higher-molecular-weight alkynes and alkenes. In alternative embodiments, after leaving high temperature reactor 110 in Fig. 3 or hydrogen combustion furnace 210 in
Fig. 4, furnace outlet stream 18 may be directed to hydrogen separator 20, bypassing hydrogenation reactor 310.
In another alternate embodiment also shown in Figs. 2, 3, and 4, light gas recycle stream 44 may be routed to secondary hydrogen separator 320. Like hydrogen separator 20, this separation step may be performed by any of a variety of processes, including membrane or pressure swing processes, described for example in: A. Malek and S. Farooq, "Hydrogen Purification from Refinery Fuel Gas by Pressure Swing Adsorption", AIChE J. 44, 1985 (1998). As shown in Fig. 2, hydrogen removed during separation in secondary hydrogen separator 320 is removed tlirough secondary hydrogen separator hydrogen stream 324. A portion of secondary hydrogen separator hydrogen stream 324 may be routed to electrical generator 50 through recycle purge stream 46. The remaining components of light gas recycle stream 44 exit secondary hydrogen separator 320 through secondary hydrogen separator outlet stream 322. A portion of secondary hydrogen separator outlet stream may be sent to electrical generator 50 through secondary hydrogen separator purge stream 328. The remainder of hydrogen separator outlet stream 322 may be routed to the inlet of catalytic reactor 30 through hydrogen separator recycle stream 326. In another embodiment as shown in Fig. 3, secondary hydrogen separator hydrogen stream 324 is combined with hydrogen separator hydrogen stream 22 and sent to electrical generator 50. Secondary hydrogen separator outlet stream 322 is sent to the inlet of catalytic reactor 30. In another embodiment, shown in Fig. 4, secondary hydrogen separator hydrogen stream 324 is combined with hydrogen separator hydrogen stream 22 and sent to hydrogen combustion furnace 210. In Fig. 6, still another embodiment is shown where secondary hydrogen separator hydrogen stream is combined with hydrogen separator hydrogen stream 22 to maximize production of hydrogen. Secondary hydrogen separator 320 may be used in lieu, instead of in addition to, hydrogen separator 20. Catalytic reactor outlet stream 32 may also be directed to product separation 40 without the use of secondary hydrogen separator 320, as shown in Fig. 1. Although the present invention has been described with reference to specific details, it is not intended that such details should be regarded as limitations
upon the scope of the invention, except as and to the extent that they are included in the accompanying claims.
Claims (54)
1. A method for converting natural gas to a hydrocarbon liquid and water, comprising the steps of: a) providing a stream of natural gas; b) separating the natural gas stream into a feed stream and a burn stream; c) conveying the feed stream and burn stream to a furnace wherein the burn stream is burned and wherein the feed stream is heated to fonn hydrogen and reactive products comprising an acetylene portion; d) quenching the reactive products and hydrogen; e) separating the reactive products and hydrogen; f) conveying the reactive products to a catalytic liquefaction reactor and providing natural gas and a catalyst in the reactor such that the reactive products and natural gas react to produce hydrogen and the hydrocarbon liquid; and g) conveying the hydrocarbon liquid storage or transport.
2. The method of claim 1 wherein the pressure of the natural gas stream is between about 1 bar and about 20 bars.
3. The method of claim 1 wherein in step b) the feed stream is heated to a temperature in the range from about 1000 K to about 1800 K.
4. The method of claim 3 wherein the feed stream is maintained at a temperature of at least 1000 K for less than 100 milliseconds.
5. The method of claim 4 wherein the feed stream is maintained at a temperature of at least 1000 K for less than 80 milliseconds.
6. The method of claim 1 wherein the catalyst in the catalytic liquefaction reactor is an acid catalyst.
7. The method of claim 1 wherein the temperature in the catalytic liquefaction reactor is in the range from about 300 K to about 1000 K.
8. The method of claim 1 wherein the burn stream is burned using oxygen-enriched air.
9. The method of claim 1 further comprising after step e) h) conveying the hydrogen to a fuel cell or turbine; i) providing oxygen to the fuel cell or turbine; j) reacting the hydrogen with the oxygen in the fuel cell or burning the hydrogen with the oxygen in the turbine to produce electricity.
10. The method of claim 9 wherein the fuel cell or turbine produce heat.
11. The method of claim 10 further comprising after step j) : k) heating water produced in the fuel cell or turbine with heat produced in the fuel cell to form steam and;
1) generating electricity from the steam.
12. The method of claim 1 wherein the step of quenching is performed by a Joule-Thompson expander, nozzle or turbo expander.
13. The method of claim 1 further comprising prior to step e) but after step d): conveying the reactive products and hydrogen to a hydrogenation reactor and reacting the acetylene portion of the reactive products with the hydrogen to fonn ethylene.
14. The method of claim 1 further comprising after step f): separating the hydrogen from the hydrocarbon liquid; providing oxygen to the a cell or turbine; and reacting the hydrogen with the oxygen in the fuel cell or burning the hydrogen with the oxygen in the turbine to produce electricity.
15. The method of claim 1, wherein the hydrocarbon liquid comprises naphtha or gasoline.
16. The method of claim 1 further comprising after step b) but before step c): segregating of portion of the feed stream to form an electrical generation stream; conveying the electrical generation stream to a fuel cell or turbine; providing oxygen to their fuel cell or turbine; reacting the electrical generation stream with the oxygen in the fuel cell or burning the electrical generation stream with the oxygen in the turbine to form electricity
17. A method for converting natural gas to a hydrocarbon liquid and water, comprising the steps of: a) providing a stream of natural gas; b) conveying the natural gas to a reactor having means for heating the natural gas using electrical power, wherein the natural gas is heated to form hydrogen and reactive products comprising an acetylene portion; c) quenching the reactive products and hydrogen; d) conveying the reactive products and hydrogen to a hydrogenation reactor; e) reacting the acetylene portion of the reactive products with hydrogen to form ethylene; f) conveying the reactive products to a catalytic liquefaction reactor and providing natural gas and a catalyst in the liquefaction reactor such that the reactive products and natural gas react to produce hydrogen and the hydrocarbon liquid; g) conveying hydrogen to a means for generating electrical power and producing water; h) conveying the electrical power from the means for generating electrical power to the reactor having means for heating using electrical power; i) conveying the hydrocarbon liquid and the water to storage or transport.
18. The method of claim 17 wherein in step b) the means for heating the natural gas using electrical power is an electric arc, resistance heating a plasma reactor, a fuel cell, or a combined cycle gas turbine drive electrical generator.
19. The method of claim 17 wherein the selected pressure of the natural gas stream is between about 1 bar and about 12 bars.
20. The method of claim 17 wherein in step b) the natural gas is heated to a temperature in the range from about 1000 K to about 1800 K.
21. The method of claim 17 wherein the feed stream is maintained at a temperature of at lest 1000 K for less than 100 milliseconds.
22. The method of claim 21 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 100 milliseconds.
23. The method of claim 22 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 80 milliseconds.
24. The method of claim 17 wherein the catalyst in the catalytic liquefaction reactor is an acid catalyst.
25. The method of claim 17 wherein the temperature in the catalytic liquefaction reactor is in the range from about 300 K to about 1000 K.
26. The method of claim 17 wherein the step of quenching is performed by a Joule- Thompson expander, nozzle or turbo expander.
27. The method of claim 17 further comprising after step a) but before step b) segregating a portion of the natural gas stream to form an electrical generation stream; conveying the electrical generation stream to a fuel cell or turbine; conveying the hydrogen to a means for generating electrical power and producing water.
28. A method for converting natural gas to a hydrocarbon liquid and water, comprising the steps of: a) providing a stream of natural gas; b) conveying the natural gas through a furnace wherein hydrogen is burned and wherein the natural gas is heated to form hydrogen and reactive products, comprising an acetylene portion; c) quenching the reactive products and hydrogen; d) conveying the reactive products and hydrogen to a hydrogenation reactor; e) reacting the acetylene portion of the reactive products with hydrogen to form ethylene; f) conveying the reactive products and hydrogen to a catalytic liquefaction reactor and providing natural gas and a catalyst in the reactor such that the reactive products and natural gas react to produce hydrogen and the hydrocarbon liquid; g) conveying hydrogen from the catalytic liquefaction reactor to the hydrogen furnace for burning so as to heat the natural gas and produce water; and h) conveying the hydrocarbon liquid and the water to storage or transport.
29. The method of claim 28 wherein the selected pressure of the natural gas stream is between about 1 bar and about 12 bars.
30. The method of claim 28 wherein in step b) the natural gas is heated to a temperature in the range from about 1000 K to about 1800 K.
31. The method of claim 30 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 100 milliseconds.
32. The method of claim 31 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 80 milliseconds.
33. The method of claim 28 wherein the catalyst in the catalytic liquefaction reactor is an acid catalyst.
34. The method of claim 28 wherein the temperature in the catalytic liquefaction reactor is in the range from about 300 K to about 1000 K.
35. The method of claim 28 wherein the hydrogen is burned using oxygen-enriched air.
36. The method of claim 28 wherein the step of quenching is performed by a Joule-Thompson expander, nozzle or turbo expander.
37. A method for converting natural gas to naphtha or gasoline and water, comprising the steps of: a) providing a stream of natural gas; b) conveying the natural gas to reactor having means for heating the natural gas using electrical power, wherein the natural gas is heated to form hydrogen and reactive products comprising an acetylene portion; c) quenching the reactive products and hydrogen; d) conveying the reactive products and hydrogen to a hydrogenation reactor; e) reacting the acetylene portion of the reactive products with hydrogen to form ethylene; f) conveying the reactive product stream to a catalytic liquefaction reactor and providing natural gas and a catalyst in the liquefaction reactor such that the reactive products and natural gas react to produce hydrogen and naphtha or gasoline; g) conveying the hydrogen to a means for generating electrical power and producing water; h) conveying the electrical power to the reactor having means for heating using electrical power; and i) conveying the naphtha or gasoline and the water to storage or transport.
38. The method of claim 36 wherein the selected pressure of the natural gas stream is between about 1 bar and about 12 bars.
39. The method of claim 36 wherein in step b) the natural gas is heated to a temperature in the range from about 1000 K to about 1800 K.
40. The method of claim 39 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 100 milliseconds.
41. The method of claim 40 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 80 milliseconds.
42. The method of claim 37 wherein the catalyst in the catalytic liquefaction reactor is an acid catalyst.
43. The method of claim 37 wherein the temperature in the catalytic liquefaction reactor is in the range from about 300 K to 1000 K.
44. The method of claim 37 wherein the hydrogen is burned using oxygen enriched air.
45. The method of claim 37 wherein the step of quenching is performed by a Joule-Thompson expander, nozzle or turbo expander.
46. A method for converting natural gas to naphtha or gasoline and water, comprising the steps of: a) providing a stream of natural gas; b) conveying the natural gas through a furnace wherein hydrogen is burned and wherein the natural gas is heated to form hydrogen and reactive products, comprising an acetylene portion; c) quenching the reactive products and hydrogen; d) conveying the reactive products and hydrogen to a hydrogenation reactor; e) reacting the acetylene portion of the reactive products with hydrogen to fonn ethylene; f) conveying the reactive products and hydrogen to a catalytic liquefaction reactor and providing natural gas and a catalyst in the reactor such that the reactive products and natural gas react to produce hydrogen and naphtha or gasoline; g) conveying hydrogen from the catalytic liquefaction reactor to the hydrogen furnace for burning so as to heat the natural gas and produce water; and h) conveying the naphtha or gasoline and the water to storage or transport.
47. The method of claim 46 wherein the selected pressure of the natural gas stream is between about 1 bar and about 12 bars.
48. The method of claim 46 wherein in step b) the natural gas is heated to a temperature in the range from about 1000 K to about 1800 K.
49. The method of claim 48 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 100 milliseconds.
50. The method of claim 49 wherein the natural gas stream is maintained at a temperature of at least 1000 K for less than 80 milliseconds.
51. The method of claim 46 wherein the catalyst in the catalytic liquefaction reactor is an acid catalyst.
52. The method of claim 46 wherein the temperature in the catalytic liquefaction reactor is in the range from about 300 K to 1000 K.
53. The method of claim 46 wherein the hydrogen is burned using oxygen enriched air.
54. The method of claim 46 wherein the step of quenching is performed by a Joule-Thompson expander, nozzle or turbo expander.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/803,122 US6602920B2 (en) | 1998-11-25 | 2001-03-09 | Method for converting natural gas to liquid hydrocarbons |
US09/803,122 | 2001-03-09 | ||
PCT/US2002/007183 WO2002072741A2 (en) | 2001-03-09 | 2002-03-07 | Method for converting natural gas to liquid hydrocarbons |
Publications (3)
Publication Number | Publication Date |
---|---|
AU2002258486A1 true AU2002258486A1 (en) | 2003-03-20 |
AU2002258486B2 AU2002258486B2 (en) | 2007-11-01 |
AU2002258486B9 AU2002258486B9 (en) | 2008-03-20 |
Family
ID=25185634
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
AU2002258486A Ceased AU2002258486B9 (en) | 2001-03-09 | 2002-03-07 | Method for converting natural gas to liquid hydrocarbons |
Country Status (5)
Country | Link |
---|---|
US (2) | US6602920B2 (en) |
EP (1) | EP1392802A2 (en) |
AU (1) | AU2002258486B9 (en) |
NZ (1) | NZ528381A (en) |
WO (1) | WO2002072741A2 (en) |
Families Citing this family (96)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6602920B2 (en) * | 1998-11-25 | 2003-08-05 | The Texas A&M University System | Method for converting natural gas to liquid hydrocarbons |
US20040157940A1 (en) * | 2003-02-07 | 2004-08-12 | Dalton Robert C. | Method of transport energy |
CA2427722C (en) | 2003-04-29 | 2007-11-13 | Ebrahim Bagherzadeh | Preparation of catalyst and use for high yield conversion of methane to ethylene |
US7045670B2 (en) * | 2003-09-03 | 2006-05-16 | Synfuels International, Inc. | Process for liquid phase hydrogenation |
US7919431B2 (en) | 2003-09-03 | 2011-04-05 | Synfuels International, Inc. | Catalyst formulation for hydrogenation |
US7208647B2 (en) * | 2003-09-23 | 2007-04-24 | Synfuels International, Inc. | Process for the conversion of natural gas to reactive gaseous products comprising ethylene |
US7183451B2 (en) * | 2003-09-23 | 2007-02-27 | Synfuels International, Inc. | Process for the conversion of natural gas to hydrocarbon liquids |
US6951111B2 (en) * | 2003-10-06 | 2005-10-04 | Chentek, Llc | Combusting hydrocarbons excluding nitrogen using mixed conductor and metal hydride compressor |
US7141709B2 (en) * | 2003-11-13 | 2006-11-28 | Chevron Phillips Chemical Company Lp | Methods and systems of producing monoolefins by the extraction-hydrogenation of highly unsaturated hydrocarbons |
WO2006078827A2 (en) * | 2005-01-21 | 2006-07-27 | Cabot Corporation | Controlling flame temperature in a flame spray reaction process |
US8013197B2 (en) * | 2005-02-18 | 2011-09-06 | Synfuels International, Inc. | Absorption and conversion of acetylenic compounds |
CN102728352A (en) | 2005-07-27 | 2012-10-17 | 切夫里昂菲利普化学有限责任公司 | Selective hydrogenation catalyst and methods of making and using same |
WO2007028153A2 (en) * | 2005-09-02 | 2007-03-08 | Hrd Corp. | Catalyst and method for converting low molecular weight paraffinic hydrocarbons into alkenes and organic compounds with carbon numbers of 2 or more |
KR100632571B1 (en) * | 2005-10-07 | 2006-10-09 | 에스케이 주식회사 | Process for the preparation of light olefins in catalytic cracking from hydrocarbon feedstock |
US7846401B2 (en) * | 2005-12-23 | 2010-12-07 | Exxonmobil Research And Engineering Company | Controlled combustion for regenerative reactors |
KR100651418B1 (en) | 2006-03-17 | 2006-11-30 | 에스케이 주식회사 | Catalytic cracking process using fast fluidization for the production of light olefins from hydrocarbon feedstock |
CN101535217B (en) * | 2006-04-13 | 2014-08-27 | 陶氏环球技术有限责任公司 | Mixed alcohol synthesis with enhanced carbon value use |
US8075869B2 (en) * | 2007-01-24 | 2011-12-13 | Eden Energy Ltd. | Method and system for producing a hydrogen enriched fuel using microwave assisted methane decomposition on catalyst |
US8092778B2 (en) * | 2007-01-24 | 2012-01-10 | Eden Energy Ltd. | Method for producing a hydrogen enriched fuel and carbon nanotubes using microwave assisted methane decomposition on catalyst |
US8021448B2 (en) * | 2007-01-25 | 2011-09-20 | Eden Energy Ltd. | Method and system for producing a hydrogen enriched fuel using microwave assisted methane plasma decomposition on catalyst |
US8608942B2 (en) * | 2007-03-15 | 2013-12-17 | Kellogg Brown & Root Llc | Systems and methods for residue upgrading |
WO2008134484A2 (en) * | 2007-04-25 | 2008-11-06 | Hrd Corp. | Catalyst and method for converting natural gas to higher carbon compounds |
US8153850B2 (en) | 2007-05-11 | 2012-04-10 | The Texas A&M University System | Integrated biofuel production system |
EP2022772A1 (en) * | 2007-08-09 | 2009-02-11 | Bp Oil International Limited | Process for converting methane into liquid alkane mixtures |
US20090205254A1 (en) * | 2008-02-14 | 2009-08-20 | Zhonghua John Zhu | Method And System For Converting A Methane Gas To A Liquid Fuel |
US7883618B2 (en) * | 2008-02-28 | 2011-02-08 | Kellogg Brown & Root Llc | Recycle of olefinic naphthas by removing aromatics |
US8863530B2 (en) | 2008-10-30 | 2014-10-21 | Power Generation Technologies Development Fund L.P. | Toroidal boundary layer gas turbine |
US9052116B2 (en) | 2008-10-30 | 2015-06-09 | Power Generation Technologies Development Fund, L.P. | Toroidal heat exchanger |
WO2011008389A2 (en) * | 2009-07-17 | 2011-01-20 | Exxonmobil Chemical Patents Inc. | Process and apparatus for converting high boiling point resid to light unsaturated hydrocarbons |
US8445739B2 (en) * | 2009-08-27 | 2013-05-21 | Synfuels International, Inc. | Process for the conversion of natural gas to acetylene and liquid fuels with externally derived hydrogen |
WO2011058619A1 (en) * | 2009-11-10 | 2011-05-19 | 進藤 隆彦 | Method for production of linear saturated hydrocarbon in direct process for gtl |
US9500362B2 (en) | 2010-01-21 | 2016-11-22 | Powerdyne, Inc. | Generating steam from carbonaceous material |
DE102010047543A1 (en) * | 2010-10-05 | 2012-04-05 | Linde Ag | Separating hydrogen |
US8674155B2 (en) | 2010-12-22 | 2014-03-18 | Kellogg Brown & Root, Llc | Systems and methods for processing hydrocarbons |
US9708232B2 (en) * | 2011-01-19 | 2017-07-18 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins |
US9676681B2 (en) * | 2011-01-19 | 2017-06-13 | Exxonmobil Chemical Patents Inc. | Method and apparatus for managing hydrogen content through the conversion of hydrocarbons into olefins |
WO2012099680A2 (en) | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins |
CN103347840B (en) * | 2011-01-19 | 2015-11-25 | 埃克森美孚化学专利公司 | The method for transformation of hydrocarbon |
US9505680B2 (en) * | 2011-01-19 | 2016-11-29 | Exxonmobil Chemical Patents Inc. | Method and apparatus for managing the conversion of hydrocarbons into olefins |
US9815751B2 (en) | 2011-01-19 | 2017-11-14 | Exxonmobil Chemical Patents Inc. | Hydrocarbon and oxygenate conversion by high severity pyrolysis to make acetylene and ethylene |
CA2822284A1 (en) * | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins |
WO2012099678A1 (en) | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patents Inc. | Method and apparatus for managing for hydrogen content through the conversion of hydrocarbons into olefins |
US9346728B2 (en) | 2011-01-19 | 2016-05-24 | Exxonmobil Chemical Patents Inc. | Hydrocarbon conversion process |
WO2012099671A1 (en) | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patent Inc. | Method and apparatus for converting hydrocarbons into olefins using hydroprocessing and thermal pyrolysis |
WO2012099677A2 (en) | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins |
US9868680B2 (en) | 2011-01-19 | 2018-01-16 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins |
WO2012099676A2 (en) | 2011-01-19 | 2012-07-26 | Exxonmobil Chemical Patents Inc. | Process and apparatus for converting hydrocarbons |
US9677014B2 (en) | 2011-01-19 | 2017-06-13 | Exxonmobil Chemical Patents Inc. | Process and apparatus for converting hydrocarbons |
US9708231B2 (en) | 2011-01-19 | 2017-07-18 | Exxonmobil Chemical Patents Inc. | Method and apparatus for converting hydrocarbons into olefins using hydroprocessing and thermal pyrolysis |
WO2012135515A2 (en) | 2011-03-29 | 2012-10-04 | Fuelina, Inc. | Hybrid fuel and method of making the same |
EP2710235B1 (en) | 2011-05-16 | 2015-07-15 | Powerdyne, Inc. | Steam generation system |
SG194978A1 (en) | 2011-07-07 | 2013-12-30 | Exxonmobil Chem Patents Inc | Hydrocarbon conversion process |
US9187699B2 (en) | 2011-11-08 | 2015-11-17 | Exxonmobil Chemical Patents Inc. | Hydrocarbon pyrolysis process |
CA3092028C (en) | 2012-01-13 | 2022-08-30 | Lummus Technology Llc | Process for separating hydrocarbon compounds |
MX350697B (en) | 2012-03-09 | 2017-09-14 | Evoenergy Llc | Plasma chemical device for conversion of hydrocarbon gases to liquid fuel. |
US9670113B2 (en) * | 2012-07-09 | 2017-06-06 | Siluria Technologies, Inc. | Natural gas processing and systems |
WO2014039695A1 (en) | 2012-09-05 | 2014-03-13 | Powerdyne, Inc. | Methods for generating hydrogen gas using plasma sources |
KR101581263B1 (en) | 2012-09-05 | 2015-12-31 | 파워다인, 인코포레이티드 | System for generating fuel materials using fischer-tropsch catalysts and plasma sources |
WO2014039711A1 (en) | 2012-09-05 | 2014-03-13 | Powerdyne, Inc. | Fuel generation using high-voltage electric fields methods |
BR112015004834A2 (en) | 2012-09-05 | 2017-07-04 | Powerdyne Inc | method to produce fuel |
US9410452B2 (en) | 2012-09-05 | 2016-08-09 | Powerdyne, Inc. | Fuel generation using high-voltage electric fields methods |
BR112015004836A2 (en) | 2012-09-05 | 2017-07-04 | Powerdyne Inc | method for sequestering toxin particles |
US9273570B2 (en) | 2012-09-05 | 2016-03-01 | Powerdyne, Inc. | Methods for power generation from H2O, CO2, O2 and a carbon feed stock |
DE102012023832A1 (en) * | 2012-12-06 | 2014-06-12 | Evonik Industries Ag | Integrated system and method for the flexible use of electricity |
DE102012023833A1 (en) * | 2012-12-06 | 2014-06-12 | Evonik Industries Ag | Integrated system and method for the flexible use of electricity |
US9598328B2 (en) | 2012-12-07 | 2017-03-21 | Siluria Technologies, Inc. | Integrated processes and systems for conversion of methane to multiple higher hydrocarbon products |
DE102012113051A1 (en) | 2012-12-21 | 2014-06-26 | Evonik Industries Ag | A method for providing control power for stabilizing an AC power network, comprising an energy storage |
EP2953893A4 (en) | 2013-03-12 | 2017-01-25 | Powerdyne, Inc. | Systems and methods for producing fuel from parallel processed syngas |
US10047020B2 (en) | 2013-11-27 | 2018-08-14 | Siluria Technologies, Inc. | Reactors and systems for oxidative coupling of methane |
US10337110B2 (en) | 2013-12-04 | 2019-07-02 | Covestro Deutschland Ag | Device and method for the flexible use of electricity |
CN110655437B (en) | 2014-01-08 | 2022-09-09 | 鲁玛斯技术有限责任公司 | System and method for ethylene to liquids |
CA3225180A1 (en) * | 2014-01-09 | 2015-07-16 | Lummus Technology Llc | Oxidative coupling of methane implementations for olefin production |
US10100200B2 (en) | 2014-01-30 | 2018-10-16 | Monolith Materials, Inc. | Use of feedstock in carbon black plasma process |
US10138378B2 (en) | 2014-01-30 | 2018-11-27 | Monolith Materials, Inc. | Plasma gas throat assembly and method |
US11939477B2 (en) | 2014-01-30 | 2024-03-26 | Monolith Materials, Inc. | High temperature heat integration method of making carbon black |
US20150211378A1 (en) * | 2014-01-30 | 2015-07-30 | Boxer Industries, Inc. | Integration of plasma and hydrogen process with combined cycle power plant, simple cycle power plant and steam reformers |
US10370539B2 (en) * | 2014-01-30 | 2019-08-06 | Monolith Materials, Inc. | System for high temperature chemical processing |
FI3100597T3 (en) | 2014-01-31 | 2023-09-07 | Monolith Mat Inc | Plasma torch with graphite electrodes |
WO2016089994A1 (en) | 2014-12-03 | 2016-06-09 | Drexel University | Direct incorporation of natural gas into hydrocarbon liquid fuels |
EP3253904B1 (en) | 2015-02-03 | 2020-07-01 | Monolith Materials, Inc. | Regenerative cooling method and apparatus |
US10793490B2 (en) | 2015-03-17 | 2020-10-06 | Lummus Technology Llc | Oxidative coupling of methane methods and systems |
US20160289143A1 (en) | 2015-04-01 | 2016-10-06 | Siluria Technologies, Inc. | Advanced oxidative coupling of methane |
CA3032246C (en) | 2015-07-29 | 2023-12-12 | Monolith Materials, Inc. | Dc plasma torch electrical power design method and apparatus |
JP6974307B2 (en) | 2015-09-14 | 2021-12-01 | モノリス マテリアルズ インコーポレイテッド | Carbon black derived from natural gas |
EP3442934A4 (en) | 2016-04-13 | 2019-12-11 | Siluria Technologies, Inc. | Oxidative coupling of methane for olefin production |
CA3060482C (en) | 2016-04-29 | 2023-04-11 | Monolith Materials, Inc. | Secondary heat addition to particle production process and apparatus |
MX2018013161A (en) | 2016-04-29 | 2019-06-24 | Monolith Mat Inc | Torch stinger method and apparatus. |
US9809519B1 (en) | 2016-05-26 | 2017-11-07 | Exxonmobil Chemical Patents Inc. | Oxygenate synthesis and homologation |
CA3055830A1 (en) | 2017-03-08 | 2018-09-13 | Monolith Materials, Inc. | Systems and methods of making carbon particles with thermal transfer gas |
CN115637064A (en) | 2017-04-20 | 2023-01-24 | 巨石材料公司 | Particle system and method |
CA3116989C (en) | 2017-10-24 | 2024-04-02 | Monolith Materials, Inc. | Particle systems and methods |
US11634323B2 (en) | 2018-08-23 | 2023-04-25 | Transform Materials Llc | Systems and methods for processing gases |
US11633710B2 (en) | 2018-08-23 | 2023-04-25 | Transform Materials Llc | Systems and methods for processing gases |
CN109361000B (en) * | 2018-09-04 | 2020-11-06 | 新地能源工程技术有限公司 | Integrated coal gasification solid oxide fuel cell-steam turbine combined power generation system and process |
US11955674B1 (en) | 2023-03-07 | 2024-04-09 | Chevron Phillips Chemical Company Lp | Use of a fuel cell to decarbonize a hydrocarbon cracking system |
US11958745B1 (en) | 2023-03-07 | 2024-04-16 | Chevron Phillips Chemical Company Lp | Use of methane pyrolysis to decarbonize a hydrocarbon cracking system |
Family Cites Families (100)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
USRE19500E (en) | 1935-03-12 | Natural gas conversion process | ||
USRE19794E (en) | 1935-12-24 | Preparation of acetylene | ||
US19500A (en) * | 1858-03-02 | Sunken vessels | ||
US1023783A (en) | 1911-10-05 | 1912-04-16 | United Gas Improvement Co | Process of treating natural gas. |
US1229886A (en) | 1916-02-21 | 1917-06-12 | Louis Bond Cherry | Synthetic production of hydrocarbon compounds. |
US1800586A (en) | 1925-05-01 | 1931-04-14 | Malcolm P Youker | Natural-gas-conversion process |
US1773611A (en) | 1926-03-15 | 1930-08-19 | Banck Martin | Preparation of acetylene and hydrogen |
US1917627A (en) | 1927-01-11 | 1933-07-11 | Robert G Wulff | Process of producing acetylene gas |
US1880307A (en) | 1927-12-27 | 1932-10-04 | Robert G Wulff | Method of producing acetylene by compression |
US1904426A (en) | 1929-01-12 | 1933-04-18 | Ig Farbenindustrie Ag | Production of acetylene and hydrogen |
US2037056A (en) | 1931-05-09 | 1936-04-14 | Wulff Process Company | Process of producing acetylene gas |
US1966779A (en) | 1931-05-11 | 1934-07-17 | Wulff Process Company | Method of producing acetylene by compression of natural gas |
US2028014A (en) | 1933-05-08 | 1936-01-14 | Reinecke Henry | Method of treating hydrocarbon fuels |
US2160170A (en) | 1935-03-18 | 1939-05-30 | Ruhrchemie Ag | Heat treatment of hydrocarbon gases to dehydrogenate the same |
US2080931A (en) | 1935-12-20 | 1937-05-18 | Michael L Benedum | Process of and apparatus for the treatment of hydrocarbon fluids |
US2328864A (en) | 1939-06-21 | 1943-09-07 | Pure Oil Co | Method for thermal polymerization of hydrocarbons |
US2558861A (en) | 1945-04-30 | 1951-07-03 | Universal Oil Prod Co | Apparatus for production of acetylene and other hydrocarbons |
US2645673A (en) | 1945-12-08 | 1953-07-14 | Eastman Kodak Co | Process of producing acetylene |
US2475282A (en) | 1946-01-21 | 1949-07-05 | Tennessee Eastman Corp | Process of producing acetylene black |
US2714126A (en) | 1946-07-19 | 1955-07-26 | Kellogg M W Co | Method of effecting conversion of gaseous hydrocarbons |
US2550089A (en) | 1946-08-31 | 1951-04-24 | Socony Vacuum Oil Co Inc | Electrochemical conversion of hydrocarbons |
US2675294A (en) | 1949-08-16 | 1954-04-13 | Kellogg M W Co | Method of effecting chemical conversions |
US2751424A (en) | 1950-09-22 | 1956-06-19 | Koppers Co Inc | Process of producing acetylene by pyrolytic reaction from a suitable hydrocarbon |
US2768223A (en) | 1952-06-19 | 1956-10-23 | Gen Aniline & Film Corp | Manufacture of acetylene |
US2986505A (en) | 1958-05-12 | 1961-05-30 | Sun Oil Co | Production of acetylene |
US3156733A (en) | 1960-12-02 | 1964-11-10 | Happel John | Selective pyrolysis of methane to acetylene and hydrogen |
NL284848A (en) | 1961-10-31 | |||
US3168592A (en) | 1962-07-19 | 1965-02-02 | Du Pont | Manufacture of acetylene by two stage pyrolysis under reduced pressure with the first stage pyrolysis conducted in a rotating arc |
US3254960A (en) | 1963-11-26 | 1966-06-07 | Sun Oil Co | Wave reactor |
US3320146A (en) | 1964-04-17 | 1967-05-16 | Du Pont | Process of making acetylene in an electric arc |
DE1468159A1 (en) | 1964-08-05 | 1969-05-08 | Knapsack Ag | Method and device for the splitting of hydrocarbons with the aid of the electric arc |
US3389189A (en) | 1965-04-06 | 1968-06-18 | Westinghouse Electric Corp | Method and equipment for the pyrolysis and synthesis of hydrocarbons and other gasesand arc heater apparatus for use therein |
US3622493A (en) | 1968-01-08 | 1971-11-23 | Francois A Crusco | Use of plasma torch to promote chemical reactions |
US3674668A (en) | 1969-02-24 | 1972-07-04 | Phillips Petroleum Co | Electric arc process for making hydrogen cyanide, acetylene and acrylonitrile |
US4014947A (en) | 1969-06-03 | 1977-03-29 | Inst Neftechimicheskogo Sintez | Method of producing vinyl chloride |
US3697612A (en) | 1969-10-24 | 1972-10-10 | Westinghouse Electric Corp | Production of acetylene with an arc heater |
US3663394A (en) | 1970-06-01 | 1972-05-16 | Dow Chemical Co | Process for the vapor phase rearrangement of hydrocarbons utilizing microwave energy |
US3703460A (en) | 1970-09-30 | 1972-11-21 | Atomic Energy Commission | Non-equilibrium plasma reactor for natural gas processing |
US3755488A (en) | 1972-01-03 | 1973-08-28 | Phillips Petroleum Co | Selective absorption and hydrogenation of acetylenes |
GB1595413A (en) | 1976-12-15 | 1981-08-12 | Ici Ltd | Engergy recovery from chemical process off-gas |
US4128595A (en) | 1977-05-02 | 1978-12-05 | Phillips Petroleum Company | Acetylene hydrogenation in liquid phase with a liquid hydrocarbon reaction medium |
DE2952519A1 (en) | 1979-12-28 | 1981-07-02 | Bergwerksverband Gmbh, 4300 Essen | METHOD FOR PRODUCING ACETYLENE FROM COAL |
US4424401A (en) | 1980-08-12 | 1984-01-03 | The Broken Hill Proprietary Company Limited | Aromatization of acetylene |
US4367363A (en) | 1980-12-23 | 1983-01-04 | Gaf Corporation | Production of acetylene |
NO160432C (en) | 1981-05-26 | 1989-04-19 | Air Prod & Chem | PROCEDURE AND APPARATUS FOR RECOVERING A HYDROGENRIC GAS FROM A MATERIAL CONTAINING METHANE, ETHYLENE, HYDROGEN AND ACETYLENE. |
DE3152893A1 (en) * | 1981-06-12 | 1983-06-16 | Rorer Int Overseas | METHOD AND COMPOSITION FOR TREATING ACNE |
US4336045A (en) | 1981-06-29 | 1982-06-22 | Union Carbide Corporation | Acetylene removal in ethylene and hydrogen separation and recovery process |
US4513164A (en) | 1981-09-01 | 1985-04-23 | Olah George A | Condensation of natural gas or methane into gasoline range hydrocarbons |
NZ203822A (en) | 1982-04-29 | 1985-04-30 | British Petroleum Co Plc | Process for converting hydrocarbon feedstock to aromatic hydrocarbons |
FR2542004B1 (en) | 1983-03-02 | 1985-06-21 | British Petroleum Co | ELECTRICALLY ASSISTED CONVERSION PROCESS OF HEAVY CARBON PRODUCTS |
DE3330750A1 (en) | 1983-08-26 | 1985-03-14 | Chemische Werke Hüls AG, 4370 Marl | METHOD FOR GENERATING ACETYLENE AND SYNTHESIS OR REDUCING GAS FROM COAL IN AN ARC PROCESS |
US4575383A (en) | 1984-04-20 | 1986-03-11 | Atlantic Richfield Company | Process for producing acetylene using a heterogeneous mixture |
DE8590173U1 (en) | 1984-12-05 | 1987-07-09 | Murabito, Luigi, Carpi, Modena, It | |
US4705908A (en) | 1984-12-31 | 1987-11-10 | Gondouin Oliver M | Natural gas conversion process |
US4895727A (en) * | 1985-05-03 | 1990-01-23 | Chemex Pharmaceuticals, Inc. | Pharmaceutical vehicles for exhancing penetration and retention in the skin |
US4795536A (en) | 1985-07-10 | 1989-01-03 | Allied-Signal Inc. | Hydrogen separation and electricity generation using novel three-component membrane |
US4797185A (en) | 1985-07-19 | 1989-01-10 | Allied-Signal Inc. | Hydrogen separation and electricity generation using novel electrolyte membrane |
FR2614615B1 (en) | 1987-04-28 | 1989-08-04 | Inst Francais Du Petrole | PROCESS FOR THE THERMAL CONVERSION OF METHANE INTO HIGHER MOLECULAR WEIGHT HYDROCARBONS, REACTOR FOR IMPLEMENTING THE PROCESS AND METHOD FOR PRODUCING THE REACTOR |
GB8529245D0 (en) | 1985-11-27 | 1986-01-02 | British Petroleum Co Plc | Chemical process |
US4704496A (en) | 1986-03-24 | 1987-11-03 | The Standard Oil Company | Process for converting light hydrocarbons to more readily transportable materials |
GB8619717D0 (en) | 1986-08-13 | 1986-09-24 | Johnson Matthey Plc | Conversion of methane |
US4906800A (en) | 1986-11-17 | 1990-03-06 | The Standard Oil Company | Procedure for imparting selectivity to hydrogenation catalysts and method for using the same |
US4822940A (en) | 1987-08-17 | 1989-04-18 | The Standard Oil Company | Process for converting light hydrocarbons and/or natural gas to liquid hydrocarbons |
US5019355A (en) | 1987-09-28 | 1991-05-28 | University Of Alaska | Electrical device for conversion of molecular weights |
US4973786A (en) | 1987-10-19 | 1990-11-27 | Karra Sankaram B | Process for the pyrolytic oxidation of methane to higher molecular weight hydrocarbons and synthesis gas |
IN170837B (en) | 1987-11-17 | 1992-05-30 | Council Scient Ind Res | |
FR2624115B1 (en) | 1987-12-03 | 1990-04-13 | Gaz De France | PROCESS AND APPARATUS FOR CONVERSION OF HYDROCARBONS |
FR2639345B1 (en) | 1988-11-24 | 1991-03-15 | Gaz De France | PROCESS FOR CONVERTING NATURAL GAS OR LIGHT ALKANES IN UNSATURATED HYDROCARBONS |
CA1304419C (en) | 1988-12-22 | 1992-06-30 | Raj N. Pandey | Conversion of methane to gasoline-range hydrocarbons via isobutene |
US5131993A (en) | 1988-12-23 | 1992-07-21 | The Univeristy Of Connecticut | Low power density plasma excitation microwave energy induced chemical reactions |
US5015349A (en) | 1988-12-23 | 1991-05-14 | University Of Connecticut | Low power density microwave discharge plasma excitation energy induced chemical reactions |
US5073666A (en) | 1989-07-14 | 1991-12-17 | Cornell Research Foundation, Inc. | Hydrocarbon synthesis from lower alkanes at advanced temperatures and high pressures |
US5012029A (en) | 1989-10-16 | 1991-04-30 | Mobil Oil Corp. | Conversion of methane |
FR2655038B1 (en) | 1989-11-28 | 1993-05-14 | Inst Francais Du Petrole | PROCESS FOR PRODUCING ALKYLAROMATIC HYDROCARBONS FROM NATURAL GAS. INVENTION OF MM. BERNARD JUGUIN, JEAN-CLAUDE COLLIN, JOSEPH LARUE AND CHRISTIAN BUSSON. |
US5026944A (en) | 1989-12-20 | 1991-06-25 | Energy Mines And Resources Canada | Synthesis of isobutene from methane and acetylene |
US5205912A (en) | 1989-12-27 | 1993-04-27 | Exxon Research & Engineering Company | Conversion of methane using pulsed microwave radiation |
US5181998A (en) | 1989-12-27 | 1993-01-26 | Exxon Research And Engineering Company | Upgrading of low value hydrocarbons using a hydrogen donor and microwave radiation |
US5205915A (en) | 1989-12-27 | 1993-04-27 | Exxon Research & Engineering Company | Conversion of methane using continuous microwave radiation (OP-3690) |
EP0435591A3 (en) | 1989-12-27 | 1991-11-06 | Exxon Research And Engineering Company | Conversion of methane using microwave radiation |
US5277773A (en) | 1989-12-27 | 1994-01-11 | Exxon Research & Engineering Co. | Conversion of hydrocarbons using microwave radiation |
US5328577A (en) | 1989-12-27 | 1994-07-12 | Exxon Research & Engineering Co. | Upgrading of low value hydrocarbons using a hydrogen donor and microwave radiation |
US5498278A (en) | 1990-08-10 | 1996-03-12 | Bend Research, Inc. | Composite hydrogen separation element and module |
US5118893A (en) | 1991-05-24 | 1992-06-02 | Board Of Regents, The University Of Texas System | Zeolite catalyzed conversion of acetylene |
US5629102A (en) | 1992-04-24 | 1997-05-13 | H Power Corporation | Electrical automobile having a fuel cell, and method of powering an electrical automobile with a fuel cell system |
US5336825A (en) | 1992-07-10 | 1994-08-09 | Council Of Scientific & Industrial Research | Integrated two step process for conversion of methane to liquid hydrocarbons of gasoline range |
IT1255710B (en) | 1992-10-01 | 1995-11-10 | Snam Progetti | INTEGRATED PROCEDURE TO PRODUCE OLEFINS FROM GASEOUS MIXTURES CONTAINING METHANE |
CA2125599A1 (en) | 1993-06-11 | 1994-12-12 | Jeffrey K. S. Wan | Microwave production of c2 hydrocarbons using a carbon catalyst |
EP0634211A1 (en) | 1993-07-16 | 1995-01-18 | Texaco Development Corporation | Oxidative coupling of methane on manganese oxide octahedral molecular sieve catalyst |
JP2991609B2 (en) | 1993-10-18 | 1999-12-20 | 日本碍子株式会社 | Joint of gas separator and metal and hydrogen gas separator |
FR2715583B1 (en) | 1994-02-02 | 1996-04-05 | Inst Francais Du Petrole | Device for carrying out chemical reactions requiring at least starting calories. |
US5714657A (en) | 1994-03-11 | 1998-02-03 | Devries; Louis | Natural gas conversion to higher hydrocarbons |
US5488024A (en) | 1994-07-01 | 1996-01-30 | Phillips Petroleum Company | Selective acetylene hydrogenation |
US5675041A (en) | 1995-01-18 | 1997-10-07 | Exxon Research & Engineering Company | Direct hydroformylation of a multi-component synthesis gas containing carbon monoxide, hydrogen, ethylene, and acetylene |
US5583274A (en) | 1995-01-20 | 1996-12-10 | Phillips Petroleum Company | Alkyne hydrogenation process |
US5749937A (en) | 1995-03-14 | 1998-05-12 | Lockheed Idaho Technologies Company | Fast quench reactor and method |
US5587348A (en) | 1995-04-19 | 1996-12-24 | Phillips Petroleum Company | Alkyne hydrogenation catalyst and process |
US6120756A (en) * | 1998-08-19 | 2000-09-19 | Philip I. Markowitz | Topical anionic salicylate for disorders of the skin |
US6130260A (en) * | 1998-11-25 | 2000-10-10 | The Texas A&M University Systems | Method for converting natural gas to liquid hydrocarbons |
US6602920B2 (en) * | 1998-11-25 | 2003-08-05 | The Texas A&M University System | Method for converting natural gas to liquid hydrocarbons |
US6433235B1 (en) | 2000-06-09 | 2002-08-13 | Bryan Research & Engineering, Inc. | Method for converting methane-containing gaseous hydrocarbon mixtures to liquid hydrocarbons |
-
2001
- 2001-03-09 US US09/803,122 patent/US6602920B2/en not_active Expired - Lifetime
-
2002
- 2002-03-07 EP EP02728435A patent/EP1392802A2/en not_active Ceased
- 2002-03-07 AU AU2002258486A patent/AU2002258486B9/en not_active Ceased
- 2002-03-07 WO PCT/US2002/007183 patent/WO2002072741A2/en not_active Application Discontinuation
- 2002-03-07 NZ NZ528381A patent/NZ528381A/en not_active IP Right Cessation
-
2003
- 2003-07-01 US US10/611,564 patent/US7119240B2/en not_active Expired - Lifetime
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6602920B2 (en) | Method for converting natural gas to liquid hydrocarbons | |
AU2002258486A1 (en) | Method for converting natural gas to liquid hydrocarbons | |
EP1140738B1 (en) | Method for converting natural gas to liquid hydrocarons | |
US7915461B2 (en) | Process for the conversion of natural gas to hydrocarbon liquids | |
US7208647B2 (en) | Process for the conversion of natural gas to reactive gaseous products comprising ethylene | |
US7250449B2 (en) | High temperature hydrocarbon cracking | |
AU2002342075A1 (en) | High temperature hydrocarbon cracking |