Process for converting gaseous alkanes to liquid hydrocarbons

Abstract

A process for converting gaseous alkanes to liquid hydrocarbons wherein a gaseous feed containing alkanes is reacted with a dry bromine vapor to form alkyl bromides and hydrobromic acid vapor. The mixture of alkyl bromides and hydrobromic acid are then reacted over a synthetic crystalline alumino-silicate catalyst, such as a ZSM-5 zeolite, at a temperature of from about 150° C. to about 450° C. so as to form higher molecular weight hydrocarbons and hydrobromic acid vapor. Propane and butane which comprise a portion of the products may be recovered or recycled back through the process to form additional C 5 + hydrocarbons. Various methods are disclosed to remove the hydrobromic acid vapor from the higher molecular weight hydrocarbons and to generate bromine from the hydrobromic acid for use in the process.

Claims

1. A process comprising: heating at least a portion of metal bromide in an oxidized valence state in a first fluidized bed to form at least bromine vapor and metal bromide in a reduced valence state; contacting at least a portion of the metal bromide in a reduced valence state in a second fluidized bed with bromine vapor to form metal bromide in an oxidized state; conveying at least a portion of the metal bromide in a reduced valence state from the first fluidized bed to the second fluidized bed; and conveying at least a portion of the metal bromide in an oxidized state from the second fluidized bed to the first fluidized bed. 2. The process of claim 1 wherein the steps of heating, contacting and conveying are performed continuously. 3. The process of claim 1 wherein the metal bromide in both the first fluidized bed and the second fluidized bed are in a solid phase. 4. The process of claim 1 further comprising: reacting a gaseous feed comprising lower molecular weight alkanes and at least a portion of the bromine vapor from said heating step to form at least alkyl bromides and hydrobromic acid. 5. The process of claim 4 wherein further comprising: reacting at least a portion of the alkyl bromides in the presence of a catalyst to form at least hydrocarbons having at least 5 carbon atoms. 6. The process of claim 1 wherein the step of conveying at least a portion of the metal bromide in a reduced valence state from the first fluidized bed to the second fluidized bed comprises flowing at least a portion of the metal bromide in a reduced valence state from near the top of the first fluidized bed to near the bottom of the second fluidized bed. 7. The process of claim 6 wherein the step of flowing is performed by gravity. 8. The process of claim 1 wherein the step of conveying at least a portion of the metal bromide in an oxidized valence state from the second fluidized bed to the first fluidized bed comprises flowing at least a portion of the metal bromide in an oxidized state from near the top of the second fluidized bed to near the bottom of the first fluidized bed. 9. The process of claim 8 wherein said flowing is performed by gravity. 10. The process of claim 4 wherein the gaseous feed comprises a recycled gas stream. 11. The process of claim 4 wherein the alkyl bromides comprise mono and multiple brominated species. 12. The process of claim 4 further comprising heating the gaseous feed to a temperature of about 150° C. to about 600° C. prior to the step of reacting. 13. The process of claim 4 wherein the catalyst comprises a crystalline alumino-silicate catalyst. 14. The process of claim 4 wherein the catalyst comprises a zeolite catalyst. 15. The process of claim 10 wherein the gaseous feed is introduced into the first fluidized bed to heat at least a portion of the metal bromide in an oxidized state. 16. The process of claim 4 wherein said reacting step occurs in a vessel separate from the first fluidized bed. 17. A process comprising: thermally decomposing a metal bromide in an oxidized valence state to form at least bromine vapor and a metal bromide in a reduced valence state; and reacting a gas comprising lower molecular weight alkanes and at least a portion of the bromine vapor to form at least alkyl bromides and hydrobromic acid. 18. The process of claim 17 further comprising: reacting at least a portion of the alkyl bromides in the presence of a catalyst to form at least hydrocarbons having at least 5 carbon atoms. 19. The process of claim 17 wherein the gas is heated to a temperature of about 150° C. to about 600° C. prior to the step of reacting. 20. The process of claim 17 further comprising: contacting the metal bromide in a reduced valence state with bromine vapor to form the metal bromide in an oxidized valence state. 21. The process of claim 17 wherein the steps of thermally decomposing the metal bromide having an oxidized valence state to form at least bromine vapor and the metal bromide in a reduced valence state and reacting the gas comprising lower molecular weight alkanes and at least a portion of the bromine vapor to form at least alkyl bromides and hydrobromic acid occur in separate vessels. 22. The process of claim 17 wherein the gas comprises a recycled gas stream. 23. The process of claim 17 wherein the alkyl bromides comprise mono and multiple brominated species. 24. The process of claim 17 further comprising heating the gas to a temperature of about 150° C. to about 600° C. prior to reaction with the bromine vapor. 25. The process of claim 18 wherein the catalyst comprises a crystalline alumino-silicate catalyst. 26. The process of claim 18 wherein the catalyst comprises a zeolite catalyst. 27. The process of claim 18 wherein the catalyst is in a fixed bed. 28. The process of claim 18 further comprising: regenerating the catalyst by contacting the catalyst with an oxygen containing gas. 29. The process of claim 28 wherein said catalyst is in a bed and the step of regeneration occurs in situ. 30. The process of claim 29 wherein the bed is fixed. 31. A process comprising: reacting HBr with a metal oxide to form at least a metal bromide; oxidizing said metal bromide with an oxygen containing gas to form at least bromine vapor; reacting said bromine vapor with a metal bromide in a reduced valence state to form a metal bromide in an oxidized valence state; contacting said metal bromide in an oxidized valence state with a gaseous feed comprising lower molecular weight alkanes at a temperature sufficient to thermally decompose said metal bromide in an oxidized valence state to form at least additional bromine vapor; and reacting at least a portion of the lower molecular weight alkanes and at least a portion of the additional bromine vapor to form at least alkyl bromides 32. The process of claim 31 further comprising: reacting at least a portion of the alkyl bromides in the presence of a catalyst to form at least hydrocarbons having at least 5 carbon atoms. 33. The process of claim 32 wherein the steps of contacting said metal bromide in an oxidized valence state with the gaseous feed and of reacting at least a portion of the lower molecular weight alkanes and at least the portion of the additional bromine vapor occur in separate vessels. 34. A process comprising: reacting HBr with a metal oxide to form at least a metal bromide; oxidizing said metal bromide with an oxygen containing gas to form at least bromine vapor; storing at least a first portion of said bromine vapor as a metal bromide in an oxidized valence state; releasing at least some quantity of said first portion of said bromine vapor by thermally decomposing at least a portion of said metal bromide in an oxidized valence state; and transporting a gas comprising lower molecular weight alkanes with the quantity of bromine vapor released by thermally decomposing at least a portion of said metal bromide in an oxidized valence state. 35. The process of claim 34 wherein at least a portion of the quantity of bromine vapor released by thermally decomposing at least a portion of said metal bromide in an oxidized valence state reacts with at least a portion of the lower molecular weight alkanes to form alkyl bromides. 36. The process of claim 35 further comprising: reacting at least a portion of the alkyl bromides in the presence of a catalyst to form at least hydrocarbons having at least 5 carbon atoms.
REFERENCE TO RELATED PATENT APPLICATION This application is a continuation of U.S. patent application Ser. No. 11/957,261, filed Dec. 14, 2007, now U.S. Pat. No. 7,560,607 issued on Jul. 14, 2009 and entitled “Process for Converting Gaseous Alkanes to Liquid Hydrocarbons”, which is a continuation of patent application Ser. No. 11/101,886, filed Apr. 8, 2005, now U.S. Pat. No. 7,348,464 issued on Mar. 25, 2008 and entitled “Process for Converting Gaseous Alkanes to Liquid Hydrocarbons”, which is a continuation-in-part of patent application Ser. No. 10/826,885, filed Apr. 16, 2004, now U.S. Pat. No. 7,244,867 issued on Jul. 17, 2007 and entitled “Process for Converting Gaseous Alkanes to Liquid Hydrocarbons”. BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a process for converting lower molecular weight, gaseous alkanes to liquid hydrocarbons useful for the production of fuels, and more particularly, to a process wherein a gas containing lower molecular weight alkanes is reacted with a dry bromine vapor to form alkyl bromides and hydrobromic acid which in turn are reacted over a crystalline alumino-silicate catalyst to form liquid hydrocarbons. 2. Description of Related Art Natural gas which is primarily composed of methane and other light alkanes has been discovered in large quantities throughout the world. Many of the locales in which natural gas has been discovered are far from populated regions which have significant gas pipeline infrastructure or market demand for natural gas. Due to the low density of natural gas, transportation thereof in gaseous form by pipeline or as compressed gas in vessels is expensive. Accordingly, practical and economic limits exist to the distance over which natural gas may be transported in gaseous form exist. Cryogenic liquefaction of natural gas (LNG) is often used to more economically transport natural gas over large distances. However, this LNG process is expensive and there are limited regasification facilities in only a few countries that are equipped to import LNG. Another use of methane found in natural gas is as feed to processes for the production of methanol. Methanol is made commercially via conversion of methane to synthesis gas (CO and H 2 ) at high temperatures (approximately 1000° C.) followed by synthesis at high pressures (approximately 100 atmospheres). There are several types of technologies for the production of synthesis gas (CO and H 2 ) from methane. Among these are steam-methane reforming (SMR), partial oxidation (POX), autothermal reforming (ATR), gas-heated reforming (GHR), and various combinations thereof. SMR and GHR operate at high pressures and temperatures, generally in excess of 600° C., and require expensive furnaces or reactors containing special heat and corrosion-resistant alloy tubes filled with expensive reforming catalyst. POX and ATR processes operate at high pressures and even higher temperatures, generally in excess of 1000° C. As there are no known practical metals or alloys that can operate at these temperatures, complex and costly refractory-lined reactors and high-pressure waste-heat boilers to quench & cool the synthesis gas effluent are required. Also, significant capital cost and large amounts of power are required for compression of oxygen or air to these high-pressure processes. Thus, due to the high temperatures and pressures involved, synthesis gas technology is expensive, resulting in a high cost methanol product which limits higher-value uses thereof, such as for chemical feedstocks and solvents. Furthermore production of synthesis gas is thermodynamically and chemically inefficient, producing large excesses of waste heat and unwanted carbon dioxide, which tends to lower the conversion efficiency of the overall process. Fischer-Tropsch Gas-to-Liquids (GTL) technology can also be used to convert synthesis gas to heavier liquid hydrocarbons, however investment cost for this process is even higher. In each case, the production of synthesis gas represents a large fraction of the capital costs for these methane conversion processes. Numerous alternatives to the conventional production of synthesis gas as a route to methanol or synthetic liquid hydrocarbons have been proposed. However, to date, none of these alternatives has attained commercial status for various reasons. Some of the previous alternative prior-art methods, such as disclosed in U.S. Pat. No. 5,243,098 or 5,334,777 to Miller, teach reacting a lower alkane, such as methane, with a metallic halide to form a metalous halide and hydrohalic acid which are in turn reduced with magnesium oxide to form the corresponding alkanol. However, halogenation of methane using chlorine as the preferred halogen results in poor selectivity to the monomethyl halide (CH 3 Cl), resulting in unwanted by-products such as CH 2 Cl 2 and CHCl 3 which are difficult to convert or require severe limitation of conversion per pass and hence very high recycle rates. Other prior art processes propose the catalytic chlorination or bromination of methane as an alternative to generation of synthesis gas (CO and H 2 ). To improve the selectivity of a methane halogenation step in an overall process for the production of methanol, U.S. Pat. No. 5,998,679 to Miller teaches the use of bromine, generated by thermal decomposition of a metal bromide, to brominate alkanes in the presence of excess alkanes, which results in improved selectivity to mono-halogenated intermediates such as methyl bromide. To avoid the drawbacks of utilizing fluidized beds of moving solids, the process utilizes a circulating liquid mixture of metal chloride hydrates and metal bromides. Processes described in U.S. Pat. Nos. 6,462,243 B1, U.S. Pat. No. 6,472,572 B1, and U.S. Pat. No. 6,525,230 to Grosso are also capable of attaining higher selectivity to mono-halogenated intermediates by the use of bromination. The resulting alkyl bromides intermediates such as methyl bromide, are further converted to the corresponding alcohols and ethers, by reaction with metal oxides in circulating beds of moving solids. Another embodiment of U.S. Pat. No. 6,525,230 avoids the drawbacks of moving beds by utilizing a zoned reactor vessel containing a fixed bed of metal oxide/metal bromide that is operated cyclically in four steps. These processes also tend to produce substantial quantities of dimethylether (DME) along with any alcohol. While DME is a promising potential diesel engine fuel substitute, as of yet, there currently exists no substantial market for DME, and hence an expensive additional catalytic process conversion step would be required to convert DME into a currently marketable product. Other processes have been proposed which circumvent the need for production of synthesis gas, such as U.S. Pat. Nos. 4,655,893 and 4,467,130 to Olah in which methane is catalytically condensed into gasoline-range hydrocarbons via catalytic condensation using superacid catalysts. However, none of these earlier alternative approaches have resulted in commercial processes. It is known that substituted alkanes, in particular methanol, can be converted to olefins and gasoline boiling-range hydrocarbons over various forms of crystalline alumino-silicates also known as zeolites. In the Methanol to Gasoline (MTG) process, a shape selective zeolite catalyst, ZSM-5, is used to convert methanol to gasoline. Coal or methane gas can thus be converted to methanol using conventional technology and subsequently converted to gasoline. However due to the high cost of methanol production, and at current or projected prices for gasoline, the MTG process is not considered economically viable. Thus, a need exists for an economic process for the conversion of methane and other alkanes found in natural gas to useful liquid hydrocarbon products which, due to their higher density and value, are more economically transported thereby significantly aiding development of remote natural gas reserves. A further need exists for a process for converting alkanes present in natural gas which is relatively inexpensive, safe and simple in operation. SUMMARY OF THE INVENTION To achieve the foregoing and other objects, and in accordance with the purposes of the present invention, as embodied and broadly described herein, one characterization of the present invention is a process for converting gaseous alkanes to liquid hydrocarbons. The process comprises reacting a gaseous feed having lower molecular weight alkanes with bromine vapor to form alkyl bromides and hydrobromic acid. The alkyl bromides and hydrobromic acid are reacted in the presence of a synthetic crystalline alumino-silicate catalyst and at a temperature sufficient to form higher molecular weight hydrocarbons and hydrobromic acid vapor. The hydrobromic acid vapor is removed from the higher molecular weight hydrocarbons by reacting the hydrobromic acid vapor with a metal oxide to form a metal bromide and steam. In another characterization of the present invention, a process is provided for converting gaseous alkanes to liquid hydrocarbons wherein a gaseous feed having lower molecular weight alkanes is reacted with bromine vapor to form alkyl bromides and hydrobromic acid. The alkyl bromides and hydrobromic acid are reacted in the presence of a synthetic crystalline alumino-silicate catalyst and at a temperature sufficient to form higher molecular weight hydrocarbons and hydrobromic acid vapor. The hydrobromic acid vapor and the higher molecular weight hydrocarbons are transported to a first vessel having a bed of metal oxide particles, the hydrobromic acid vapor reacting with the bed of metal oxide particles to form metal bromide particles and steam. In still another characterization of the present invention, a process is provided for converting gaseous alkanes to liquid hydrocarbons wherein a gaseous feed having lower molecular weight alkanes is reacted with bromine vapor to form alkyl bromides and hydrobromic acid. The alkyl bromides and hydrobromic acid are reacted in the presence of a synthetic crystalline alumino-silicate catalyst and at a temperature sufficient to form higher molecular weight hydrocarbons and hydrobromic acid vapor. The hydrobromic acid vapor is removed from said higher molecular weight hydrocarbons by reaction with a metal oxide to form a first metal bromide and steam. The first metal bromide is oxidized with an oxygen containing gas to form bromine vapor. The bromine vapor is reacted a reduced metal bromide to form a second metal bromide. BRIEF DESCRIPTION OF THE DRAWINGS The accompanying drawings, which are incorporated in and form a part of the specification, illustrate the embodiments of the present invention and, together with the description, serve to explain the principles of the invention. In the drawings: FIG. 1 is a simplified block flow diagram of the process of the present invention; FIG. 2 is a schematic view of one embodiment of the process of the present invention; FIG. 3 is a schematic view of another embodiment of the process of the present invention; FIG. 4 is a graph of methyl bromide conversion and product selectivity for the oligomerization reaction of the process of the present invention as a function of temperature; FIG. 5 is a graph comparing conversion and selectivity for the example of methyl bromide, dry hydrobromic acid and methane versus only methyl bromide plus methane; FIG. 6 is a graph of product selectivity from reaction of methyl bromide and dibromomethane vs. product selectivity from reaction of methyl bromide only; FIG. 7 is a graph of a Paraffinic Olefinic Napthenic and Aromatic (PONA) analysis of a typical condensed product sample of the process of the present invention; FIG. 8 is a graph of a PONA analysis of another typical condensed product sample of the present invention; FIG. 9A is a schematic view of another embodiment of the process of the present invention; FIG. 9B is a schematic view of the embodiment of the process of the present invention illustrated in FIG. 9A depicting an alternative processing scheme which may be employed when oxygen is used in lieu of air in the oxidation stage; FIG. 10A is a schematic view of the embodiment of the process of the present invention illustrated in FIG. 9A with the flow through the metal oxide beds being reversed; FIG. 10B is a schematic view of the embodiment of the process of the present invention illustrated in FIG. 10A depicting an alternative processing scheme which may be employed when oxygen is used in lieu of air in the oxidation stage; FIG. 11A is a schematic view of another embodiment of the process of the present invention; FIG. 11B is a schematic view of the embodiment of the process of the present invention illustrated in FIG. 11A depicting an alternative processing scheme which may be employed when oxygen is used in lieu of air in the oxidation stage; FIG. 12 is a schematic view of another embodiment of the process of the present invention; FIG. 13 is a schematic view of the embodiment of the process of the present invention illustrated in FIG. 12 with the flow through the metal oxide beds being reversed; and FIG. 14 is a schematic view of another embodiment of the process of the present invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS As utilized throughout this description, the term “lower molecular weight alkanes” refers to methane, ethane, propane, butane, pentane or mixtures thereof. As also utilized throughout this description, “alkyl bromides” refers to mono, di, and tri brominated alkanes. Also, the feed gas in lines 11 and 111 in the embodiments of the process of the present invention as illustrated in FIGS. 2 and 3 , respectively, is preferably natural gas which may be treated to remove sulfur compounds and carbon dioxide. In any event, it is important to note that small amounts of carbon dioxide, e.g. less than about 2 mol %, can be tolerated in the feed gas to the process of the present invention. A block flow diagram generally depicting the process of the present invention is illustrated in FIG. 1 , while specific embodiments of the process of the present invention are illustrated in FIGS. 2 and 3 . Referring to FIG. 2 , a gas stream containing lower molecular weight alkanes, comprised of a mixture of a feed gas plus a recycled gas stream at a pressure in the range of about 1 bar to about 30 bar, is transported or conveyed via line, pipe or conduit 62 , mixed with dry bromine liquid transported via line 25 and pump 24 , and passed to heat exchanger 26 wherein the liquid bromine is vaporized. The mixture of lower molecular weight alkanes and dry bromine vapor is fed to reactor 30 . Preferably, the molar ratio of lower molecular weight alkanes to dry bromine vapor in the mixture introduced into reactor 30 is in excess of 2.5:1. Reactor 30 has an inlet pre-heater zone 28 which heats the mixture to a reaction initiation temperature in the range of about 250° C. to about 400° C. In first reactor 30 , the lower molecular weight alkanes are reacted exothermically with dry bromine vapor at a relatively low temperature in the range of about 250° C. to about 600° C., and at a pressure in the range of about 1 bar to about 30 bar to produce gaseous alkyl bromides and hydrobromic acid vapors. The upper limit of the operating temperature range is greater than the upper limit of the reaction initiation temperature range to which the feed mixture is heated due to the exothermic nature of the bromination reaction. In the case of methane, the formation of methyl bromide occurs in accordance with the following general reaction: CH 4 ( g )+Br 2 ( g )→CH 3 Br( g )+HBr( g ) This reaction occurs with a significantly high degree of selectivity to methyl bromide. For example, in the case of bromination of methane with a methane to bromine ratio of about 4.5:1 selectivity to the mono-halogenated methyl bromide is in the range of 90 to 95%. Small amounts of dibromomethane and tribromomethane are also formed in the bromination reaction. Higher alkanes, such as ethane, propane and butane, are also readily brominated resulting in mono and multiple brominated species. If an alkane to bromine ratio of significantly less than about 2.5 to 1 is utilized, selectivity to methyl bromide substantially lower than 90% occurs and significant formation of undesirable carbon soot is observed. It has also been shown that other alkanes such as ethane, propane and butane which may be present in the feed gas to the bromination reactor are readily brominated to form ethyl bromides, propyl bromides and butyl bromides. Further, the dry bromine vapor that is fed into first reactor 30 is substantially water-free. Applicant has discovered that elimination of substantially all water vapor from the bromination step in first reactor 30 substantially eliminates the formation of unwanted carbon dioxide thereby increasing the selectivity of alkane bromination to alkyl bromides and eliminating the large amount of waste heat generated in the formation of carbon dioxide from alkanes. The effluent that contains alkyl bromides and hydrobromic acid is withdrawn from the first reactor via line 31 and is partially cooled to a temperature in the range of about 150° C. to about 350° C. in heat exchanger 32 before flowing to a second reactor 34 . In second reactor 34 , the alkyl bromides are reacted exothermically at a temperature range of from about 150° C. to about 450° C., and a pressure in the range of about 1 to 30 bar, over a fixed bed 33 of crystalline alumino-silicate catalyst, preferably a zeolite catalyst, and most preferably a ZSM-5 zeolite catalyst. Although the zeolite catalyst is preferably used in the hydrogen, sodium or magnesium form, the zeolite may also be modified by ion exchange with other alkali metal cations, such as Li, Na, K or Cs, with alkali-earth metal cations, such as Mg, Ca, Sr or Ba, or with transition metal cations, such as Ni, Mn, V, W, or to the hydrogen form. Other zeolite catalysts having varying pore sizes and acidities, which are synthesized by varying the alumina-to-silica ratio may be used in the second reactor 34 as will be evident to a skilled artisan. In this reactor, the alkyl bromides are oligomerized to produce a mixture of higher molecular weight hydrocarbon products, primarily C 3 , C 4 and C 5 +gasoline-range and heavier hydrocarbon fractions, and additional hydrobromic acid vapor. The temperature at which the second reactor 34 is operated is an important parameter in determining the selectivity of the oligomerization reaction to various higher molecular weight liquid hydrocarbon products. It is preferred to operate second reactor 34 at a temperature within the range of about 150° to 450° . Temperatures above about 300° C. in the second reactor result in increased yields of light hydrocarbons, such as undesirable methane, whereas lower temperatures increase yields of heavier molecular weight hydrocarbon products. At the low end of the temperature range, with methyl bromide reacting over ZSM-5 zeolite at temperatures as low as 150° C. significant methyl bromide conversion on the order of 20% is noted, with a high selectivity towards C 5 +products. Also it is noted that methyl bromide appears to be more reactive over a lower temperature range relative to methyl chloride or other substituted methyl compounds such as methanol. Notably, in the case of the alkyl bromide reaction over the preferred zeolite ZSM-5 catalyst, cyclization reactions also occur such that the C7+fractions are composed primarily of substituted aromatics. At increasing temperatures approaching 300° C., methyl bromide conversion increases towards 90% or greater, however selectivity towards C 5 +products decreases and selectivity towards lighter products, particularly undesirable methane, increases. Surprisingly, very little ethane or C 2 ,-C 3 olefin components are formed. At temperatures approaching 450° C., almost complete conversion of methyl bromide to methane occurs. In the optimum operating temperature range of between about 300° C. and 400° C., as a byproduct of the reaction, a small amount of carbon will build up on the catalyst over time during operation, causing a decline in catalyst activity over a range of hours, up to hundreds of hours, depending on the reaction conditions and the composition of the feed gas. It is believed that higher reaction temperatures above about 400° C., associated with the formation of methane favor the thermal cracking of alkyl bromides and formation of carbon or coke and hence an increase in the rate of deactivation of the catalyst. Conversely, temperatures at the lower end of the range, particularly below about 300° C. may also contribute to coking due to a reduced rate of desorption of heavier products from the catalyst. Hence, operating temperatures within the range of about 150° C. to about 450° C., but preferably in the range of about 300° C. to about 400° C. in the second reactor 34 balance increased selectivity of the desired C 5 +products and lower rates of deactivation due to carbon formation, against higher conversion per pass, which minimizes the quantity of catalyst, recycle rates and equipment size required. The catalyst may be periodically regenerated in situ, by isolating reactor 34 from the normal process flow, purging with an inert gas via line 70 at a pressure in a range from about 1 to about 5 bar at an elevated temperature in the range of about 400° C. to about 650° C. to remove unreacted material adsorbed on the catalyst insofar as is practical, and then subsequently oxidizing the deposited carbon to CO 2 by addition of air or inert gas-diluted oxygen to reactor 34 via line 70 at a pressure in the range of about 1 bar to about 5 bar at an elevated temperature in the range of about 400° C. to about 650° C. Carbon dioxide and residual air or inert gas is vented from reactor 34 via line 75 during the regeneration period. The effluent which comprises the higher molecular weight hydrocarbon products and hydrobromic acid is withdrawn from the second reactor 34 via line 35 and is cooled to a temperature in the range of 0° C. to about 100° C. in exchanger 36 and combined with vapor effluent in line 12 from hydrocarbon stripper 47 , which contains feed gas and residual hydrocarbon products stripped-out by contact with the feed gas in hydrocarbon stripper 47 . The combined vapor mixture is passed to a scrubber 38 and contacted with a concentrated aqueous partially-oxidized metal bromide salt solution containing metal hydroxide and/or metal oxide and/or metal oxy-bromide species, which is transported to scrubber 38 via line 41 . The preferred metal of the bromide salt is Fe(III), Cu(II) or Zn(II), or mixtures thereof, as these are less expensive and readily oxidize at lower temperatures in the range of about 120° C. to about 180° C., allowing the use of fluorpolymer-lined equipment; although Co(II), Ni(II), Mn(II), V(II), Cr(II) or other transition-metals which form oxidizable bromide salts may be used in the process of the present invention. Alternatively, alkaline-earth metals which also form oxidizable bromide salts, such as Ca (II) or Mg(II) may be used. Any liquid hydrocarbon product condensed in scrubber 38 may be skimmed and withdrawn in line 37 and added to liquid hydrocarbon product exiting the product recovery unit 52 in line 54 . Hydrobromic acid is dissolved in the aqueous solution and neutralized by the metal hydroxide and/or metal oxide and/or metal oxybromide species to yield metal bromide salt in solution and water which is removed from the scrubber 38 via line 44 . The residual vapor phase containing the higher molecular weight hydrocarbon products that is removed as effluent from the scrubber 38 is forwarded via line 39 to dehydrator 50 to remove substantially all water via line 53 from the vapor stream. The water is then removed from the dehydrator 50 via line 53 . The dried vapor stream containing the higher molecular weight hydrocarbon products is further passed via line 51 to product recovery unit 52 to recover propane and butane as desired, but primarily the C 5 + fraction as a liquid product in line 54 . Any conventional method of dehydration and liquids recovery, such as solid-bed dessicant adsorption followed by refrigerated condensation, cryogenic expansion, or circulating absorption oil, as used to process natural gas or refinery gas streams, as will be evident to a skilled artisan, may be employed in the process of the present invention. The residual vapor effluent from product recovery unit 52 is then split into a purge stream 57 which may be utilized as fuel for the process and a recycled residual vapor which is compressed via compressor 58 . The recycled residual vapor discharged from compressor 58 is split into two fractions. A first fraction that is equal to at least 2.5 times the feed gas molar volume is transported via line 62 and is combined with dry liquid bromine conveyed by pump 24 , heated in exchanger 26 to vaporize the bromine and fed into first reactor 30 . The second fraction is drawn off of line 62 via line 63 and is regulated by control valve 60 , at a rate sufficient to dilute the alkyl bromide concentration to reactor 34 and absorb the heat of reaction such that reactor 34 is maintained at the selected operating temperature, preferably in the range of about 300° C. to about 400° C. in order to optimize conversion versus selectivity and to minimize the rate of catalyst deactivation due to the deposition of carbon. Thus, the dilution provided by the recycled vapor effluent permits selectivity of bromination in the first reactor 30 to be controlled in addition to moderating the temperature in second reactor 34 . Water containing metal bromide salt in solution which is removed from scrubber 38 via line 44 is passed to hydrocarbon stripper 47 wherein residual dissolved hydrocarbons are stripped from the aqueous phase by contact with incoming feed gas transported via line 11 . The stripped aqueous solution is transported from hydrocarbon stripper 47 via line 65 and is cooled to a temperature in the range of about 0° C. to about 70° C. in heat exchanger 46 and then passed to absorber 48 in which residual bromine is recovered from vent stream in line 67 . The aqueous solution effluent from scrubber 48 is transported via line 49 to a heat exchanger 40 to be preheated to a temperature in the range of about 100° C. to about 600° C., and most preferably in the range of about 120° C. to about 180° C. and passed to third reactor 16 . Oxygen or air is delivered via line 10 by blower or compressor 13 at a pressure in the range of about ambient to about 5 bar to bromine stripper 14 to strip residual bromine from water which is removed from stripper 14 in line 64 and is combined with water stream 53 from dehydrator 50 to form water effluent stream in line 56 which is removed from the process. The oxygen or air leaving bromine stripper 14 is fed via line 15 to reactor 16 which operates at a pressure in the range of about ambient to about 5 bar and at a temperature in the range of about 100° C. to about 600° C., but most preferably in the range of about 120° C. to about 180° C. so as to oxidize an aqueous metal bromide salt solution to yield elemental bromine and metal hydroxide and/or metal oxide and or metal oxy-bromide species. As stated above, although Co(II), Ni(II), Mn(II), V(II), Cr(II) or other transition-metals which form oxidizable bromide salts can be used, the preferred metal of the bromide salt is Fe(III), Cu(II), or Zn(II), or mixtures thereof, as these are less expensive and readily oxidize at lower temperatures in the range of about 120° C. to about 180° C., allowing the use of fluorpolymer-lined equipment. Alternatively, alkaline-earth metals which also form oxidizable bromide salts, such as Ca (II) or Mg(II) could be used. Hydrobromic acid reacts with the metal hydroxide and/or metal oxide and/or metal oxy-bromide species so formed to once again yield the metal bromide salt and water. Heat exchanger 18 in reactor 16 supplies heat to vaporize water and bromine. Thus, the overall reactions result in the net oxidation of hydrobromic acid produced in first reactor 30 and second reactor 34 to elemental bromine and steam in the liquid phase catalyzed by the metal bromide/metal oxide or metal hydroxide operating in a catalytic cycle. In the case of the metal bromide being Fe(III)Br3, the reactions are believed to be: Fe(+3 a )+6Br(− a )+3H(+ a )+ 3/2O2( g )=3Br2( g )+Fe(OH)3  1) 3HBr( g )+H 2 O=3H(+ a )+3Br(− a )+H 2 O  2) 3H(+ a )+3Br(− a )+Fe(OH)3=Fe(+3 a )+3Br(− a )+3H 2 O  3) The elemental bromine and water and any residual oxygen or nitrogen (if air is utilized as the oxidant) leaving as vapor from the outlet of third reactor 16 via line 19 , are cooled in condenser 20 at a temperature in the range of about 0° C. to about 70° C. and a pressure in the range of about ambient to 5 bar to condense the bromine and water and passed to three-phase separator 22 . In three-phase separator 22 , since liquid water has a limited solubility for bromine, on the order of about 3% by weight, any additional bromine which is condensed forms a separate, denser liquid bromine phase. The liquid bromine phase, however, has a notably lower solubility for water, on the order of less than 0.1%. Thus a substantially dry bromine vapor can be easily obtained by condensing liquid bromine and water, decanting water by simple physical separation and subsequently re-vaporizing liquid bromine. Liquid bromine is pumped in line 25 from three-phase separator 22 via pump 24 to a pressure sufficient to mix with vapor stream 62 . Thus bromine is recovered and recycled within the process. The residual oxygen or nitrogen and any residual bromine vapor which is not condensed exits three-phase separator 22 and is passed via line 23 to bromine scrubber 48 , wherein residual bromine is recovered by solution into and by reaction with reduced metal bromides in the aqueous metal bromide solution stream 65 . Water is removed from separator 22 via line 27 and introduced into stripper 14 . In another embodiment of the invention, referring to FIG. 3 , a gas stream containing lower molecular weight alkanes, comprised of mixture of a feed gas plus a recycled gas stream at a pressure in the range of about 1 bar to about 30 bar, is transported or conveyed via line, pipe or conduit 162 , mixed with dry bromine liquid transported via pump 124 and passed to heat exchanger 126 wherein the liquid bromine is vaporized. The mixture of lower molecular weight alkanes and dry bromine vapor is fed to reactor 130 . Preferably, the molar ratio of lower molecular weight alkanes to dry bromine vapor in the mixture introduced into reactor 130 is in excess of 2.5:1. Reactor 130 has an inlet pre-heater zone 128 which heats the mixture to a reaction initiation temperature in the range of about 250° C. to about 400° C. In first reactor 130 , the lower molecular weight alkanes are reacted exothermically with dry bromine vapor at a relatively low temperature in the range of about 250° C. to about 600° C., and at a pressure in the range of about 1 bar to about 30 bar to produce gaseous alkyl bromides and hydrobromic acid vapors. The upper limit of the operating temperature range is greater than the upper limit of the reaction initiation temperature range to which the feed mixture is heated due to the exothermic nature of the bromination reaction. In the case of methane, the formation of methyl bromide occurs in accordance with the following general reaction: CH 4 ( g )+Br 2 ( g ) CH 3 Br( g ) +HBr( g ) This reaction occurs with a significantly high degree of selectivity to methyl bromide. For example, in the case of bromine reacting with a molar excess of methane at a methane to bromine ratio of 4.5:1, selectivity to the mono-halogenated methyl bromide is in the range of 90 to 95%. Small amounts of dibromomethane and tribromomethane are also formed in the bromination reaction. Higher alkanes, such as ethane, propane and butane, are also readily brominated resulting in mono and multiple brominated species. If an alkane to bromine ratio of significantly less than 2.5 to 1 is utilized, selectivity to methyl bromide substantially lower than 90% occurs and significant formation of undesirable carbon soot is observed. It has also been shown that other alkanes such as ethane, propane and butane which may be present in the feed gas to the bromination are readily brominated to form ethyl bromides, propyl bromides and butyl bromides. Further, the dry bromine vapor that is fed into first reactor 130 is substantially water-free. Applicant has discovered that elimination of substantially all water vapor from the bromination step in first reactor 130 substantially eliminates the formation of unwanted carbon dioxide thereby increasing the selectivity of alkane bromination to alkyl bromides and eliminating the large amount of waste heat generated in the formation of carbon dioxide from alkanes. The effluent that contains alkyl bromides and hydrobromic acid is withdrawn from the first reactor 130 via line 131 and is partially cooled to a temperature in the range of about 150° C. to 350° C. in heat exchanger 132 before flowing to a second reactor 134 . In second reactor 134 , the alkyl bromides are reacted exothermically at a temperature range of from about 150° C. to about 450° C., and a pressure in the range of about 1 bar to 30 bar, over a fixed bed of crystalline alumino-silicate catalyst, preferably a zeolite catalyst, and most preferably a ZSM-5 zeolite catalyst. Although the zeolite catalyst is preferably used in the hydrogen, sodium or magnesium form, the zeolite may also be modified by ion exchange with other alkali metal cations, such as Li, Na, K or Cs, with alkali-earth metal cations, such as Mg, Ca, Sr or Ba, or with transition metal cations, such as Ni, Mn, V, W, or to the hydrogen form. Other zeolite catalysts having varying pore sizes and acidities, which are synthesized by varying the alumina-to-silica ratio may be used in the second reactor 134 as will be evident to a skilled artisan. In this reactor, the alkyl bromides are oligomerized to produce a mixture of higher molecular weight hydrocarbon products and additional hydrobromic acid vapor. The temperature at which the second reactor 134 is operated is an important parameter in determining the selectivity of the oligomerization reaction to various higher molecular weight liquid hydrocarbon products. It is preferred to operate second reactor 134 at a temperature within the range of about 150° to 450°, but more preferably within the range of about 300° C. to 400° C. Temperatures above about 300° C. in the second reactor result in increased yields of light hydrocarbons, such as undesirable methane, whereas lower temperatures increase yields of heavier molecular weight hydrocarbon products. At the low end of the temperature range, methyl bromide reacting over ZSM-5 zeolite at temperatures as low as 150° C. significant methyl bromide conversion on the order of 20% is noted, with a high selectivity towards C 5 +products. Notably, in the case of alkyl bromides reacting over the preferred ZSM-5 zeolite catalyst, cyclization reactions occur such that the C 7 +fractions produced contain a high percentage of substituted aromatics. At increasing temperatures approaching 300° C., methyl bromide conversion increases towards 90% or greater, however selectivity towards C 5 +products decreases and selectivity towards lighter products, particularly undesirable methane, increases. Surprisingly, very little ethane or C 2 -C 4 olefin compounds are produced. At temperatures approaching 450° C. almost complete conversion of methyl bromide to methane occurs. In the optimum range of operating temperatures of about 300° C. to 400° C., as a byproduct of the reaction, a small amount of carbon will build up on the catalyst over time during operation, causing a decline in catalyst activity over a range of several hundred hours, depending on the reaction conditions and feed gas composition. It is observed that higher reaction temperatures above about 400° C. favor the thermal cracking of alkyl bromides with formation of carbon and hence increases the rate of deactivation of the catalyst. Conversely, operation at the lower end of the temperature range, particularly below about 300° C. may also promote coking, likely to the reduced rate of desorption of hydrocarbon products. Hence, operating temperatures within the range of about 150° C. to 450° C. but more preferably in the range of about 300° C. to 400° C. in the second reactor 134 balance increased selectivity towards the desired products and lower rates of deactivation due to carbon formation, against higher conversion per pass, which minimizes the quantity of catalyst, recycle rates and equipment size required. The catalyst may be periodically regenerated in situ, by isolating reactor 134 from the normal process flow, purging with an inert gas via line 170 at a pressure in the range of about 1 bar to about 5 bar and an elevated temperature in the range of 400° C. to 650° C. to remove unreacted material adsorbed on the catalyst insofar as is practical, and then subsequently oxidizing the deposited carbon to CO 2 by addition of air or inert gas-diluted oxygen via line 170 to reactor 134 at a pressure in the range of about 1 bar to about 5 bar and an elevated temperature in the range of 400° C. to 650° C. Carbon dioxide and residual air or inert gas are vented from reactor 134 via line 175 during the regeneration period. The effluent which comprises the higher molecular weight hydrocarbon products and hydrobromic acid is withdrawn from the second reactor 134 via line 135 , cooled to a temperature in the range of about 0° C. to about 100° C. in exchanger 136 , and combined with vapor effluent in line 112 from hydrocarbon stripper 147 . The mixture is then passed to a scrubber 138 and contacted with a stripped, recirculated water that is transported to scrubber 138 in line 164 by any suitable means, such as pump 143 , and is cooled to a temperature in the range of about 0° C. to about 50° C. in heat exchanger 155 . Any liquid hydrocarbon product condensed in scrubber 138 may be skimmed and withdrawn as stream 137 and added to liquid hydrocarbon product 154 . Hydrobromic acid is dissolved in scrubber 138 in the aqueous solution which is removed from the scrubber 138 via line 144 , and passed to hydrocarbon stripper 147 wherein residual hydrocarbons dissolved in the aqueous solution are stripped-out by contact with feed gas 111 . The stripped aqueous phase effluent from hydrocarbon stripper 147 is cooled to a temperature in the range of about 0° C. to about 50° C. in heat exchanger 146 and then passed via line 165 to absorber 148 in which residual bromine is recovered from vent stream 167 . The residual vapor phase containing the higher molecular weight hydrocarbon products is removed as effluent from the scrubber 138 and forwarded to dehydrator 150 to remove substantially all water from the gas stream. The water is then removed from the dehydrator 150 via line 153 . The dried gas stream containing the higher molecular weight hydrocarbon products is further passed via line 151 to product recovery unit 152 to recover C 3 and C 4 as desired, but primarily the C 5 + fraction as a liquid product in line 154 . Any conventional method of dehydration and liquids recovery such as solid-bed dessicant adsorption followed by, for example, refrigerated condensation, cryogenic expansion, or circulating absorption oil, as used to process natural gas or refinery gas streams, as known to a skilled artisan, may be employed in the implementation of this invention. The residual vapor effluent from product recovery unit 152 is then split into a purge stream 157 that may be utilized as fuel for the process and a recycled residual vapor which is compressed via compressor 158 . The recycled residual vapor discharged from compressor 158 is split into two fractions. A first fraction that is equal to at least 2.5 times the feed gas volume is transported via line 162 , combined with the liquid bromine conveyed in line 125 and passed to heat exchanger 126 wherein the liquid bromine is vaporized and fed into first reactor 130 . The second fraction which is drawn off line 162 via line 163 and is regulated by control valve 160 , at a rate sufficient to dilute the alkyl bromide concentration to reactor 134 and absorb the heat of reaction such that reactor 134 is maintained at the selected operating temperature, preferably in the range of about 300° C. to about 400° C. in order to optimize conversion vs. selectivity and to minimize the rate of catalyst deactivation due to the deposition of carbon. Thus, the dilution provided by the recycled vapor effluent permits selectivity of bromination in the first reactor 130 to be controlled in addition to moderating the temperature in second reactor 134 . Oxygen, oxygen enriched air or air 110 is delivered via blower or compressor 113 at a pressure in the range of about ambient to about 5 bar to bromine stripper 114 to strip residual bromine from water which leaves stripper 114 via line 164 and is divided into two portions. The first portion of the stripped water is recycled via line 164 , cooled in heat exchanger 155 to a temperature in the range of about 20° C. to about 50° C., and maintained at a pressure sufficient to enter scrubber 138 by any suitable means, such as pump 143 . The portion of water that is recycled is selected such that the hydrobromic acid solution effluent removed from scrubber 138 via line 144 has a concentration in the range from about 10% to about 50% by weight hydrobromic acid, but more preferably in the range of about 30% to about 48% by weight to minimize the amount of water which must be vaporized in exchanger 141 and preheater 119 and to minimize the vapor pressure of HBr over the resulting acid. A second portion of water from stripper 114 is removed from line 164 and the process via line 156 . The dissolved hydrobromic acid that is contained in the aqueous solution effluent from scrubber 148 is transported via line 149 and is combined with the oxygen, oxygen enriched air or air leaving bromine stripper 114 in line 115 . The combined aqueous solution effluent and oxygen, oxygen enriched air or air is passed to a first side of heat exchanger 141 and through preheater 119 wherein the mixture is preheated to a temperature in the range of about 100° C. to about 600° C. and most preferably in the range of about 120° C. to about 180° C. and passed to third reactor 117 that contains a metal bromide salt. The preferred metal of the bromide salt is Fe(III), Cu(II) or Zn(II) although Co(II), Ni(II), Mn(II), V(II), Cr(II) or other transition-metals which form oxidizable bromide salts can be used. Alternatively, alkaline-earth metals which also form oxidizable bromide salts, such as Ca (II) or Mg(II) could be used. The metal bromide salt in the oxidation reactor 117 can be utilized as a concentrated aqueous solution or preferably, the concentrated aqueous salt solution may be imbibed into a porous, high surface area, acid resistant inert support such as a silica gel. The oxidation reactor 117 operates at a pressure in the range of about ambient to about 5 bar and at a temperature in the range of about 100° C. to 600° C., but most preferably in the range of about 120° C. to 180° C.; therein, the metal bromide is oxidized by oxygen, yielding elemental bromine and metal hydroxide, metal oxide or metal oxy-bromide species or, metal oxides in the case of the supported metal bromide salt operated at higher temperatures and lower pressures at which water may primarily exist as a vapor. In either case, the hydrobromic acid reacts with the metal hydroxide, metal oxy-bromide or metal oxide species and is neutralized, restoring the metal bromide salt and yielding water. Thus, the overall reaction results in the net oxidation of hydrobromic acid produced in first reactor 130 and second reactor 134 to elemental bromine and steam, catalyzed by the metal bromide/metal hydroxide or metal oxide operating in a catalytic cycle. In the case of the metal bromide being Fe(III)Br2 in an aqueous solution and operated in a pressure and temperature range in which water may exist as a liquid the reactions are believed to be: Fe(+3 a )+6Br(− a )+3H(+ a )+ 3/2O 2( g )=3Br 2 ( g )+Fe(OH)3  1) 3HBr( g )+H 2 O=3H(+ a )+3Br(− a )+H 2 O  2) 3H(+ a )+3Br(− a )+Fe(OH)3=Fe(+3 a )+3Br(− a )+3H 2 O  3) In the case of the metal bromide being Cu(II)Br2 supported on an inert support and operated at higher temperature and lower pressure conditions at which water primarily exists as a vapor, the reactions are believed to be: 2Cu(II)Br2=2Cu(I)Br+B2( g )  1) 2Cu(I)Br+O 2 ( g )=Br2( g )+2Cu(II)O  2) 2HBr( g )+Cu(II)O═Cu(II)Br 2 +H 2 O( g )  3) The elemental bromine and water and any residual oxygen or nitrogen (if air or oxygen enriched air is utilized as the oxidant) leaving as vapor from the outlet of third reactor 117 , are cooled in the second side of exchanger 141 and condenser 120 to a temperature in the range of about 0° C. to about 70° C. wherein the bromine and water are condensed and passed to three-phase separator 122 . In three-phase separator 122 , since liquid water has a limited solubility for bromine, on the order of about 3% by weight, any additional bromine which is condensed forms a separate, denser liquid bromine phase. The liquid bromine phase, however, has a notably lower solubility for water, on the order of less than 0.1%. Thus, a substantially dry bromine vapor can be easily obtained by condensing liquid bromine and water, decanting water by simple physical separation and subsequently re-vaporizing liquid bromine. It is important to operate at conditions that result in the near complete reaction of HBr so as to avoid significant residual HBr in the condensed liquid bromine and water, as HBr increases the miscibility of bromine in the aqueous phase, and at sufficiently high concentrations, results in a single ternary liquid phase. Liquid bromine is pumped from three-phase separator 122 via pump 124 to a pressure sufficient to mix with vapor stream 162 . Thus the bromine is recovered and recycled within the process. The residual air, oxygen enriched air or oxygen and any bromine vapor which is not condensed exits three-phase separator 122 and is passed via line 123 to bromine scrubber 148 , wherein residual bromine is recovered by dissolution into hydrobromic acid solution stream conveyed to scrubber 148 via line 165 . Water is removed from the three-phase separator 122 via line 129 and passed to stripper 114 . The following examples demonstrate the practice and utility of the present invention, but are not to be construed as limiting the scope thereof. EXAMPLE 1 Various mixtures of dry bromine and methane are reacted homogeneously at temperatures in the range of 459° C. to 491° C. at a Gas Hourly Space Velocity (GHSV which is defined as the gas flow rate in standard liters per hour divided by the gross reactor catalyst-bed volume, including catalyst-bed porosity, in liters) of approximately 7200 hr −1 . The results of this example indicate that for molar ratios of methane to bromine greater than 4.5:1 selectivity to methyl bromide is in the range of 90 to 95%, with near-complete conversion of bromine. EXAMPLE 2 FIG. 7 and FIG. 8 illustrate two exemplary PONA analyses of two C 6 + liquid product samples that are recovered during two test runs with methyl bromide and methane reacting over ZSM-5 zeolite catalyst. These analyses show the substantially aromatic content of the C 6 + fractions produced. EXAMPLE 3 Methyl bromide is reacted over a ZSM-5 zeolite catalyst at a Gas Hourly Space Velocity (GHSV) of approximately 94 hr −1 over a range of temperatures from about 100° C. to about 460° C. at approximately 2 bar pressure. As illustrated in FIG. 4 , which is a graph of methyl bromide conversion and product selectivity for the oligomerization reaction as a function of temperature, methyl bromide conversion increases rapidly in the range of about 200° C. to about 350° C. Lower temperatures in the range of about 100° C. to about 250° C. favor selectivity towards higher molecular weight products however conversion is low. Higher temperatures in the range of about 250° C. to about 350° C. show higher conversions in the range of 50% to near 100%, however increasing selectivity to lower molecular weight products, in particular undesirable methane is observed. At higher temperatures above 350° C. selectivity to methane rapidly increases. At about 450° C., almost complete conversion to methane occurs. EXAMPLE 4 Methyl bromide, hydrogen bromide and methane are reacted over a ZSM-5 zeolite catalyst at approximately 2 bar pressure at about 250° C. and also at about 260° C. at a GHSV of approximately 76 hr −1 . Comparison tests utilizing a mixture of only methyl bromide and methane without hydrogen bromide over the same ZSM-5 catalyst at approximately the same pressure at about 250° C. and at about 260° C. at a GHSV of approximately 73 hr −1 were also run. FIG. 5 , which is a graph that illustrates the comparative conversions and selectivities of several example test runs, shows only a very minor effect due to the presence of HBr on product selectivities. Because hydrobromic acid has only a minor effect on conversion and selectivity, it is not necessary to remove the hydrobromic acid generated in the bromination reaction step prior to the conversion reaction of the alkyl bromides, in which additional hydrobromic acid is formed in any case. Thus, the process can be substantially simplified. EXAMPLE 5 Methyl bromide is reacted over a ZSM-5 zeolite catalyst at 230° C. Dibromomethane is added to the reactor. FIG. 6 , which is a graph of product selectivity, indicates that reaction of methyl bromide and dibromomethane results in a shift in selectivity towards C 5+ products versus methyl bromide alone. Thus, these results demonstrate that dibromomethane is also reactive and therefore very high selectivity to bromomethane in the bromination step is not required in the process of the present invention. It has been observed, however, that the presence of dibromomethane increases the rate of catalyst deactivation, requiring a higher operating temperature to optimize the tradeoff between selectivity and deactivation rate, as compared to pure methyl bromide. EXAMPLE 6 A mixture of 12.1 mol% methyl bromide and 2.8 mol% propyl bromide in methane are reacted over a ZSM-5 zeolite catalyst at 295° C. and a GHSV of approximately 260 hr −1 . A methyl bromide conversion of approximately 86% and a propyl bromide conversion of approximately 98% is observed. Thus, in accordance with all embodiments of the present invention set forth above, the metal bromide/metal hydroxide, metal oxy-bromide or metal oxide operates in a catalytic cycle allowing bromine to be easily recycled within the process. The metal bromide is readily oxidized by oxygen, oxygen enriched air or air either in the aqueous phase or the vapor phase at temperatures in the range of about 100° C. to about 600° C. and most preferably in the range of about 120° C. to about 180° C. to yield elemental bromine vapor and metal hydroxide, metal oxy-bromide or metal oxide. Operation at temperatures below about 180° C. is advantageous, thereby allowing the use of low-cost corrosion-resistant fluoropolymer-lined equipment. Hydrobromic acid is neutralized by reaction with the metal hydroxide or metal oxide yielding steam and the metal bromide. The elemental bromine vapor and steam are condensed and easily separated in the liquid phase by simple physical separation, yielding substantially dry bromine. The absence of significant water allows selective bromination of alkanes, without production of CO 2 and the subsequent efficient and selective oligomerization and cyclization reactions of alkyl bromides to primarily propane and heavier products, the C 5 +fraction of which contains substantial branched alkanes and substituted aromatics. Byproduct hydrobromic acid vapor from the bromination and oligomerization reaction are readily dissolved into an aqueous phase and neutralized by the metal hydroxide or metal oxide species resulting from oxidation of the metal bromide. In accordance with another embodiment of the process of the present invention illustrated in FIG. 9A , the alkyl bromination and alkyl bromide conversion stages are operated in a substantially similar manner to those corresponding stages described with respect to FIGS. 2 and 3 above. More particularly, a gas stream containing lower molecular weight alkanes, comprised of mixture of a feed gas and a recycled gas stream at a pressure in the range of about 1 bar to about 30 bar, is transported or conveyed via line, pipe or conduits 262 and 211 , respectively, and mixed with dry bromine liquid in line 225 . The resultant mixture is transported via pump 224 and passed to heat exchanger 226 wherein the liquid bromine is vaporized. The mixture of lower molecular weight alkanes and dry bromine vapor is fed to reactor 230 . Preferably, the molar ratio of lower molecular weight alkanes to dry bromine vapor in the mixture introduced into reactor 230 is in excess of 2.5:1. Reactor 230 has an inlet pre-heater zone 228 which heats the mixture to a reaction initiation temperature in the range of 250° C. to 400° C. In first reactor 230 , the lower molecular weight alkanes are reacted exothermically with dry bromine vapor at a relatively low temperature in the range of about 250° C. to about 600° C., and at a pressure in the range of about 1 bar to about 30 bar to produce gaseous alkyl bromides and hydrobromic acid vapors. The upper limit of the operating temperature range is greater than the upper limit of the reaction initiation temperature range to which the feed mixture is heated due to the exothermic nature of the bromination reaction. In the case of methane, the formation of methyl bromide occurs in accordance with the following general reaction: CH 4 ( g )+Br 2 ( g )→CH 3 Br( g )+HBr( g ) This reaction occurs with a significantly high degree of selectivity to methyl bromide. For example, in the case of bromine reacting with a molar excess of methane at a methane to bromine ratio of 4.5:1, selectivity to the mono-halogenated methyl bromide is in the range of 90 to 95%. Small amounts of dibromomethane and tribromomethane are also formed in the bromination reaction. Higher alkanes, such as ethane, propane and butane, are also readily bromoninated resulting in mono and multiple brominated species. If an alkane to bromine ratio of significantly less than 2.5 to 1 is utilized, selectivity to methyl bromide substantially lower than 90% occurs and significant formation of undesirable carbon soot is observed. It has also been shown that other alkanes such as ethane and propane which may be present in the feed gas to the bromination are readily brominated to form ethyl bromides and propyl bromides. Further, the dry bromine vapor that is fed into first reactor 230 is substantially water-free. Applicant has discovered that elimination of substantially all water vapor from the bromination step in first reactor 230 substantially eliminates the formation of unwanted carbon dioxide thereby increasing the selectivity of alkane bromination to alkyl bromides and eliminating the large amount of waste heat generated in the formation of carbon dioxide from alkanes. The effluent that contains alkyl bromides and hydrobromic acid is withdrawn from the first reactor 230 via line 231 and is partially cooled to a temperature in the range of about 150° C. to 350° C. in heat exchanger 232 before flowing to a second reactor 234 . In second reactor 234 , the alkyl bromides are reacted exothermically at a temperature range of from about 150° C. to about 450° C., and a pressure in the range of about 1 bar to 30 bar, over a fixed bed of crystalline alumino-silicate catalyst, preferably a zeolite catalyst, and most preferably a ZSM-5 zeolite catalyst. Although the zeolite catalyst is preferably used in the hydrogen, sodium or magnesium form, the zeolite may also be modified by ion exchange with other alkali metal cations, such as Li, K, Na or Cs, with alkali-earth metal cations, such as Mg, Ca, Sr or Ba, with transition metal cations, such as Ni, Mn, V, W, or to the hydrogen form. Other zeolite catalysts having varying pore sizes and acidities, which are synthesized by varying the alumina-to-silica ratio may be used in the second reactor 234 as will be evident to a skilled artisan. In this reactor, the alkyl bromides are oligomerized to produce a mixture of higher molecular weight hydrocarbon products and additional hydrobromic acid vapor. The temperature at which the second reactor 234 is operated is an important parameter in determining the selectivity of the oligomerization reaction to various higher molecular weight liquid hydrocarbon products. It is preferred to operate second reactor 234 at a temperature within the range of about 150° C. to about 450° C., but more preferably within the range of about 300° C. to about 400° C. Temperatures above about 300° C. in the second reactor result in increased yields of light hydrocarbons, such as undesirable methane, whereas lower temperatures increase yields of heavier molecular weight hydrocarbon products. At the low end of the temperature range, methyl bromide reacting over ZSM-5 zeolite at temperatures as low as about 150° C. significant methyl bromide conversion on the order of 20% is noted, with a high selectivity towards C 5 + products. Notably, in the case of alkyl bromides reacting over the preferred ZSM-5 zeolite catalyst, cyclization reactions occur such that the C 7 + fractions produced contain a high percentage of substituted aromatics. At increasing temperatures approaching about 300° C., methyl bromide conversion increases towards 90% or greater, however selectivity towards C 5 + products decreases and selectivity towards lighter products, particularly undesirable methane, increases. Surprisingly, very little ethane or C 2 -C 4 olefin compounds are produced. At temperatures approaching about 450° C. almost complete conversion of methyl bromide to methane occurs. In the optimum temperature range of about 300° C. to about 400° C., as a byproduct of the reaction, a small amount of carbon will build up on the catalyst over time during operation, causing a decline in catalyst activity over a range of hours to several hundred hours, depending on the reaction conditions and feed gas composition. It is believed that higher reaction temperatures over about 400° C. favor the formation of carbon and hence rate of deactivation of the catalyst. Conversely, operation at the lower end of the temperature range, particularly below about 300° C. may also promote coking, likely to the reduced rate of desorption of hydrocarbon products. Hence, operating temperatures within the range of about 150° C. to about 400° C., but more preferably in the range of about 300° C. to about 400° C., in the second reactor 234 balance increased selectivity towards the desired products and lower rates of deactivation due to carbon formation, against higher conversion per pass, which minimizes the quantity of catalyst, recycle rates and equipment size required. The catalyst may be periodically regenerated in situ, by isolating reactor 234 from the normal process flow, purging with an inert gas via line 270 at a pressure in a range from about 1 to about 5 bar at an elevated temperature in the range of about 400° C. to about 650° C. to remove unreacted material adsorbed on the catalyst insofar as is practical, and then subsequently oxidizing the deposited carbon to CO 2 by addition of air or inert gas-diluted oxygen via line 270 to reactor 234 at a pressure in the range of about 1 bar to about 5 bar at an elevated temperature in the range of about 400° C. to about 650° C. Carbon dioxide and residual air or inert gas is are vented from reactor 234 via line 275 during the regeneration period. The effluent which comprises the higher molecular weight hydrocarbon products and hydrobromic acid is withdrawn from the second reactor 234 via line 235 and cooled to a temperature in the range of about 100° C. to about 600° C. in exchanger 236 . As illustrated in FIG. 9A , the cooled effluent is transported via lines 235 and 241 with valve 238 in the opened position and valves 239 and 243 in the closed position and introduced into a vessel or reactor 240 containing a bed 298 of a solid phase metal oxide. The metal of the metal oxide is selected form magnesium (Mg), calcium (Ca), vanadium (V), chromium (Cr), manganese (Mn), iron (Fe), cobalt (Co), nickel (Ni), copper (Cu), zinc (Zn), or tin (Sn). The metal is selected for the impact of its physical and thermodynamic properties relative to the desired temperature of operation, and also for potential environmental and health impacts and cost. Preferably, magnesium, copper and iron are employed as the metal, with magnesium being the most preferred. These metals have the property of not only forming oxides but bromide salts as well, with the reactions being reversible in a temperature range of less than about 500° C. The solid metal oxide is preferably immobilized on a suitable attrition-resistant support, for example a synthetic amorphous silica, such as Davicat Grade 57 , manufactured by Davison Catalysts of Columbia, Maryland. In reactor 240 , hydrobromic acid is reacted with the metal oxide at temperatures below about 600° C. and preferably between about 300° C. to about 500° C. in accordance with the following general formula wherein M represents the metal: 2HBr+MO→MBr 2 +H 2 O The steam resulting from this reaction is transported together with the high molecular hydrocarbon products in line 244 , 218 and 216 via opened valve 219 to heat exchanger 220 wherein the mixture is cooled to a temperature in the range of about 0° C. to about 70° C. This cooled mixture is forwarded to dehydrator 250 to remove substantially all water from the gas stream. The water is then removed from the dehydrator 250 via line 253 . The dried gas stream containing the higher molecular weight hydrocarbon products is further passed via line 251 to product recovery unit 252 to recover C 3 and C 4 as desired, but primarily the C 5 + fraction as a liquid product in line 254 . Any conventional method of dehydration and liquids recovery such as solid-bed dessicant adsorption followed by, for example, refrigerated condensation, cryogenic expansion, or circulating absorption oil, as used to process natural gas or refinery gas streams, as known to a skilled artisan, may be employed in the implementation of this invention. The residual vapor effluent from product recovery unit 252 is then split into a purge stream 257 that may be utilized as fuel for the process and a recycled residual vapor which is compressed via compressor 258 . The recycled residual vapor discharged from compressor 258 is split into two fractions. A first fraction that is equal to at least 1.5 times the feed gas volume is transported via line 262 , combined with the liquid bromine and feed gas conveyed in line 225 and passed to heat exchanger 226 wherein the liquid bromine is vaporized and fed into first reactor 230 in a manner as described above. The second fraction which is drawn off line 262 via line 263 and is regulated by control valve 260 , at a rate sufficient to dilute the alkyl bromide concentration to reactor 234 and absorb the heat of reaction such that reactor 234 is maintained at the selected operating temperature, preferably in the range of about 300° C. to about 400° C. in order to optimize conversion vs. selectivity and to minimize the rate of catalyst deactivation due to the deposition of carbon. Thus, the dilution provided by the recycled vapor effluent permits selectivity of bromination in the first reactor 230 to be controlled in addition to moderating the temperature in second reactor 234 . Oxygen, oxygen enriched air or air 210 is delivered via blower or compressor 213 at a pressure in the range of about ambient to about 10 bar to bromine via line 214 , line 215 and valve 249 through heat exchanger 215 , wherein oxygen, oxygen enriched air or air is preheated to a temperature in the range of about 100° C. to about 500° C. to a second vessel or reactor 246 containing a bed 299 of a solid phase metal bromide. Oxygen reacts with the metal bromide in accordance with the following general reaction wherein M represents the metal: MBr 2 +½O 2 →MO+Br 2 In this manner, a dry, substantially HBr free bromine vapor is produced thereby eliminating the need for subsequent separation of water or hydrobromic acid from the liquid bromine. Reactor 246 is operated below 600° C., and more preferably between about 300° C. to about 500° C. The resultant bromine vapor is transported from reactor 246 via line 247 , valve 248 and line 242 to heat exchanger or condenser 221 where the bromine is condensed into a liquid. The liquid bromine is transported via line 242 to separator 222 wherein liquid bromine is removed via line 225 and transported via line 225 to heat exchanger 226 and first reactor 230 by any suitable means, such as by pump 224 . The residual air or unreacted oxygen is transported from separator 222 via line 227 to a bromine scrubbing unit 223 , such as venturi scrubbing system containing a suitable solvent, or suitable solid adsorbant medium, as selected by a skilled artisan, wherein the remaining bromine is captured. The captured bromine is desorbed from the scrubbing solvent or adsorbant by heating or other suitable means and the thus recovered bromine transported via line 212 to line 225 . The scrubbed air or oxygen is vented via line 229 . In this manner, nitrogen and any other substantially non-reactive components are removed from the system of the present invention and thereby not permitted to enter the hydrocarbon-containing portion of the process; also loss of bromine to the surrounding environment is avoided. One advantage of removing the HBr by chemical reaction in accordance with this embodiment, rather than by simple physical solubility, is the substantially complete scavenging of the HBr to low levels at higher process temperatures. Another distinct advantage is the elimination of water from the bromine removed thereby eliminating the need for separation of bromine and water phases and for stripping of residual bromine from the water phase. Reactors 240 and 246 may be operated in a cyclic fashion. As illustrated in FIG. 9A , valves 238 and 219 are operated in the open mode to permit hydrobromic acid to be removed from the effluent that is withdrawn from the second reactor 234 , while valves 248 and 249 are operated in the open mode to permit air, oxygen enriched air or oxygen to flow through reactor 246 to oxidize the solid metal bromide contained therein. Once significant conversion of the metal oxide and metal bromide in reactors 240 and 246 , respectively, has occurred, these valves are closed. At this point, bed 299 in reactor 246 is a bed of substantially solid metal bromide, while bed 298 in reactor 240 is substantially solid metal oxide. As illustrated in FIG. 10A , valves 245 and 243 are then opened to permit oxygen, oxygen enriched air or air to flow through reactor 240 to oxidize the solid metal bromide contained therein, while valves 239 and 217 are opened to permit effluent which comprises the higher molecular weight hydrocarbon products and hydrobromic acid that is withdrawn from the second reactor 234 to be introduced into reactor 246 . The reactors are operated in this manner until significant conversion of the metal oxide and metal bromide in reactors 246 and 240 , respectively, has occurred and then the reactors are cycled back to the flow schematic illustrated in FIG. 9A by opening and closing valves as previously discussed. When oxygen is utilized as the oxidizing gas transported in via line 210 to the reactor being used to oxidize the solid metal bromide contained therein, the embodiment of the process of the present invention illustrated in FIGS. 9A and 10A can be modified such that the bromine vapor produced from either reactor 246 ( FIG. 9B ) or 240 ( FIG. 10B ) is transported via lines 242 and 225 directly to first reactor 230 . Since oxygen is reactive and will not build up in the system, the need to condense the bromine vapor to a liquid to remove unreactive components, such as nitrogen, is obviated. Compressor 213 is not illustrated in FIGS. 9B and 10B as substantially all commercial sources of oxygen, such as a commercial air separator unit, will provide oxygen to line 210 at the required pressure. If not, a compressor 213 could be utilized to achieve such pressure as will be evident to a skilled artisan. In the embodiment of the present invention illustrated in FIG. 11A , the beds of solid metal oxide particles and solid metal bromide particles contained in reactors 240 and 246 , respectively, are fluidized and are connected in the manner described below to provide for continuous operation of the beds without the need to provide for equipment, such as valves, to change flow direction to and from each reactor. In accordance with this embodiment, the effluent which comprises the higher molecular weight hydrocarbon products and hydrobromic acid is withdrawn from the second reactor 234 via line 235 , cooled to a temperature in the range of about 100° C. to about 500° C. in exchanger 236 , and introduced into the bottom of reactor 240 which contains a bed 298 of solid metal oxide particles. The flow of this introduced fluid induces the particles in bed 298 to move upwardly within reactor 240 as the hydrobromic acid is reacted with the metal oxide in the manner as described above with respect to FIG. 9A . At or near the top of the bed 298 , the particles which contain substantially solid metal bromide on the attrition-resistant support due to the substantially complete reaction of the solid metal oxide with hydrobromic acid in reactor 240 are withdrawn via a weir or cyclone or other conventional means of solid/gas separation, flow by gravity down line 259 and are introduced at or near the bottom of the bed 299 of solid metal bromide particles in reactor 246 . In the embodiment illustrated in FIG. 11A , oxygen, oxygen enriched air or air 210 is delivered via blower or compressor 213 at a pressure in the range of about ambient to about 10 bar, transported via line 214 through heat exchanger 215 , wherein the oxygen, oxygen enriched air or air is preheated to a temperature in the range of about 100° C. to about 500° C. and introduced into second vessel or reactor 246 below bed 299 of a solid phase metal bromide. Oxygen reacts with the metal bromide in the manner described above with respect to FIG. 9A to produce a dry, substantially HBr free bromine vapor. The flow of this introduced gas induces the particles in bed 299 to flow upwardly within reactor 246 as oxygen is reacted with the metal bromide. At or near the top of the bed 298 , the particles which contain substantially solid metal oxide on the attrition-resistant support due to the substantially complete reaction of the solid metal bromide with oxygen in reactor 246 are withdrawn via a weir or cyclone or other conventional means of solid/gas separation, flow by gravity down line 264 and are introduced at or near the bottom of the bed 298 of solid metal oxide particles in reactor 240 . In this manner, reactors 240 and 246 can be operated continuously without changing the parameters of operation. In the embodiment illustrated in FIG. 11B , oxygen is utilized as the oxidizing gas and is transported in via line 210 to reactor 246 . Accordingly, the embodiment of the process of the present invention illustrated in FIG. 11A is modified such that the bromine vapor produced from reactor 246 is transported via lines 242 and 225 directly to first reactor 230 . Since oxygen is reactive and will not build up in the system, the need to condense the bromine vapor to a liquid to remove unreactive components, such as nitrogen, is obviated. Compressor 213 is not illustrated in FIG. 11B as substantially all commercial sources of oxygen, such as a commercial air separator unit, will provide oxygen to line 210 at the required pressure. If not, a compressor 213 could be utilized to achieve such pressure as will be evident to a skilled artisan. In accordance with another embodiment of the process of the present invention that is illustrated in FIG. 12 , the alkyl bromination and alkyl bromide conversion stages are operated in a substantially similar manner to those corresponding stages described in detail with respect to FIG. 9A except as discussed below. Residual air or oxygen and bromine vapor emanating from reactor 246 is transported via line 247 , valve 248 and line 242 and valve 300 to heat exchanger or condenser 221 wherein the bromine-containing gas is cooled to a temperature in the range of about 30° C. to about 300° C. The bromine-containing vapor is then transported via line 242 to vessel or reactor 320 containing a bed 322 of a solid phase metal bromide in a reduced valence state. The metal of the metal bromide in a reduced valence state is selected from copper (Cu), iron (Fe), or molybdenum (Mo). The metal is selected for the impact of its physical and thermodynamic properties relative to the desired temperature of operation, and also for potential environmental and health impacts and cost. Preferably, copper or iron are employed as the metal, with copper being the most preferred. The solid metal bromide is preferably immobilized on a suitable attrition-resistant support, for example a synthetic amorphous silica, such as Davicat Grade 57, manufactured by Davison Catalysts of Columbia, Md. In reactor 320 , bromine vapor is reacted with the solid phase metal bromide, preferably retained on a suitable attrition-resistant support at temperatures below about 300° C. and preferably between about 30° C. to about 200° C. in accordance with the following general formula wherein M 2 represents the metal: 2M 2 Br n +Br 2 →2M 2 Br n+1 In this manner, bromine is stored as a second metal bromide, i.e. 2M 2 Br n+1 , in reactor 320 while the resultant vapor containing residual air or oxygen is vented from reactor 320 via line 324 , valve 326 and line 318 . The gas stream containing lower molecular weight alkanes, comprised of mixture of a feed gas (line 211 ) and a recycled gas stream, is transported or conveyed via line 262 , heat exchanger 352 , wherein the gas stream is preheated to a temperature in the range of about 150° C. to about 600° C., valve 304 and line 302 to a second vessel or reactor 310 containing a bed 312 of a solid phase metal bromide in an oxidized valence state. The metal of the metal bromide in an oxidized valence state is selected from copper (Cu), iron (Fe), or molybdenum (Mo). The metal is selected for the impact of its physical and thermodynamic properties relative to the desired temperature of operation, and also for potential environmental and health impacts and cost. Preferably, copper or iron are employed as the metal, with copper being the most preferred. The solid metal bromide in an oxidized state is preferably immobilized on a suitable attrition-resistant support, for example a synthetic amorphous silica such as Davicat Grade 57, manufactured by Davison Catalysts of Columbia, Md. The temperature of the gas stream is from about 150° C. to about 600° C., and preferably from about 200° C. to about 450° C. In second reactor 310 , the temperature of the gas stream thermally decomposes the solid phase metal bromide in an oxidized valence state to yield elemental bromine vapor and a solid metal bromide in a reduced state in accordance with the following general formula wherein M 2 represents the metal: 2M 2 Br n+1 →2M 2 Br n +Br 2 The resultant bromine vapor is transported with the gas stream containing lower molecular weight alkanes via lines 314 , 315 , valve 317 , line 330 , heat exchanger 226 prior to being introduced into alkyl bromination reactor 230 . Reactors 310 and 320 may be operated in a cyclic fashion. As illustrated in FIG. 12 , valve 304 is operated in the open mode to permit the gas stream containing lower molecular weight alkanes to be transported to the second reactor 310 , while valve 317 is operated in the open mode to permit this gas stream with bromine vapor that is generated in reactor 310 to be transported to alkyl bromination reactor 230 . Likewise, valve 306 is operated in the open mode to permit bromine vapor from reactor 246 to be transported to reactor 320 , while valve 326 is operated in the open mode to permit residual air or oxygen to be vented from reactor 320 . Once significant conversion of the reduced metal bromide and oxidized metal bromide in reactors 320 and 310 , respectively, to the corresponding oxidized and reduced states has occurred, these valves are closed as illustrated in FIG. 13 . At this point, bed 322 in reactor 320 is a bed of substantially metal bromide in an oxidized state, while bed 312 in reactor 310 is substantially metal bromide in a reduced state. As illustrated in FIG. 13 , valves 304 , 317 , 306 and 326 are closed, and then valves 308 and 332 are opened to permit the gas stream containing lower molecular weight alkanes to be transported or conveyed via lines 262 , heat exchanger 352 , wherein gas stream is heated to a range of about 150° C. to about 600° C., valve 308 and line, 309 to reactor 320 to thermally decompose the solid phase metal bromide in an oxidized valence state to yield elemental bromine vapor and a solid metal bromide in a reduced state. Valve 332 is also opened to permit the resultant bromine vapor to be transported with the gas stream containing lower molecular weight alkanes via lines 324 and 330 and heat exchanger 226 prior to being introduced into alkyl bromination reactor 230 . In addition, valve 300 is opened to permit. bromine vapor emanating from reactor 246 to be transported via line 242 through exchanger 221 into reactor 310 wherein the solid phase metal bromide in a reduced valence state reacts with bromine to effectively store bromine as a metal bromide. In addition, valve 316 is opened to permit the resulting gas, which is substantially devoid of bromine to be vented via lines 314 and 318 . The reactors are operated in this manner until significant conversion of the beds of reduced metal bromide and oxidized metal bromide in reactors 310 and 320 , respectively, to the corresponding oxidized and reduced states has occurred and then the reactors are cycled back to the flow schematic illustrated in FIG. 12 by opening and closing valves as previously discussed. In the embodiment of the present invention illustrated in FIG. 14 , the beds 312 and 322 contained in reactors 310 and 320 , respectively, are fluidized and are connected in the manner described below to provide for continuous operation of the beds without the need to provide for equipment, such as valves, to change flow direction to and from each reactor. In accordance with this embodiment, the bromine-containing gas withdrawn from the reactor 246 via line 242 is cooled to a temperature in the range of about 30° C. to about 300° C. in exchangers 370 and 372 , and introduced into the bottom of reactor 320 which contains a moving solid bed 322 in a fluidized state. The flow of this introduced fluid induces the particles in bed 322 to flow upwardly within reactor 320 as the bromine vapor is reacted with the reduced metal bromide entering the bottom of bed 322 in the manner as described above with respect to FIG. 12 . At or near the top of the bed 322 , the particles which contain substantially oxidized metal bromide on the attrition-resistant support due to the substantially complete reaction of the reduced metal bromide with bromine vapor in reactor 320 are withdrawn via a weir, cyclone or other conventional means of solid/gas separation, flow by gravity down line 359 and are introduced at or near the bottom of the bed 312 in reactor 310 . In the embodiment illustrated in FIG. 14 , the gas stream containing lower molecular weight alkanes, comprised of mixture of a feed gas (line 211 ) and a recycled gas stream, is transported or conveyed via line 262 and heat exchanger 352 wherein the gas stream is heated to a range of about 150° C. to about 600° C. and introduced into reactor 310 . The heated gas stream thermally decomposes the solid phase metal bromide in an oxidized valence state present entering at or near the bottom of bed 312 to yield elemental bromine vapor and a solid metal bromide in a reduced state. The flow of this introduced gas induces the particles in bed 312 to flow upwardly within reactor 310 as the oxidized metal bromide is thermally decomposed. At or near the top of the bed 312 , the particles which contain substantially reduced solid metal bromide on the attrition-resistant support due to the substantially complete thermal decomposition in reactor 310 are withdrawn via a weir or cyclone or other conventional means of gas/solid separation and flow by gravity down line 364 and introduced at or near the bottom of the bed 322 of particles in reactor 310 . In this manner, reactors 310 and 320 can be operated continuously with changing the parameters of operation. The process of the present invention is less expensive than conventional processes since it operates at low pressures in the range of about 1 bar to about 30 bar and at relatively low temperatures in the range of about 20° C. to about 600° C. for the gas phase, and preferably about 20° C. to about 180° C. for the liquid phase. These operating conditions permit the use of less expensive equipment of relatively simple design that are constructed from readily available metal alloys for the gas phase and polymer-lined vessels, piping and pumps for the liquid phase. The process of the present invention is also more efficient because less energy is required for operation and the production of excessive carbon dioxide as an unwanted byproduct is minimized. The process is capable of directly producing a mixed hydrocarbon product containing various molecular-weight components in the liquefied petroleum gas (LPG) and motor gasoline fuels range that have substantial aromatic content thereby significantly increasing the octane value of the gasoline-range fuel components. While the foregoing preferred embodiments of the invention have been described and shown, it is understood that the alternatives and modifications, such as those suggested and others, may be made thereto and fall within the scope of the invention.

Description

Topics

Download Full PDF Version (Non-Commercial Use)

Patent Citations (836)

    Publication numberPublication dateAssigneeTitle
    US-3670037-AJune 13, 1972Exxon Research Engineering CoCatalyst system
    US-5013793-AMay 07, 1991Exxon Chemical Patents Inc.Dynamically cured thermoplastic olefin polymers and process for producing the same
    US-7244867-B2July 17, 2007Marathon Oil CompanyProcess for converting gaseous alkanes to liquid hydrocarbons
    US-5399258-AMarch 21, 1995Mobil Oil CorporationHydrocarbon upgrading process
    US-6821924-B2November 23, 2004Dow Global Technologies Inc.Oxyhalogenation process using catalyst having porous rare earth halide support
    US-5233113-AAugust 03, 1993Catalytica, Inc.Process for converting lower alkanes to esters
    US-2005215837-A1September 29, 2005Shell Oil CompanyThe utilization of zirconium and zirconium based alloys for the containment of halogen containing environments used in the production of olefins, alcohols, ethers, and olefin oxides from alkanes
    US-5316995-AMay 31, 1994Amoco CorporationHydrocarbon conversion catalyst
    US-5043502-AAugust 27, 1991UopProduction of xylenes from light aliphatic hydrocarbons via dehydrocyclodimerization and methylation
    US-6825307-B2November 30, 2004Promerus, LlcCatalyst and methods for polymerizing cycloolefins
    US-5223471-AJune 29, 1993Amoco CorporationFluorine-containing materials
    US-5055625-AOctober 08, 1991Fred NeidifferGasoline additive composition and method for using same
    US-6380328-B1April 30, 2002Univation Technologies, LlcCatalyst systems and their use in a polymerization process
    US-2007149837-A1June 28, 2007Chevron U.S.A. Inc.Oxygenate conversion using molecular sieve ssz-74
    US-6514319-B2February 04, 2003Questair Technologies Inc.Life support oxygen concentrator
    US-4443620-AApril 17, 1984The Lummus CompanyProduction of epoxy compounds from olefinic compounds
    US-4282159-AAugust 04, 1981Wisconsin Alumni Research FoundationPreparation of alkylene oxides
    US-4347391-AAugust 31, 1982Stauffer Chemical CompanyProcess for preparing ethylene dichloride
    US-5609654-AMarch 11, 1997Mobil Oil CorporationProcess for hydroisomerization and etherification of isoalkenes
    US-4690903-ASeptember 01, 1987Mobil Oil CorporationProcess for preparing organic fuels and chemicals from biomass
    US-4433192-AFebruary 21, 1984Olah George ACondensation of natural gas or methane into gasoline range hydrocarbons
    US-6525228-B2February 25, 2003Celanese Chemicals Europe GmbhProcess of telomerizing conjugated dienes
    US-4704493-ANovember 03, 1987Chevron CorporationConversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a metal compound-containing catalyst (II-A)
    US-7196239-B2March 27, 2007Exxonmobil Chemical Patents Inc.Methanol and ethanol production for an oxygenate to olefin reaction system
    US-7161050-B2January 09, 2007Grt, Inc., The Regents Of The University Of CaliforniaMethod and apparatus for synthesizing olefins, alcohols, ethers, and aldehydes
    US-7348295-B2March 25, 2008Chevron CorporationGas separation using molecular sieve SSZ-74
    US-5132343-AJuly 21, 1992Basf AktiengesellschaftLow-evaporation polyester resins
    US-6248218-B1June 19, 2001Clovis A. Linkous, Nazim Z. MuradovClosed cycle photocatalytic process for decomposition of hydrogen sulfide to its constituent elements
    US-4808763-AFebruary 28, 1989Amoco CorporationProcess for upgrading light paraffins
    US-6093306-AJuly 25, 2000Solar Reactor Technologies Inc.Comprehensive system for utility load leveling, hydrogen production, stack gas cleanup, greenhouse gas abatement, and methanol synthesis
    US-4489210-ADecember 18, 1984Bayer AktiengesellschaftProcess for the halogenation of organic compounds
    US-3172915-AMarch 09, 1965Preparation of oxygenated methane derivatives
    US-4804797-AFebruary 14, 1989Gas Research InstituteProduction of commodity chemicals from natural gas by methane chlorination
    US-5406017-AApril 11, 1995Atlantic Richfield CompanyMethane conversion process
    US-5510525-AApril 23, 1996Gas Research InstituteDirect catalytic oxidative carbonylation of lower alkanes to acids
    US-6072091-AJune 06, 2000Institut Francais Du PetroleProcess for selective hydrogenation of a hydrocarbon cut containing at least three carbon atoms
    US-4467130-AAugust 21, 1984Olah George ACondensation of natural gas or methane into gasoline-range hydrocarbons
    US-4311865-AJanuary 19, 1982Mobil Oil CorporationManufacture of hydrocarbons from oxygenates
    WO-2006083427-A2August 10, 2006John Lee MassingillUtilisation de reacteurs de film de fibre pour effectuer la separation et la reaction entre deux composants de reaction non miscibles
    US-5744669-AApril 28, 1998UopProcess for the conversion of a halogenated organic stream containing trace quantities of organic nitrates
    US-6482997-B2November 19, 2002Institut Francais Du PetroleConversion reactions for organic compounds
    US-6518476-B1February 11, 2003Union Carbide Chemicals & Plastics Technology CorporationMethods for manufacturing olefins from lower alkans by oxidative dehydrogenation
    US-6465696-B1October 15, 2002Grt, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols, ethers, and olefins from alkanes
    US-7067448-B1June 27, 2006Veba Oil Refining And Petrochemicals GmbhMethod for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method
    US-2004171779-A1September 02, 2004Carnegie Mellon University (A Non-Profit Pennsylvania Organization)Catalytic processes for the controlled polymerization of free radically (Co)polymerizable monomers and functional polymeric systems prepared thereby
    US-4197420-AApril 08, 1980Sebastiano Cesca, Giuseppe Ferraris, Aldo PriolaMethod for producing oligomers from straight-chain alpha olefins, subsequently hydrogenating such oligomers and saturated products so obtained
    US-2006288690-A1December 28, 2006Chevron U.S.A. Inc.Treatment of engine exhaust using molecular sieve SSZ-56
    US-3291708-ADecember 13, 1966IonicsElectrolytic process for producing a halogen from its respective acid and the apparatus therefor
    US-5382744-AJanuary 17, 1995Phillips Petroleum CompanyControl of synthetic isopentane production during alkylation of amylenes
    US-5444168-AAugust 22, 1995Mobil Oil CorporationProcess for the production of symmetrical ethers from secondary alcohols
    US-2007197847-A1August 23, 2007Yumin LiuNi catalysts and methods for alkane dehydrogenation
    US-5334777-AAugust 02, 1994Energia Andina Ltd.Conversion of alkanes to alkanols and glycols
    US-6672572-B2January 06, 2004L'air Liquide - Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes Georges ClaudePacked column for exchanging heat and/or mass
    US-4633027-ADecember 30, 1986Mobil Oil CorporationProcess for converting olefins to gasoline, distillate and alkylate liquid hydrocarbons
    US-5998686-ADecember 07, 1999Exxon Chemical Patents Inc.Process for producing aromatic compounds from aliphatic hydrocarbons
    US-7045670-B2May 16, 2006Synfuels International, Inc.Process for liquid phase hydrogenation
    US-4270929-AJune 02, 1981Institut Francais Du PetroleProcess for producing gasoline of high octane number, in particular lead-free gasoline
    US-6765120-B2July 20, 2004Exxonmobil Chemical Patents Inc.Selective production of meta-diisopropylbenzene
    US-4440871-AApril 03, 1984Union Carbide CorporationCrystalline silicoaluminophosphates
    US-5354931-AOctober 11, 1994UopProcess for hydrotreating an organic feedstock containing oxygen compounds and a halogen component
    US-5071449-ADecember 10, 1991Air Products And Chemicals, Inc.Gas separation by rapid pressure swing adsorption
    EP-1235772-B1January 19, 2005Dow Global Technologies, Inc.Verfahren zur umwandlung von ethylen zu vinylchlorid und katalysatorzusammensetzungen verwendbar für solches verfahren
    US-4513092-AApril 23, 1985Mobil Oil CorporationComposite catalyst for halogenation and condensation of alkanes
    US-5284990-AFebruary 08, 1994Stratco, Inc.Method for converting a hydrogen fluoride alkylation unit to a sulfuric acid alkylation unit
    US-5525230-AJune 11, 1996Thames Water Utilities LimitedProcess of and apparatus for treating a fluid
    US-2246082-AJune 17, 1941Shell DevPreparation of alkyl halides
    US-4550218-AOctober 29, 1985Mobil Oil CorporationHydrocarbon synthesis with zeolite catalyst of improved hydrothermal stability
    US-2008188697-A1August 07, 2008Grt, Inc.Hydrocarbon synthesis
    US-5276226-AJanuary 04, 1994Exxon Research & Engineering CompanyLow temperature halogenation of alkanes
    US-4655893-AApril 07, 1987Battelle Development CorporationCubic boron nitride preparation utilizing a boron and nitrogen bearing gas
    US-5175382-ADecember 29, 1992Werner Hebgen, Gerd Krome, Erhard StahneckerPreparation of 1,2-Dichloroethane
    US-7138534-B2November 21, 2006Dow Global Technologies Inc.Process for the continuous production of an olefinic oxide
    US-4389391-AJune 21, 1983Dunn Jr Wendell EProcess for beneficiating titaniferous ores
    CA-2542857-A1May 12, 20053M Innovative Properties Company, Markus A. Wicki, Kent E. NielsenProcess for preparing functional group-containing olefinic compounds
    US-4088706-AMay 09, 1978Mobil Oil CorporationMethanol conversion to para-xylene using a zeolite catalyst containing an oxide of boron, magnesium, phosphorus, or mixtures
    US-3816599-AJune 11, 1974Lummus CoHydrogen chloride recovery
    US-4599474-AJuly 08, 1986Chevron Research CompanyConversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a metal-containing catalyst
    US-6127588-AOctober 03, 2000Phillips Petroleum CompanyHydrocarbon hydrogenation catalyst and process
    US-2007148086-A1June 28, 2007Chevron U.S.A. Inc.Molecular sieve ssz-74 composition of matter and synthesis thereof
    US-4317943-AMarch 02, 1982Texaco Inc.Process for preparing glycol ethers
    US-6018088-AJanuary 25, 2000Olah; George A.Superacid catalyzed formylation-rearrangement of saturated hydrocarbons
    US-4540826-ASeptember 10, 1985Phillips Petroleum CompanyProcess for preparing olefinic aldehydes
    US-6087294-AJuly 11, 2000Kansas State University Research FoundationDispersion and stabilization of reactive atoms on the surface of metal oxides
    US-6852896-B2February 08, 2005John E. StaufferConcerted process for the production of an alkenyl substituted aromatic compound
    US-5814715-ASeptember 29, 1998Exxon Chemical Patents IncAmorphous olefin polymers, copolymers, methods of preparation and derivatives thereof
    US-6710213-B2March 23, 2004Showa Denko K.K.Production process and use for propargyl alcohol and its intermediate
    US-4467133-AAugust 21, 1984Mobil Oil CorporationConversion of alcohols and ethers to distillate range hydrocarbons
    US-3920764-ANovember 18, 1975Lummus CoDehydrogenation process
    US-5486627-AJanuary 23, 1996The Dow Chemical CompanyMethod for producing epoxides
    US-6903171-B2June 07, 2005Promerus, LlcPolymerized cycloolefins using transition metal catalyst and end products thereof
    US-4588835-AMay 13, 1986Otsuka Kagaku Yakuhin Kabushiki KaishaProcess for preparing alkoxyphenols
    US-6187983-B1February 13, 2001Exxon Chemical Patents IncConverting oxygenates to olefins in the presence of electromagnetic energy
    US-2007149824-A1June 28, 2007Chevron U.S.A. Inc.Acylation using molecular sieve ssz-74
    US-4462814-AJuly 31, 1984Koch Process Systems, Inc.Distillative separations of gas mixtures containing methane, carbon dioxide and other components
    US-4129604-ADecember 12, 1978The Lummus CompanyReactor effluent quench system
    US-6130260-AOctober 10, 2000The Texas A&M University SystemsMethod for converting natural gas to liquid hydrocarbons
    US-7176340-B2February 13, 2007Albemarle Netherlands B.V.Continuous process for the alkylation of hydrocarbons
    US-5969195-AOctober 19, 1999Basf AktiengesellschaftHydrolysis of alkyl monohalides
    US-5055235-AOctober 08, 1991Ethyl CorporationBromination process
    US-4219680-AAugust 26, 1980Hoechst AktiengesellschaftProcess for obtaining pure 2-(perfluoroalkyl)-ethanols from their mixtures with 2-(perfluoroalkyl)-ethylenes and possibly 2-(perfluoroalkyl)-ethyl esters
    US-4249031-AFebruary 03, 1981Shell Oil CompanyProcess for the preparation of a hydrocarbon mixture
    US-6096933-AAugust 01, 2000Phillips Petroleum CompanyHydrocarbon hydrogenation and catalyst therefor
    US-5464799-ANovember 07, 1995Imperial Chemical Industries PlcZeolite NU-85 catalyst
    US-3965205-AJune 22, 1976Mobil Oil CorporationConversion of low octane hydrocarbons to high octane gasoline
    US-7348464-B2March 25, 2008Marathon Oil CompanyProcess for converting gaseous alkanes to liquid hydrocarbons
    US-4039600-AAugust 02, 1977Mobil Oil CorporationConversion of synthesis gas to aromatic hydrocarbons
    US-5160502-ANovember 03, 1992Phillips Petroleum CompanyComposition of matter and method of oxidative conversion of organic compounds therewith
    US-5108579-AApril 28, 1992Imperial Chemical Industries PlcZeolites
    US-4025571-AMay 24, 1977Mobil Oil CorporationManufacture of hydrocarbons
    US-4499314-AFebruary 12, 1985Imperial Chemical Industries PlcMethanol conversion to hydrocarbons with zeolites and cocatalysts
    US-4025575-AMay 24, 1977Mobil Oil CorporationProcess for manufacturing olefins
    US-6472345-B2October 29, 2002Solvias AgCatalytic halogenation of activated methylene and methine compounds
    US-4513164-AApril 23, 1985Olah George ACondensation of natural gas or methane into gasoline range hydrocarbons
    US-7230151-B2June 12, 2007Exxonmobil Chemical Patents Inc.Two catalyst process for making olefin
    US-4156698-AMay 29, 1979Mobil Oil CorporationConversion of alcohols or ethers using rare earth crystalline aluminosilicate in an alumina matrix
    US-3379506-AApril 23, 1968Kali Chemie AgBromine recovery
    US-4795737-AJanuary 03, 1989Eastman Kodak CompanyProcess for the iodination of aromatic compounds over solid catalysts
    US-6831032-B2December 14, 2004Novolen Technology Holdings C.V.Ziegler-Natta catalyst and methods of making and using same
    US-4380682-AApril 19, 1983Diamond Shamrock CorporationBalanced chlorination process
    US-5085674-AFebruary 04, 1992Union Carbide Industrial Gases Technology CorporationDuplex adsorption process
    US-4317934-AMarch 02, 1982Ethyl CorporationPreparation of carbonyl compounds
    US-4695663-ASeptember 22, 1987The British Petroleum Company P.L.C.Production of aromatics from hydrocarbon feedstock
    US-4939310-AJuly 03, 1990The British Petroleum Company P.L.C.Conversion of methane to higher hydrocarbons
    US-6869903-B2March 22, 2005Univation Technologies, LlcSynthesis of polymerization catalyst components
    US-6646102-B2November 11, 2003Dow Global Technologies Inc.Process for manufacturing an alpha-dihydroxy derivative and epoxy resins prepared therefrom
    US-5986158-ANovember 16, 1999Akzo Nobel NvProcess for alkylating hydrocarbons
    US-5684213-ANovember 04, 1997Chemical Research & Licensing CompanyMethod for the preparation of dialkyl ethers
    US-6875339-B2April 05, 2005Conocophillips CompanyOctane improvement of a hydrocarbon stream
    US-3562321-AFebruary 09, 1971Sun Oil CoPreparation of oxygenated hydrocarbons
    US-4737594-AApril 12, 1988Produits Chimiques Ugine KuhlmannProcess for the manufacture of vinyl chloride
    US-4939314-AJuly 03, 1990Mobil Oil CorporationMethod for on-stream low-pressure regeneration of an oligomerization catalyst from a fluid-bed reactor operating at high pressure with hydrocarbons in a non-liquid phase
    US-2666024-AJanuary 12, 1954Fmc CorpOxidation and chlorine recovery process
    US-7105710-B2September 12, 2006Shell Oil CompanyProcess of preparing an alkylene glycol
    US-3273964-ASeptember 20, 1966Universal Oil Prod CoProcess for producing bromine from a mixture of hydrogen bromide and olefinic hydrocarbon
    US-5849978-ADecember 15, 1998Institut Francais Du PetroleLiquid catalyst for aliphatic alkylation
    US-2005027084-A1February 03, 2005Clarke William D., Haymon Terry D., Henley John P., Hickman Daniel A., Jones Mark E., Miller Matt C., Morris Thomas E., Reed Daniel J., Samson Lawrence J., Schweizer Albert E., Smith Steve A.Production of vinyl halide from single carbon feedstocks
    GB-1542112-AMarch 14, 1979Shell Int ResearchProcess for the preparation of 2-phenylethanol or derivatives thereof
    US-4590310-AMay 20, 1986The Boc Group, Inc.Process for the preparation of 2,2,2-trifluoroethanol
    US-5146027-ASeptember 08, 1992Atlantic Richfield Co., Phillips Petroleum Co.Methane conversion process
    US-4720600-AJanuary 19, 1988Mobil Oil CorporationProduction of middle distillate range hydrocarbons by light olefin upgrading
    US-5728897-AMarch 17, 1998Bayer AktiengesellschaftProcess for the preparation of benzyl alcohol
    US-4350511-ASeptember 21, 1982Koch Process Systems, Inc.Distillative separation of carbon dioxide from light hydrocarbons
    US-5087779-AFebruary 11, 1992Amoco CorporationHydrocarbon halogenation
    US-2006100469-A1May 11, 2006Waycuilis John JProcess for converting gaseous alkanes to olefins and liquid hydrocarbons
    US-6669846-B2December 30, 2003Global Biosciences, Inc.Wastewater treatment with alkanes
    US-7268263-B1September 11, 2007Uop LlcIntegrated process for aromatics production
    US-6878853-B2April 12, 2005Tokuyama CorporationProcess for preparing dihalogenated adamantanes
    US-5430210-AJuly 04, 1995Mobil Oil CorporationSelective hydrogen combustion processes
    US-5500297-AMarch 19, 1996The Trustees Of Princeton UniversityElectron acceptor compositions technical field
    US-4634800-AJanuary 06, 1987Atlantic Richfield CompanyMethane conversion process
    US-6572829-B2June 03, 2003University Of Central FloridaClosed cycle photocatalytic process for decomposition of hydrogen sulfide to its constituent elements
    US-4990696-AFebruary 05, 1991Stauffer John EMethyl alcohol process
    US-6169218-B1January 02, 2001Catalytic Distillation TechnologiesSelective hydrogenation of highly unsaturated compounds in hydrocarbon streams
    US-5026937-AJune 25, 1991UopAromatization of methane using zeolite incorporated in a phosphorus-containing alumina
    US-3992466-ANovember 16, 1976Mobil Oil CorporationHydrocarbon conversion
    US-7214750-B2May 08, 2007Exxonmobil Chemical Patents Inc.Polymerization processes
    US-4117251-ASeptember 26, 1978Chemische Werke Huls AgMethod for preparing straight chain primary alcohols from 1-bromoalkanes
    US-5096469-AMarch 17, 1992Keefer BowieAdsorptive gas separator with inertial energy exchange
    CA-2236126-CAugust 15, 2006Mitsubishi Chemical Corporation, Tomoatsu Iwakura, Hidekazu MiyagiProcede de production d'alkyleneglycol
    US-6540905-B1April 01, 2003Chevron U.S.A. Inc.Hydrocarbon conversion using zeolite SSZ-58
    US-4849562-AJuly 18, 1989The Dow Chemical CompanyProcess for producing ethylene dichloride
    WO-2006067192-A1June 29, 2006Solvay (Société Anonyme)Procede de fabrication de 1,2-dichloroethane
    US-4025572-AMay 24, 1977Mobil Oil CorporationManufacture of hydrocarbons
    US-6548040-B1April 15, 2003Institut Francais Du PetroleProcess for preparing a zeolite with structure type MTT using specific template precursors
    GB-2185754-AJuly 29, 1987Labofina SaProcess for producing gasoline
    US-5097083-AMarch 17, 1992Stauffer John EProcess for the chlorination of ethane
    US-7098371-B2August 29, 2006Clarient GmbhMethod of hydrodechlorinating nuclear-chlorinated ortho-xylenes
    US-4538014-AAugust 27, 1985Mobil Oil CorporationCatalysis over activated zeolites
    US-5191142-AMarch 02, 1993Amoco CorporationProcess for converting methanol to olefins or gasoline
    US-4194990-AMarch 25, 1980Allied Chemical CorporationCatalyst and process for the production of chlorofluorinated hydrocarbons
    US-4814527-AMarch 21, 1989The Dow Chemical CompanyCatalytic process for ethylene dichloride
    US-2007238905-A1October 11, 2007Victor Manuel Arredondo, Deborah Jean Back, Patrick Joseph Corrigan, David Patrick Kreuzer, Angella Christine CearleyProcesses for converting glycerol to glycerol ethers
    US-5977402-ANovember 02, 1999Sumitomo Chemical Company, LimitedProcesses for preparing 4-tert.-butylcyclohexanol and 4-tert.-butylcyclohexyl acetate
    US-4439409-AMarch 27, 1984Bayer AktiengesellschaftCrystalline aluminosilicate PSH-3 and its process of preparation
    US-3254023-AMay 31, 1966Socony Mobil Oil Co IncMethod of heat balancing in organic catalytic reactions
    US-8008535-B2August 30, 2011Marathon Gtf Technology, Ltd.Process for converting gaseous alkanes to olefins and liquid hydrocarbons
    US-4579996-AApril 01, 1986The British Petroleum Company P.L.C.Process for the production of hydrocarbons from C1 to C4 monohaloalkanes
    US-4410714-AOctober 18, 1983The Lummus CompanyProduction of epoxy compounds from olefinic compounds
    US-6368490-B1April 09, 2002Bayer AktiengesellschaftMethod for electrochemically processing HCL gas into highly pure chlorine
    US-5695890-ADecember 09, 1997The Trustees Of Princeton UniversityHeterolamellar photoelectrochemical films and devices
    US-5465699-ANovember 14, 1995Volkswagen AgIntake pipe arrangement for an internal combustion engine having individual arc-shaped cylinder intake pipes
    US-5776871-AJuly 07, 1998The Procter & Gamble CompanyShampoos with insoluble silicone conditioning agent and cationic polymer
    US-7057081-B2June 06, 2006Conocophillips CompanyMethod for treating alkanes
    US-7285698-B2October 23, 2007University Of Petroleum, BeijingMethod for manufacturing alkylate oil with composite ionic liquid used as catalyst
    US-6281405-B1August 28, 2001Uop LlcAlkylation process using membrane for recovery of halides
    WO-2006111997-A1October 26, 2006Consiglio Nazionale Delle Ricerche - Istituto Di Scienze E Tecnologie Molecolari, Universita'degli Studi Di MilanoProcede de production de biodiesel, a partir de substances grasses a fort indice d'iode
    US-5679134-AOctober 21, 1997L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges ClaudeDevice and process for the separation of gas by adsorption
    US-5254790-AOctober 19, 1993Phillips Petroleum CompanyIntegrated process for producing motor fuels
    WO-2005037758-A1April 28, 2005Applied Research Systems Ars Holding N.V.Method for preparing para-phenyl alkynyl benzaldehydes
    US-4371716-AFebruary 01, 1983Shell Oil Companyβ-(Sec-alkoxy) ethanol process
    US-5489719-AFebruary 06, 1996Mobil Oil CorporationProcess for the production of tertiary alkyl ether rich FCC gasoline
    US-2009005620-A1January 01, 2009Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons
    US-2006025617-A1February 02, 2006Eastman Kodak CompanySynthesis process
    US-7151199-B2December 19, 2006Exxonmobil Chemical Patents Inc.Hydrocarbon conversion processes using non-zeolitic molecular sieve catalysts
    US-3705196-ADecember 05, 1972Sun Oil CoSynthesis of aliphatic and alicyclic ethers
    US-4035430-AJuly 12, 1977Mobil Oil CorporationConversion of methanol to gasoline product
    US-7244795-B2July 17, 2007Univation Technologies, LlcPolymerization process using metallocene catalyst systems
    US-6753390-B2June 22, 2004Univation Technologies, LlcGas phase polymerization process
    US-4962252-AOctober 09, 1990The British Petroleum Company P.L.C.Process for the production of alkenyl-substituted benzene derivatives
    US-4492657-AJanuary 08, 1985Hoechst AktiengesellschaftImines of alkyl 4-halomethylbenzoates
    US-5456822-AOctober 10, 1995Institut Francais Du PetroleCatalyst of the galloaluminosilicate type containing gallium, a nobel metal of the platinum family and at least on additional metal, and its use in the aromatization of hydrocarbons
    US-3353919-ANovember 21, 1967Air PreheaterApparatus for the elimination of odors from noxious gases
    US-3679758-AJuly 25, 1972Sun Oil CoDihalogenation of branched alkanes
    US-5600045-AFebruary 04, 1997The Dow Chemical CompanyProcess for conversion of crude hydrocarbon mixtures
    US-5188725-AFebruary 23, 1993Mobil Oil CorporationFluidized catalyst process for production and etherification of olefins
    US-7232872-B2June 19, 2007Exxonmobil Chemical Patents Inc.Polymerization processes
    US-5087787-AFebruary 11, 1992Phillips Petroleum CompanyMethod of oxidative conversion
    US-6538162-B2March 25, 2003Exxonmobil Chemical Patents Inc.Method for converting alkanes to oxygenates
    US-5446234-AAugust 29, 1995Imperial Chemical Industries PlcHydrocarbon conversion process using a specified zeolite
    US-2168260-AAugust 01, 1939Ig Farbenindustrie AgProcess of preparing monohalogenation products
    US-4187255-AFebruary 05, 1980Conoco, Inc.Process for methylating naphthalene
    US-4356159-AOctober 26, 1982Imperial Chemical Industries LimitedMethod of recovering bromine from methyl bromide
    US-4011278-AMarch 08, 1977Mobil Oil CorporationConversion of polar compounds using a zsm-5 zeolite catalyst
    US-4300005-ANovember 10, 1981Monsanto Co.Preparation of vinyl chloride
    US-6491809-B1December 10, 2002Institut Francais Du Petrole, Industrias Venoco C.A.Synthetic oil with a high viscosity number and a low pour point
    US-7357904-B2April 15, 2008Chevron CorporationReduction of oxides of nitrogen in a gas stream using molecular sieve SSZ-74
    US-5371313-ADecember 06, 1994Polysar Rubber CorporationPurification of hydrocarbon streams
    US-5345021-ASeptember 06, 1994Imperial Chemical Industries PlcCatalytic reactions using zeolites
    US-4433189-AFebruary 21, 1984Mobil Oil CorporationCatalytic conversion of methanol to light olefins
    US-5571885-ANovember 05, 1996Exxon Chemical Patents Inc.Immobilized lewis acid catalysts
    US-5679879-AOctober 21, 1997Rhone-Poulenc Chemicals LimitedProcess for the production of substituted aromatic hydrocarbons from corresponding anilines by dediazoniation
    US-6180841-B1January 30, 2001Evc Technology AgSingle stage fixed bed oxychlorination of ethylene
    US-3894103-AJuly 08, 1975Mobil Oil CorpAromatization reactions
    WO-2006100312-A2September 28, 2006Solvay (Societe Anonyme)Process for producing a chlorhydrin from a multihydroxylated aliphatic hydrocarbon and/or ester thereof in the presence of metal salts
    US-3894104-AJuly 08, 1975Mobil Oil CorpAromatization of hetero-atom substituted hydrocarbons
    US-4143084-AMarch 06, 1979Mobil Oil CorporationDi-alkylbenzene isomer mixtures
    US-4886932-ADecember 12, 1989Atlantic Richfield CompanyThin bed cofeed reaction system for methane conversion
    US-5082816-AJanuary 21, 1992The Standard Oil CompanyLead-zirconate catalysts
    US-4046825-ASeptember 06, 1977Mobil Oil CorporationConversion of oxygenated compounds to gasoline
    US-7365102-B1April 29, 2008Delphi Technologies, Inc.Process for pre-reforming hydrocarbon fuels
    US-4308403-ADecember 29, 1981Texaco Inc.Process for preparing glycol ethers
    US-4696985-ASeptember 29, 1987Hercules IncorporatedCatalyst composition for polymerization of cycloolefins
    US-6641644-B2November 04, 2003Vbox, IncorporatedPressure swing adsorption gas separation method and apparatus
    US-4665259-AMay 12, 1987The Standard Oil CompanyMethane conversion process using phosphate-containing catalysts
    US-5994604-ANovember 30, 1999Lockheed Martin Idaho Technologies CompanyMethod and apparatus for low temperature destruction of halogenated hydrocarbons
    US-4762596-AAugust 09, 1988The United States Of America As Represented By The United States Department Of EnergyProcess for removal of hydrogen halides or halogens from incinerator gas
    US-4272338-AJune 09, 1981Olin CorporationProcess for the treatment of anolyte brine
    US-5254772-AOctober 19, 1993Imperial Chemical Industries PlcChemical process
    US-4465884-AAugust 14, 1984Mobil Oil CorporationOlefin processing
    US-6395945-B1May 28, 2002Phillips Petroleum CompanyIntegrated hydroisomerization alkylation process
    GB-2095243-ASeptember 29, 1982Ici PlcProduction of methylene chloride
    US-5178748-AJanuary 12, 1993Imperial Chemical IndustriesCatalytic reactions using zeolites
    US-4950822-AAugust 21, 1990Ethyl CorporationOlefin oligomer synlube process
    US-4579992-AApril 01, 1986Huels AktiengesellschaftProduction of 3,3- and 2,3-dimethylbutenes, 2,3-dimethylbutadiene and/or glycol or polyglycol N-alkyl-3,3- and -2,3-dimethylbutyl ether
    US-4769504-ASeptember 06, 1988The United States Of America As Represented By The United States Department Of EnergyProcess for converting light alkanes to higher hydrocarbons
    WO-2005104689-A2November 10, 2005Marathon Oil CompanyProcess for converting gaseous alkanes to liquid hydrocarbons
    US-5817904-AOctober 06, 1998Repsol Petroleo S.A.Method for the conversion of methane into longer chain hydrocarbons
    US-3923913-ADecember 02, 1975Pechiney Saint GobainProcess for obtaining chlorinated derivatives of ethylene
    US-4792642-ADecember 20, 1988Eastman Kodak CompanyProcess for preparing iodinated aromatic compounds
    US-4509955-AApril 09, 1985The Lubrizol CorporationCombinations of carboxylic acylating agents substituted with olefin polymers of high and low molecular weight mono-olefins, derivatives thereof, and fuels and lubricants containing same
    US-2677598-AMay 04, 1954Dow Chemical CoOxidation of ferrous halides to form ferric halides
    US-5026944-AJune 25, 1991Energy Mines And Resources CanadaSynthesis of isobutene from methane and acetylene
    US-5489727-AFebruary 06, 1996Phillips Petroleum CompanyIsopentane disproportionation
    US-6727400-B2April 27, 2004Triosyn Holdings, Inc.Deactivation of toxic chemical agents
    US-5319132-AJune 07, 1994Ihara Chemical Industry Co., Ltd.Process for producing halomethyl ester of aliphatic carboxylic acid
    US-6320085-B1November 20, 2001Agro-Chemie Novenyvedoszer Gyarto Ertekesito Est Forgalmazo Kft.Process for the preparation of benzyl-ethers
    US-6822123-B2November 23, 2004John E. StaufferFormaldehyde process
    US-5208402-AMay 04, 1993Interstate Chemical, Inc.Liquid fuels for internal combustion engines and process and apparatus for making same
    US-6265505-B1July 24, 2001Univation Technologies, LlcCatalyst system and its use in a polymerization process
    WO-2004067487-A2August 12, 2004Ruhrgas AktiengesellschaftVerfahren zum herstellen nichtaromatischer kohlenwasserstoffe
    US-4988660-AJanuary 29, 1991Union Carbide Chemicals And Plastics Company Inc.Double perovskite catalysts for oxidative coupling
    US-6117371-ASeptember 12, 2000Great Lakes Chemical CorporationContinuous bromination process and products thereof
    US-6455650-B1September 24, 2002The B.F. Goodrich Company, The Penn State Research FoundationCatalyst and methods for polymerizing cycloolefins
    US-6207864-B1March 27, 2001Basf AktiengesellschaftProcess for preparing cyclopropylacetylene
    US-4579977-AApril 01, 1986Phillips Petroleum CompanyProcess for the oxidation of organic halides to organic aldehydes
    US-4621161-ANovember 04, 1986Mobil Oil CorporationOxygenate conversion over activated zeolite catalyst
    US-7064238-B2June 20, 2006Marathon Oil CompanyConversion of alkanes to oxygenates
    US-4956521-ASeptember 11, 1990UopAdsorption and isomerization of normal and mono-methyl paraffins
    US-5013424-AMay 07, 1991UopProcess for the simultaneous hydrogenation of a first feedstock comprising hydrocarbonaceous compounds and having a non-distillable component and a second feedstock comprising halogenated organic compounds
    US-2941014-AJune 14, 1960Hoechst AgManufacture of alkyl chlorination products
    US-3346340-AOctober 10, 1967Universal Oil Prod CoProduction of bromine by oxidation of hydrogen bromide
    US-5001293-AMarch 19, 1991Amoco CorporationHalocarbon conversion
    EP-0418974-A1March 27, 1991Union Carbide Chemicals And Plastics Company, Inc.Silver-containing catalysts for oxidative coupling
    US-6187871-B1February 13, 2001The Trustees Of Princeton UniversityElectron acceptor compositions on polymer templates
    US-5194244-AMarch 16, 1993Shell Oil CompanyBasic alkali metal-zeolite compositions
    CA-1202610-A1December 31, 1969
    US-6426441-B1July 30, 2002Phillips Petroleum CompanyMethod for reducing organic fluoride levels in hydrocarbons
    US-6107561-AAugust 22, 2000University Of Southern CaliforniaCharge generators in heterolamellar multilayer thin films
    US-3657367-AApril 18, 1972Stauffer Chemical CoOxychlorination of saturated and unsaturated hydrocarbons in the presence of a fluidized catalyst containing lanthanum and didymium
    US-3468968-ASeptember 23, 1969Ethyl CorpManufacture of halohydrocarbons
    US-4110180-AAugust 29, 1978Diamond Shamrock Technologies S.A.Process for electrolysis of bromide containing electrolytes
    US-6841063-B2January 11, 2005Chevron U.S.A. Inc.Hydrocarbon conversion using zeolite SSZ-53
    WO-2006019399-A2February 23, 2006Grt, Inc.Reacteur a zones
    WO-2007114479-A1October 11, 2007Sumitomo Chemical Company, LimitedProcédé de production d'oléfine tertiaire et d'alcool aliphatique
    US-4720602-AJanuary 19, 1988Mobil Oil CorporationProcess for converting C2 to C12 aliphatics to aromatics over a zinc-activated zeolite
    US-4133838-AJanuary 09, 1979Pearson Research Corp.Process for preparing hydrocarbons from methanol and phosphorus pentoxide
    US-4774216-ASeptember 27, 1988Phillips Petroleum CompanyComposition of matter for oxidative conversion of organic compounds
    US-4418236-ANovember 29, 1983Metallgesellschaft AktiengesellschaftMethod of producing gasoline hydrocarbons from methanol
    US-6509485-B2January 21, 2003Sri InternationalPreparation of epoxides from alkanes using lanthanide-promoted silver catalysts
    US-5983476-ANovember 16, 1999Uop LlcConversion of an HF alkylation unit
    US-3919336-ANovember 11, 1975Allied ChemMethod of preparing vinyl chloride from liquid ethylene dichloride
    US-3894105-AJuly 08, 1975Mobil Oil CorpProduction of durene
    EP-1235769-B1May 26, 2004Dow Global Technologies, Inc.Oxyhalogenation process using catalyst having porous rare earth halide support
    US-2008200740-A1August 21, 2008Marathon Oil CompanyProcess for converting gaseous alkanes to olefins and liquid hydrocarbons
    US-4605796-AAugust 12, 1986Agency Of Industrial Science And TechnologyProcess for producing ethanol
    US-4665270-AMay 12, 1987The British Petroleum Company, P.L.C.Process for the production of hydrocarbons from hetero-substituted alkanes
    GB-1446803-AAugust 18, 1976Montedison SpaPreparation of bromofluorinated methanes
    US-5385650-AJanuary 31, 1995Great Lakes Chemical CorporationRecovery of bromine and preparation of hypobromous acid from bromide solution
    US-5653956-AAugust 05, 1997Chevron U.S.A. Inc.Zeolite SSZ-42
    US-5157189-AOctober 20, 1992Karra Sankaram BConversion of light hydrocarbons to higher hydrocarbons
    WO-2007107031-A1September 27, 2007Eth ZurichProduction of saturated c2 to c5 hydrocarbons
    CA-1099656-A1December 31, 1969
    US-5071815-ADecember 10, 1991British Columbia Research CorporationMethod for producing catalysts
    US-5395981-AMarch 07, 1995UopHydrocarbon conversion by catalytic distillation
    GB-2120249-ANovember 30, 1983British Petroleum Co PlcProcess for the production of methyl or ethyl mono-halide
    US-4550217-AOctober 29, 1985Mobil Oil CorporationConversion of methanol to olefins using large size catalyst particles
    US-5138112-AAugust 11, 1992UopProcess for converting a C2 -C6 aliphatic hydrocarbon to high octane transportable fuel
    US-3974062-AAugust 10, 1976Mobil Oil CorporationConversion of full range crude oils with low molecular weight carbon-hydrogen fragment contributors over zeolite catalysts
    US-5998679-ADecember 07, 1999Jlm Technology, Ltd.Methods for converting lower alkanes and alkanes to alcohols and diols
    US-5898086-AApril 27, 1999Henkel CorporationProcess for making alkyl ether glycerols
    US-2005148805-A1July 07, 2005Jones Mark E., Hickman Daniel A., Olken Michael M.Process for the conversion of ethylene to vinyl chloride, and novel catalyst compositions useful for such process
    WO-2009152408-A1December 17, 2009Marathon Gtf Technology, Ltd.Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery
    US-6511526-B2January 28, 2003Vbox, IncorporatedPressure swing adsorption gas separation method and apparatus
    US-5905169-AMay 18, 1999E. I. Du Pont De Nemours And CompanyProcess for producing polyfluoroacyl compositions
    EP-1689728-B1April 11, 2007Firmenich SaMusk odorant compounds
    US-7026519-B2April 11, 2006Oxeno Olefinchemie GmbhObtaining tert-butanol
    US-7001872-B2February 21, 2006Halliburton Energy Services, Inc.Subterranean formation treating fluid and methods of fracturing subterranean formations
    US-6956140-B2October 18, 2005Halocarbon Products CorporationHydrothermal hydrolysis of halogenated compounds
    WO-2005014168-A1February 17, 2005Solvay (Société Anonyme)Procédé de régénération d'un catalyseur d'hydrogénation
    US-6866950-B2March 15, 2005Questair Technologies Inc.Methods and apparatuses for gas separation by pressure swing adsorption with partial gas product feed to fuel cell power source
    US-5237115-AAugust 17, 1993Phillips Petroleum CompanyIntegrated olefin processing
    US-7141708-B2November 28, 2006Ineos Vinyls Uk Ltd.Hollow pellet suitable as carrier of catalysts for selective exothermic reactions
    US-4035285-AJuly 12, 1977Mobil Oil CorporationHydrocarbon conversion process
    US-2005267224-A1December 01, 2005Battelle Memorial InstituteMethod of generating hydrocarbon reagents from diesel, natural gas and other logistical fuels
    US-4172099-AOctober 23, 1979Stauffer Chemical CompanyProcess for chlorination of ethylene
    US-6472572-B1October 29, 2002Grt, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols and ethers from alkanes
    US-6462243-B1October 08, 2002Grt, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols and ethers from alkanes
    WO-2007079038-A2July 12, 2007Chevron U.S.A Inc.Composition de tamis moleculaire ssz- 74 et sa synthese
    US-4300009-ANovember 10, 1981Mobil Oil CorporationConversion of biological material to liquid fuels
    US-6376731-B1April 23, 2002Arco Chemical Technology, L.P.Selective olefin oligomerization
    WO-2008157046-A1December 24, 2008Albemarle CorporationProcesses for producing higher hydrocarbons from methane
    US-4496752-AJanuary 29, 1985The Lummus CompanyProduction of epoxy compounds from olefinic compounds
    US-6479705-B2November 12, 2002Sumitomo Chemical Company, Limited, Daicel Chemical Industries, Ltd.Process for preparing ketone, alcohol and hydroperoxide
    WO-2006076942-A1July 27, 2006Lurgi AgVerfahren zur herstellung von synthetischen kraftstoffen aus oxigenaten
    WO-2005021468-A1March 10, 2005Grt, Inc., The Regents Of The University Of CaliforniaSynthese d'hydrocarbures
    US-4804800-AFebruary 14, 1989Exxon Research & Engineering Co.Process for synthesizing a zeolite catalyst on a pH controlled basis to improve catalyst life
    US-5139991-AAugust 18, 1992The United States Of American As Represented By The United States Department Of EnergyOxyhydrochlorination catalyst
    US-5599381-AFebruary 04, 1997Whitlock; David R.Separation of solutes in gaseous solvents
    US-7253328-B2August 07, 2007John StaufferMethod for producing vinyl chloride monomer
    US-6528693-B1March 04, 2003Great Lakes (Uk) LimitedPreparation of cyclopropylethyne and intermediates for preparation of cyclopropylethyne
    US-3987119-AOctober 19, 1976Allied Chemical CorporationProduction of vinyl chloride from ethane
    US-4568660-AFebruary 04, 1986Hercules IncorporatedCycloolefin polymerization catalyst composition
    US-5895831-AApril 20, 1999Uop LlcSolid catalyst alkylation process
    US-5663474-ASeptember 02, 1997Alliedsignal Inc.Alkylation process using hydrogen fluoride-containing alkylation catalysts
    WO-2004018093-A2March 04, 2004E.I. Du Pont De Nemours And CompanyCompositions d'oxyde de chrome a substitution cobalt, preparation de ces compositions et utilisation de ces compositions en tant que catalyseurs et precurseurs de catalyseurs
    US-6518474-B1February 11, 2003Huntsman International LlcProcess for producing isobutylene from tertiary butyl alcohol
    US-2005245771-A1November 03, 2005Fong Howard L, Trevino Lizbeth Olivia C, Murray Brendan D, Cano Manuel LProcess to convert alkanes into primary alcohols
    US-5382704-AJanuary 17, 1995E. I. Du Pont De Nemours And CompanyFluorinated methyl ethers
    US-5571762-ANovember 05, 1996Eniricerche S.P.A., Agip Petroli S.P.A.Catalyst and process for the alkylation of aliphatic hydrocarbons with olefins
    US-4665267-AMay 12, 1987The British Petroleum CompanyChemical process and catalyst
    US-6475464-B1November 05, 2002Institut Francais Du PetroleProcess for preparing a zeolite with structure type MTT using zeolitic material seeds
    US-4814536-AMarch 21, 1989Mobil Oil CorporationConversion of oxygenates to gasoline at variable space velocity
    US-4301253-ANovember 17, 1981Union Carbide CorporationProcess for the selective production of ethanol and methanol directly from synthesis gas
    WO-2005054120-A2June 16, 2005Idaho Research Foundation, Inc.Nanoparticules metalliques a support de polymere et leur procede de fabrication et d'utilisation
    US-4929781-AMay 29, 1990UopProcess for the simultaneous hydroconversion of a first feedstock comprising unsaturated, halogenated organic compounds and a second feedstock comprising saturated, halogenated organic compounds
    US-7304193-B1December 04, 2007Uop LlcIntegrated process for aromatics production
    US-2009308759-A1December 17, 2009Marathon Gtf Technology, Ltd.Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery
    US-6369283-B1April 09, 2002Union Carbide Chemicals & Plastics Technology Corp.Processes for producing unsaturated alcohols
    US-5382743-AJanuary 17, 1995Mobil Oil CorporationSkeletal isomerization of n-pentenes using ZSM-35 in the presence of hydrogen
    US-4795843-AJanuary 03, 1989Uop Inc.Conversion of methane into larger organic hydrocarbons
    US-6372949-B1April 16, 2002Mobil Oil CorporationSingle stage process for converting oxygenates to gasoline and distillate in the presence of undimensional ten member ring zeolite
    US-5968236-AOctober 19, 1999Bassine; StuartValve free oxygen concentrator
    US-6380423-B2April 30, 2002Xerox CorporationColorless compounds
    US-4384159-AMay 17, 1983The Dow Chemical CompanyCatalytic dehydrohalogenation process
    US-5093533-AMarch 03, 1992Interstate Chemical, Inc.Blended gasolines and process for making same
    US-3907917-ASeptember 23, 1975British Petroleum CoIsoprene production
    US-5523503-AJune 04, 1996UopCocurrent simulated moving bed hydrocarbon alkylation process
    US-6495484-B1December 17, 2002Univation Technologies, LlcCatalyst system and its use in a polymerization process
    US-6486368-B1November 26, 2002Grt, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols, ethers, and olefins from alkanes
    US-4302619-ANovember 24, 1981Mobil Oil CorporationControl of CO emissions in a process for producing gasoline from methanol
    US-4373109-AFebruary 08, 1983Olah George ABifunctional acid-base catalyzed conversion of hetero-substituted methanes into olefins
    US-2006270863-A1November 30, 2006Amyris BiotechnologiesConversion of amorpha-4,11-diene to artemisinin and artemisinin precursors
    US-4939311-AJuly 03, 1990Amoco CorporationCatalysts for the oxidative conversion of methane to higher hydrocarbons
    US-6680415-B1January 20, 2004Dow Global Technologies Inc.Oxyhalogenation process using catalyst having porous rare earth halide support
    US-5245109-ASeptember 14, 1993Amoco CorporationHydrocarbon conversion
    US-4489211-ADecember 18, 1984Onoda Cement Co., Ltd., Toyo Soda Manufacturing Co., Ltd.Process for producing 2,2,2-trifluoroethanol
    US-5401894-AMarch 28, 1995UopProcess for the treatment of halogenated organic feedstocks
    WO-2006067191-A1June 29, 2006Solvay (Société Anonyme)Procede de fabrication de 1,2-dichloroethane
    US-5453557-ASeptember 26, 1995The Dow Chemical CompanyProcesses for converting chlorinated byproducts and waste products to useful materials
    US-5366949-ANovember 22, 1994Catalytica, Inc.CeBr3 catalyst
    US-4902842-AFebruary 20, 1990UopProcess for the simultaneous hydroconversion of a first feedstock comprising unsaturated, halogenated organic compounds and a second feedstock comprising saturated, halogenated organic compounds
    US-4547612-AOctober 15, 1985Mobil Oil CorporationProduction of lubricant and/or heavy distillate range hydrocarbons by light olefin upgrading
    WO-2007142745-A1December 13, 2007Exxonmobil Chemical Patents Inc.Tamis moléculaire interpénétré, sa synthèse et son utilisation dans la conversion d'oxygénates en oléfines
    US-5073657-ADecember 17, 1991Union Carbide Chemicals And Plastics Company Inc.Vapor phase modifiers for oxidative coupling
    US-4990711-AFebruary 05, 1991Mobil Oil CorporationSynthetic polyolefin lubricant blends having high viscosity indices
    US-4049734-ASeptember 20, 1977Mobil Oil CorporationConversion of coal to high octane gasoline
    US-4058576-ANovember 15, 1977Mobil Oil CorporationConversion of methanol to gasoline components
    US-4524231-AJune 18, 1985Mobil Oil CorporationProduction of durene from alcohols and ethers
    US-5639930-AJune 17, 1997Penick; Joe E.Process of producing alkylates
    US-5082473-AJanuary 21, 1992Keefer BowieExtraction and concentration of a gas component
    GB-950976-AMarch 04, 1964British Hydrocarbon Chem LtdImprovements in and relating to the production of olefines
    GB-2116546-ASeptember 28, 1983Snam ProgettiProduction of t-butyl alkyl ethers
    US-3353916-ANovember 21, 1967Universal Oil Prod CoQuantitative recovery of bromine by two stage catalytic oxidation of hydrogen bromide
    US-5633419-AMay 27, 1997The Dow Chemical CompanyPolymerization of olefins in the presence of a supported catalyst
    US-6143939-ANovember 07, 2000The United States Of America As Represented By The United States Department Of EnergyMethod of dehalogenation using diamonds
    US-3879480-AApril 22, 1975Lummus CoVinyl chloride process
    WO-2008036562-A1March 27, 2008Albemarle CorporationProcédés pour convertir du méthane en hydrocarbures utiles, catalyseur appropriés et régénération de catalyseur
    US-5306855-AApril 26, 1994Catalytica, Inc.Catalytic process for converting lower alkanes to esters, alcohols, and to hydrocarbons
    US-2011015458-A1January 20, 2011Marathon Gtf Technology, Ltd.Conversion of hydrogen bromide to elemental bromine
    US-7265193-B2September 04, 2007Exxonmobil Chemical Patents Inc.Polymerization process
    US-4642403-AFebruary 10, 1987The British Petroleum Company P.L.C.Production of aromatics from ethane and/or ethylene
    US-4431856-AFebruary 14, 1984Mobil Oil CorporationFluid zeolite catalyst conversion of alcohols and oxygenated derivatives to hydrocarbons
    US-3076784-AFebruary 05, 1963Bayer Ag, Mobay Chemical CorpPolyethers from aryl halides and organic diols
    US-5728905-AMarch 17, 1998Evc Technology AgVinyl chloride production process
    US-4925995-AMay 15, 1990Shell Oil CompanyProcess for preparing liquid hydrocarbons
    EP-0418971-A1March 27, 1991Union Carbide Chemicals And Plastics Company, Inc.Procédé de couplage oxydatif à haut rapport éthylène/éthane
    US-5120332-AJune 09, 1992The Haser Company LimitedGas resonance device
    US-4191618-AMarch 04, 1980General Electric CompanyProduction of halogens in an electrolysis cell with catalytic electrodes bonded to an ion transporting membrane and an oxygen depolarized cathode
    US-7060865-B2June 13, 2006Exxonmobil Chemical Patents Inc.Recovery of C4 olefins from a product stream comprising C4 olefins, dimethyl ether and C5+ hydrocarbons
    US-4982041-AJanuary 01, 1991Union Carbide Chemicals And Plastics Company Inc.Double perovskite catalysts for oxidative coupling
    US-6426442-B1July 30, 2002Uop LlcCatalyst for the conversion of low carbon number aliphatic hydrocarbons to higher carbon number hydrocarbons, process for preparing the catalyst and process using the catalyst
    US-7361794-B2April 22, 2008Grt, Inc.Zone reactor
    WO-2006069107-A2June 29, 2006E.I. Dupont De Nemours And CompanyCopolymers of perfluoro (alkyl venyl ether) for photochemical reactor, process for increasing fluorine content and production of olefinic compound by photochlorination
    US-4709108-ANovember 24, 1987Chevron Research CompanyConversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a metal compound-containing catalyst
    US-6632971-B2October 14, 2003Exxonmobil Chemical Patents Inc.Process for converting natural gas to higher value products using a methanol refinery remote from the natural gas source
    US-7226576-B2June 05, 2007Chevron U.S.A. Inc.Molecular sieve SSZ-56 composition of matter and synthesis thereof
    US-4169862-AOctober 02, 1979The B. F. Goodrich CompanyLow temperature catalytic combustion of chlorohydrocarbons
    US-5882614-AMarch 16, 1999Exxon Research And Engineering CompanyVery low sulfur gas feeds for sulfur sensitive syngas and hydrocarbon synthesis processes
    US-2008183022-A1July 31, 2008Waycuilis John JProcess for converting gaseous alkanes to liquid hydrocarbons
    US-4886925-ADecember 12, 1989Mobil Oil CorpOlefins interconversion and etherification process
    US-5750801-AMay 12, 1998Bayer AktiengesellschaftProcess for the continuous preparation of benzyl alcohol
    US-4851606-AJuly 25, 1989Mobil Oil CorporationControl of waste water chemical oxygen demand in an oxygenate to hydrocarbon conversion process
    EP-0346612-B1August 25, 1993Daikin Industries, LimitedVerfahren zur Herstellung von 1,1,1-Trifluor-2,2-dichlorethan
    US-6953870-B2October 11, 2005Tsoung Y Yan, Yan Tsang-Po, Yen Tsung-CheSelf-propelled liquid fuel
    US-2004188324-A1September 30, 2004Saleh ElomariHydrocarbon conversion using molecular sieve SSZ-65
    US-2004220433-A1November 04, 2004Evert Van Der Heide, Jean-Paul Lange, Arjen MiedemaProcess for the preparation of propylene glycol
    US-4025576-AMay 24, 1977Mobil Oil CorporationProcess for manufacturing olefins
    US-5107032-AApril 21, 1992Noramco, Inc.Process for the preparation of o-phthalaldehydes
    US-4781733-ANovember 01, 1988Bend Research, Inc.Semipermeable thin-film membranes comprising siloxane, alkoxysilyl and aryloxysilyl oligomers and copolymers
    WO-2006043075-A1April 27, 2006U.S. Borax, Inc.Oxydation selective de composes organiques
    US-4675410-AJune 23, 1987Nepera Inc.Process for the production of pyridine or alkyl substituted pyridines
    US-2005245772-A1November 03, 2005Fong Howard L, Trevino Lizbeth O C, Murray Brendan D, Cano Manuel L, Thomason Terry BDerivatives of alcohols and olefins
    US-3876715-AApril 08, 1975Gulf Research Development CoProcess for preparing 2,3-dibromo-2-alkylalkanes
    US-2002102672-A1August 01, 2002Joseph Mizrahi, Aharon Eyal, Canari Riki, Betty Hazan, John StarrProcess for producing a purified lactic acid solution
    US-5202506-AApril 13, 1993E. I. Du Pont De Nemours And CompanyOxidative drown process for 2-perfluoroalkylethyl alcohols
    US-5705728-AJanuary 06, 1998Occidental Chemical CorporationProcess for the production of ethylene and mixture containing ethylene
    US-7674941-B2March 09, 2010Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons
    US-4895995-AJanuary 23, 1990UopProcess for the simultaneous hydroconversion of a first feedstock comprising unsaturated, halogenated organic compounds and a second feedstock comprising saturated, halogenated organic compounds
    US-6015867-AJanuary 18, 2000Showa Denko K.K.3-alkoxypropionic ester derivative, olefin polymerization catalyst, and process for preparation of polyolefin
    US-4465893-AAugust 14, 1984Olah George AOxidative condensation of natural gas or methane into gasoline range hydrocarbons
    US-2005234276-A1October 20, 2005Waycuilis John JProcess for converting gaseous alkanes to liquid hydrocarbons
    US-5264635-ANovember 23, 1993Mobil Oil CorporationSelective cracking and etherification of olefins
    US-6342200-B1January 29, 2002Institut Francais Du PetroleProcess for preparing a zeolite with structure type EUO
    US-4795732-AJanuary 03, 1989The British Petroleum Company P.L.C.Sulphided platinum group metal-silicalite dehydrogenation catalysts
    US-5202511-AApril 13, 1993The Dow Chemical CompanyCatalyst diluent for oxychlorination process
    US-6403840-B1June 11, 2002Grt, Inc.Process for synthesizing olefin oxides
    US-4788377-ANovember 29, 1988Mobil Oil CorporationProcess for manufacturing olefins
    US-4072733-AFebruary 07, 1978Ethyl CorporationConversion of methanol and dimethyl ether
    US-7238846-B2July 03, 2007Exxonmobil Chemical Patents Inc.Conversion process
    US-4092368-AMay 30, 1978General Electric CompanyVapor phase transesterification
    US-3799997-AMarch 26, 1974Universal Oil Prod CoPreparation of alkenynes
    US-2010234637-A1September 16, 2010Fong Howard Lam Ho, Swain Richard DaleIntegrated process to coproduce aromatic hydrocarbons and ethylene and propylene
    US-5268518-ADecember 07, 1993The Dow Chemical CompanyReactor feed pipe design
    US-4506105-AMarch 19, 1985Chemische Werke Huls AgProcess for preparing cyclooctene-4-ol-1 from cyclooctadiene-1,5
    US-5952538-ASeptember 14, 1999Exxon Chemical Patents Inc.Use of short contact time in oxygenate conversion
    US-4087475-AMay 02, 1978Robert Kenneth JordanCarbonyl fluorination process
    US-4320241-AMarch 16, 1982Occidental Research CorporationProcess for converting oxygenated hydrocarbons into hydrocarbons
    US-5433828-AJuly 18, 1995European Atomic Energy Community (Euratom)Method for the removal of hydrogen sulfide and/or carbon disulfide from waste gases
    US-7342144-B2March 11, 2008Oxeno Olefinchemie GmbhMethod for producing 1-olefins by catalytically splitting 1-alkoxyalkanes
    US-7880041-B2February 01, 2011Marathon Gtf Technology, Ltd.Process for converting gaseous alkanes to liquid hydrocarbons
    US-2007100189-A1May 03, 2007Stauffer John EMethyl bromide to olefins
    US-3673264-AJune 27, 1972Dow Chemical CoMethod of preparing optically active propylene chlorohydrins and propylene oxides
    US-5034566-AJuly 23, 1991Sumitomo Chemical Company, LimitedProcess for the production of 2,3-dimethylbutenes
    US-6585953-B2July 01, 2003Wisconsin Alumni Research FoundationSynthesis of 17F labeled fluoroalkanes
    US-6475463-B1November 05, 2002Chevron U.S.A. Inc.Zeolite SSZ-55
    US-4724275-AFebruary 09, 1988National Distillers And Chemical CorporationCrystalline aluminosilicates and their use in the conversion of methanol to low molecular weight hydrocarbons
    WO-2006067190-A1June 29, 2006Solvay (Société Anonyme)Procede de fabrication de 1,2-dichloroethane
    WO-2007071046-A1June 28, 2007University Of SaskatchewanProcess for the preparation of biodiesel
    US-5693191-ADecember 02, 1997The Dow Chemical CompanyProcess for recovery of anhydrous hydrogen chloride from mixtures with non-condensable gases
    US-6103215-AAugust 15, 2000Chevron U.S.A. Inc.Zeolite Me-UTD-1
    US-5734073-AMarch 31, 1998Bnfl Fluorochemicals LtdHalogenation reactions
    US-5661097-AAugust 26, 1997The Dow Chemical CompanySupported olefin polymerization catalyst
    US-2005042159-A1February 24, 2005Chevron U.S.A. Inc.Using molecular sieve SSZ-65 for reduction of oxides of nitrogen in a gas stream
    WO-2010009376-A1January 21, 2010Gas Reaction Technologies, Inc.Processus continu pour une conversion de gaz naturel en hydrocarbures liquides
    US-2007129584-A1June 07, 2007Jean-Marie Basset, Christophe Coperet, Daravong Soulivong, Mostafa Taoufik, Jean Thivolle-CazatMetallic compound fixed to a support, method for production and use of said compound in hydrocarbon metathesis reactions
    WO-2006113205-A2October 26, 2006E. I. Du Pont De Nemours And CompanyComposes aromatiques aryl-ethylene substitues et utilisation comme semiconducteurs organiques
    US-4412086-AOctober 25, 1983Vulcan Materials CompanyProcess for separating ferric iron from chlorinated hydrocarbons
    US-5059744-AOctober 22, 1991Mobil Oil CorporationReactor and recovery system for upgrading lower olefins
    US-7199255-B2April 03, 2007Univation Technologies, LlcImino-amide catalysts for olefin polymerization
    US-2007149789-A1June 28, 2007Chevron U.S.A. Inc.Partial oxidation using molecular sieve ssz-74
    GB-1263806-AFebruary 16, 1972Exxon Research Engineering CoOxidation of hydrogen halides using 13x molecular sieve catalysts
    WO-2007130055-A1November 15, 2007Exxonmobil Chemical Patents Inc.Processus de transformation de composés organiques
    US-5068478-ANovember 26, 1991Energia Andina, Ltd.Producing alkenes and alkynes from alkanes and alkenes
    EP-1253126-A1October 30, 2002Daikin Industries, Ltd.Procede de production d'hydrofluorocarbones
    US-4795848-AJanuary 03, 1989The Standard Oil CompanyMethod for upgrading a low molecular weight alkane with a lead-zirconate catalyst
    US-6616830-B2September 09, 2003Chevron U.S.A. Inc.Hydrocarbon conversion using zeolite SSZ-57
    US-5720858-AFebruary 24, 1998The United States Of America As Represented By The United States Department Of EnergyMethod for the photocatalytic conversion of methane
    US-5430219-AJuly 04, 1995Snamprogetti S.P.A., Eniricerche S.P.A.Integrated process for producing olefins from methane-containing gas mixtures
    US-4524227-AJune 18, 1985Mobil Oil CorporationCoproduction of durene and gasoline from synthesis gas and alcohols and separation of durene-gasoline mixtures
    US-2006135823-A1June 22, 2006Sk CorporationProcess for preparing dimethylether from methanol
    US-2007149778-A1June 28, 2007Chevron U.S.A. Inc.Beckmann rearrangement using molecular sieve ssz-74
    US-5563313-AOctober 08, 1996Exxon Chemical Patents Inc.Immobilized Lewis Acid catalysts
    US-5243098-ASeptember 07, 1993Energia Andina Ltd.Conversion of methane to methanol
    US-4652688-AMarch 24, 1987The British Petroleum Company, P.L.C.Process for the production of hydrocarbons from hetero-substituted methanes
    WO-2008106319-A1September 04, 2008Albemarle CorporationProcédés de production d'hydrocarbures supérieurs à partir du méthane et du brome
    WO-2011008573-A1January 20, 2011Marathon Gtf Technology, Ltd.Conversion de bromure d'hydrogène en brome élémentaire
    US-4849573-AJuly 18, 1989Mobil Oil CorporationProcess for manufacturing light olefins
    US-5105045-AApril 14, 1992Phillips Petroleum CompanyMethod of oxidative conversion
    US-7145045-B2December 05, 2006Shell Oil CompanyProcess for the preparation of alkanediol
    US-4950811-AAugust 21, 1990Rhone Poulenc ChimieProcess for the preparation of trifluoro-ethanol by hydrolysis, in the gas phase, of chlorotrifluoroethane
    US-5698747-ADecember 16, 1997Exxon Chemical Patents Inc.Ester-free ethers
    US-7091270-B2August 15, 2006Bromine Compounds Ltd.Pentabromobenzyl alkyl ethers and their use as fire retardants
    US-4777321-AOctober 11, 1988Mobil Oil CorporationFeedstock preparation and conversion of oxygenates to olefins
    US-5019652-AMay 28, 1991The United States As Represented By The United States Department Of EnergyCatalysts and method
    US-2002193649-A1December 19, 2002O'rear Dennis J., Schinski William L., Saleh Elomari, Reynolds Richard N., Herron Steven J.Synthesis of high quality normal alpha olefins
    US-5847224-ADecember 08, 1998Global Octanes CorporationMethod for improving the color of MTBE, ETBE and TAME
    US-7220391-B1May 22, 2007University Of Central Florida Research Foundation, Inc.UV photochemical option for closed cycle decomposition of hydrogen sulfide
    US-2005047927-A1March 03, 2005Lee Chung J., Oanh Nguyen, Lee Wei Shiang Charles, Michael Solomensky, Atul Kumar, Chung Chang James Yu, Binh NguyenProcess modules for transport polymerization of low epsilon thin films
    US-2008275284-A1November 06, 2008Marathon Oil CompanyProcess for converting gaseous alkanes to liquid hydrocarbons
    US-5107051-AApril 21, 1992Exxon Chemical Patents Inc.Halogen resistant hydrotreating process and catalyst
    WO-2005110953-A1November 24, 2005Shell Internationale Research Maatschappij B.V.Derivatives of alcohols and olefins
    WO-2008157044-A1December 24, 2008Albemarle CorporationProcédés de production d'hydrocarbures supérieurs à partir de méthane
    US-5959170-ASeptember 28, 1999Atlantic Richfield CompanyMethane conversion process
    US-5782936-AJuly 21, 1998Suburban Propane, L.P.Additive compositions for LPG fuel
    US-2005038310-A1February 17, 2005Lorkovic Ivan M., Maria Noy, Sherman Jeffrey H., Weiss Michael J., Stucky Galen D.Hydrocarbon synthesis
    US-4587375-AMay 06, 1986Labofina, S.A.Process for the isomerization of olefins
    US-6635793-B2October 21, 2003Sri InternationalPreparation of epoxides from alkanes using lanthanide-promoted silver catalysts
    EP-0164798-A1December 18, 1985George Andrew OlahProcédé pour la préparation de monohalogénures de méthyle
    US-7713510-B2May 11, 2010Albemarle CorporationProcesses for oxidation of bromides to produce bromine and catalysts useful therein
    WO-2007125332-A1November 08, 2007Petroleo Brasileiro S.A. Petrobras, Benson, John, EverettProcede d'hydroconversion d'un melange d'huiles organiques de differentes origines
    US-7390395-B2June 24, 2008Saleh ElomariHydrocarbon conversion using molecular sieve SSZ-56
    WO-2006118935-A2November 09, 2006Dow Global Technologies Inc.Halogenation oxydative d'hydrocarbures c1 en hydrocarbures c1 halogenes
    US-3496242-AFebruary 17, 1970Fmc CorpOxychlorination of mixed hydrocarbons
    WO-2005113440-A1December 01, 2005Uop LlcComposition zéolitique d'aluminosilicate cristallin: uzm-15
    US-5906892-AMay 25, 1999The Trustees Of Princeton UniversityElectron acceptor compositions on polymer templates
    US-6566572-B2May 20, 2003Wako Pure Chemical Industries, Ltd.Process for producing 9,10-diphenylanthracene
    US-4252687-AFebruary 24, 1981Gallaher LimitedCatalysts
    US-6713087-B2March 30, 2004Alkermes Controlled Therapeutics, Inc.Method of producing submicron particles of a labile agent and use thereof
    US-5087786-AFebruary 11, 1992Amoco CorporationHalogen-assisted conversion of lower alkanes
    US-6452058-B1September 17, 2002Dow Global Technologies Inc.Oxidative halogenation of C1 hydrocarbons to halogenated C1 hydrocarbons and integrated processes related thereto
    GB-950975-AMarch 04, 1964British Hydrocarbon Chem LtdProduction of detergent alkylate
    WO-2006007093-A1January 19, 2006Dow Global Technologies Inc.Apparatus and method for ziegler-natta research
    US-5798314-AAugust 25, 1998The Dow Chemical CompanySupported olefin polymerization catalyst
    US-4775462-AOctober 04, 1988Uop Inc.Non-oxidative method of sweetening a sour hydrocarbon fraction
    US-5073656-ADecember 17, 1991Union Carbide Chemicals And Plastics Company, Inc.High ethylene to ethane processes for oxidative coupling
    US-5055633-AOctober 08, 1991UopAdsorption and isomerization of normal and mono-methyl paraffins
    US-3894107-AJuly 08, 1975Mobil Oil CorpConversion of alcohols, mercaptans, sulfides, halides and/or amines
    US-4982024-AJanuary 01, 1991Ethyl CorporationProcess for the selective dehydrohalogenation of an admixture of alkylhalides
    US-4219604-AAugust 26, 1980Fuji Photo Film Co., Ltd.Method of forming microcapsules, microcapsular dispersion, and pressure sensitive recording sheet
    US-4814535-AMarch 21, 1989Mobil Oil CorporationConversion of oxygenates to gasoline at variable inlet temperature
    US-7226569-B2June 05, 2007Chevron U.S.A. Inc.Reduction of oxides of nitrogen in a gas stream using molecular sieve SSZ-56
    US-5705729-AJanuary 06, 1998Mobil Oil CorporationIsoparaffin-olefin alkylation process
    US-5401890-AMarch 28, 1995Albemarle CorporationProcess and apparatus for heat treating halogenated compounds
    US-5118899-AJune 02, 1992Phillips Petroleum CompanyComposition of matter and method of oxidative conversion of organic compounds therewith
    US-5928488-AJuly 27, 1999David S. NewmanElectrolytic sodium sulfate salt splitter comprising a polymeric ion conductor
    WO-2005019143-A1March 03, 2005Grt, Inc., The Regents Of The University Of CaliforniaMethod and apparatus for synthesizing olefins, alcohols, ethers, and aldehydes
    US-7271303-B1September 18, 2007Uop LlcMulti-zone process for the production of diesel and aromatic compounds
    WO-2006020234-A1February 23, 2006Dow Global Technologies Inc.Conversion of a multihydroxylated-aliphatic hydrocarbon or ester thereof to a chlorohydrin
    US-2008152555-A1June 26, 2008Yong Wang, White James FStaged alkylation in microchannels
    US-7250542-B2July 31, 2007Catalytic Distillation TechnologiesParaffin alkylation
    US-5480629-AJanuary 02, 1996The Trustees Of Princeton UniversityCatalytic production of hydrogen peroxide
    US-4071753-AJanuary 31, 1978Gte Laboratories IncorporatedTransducer for converting acoustic energy directly into optical energy
    US-4497967-AFebruary 05, 1985The Halcon Sd Group, Inc.Process for the preparation of ethanol from methanol, carbon monoxide _and hydrogen
    US-4060568-ANovember 29, 1977Mobil Oil CorporationSilica-modified zeolite catalyst and conversion therewith
    US-5470377-ANovember 28, 1995Whitlock; David R.Separation of solutes in gaseous solvents
    EP-0418975-A1March 27, 1991Union Carbide Chemicals And Plastics Company, Inc.Low temperature catalysts for oxidative coupling processes
    US-7282603-B2October 16, 2007Richards Alan KAnhydrous processing of methane into methane-sulfonic acid, methanol, and other compounds
    WO-2005058782-A1June 30, 2005Exxonmobil Chemical Patents Inc.Perfectionnements relatifs a l'hydrogenation
    US-3310380-AMarch 21, 1967Universal Oil Prod CoBromine recovery
    US-7011811-B2March 14, 2006Chevron U.S.A. Inc.Molecular sieve SSZ-65 composition of matter and synthesis thereof
    US-7253327-B2August 07, 2007Solvay S.A.Method of manufacture of a hydrofluoroalkane
    US-7148390-B2December 12, 2006Grt, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols, ethers, aldehydes, and olefins from alkanes
    US-7002050-B2February 21, 2006Oxeno Olefinchemie GmbhProcess for preparing tert-butanol from isobutene-containing hydrocarbon mixtures
    WO-2006067188-A1June 29, 2006Solvay (Société Anonyme)Procede de fabrication de 1,2-dichloroethane
    US-4044061-AAugust 23, 1977Mobil Oil CorporationPreheating methanol effects steady state operation of conversion to gasoline
    US-2536457-AJanuary 02, 1951Distillers Co Yeast LtdRecovery of bromine from hydrogen bromide
    US-2007284284-A1December 13, 2007Chevron U.S.A. Inc.Hydrocarbon conversion using molecular sieve ssz-75
    US-2007149819-A1June 28, 2007Chevron U.S.A. Inc.Synthesis of amines using molecular sieve ssz-74
    US-5908963-AJune 01, 1999Holdor Topsoe A/SPreparation of fuel grade dimethyl ether
    US-4704488-ANovember 03, 1987Chevron Research CompanyConversions of low molecular weight hydrocarbons to higher molecular weight hydrocarbons using a metal compound-containing catalyst (111-A)
    US-3886287-AMay 27, 1975Shiseido Co LtdCosmetics containing saturated, branched synthetic higher hydrocarbon
    GB-363009-ADecember 17, 1931John Philip Baxter, William Arthur Meredith Edward, Ramsay Middleton Winter, Ici LtdProduction of acetylene and vinyl chloride from ethylene dichloride
    GB-793214-AApril 09, 1958Bataafsche PetroleumProcess for the conversion of hydrocarbons containing acyclic carbon atoms
    US-3879473-AApril 22, 1975Phillips Petroleum CoPreparation of ethers from alcohols and olefins catalyzed by iodine
    US-6380444-B1April 30, 2002Statoil Research Centre, Niels J. Bjerrum, Gang Xiao, Hans Aage HjulerProcess for the catalytic oxidation of hydrocarbons
    US-5565616-AOctober 15, 1996Board Of Regents, The University Of Texas SystemControlled hydrothermal processing
    CA-2510093-CSeptember 29, 2009Apotex Pharmachem Inc., Allan W. Rey, K.S. Keshava MurthyNouveau procede de preparation d'.alpha.-chlorovinyle, de composes .alpha.,.alpha.-dichlores et de composes acetyleniques a partir de cetones
    US-4605803-AAugust 12, 1986Mobil Oil CorporationAcid-catalyzed organic compound conversion
    US-6022929-AFebruary 08, 2000Exxon Chemical Patents Inc.Amorphous olefin polymers, copolymers, methods of preparation and derivatives thereof
    WO-2007091009-A2August 16, 2007Sinclair Pharmaceuticals LimitedPreparation of delmopinol
    US-4735747-AApril 05, 1988Societe Nationale Elf Aquitaine (Production)Process and apparatus for the photochemical sulphochlorination of gaseous alkanes
    US-6692723-B2February 17, 2004Institut Francais Du PetroleMTT zeolite comprising crystals and crystal aggregates with specific granulometries, and its use as a catalyst for isomerizing straight chain paraffins
    EP-1186591-A2March 13, 2002The NutraSweet CompanyVerfahren zur Herstellung von 3,3-Dimethylbutyraldehyd durch Oxidation von 3,3-Dimethylbutanol
    US-5385718-AJanuary 31, 1995Imperial Chemical Industries PlcZeolites
    US-4052471-AOctober 04, 1977Pearsall Chemical CorporationProcess for chlorinating C8 to C30 linear hydrocarbons
    GB-883256-ANovember 29, 1961Columbia Southern Chem CorpHalogenation process
    WO-2007017900-A2February 15, 2007Sisir Kumar Mandal, Suleman Mohammad Shafi InamdarPreparation of para dichlorobenzene from benzene or mono chlorobenzene
    US-2004158107-A1August 12, 2004Showa Denko K.K.Production process and use for propargyl alcohol and its intermediate
    US-2006138025-A1June 29, 2006Chevron U.S.A. Inc.Hydrocarbon conversion using molecular sieve SSZ-70
    US-6056804-AMay 02, 2000Questor Industries Inc.High frequency rotary pressure swing adsorption apparatus
    US-4899001-AFebruary 06, 1990UopProcess for the simultaneous hydroconversion of a first feedstock comprising unsaturated, halogenated organic compounds and a second feedstock comprising saturated, halogenated organic compounds
    US-3928483-ADecember 23, 1975Mobil Oil CorpProduction of gasoline hydrocarbons
    US-5436378-AJuly 25, 1995AtochemDrying of hydrocarbon/hydrochloric acid/water admixtures
    US-5821394-AOctober 13, 1998SolvayProcess for converting a chlorinated alkane into a less chlorinated alkene
    US-6713655-B2March 30, 2004Grt Inc, Univ CaliforniaIntegrated process for synthesizing alcohols, ethers, aldehydes, and olefins from alkanes
    US-4945175-AJuly 31, 1990UopDehydrocyclodimerization process start-up procedure
    WO-2005095310-A2October 13, 2005Shell Internationale Research Maatschappij B.V.The utilization of zirconium and zirconium based alloys for the containment of halogen containing environments used in the production of olefins, alcohols, ethers, ethoxylates glycols, and olefin oxides from alkanes
    US-6946566-B2September 20, 2005Daiso Co., Ltd.Process for preparation of optically active halogeno hydroxypropyl compound and glycidyl compound
    US-5780703-AJuly 14, 1998Mobil Oil CorporationProcess for producing low aromatic diesel fuel with high cetane index
    CA-2203115-CSeptember 19, 2006Pierluigi Fatutto, Andrea Marsella, Dario Vio, Evc Technology AgOxychloration de l'ethylene dans un reacteur a lit fixe en une seule etape
    US-4307261-ADecember 22, 1981Vulcan Materials CompanyProcess for separating ferric iron from chlorinated hydrocarbons
    US-4654449-AMarch 31, 1987Mobil Oil CorporationFormation of halogenated hydrocarbons from hydrocarbons
    US-6034288-AMarch 07, 2000Imperial Chemical Industries PlcProcess for vaporization of halocarbons
    US-6692626-B2February 17, 2004Questair Technologies Inc.Adsorbent laminate structures
    US-4748013-AMay 31, 1988Toyo Soda Manufacturing Co., Ltd.Adsorbent for recovery of bromine and bromine-recovering process using same
    US-6547958-B1April 15, 2003Chevron U.S.A. Inc.Hydrocarbon conversion using zeolite SSZ-59
    US-6337063-B1January 08, 2002Institut Francais Du PetroleProcess for preparing a zeolite with structure type EUO using structuring agent precursors and its use as an AC8 isomerisation catalyst
    US-5538540-AJuly 23, 1996Whitlock; David R.Separation of solutes in gaseous solvents
    CA-1101441-A1December 31, 1969
    WO-2005056525-A2June 23, 2005Bio-Technical ResourcesDeacetylation of n-acetylglucosamine
    US-2010087686-A1April 08, 2010Fong Howard Lam Ho, Swain Richard DaleIntegrated process to coproduce aromatic hydrocarbons and ethylene and propylene
    US-7560607-B2July 14, 2009Marathon Gtf Technology, Ltd.Process for converting gaseous alkanes to liquid hydrocarbons
    US-2005234277-A1October 20, 2005Waycuilis John JProcess for converting gaseous alkanes to liquid hydrocarbons
    US-7252920-B2August 07, 2007Zeon CorporationMethod for manufacturing polymerized toner
    US-4052472-AOctober 04, 1977Mobil Oil CorporationMordenite conversion of alkanols to penta- and hexamethyl benzenes
    US-4899002-AFebruary 06, 1990Mobil Oil Corp.Integrated staged conversion of methanol to gasoline and distillate
    US-5243114-ASeptember 07, 1993Mobil Oil CorporationOligomerization of alpha-olefins over layered silicate compositions containing pillars of silica and group VIB metal oxide
    US-5675052-AOctober 07, 1997The Boc Group, Inc.Hydrocarbon alkylation process
    US-5300126-AApril 05, 1994Mobil Oil CorporationProcess for improving olefin etherification catalyst life
    US-5414173-AMay 09, 1995The Dow Chemical CompanyProcess of preparing cyclopentadiene and substituted derivatives thereof
    US-2010096588-A1April 22, 2010Sagar Gadewar, Saydul Amin Sardar, Philip Grosso, Aihua Zhang, Vivek Julka, Peter StolmanovContinuous Process for Converting Natural Gas to Liquid Hydrocarbons
    US-6423211-B1July 23, 2002Phillips Petroleum CompanyMethod for reducing organic fluoride levels in hydrocarbons
    US-6921597-B2July 26, 2005Questair Technologies Inc.Electrical current generation system
    US-5166452-ANovember 24, 1992Hoechst AktiengesellschaftProcess for inhibiting and destroying peroxides in dialkyl ethers
    US-5210357-AMay 11, 1993Phillips Petroleum Company, Atlantic Richfield CompanyComposition of matter and method of oxidative conversion of organic compounds therewith
    US-7230150-B2June 12, 2007Grt, Inc.Zone reactor
    WO-2008157045-A1December 24, 2008Albemarle CorporationProcesses for producing higher hydrocarbons from hydrocarbon feed sources
    US-4973786-ANovember 27, 1990Karra Sankaram BProcess for the pyrolytic oxidation of methane to higher molecular weight hydrocarbons and synthesis gas
    US-4523040-AJune 11, 1985Olah George AMethyl halides and methyl alcohol from methane
    EP-0526908-A2February 10, 1993Daikin Industries, LimitedVerfahren zur Herstellung von 1,1,1-Trifluoro-2,2-Dichlorethan
    EP-0510238-A1October 28, 1992NOVAMONT S.p.A.Process for producing lower poliols and mixtures thereof
    US-4376019-AMarch 08, 1983Imperial Chemical Industries PlcHalogenation process
    US-6679986-B1January 20, 2004Total Raffinage Distribution S.A.Catalytic support with an oxide base from a metal belonging to the SVI group of the periodic table, its preparation and its uses
    US-4105755-AAugust 08, 1978Rockwell International CorporationHydrogen production
    US-5055634-AOctober 08, 1991UopAdsorption and isomerization of normal and mono-methyl paraffins
    US-2003004380-A1January 02, 2003Helmut Grumann, Manfred Stoger, Jurgen Eichler, Dieter Jaculi, Winfried Lork, Arend Greve, Jan WilkensMethod for producing 1,2-dichloroethane
    US-2006138026-A1June 29, 2006Chevron U.S.A. Inc.Hydrocarbon conversion using molecular sieve SSZ-71
    WO-2005113437-A1December 01, 2005Uop LlcHigh silica zeolites uzm-5hs
    GB-796085-AJune 04, 1958Bataafsche PetroleumHydrocarbon conversion process
    US-2004006246-A1January 08, 2004Sherman Jeffrey H., Mcfarland Eric W., Weiss Michael J., Lorkovic Ivan Marc, Laverman Leroy E., Shouli Sun, Schaefer Dieter J., Galen Stucky, Peter FordMethod and apparatus for synthesizing olefins, alcohols, ethers, and aldehydes
    US-2007004955-A1January 04, 2007Richard Kay, Morris George E, Sunley John GProcess for preparing branched chain hydrocarbons
    US-5457255-AOctober 10, 1995Mitsubishi Oil Co., Ltd.Catalysts for hydrogenolytic dealkylation and use thereof
    US-4658077-AApril 14, 1987Phillips Petroleum CompanyComposition of matter and method of oxidative conversion of organic compounds therewith
    US-5430214-AJuly 04, 1995The Dow Chemical CompanyHydrodehalogenation process and catalyst for use therein
    WO-2006039213-A1April 13, 2006Chevron U.S.A. Inc.Molecular sieve ssz-65
    US-7049388-B2May 23, 2006Dow Global Technologies Inc.Process for manufacturing an α-dihydroxy derivative and epoxy resins prepared therefrom
    US-6225517-B1May 01, 2001Total Raffinage Distribution S.A.Alkylation catalyst, method for preparing same, and use thereof in alkylation methods
    US-4814532-AMarch 21, 1989Chemical Company, Ltd. Asahi, Zenichi YoshidaProcess for producing alkylcyclopentadiene derivatives
    US-5215648-AJune 01, 1993Chevron Research And Technology CompanyHydrocarbon conversion processes using SSZ-31
    US-4891463-AJanuary 02, 1990Mobil Oil CorporationAromatization of aliphatics over a zeolite containing framework gallium
    US-4658073-AApril 14, 1987Mobil Oil CorporationControl system for multistage chemical upgrading
    US-4851602-AJuly 25, 1989Mobil Oil CorporationAlkanes and alkenes conversion to high octane gasoline
    GB-2095249-ASeptember 29, 1982PfizerBis-esters of methanediol with acetonides of ampicillin or amoxillin and penicillanic acid 1,1-dioxide
    WO-2007044139-A1April 19, 2007Badger Licensing LlcAccroissement du rendement de production d'une installation de production de bisphénol a
    GB-1104294-AFebruary 21, 1968Ralph William KingProduction of lower alkanols and lower alkyl bromides
    US-5656149-AAugust 12, 1997Chevron U.S.A. Inc.Hydrocarbon conversion processes using zeolite SSZ-41
    US-2008171898-A1July 17, 2008Waycuilis John JProcess for converting gaseous alkanes to liquid hydrocarbons
    US-4783566-ANovember 08, 1988Uop Inc.Hydrocarbon conversion process
    GB-156122-AMarch 30, 1922Otto Traun S ForschungslaboratProcess for the manufacture of diolefines and derivatives thereof
    US-4333852-AJune 08, 1982Union Carbide CorporationCatalyst for the selective production of ethanol and methanol directly from synthesis gas
    US-2004158108-A1August 12, 2004Snoble Karel A.J., Shihan Chen, Russ Johnson, Yates Stephen F., Bershitsky Alexander M., Garibaldi Chad D.Purification of alcohol
    US-2007276168-A1November 29, 2007Laurent Garel, Laurent Saint-JalmesMethod For Preparation Of A Fluoroaromatic Compound From An Aminoaromatic Compound
    US-7064240-B2June 20, 2006Showa Denko K.K.Process for producing perfluorocarbons and use thereof
    US-5004847-AApril 02, 1991Ethyl CorporationRecovery of hexabromocyclododecane particles
    US-5099084-AMarch 24, 1992Stauffer John EProcess for the chlorination of methane
    US-5228888-AJuly 20, 1993The Boc Group, Inc.Economical air separator
    US-5093542-AMarch 03, 1992Atlantic Richfield CompanyMethane conversion process
    US-6124514-ASeptember 26, 2000Krupp Uhde GmbhProcess for generating pure benzene from reformed gasoline
    US-2002198416-A1December 26, 2002Zhou Xiao Ping, Lorkovic Ivan Marc, Sherman Jeffrey H.Integrated process for synthesizing alcohols, ethers, and olefins from alkanes
    US-6545191-B1April 08, 2003John E. StaufferProcess for preparing ethanol
    US-4138440-AFebruary 06, 1979Mobil Oil CorporationConversion of liquid alcohols and ethers with a fluid mass of ZSM-5 type catalyst
    US-6465699-B1October 15, 2002Gri, Inc., The Regents Of The University Of CaliforniaIntegrated process for synthesizing alcohols, ethers, and olefins from alkanes
    US-4788369-ANovember 29, 1988Mobil Oil CorporationConversion of methanol to gasoline
    US-6822125-B2November 23, 2004Korea Research Institute Of Chemical TechnologyMethod for preparing dimethylether using a membrane reactor for separation and reaction
    US-7091391-B2August 15, 2006Stauffer John EMethane to olefins
    US-7193093-B2March 20, 2007Shell Oil CompanyProcess for producing alkylene oxide
    EP-0560546-A1September 15, 1993Exxon Research And Engineering CompanyVerfahren zur Herstellung von Alkanolen und Alkylhalogeniden
    US-4899000-AFebruary 06, 1990Stauffer John EProduction of allyl chloride
    US-6723808-B2April 20, 2004Univation Technologies, LlcCatalyst system and its use in a polymerization process
    WO-2007094995-A2August 23, 2007Grt, Inc.Continuous process for converting natural gas to liquid hydrocarbons
    US-7250107-B2July 31, 2007Institut Francais Du PetroleFlexible method for producing oil bases and distillates from feedstock containing heteroatoms
    WO-2006036293-A1April 06, 2006Uop LlcConversion d'un compose oxygene alcoolique en propylene au moyen d'une technologie a lit mobile et par une etape d'etherification
    US-2004187684-A1September 30, 2004Saleh ElomariUsing molecular sieve SSZ-65 for reduction of oxides of nitrogen in a gas stream
    US-4133966-AJanuary 09, 1979Gulf Research & Development CompanySelective formation of ethanol from methanol, hydrogen and carbon monoxide
    US-5354916-AOctober 11, 1994Exxon Research And Engineering CompanyLow temperature conversion of alkanes
    US-4544781-AOctober 01, 1985Mobil Oil CorporationControl of temperature exotherms in the conversion of methanol to gasoline hydrocarbons
    US-2006229475-A1October 12, 2006Weiss Michael J, Shouli SunSynthesis of hydroxylated hydrocarbons
    US-2007238909-A1October 11, 2007Gadewar Sagar B, Wyrsta Michael D, Philip Grosso, Aihua Zhang, Mcfarland Eric W, Komon Zachary J, Sherman Jeffrey HContinuous process for converting natural gas to liquid hydrocarbons
    US-2488083-ANovember 15, 1949Socony Vacuum Oil Co IncManufacture of liquid hydrocarbons
    GB-553950-AJune 11, 1943Du PontImprovements in or relating to the manufacture of halogenated hydrocarbons
    GB-474922-ANovember 15, 1937Ig Farbenindustrie AgProcess for chlorinating and brominating hydrocarbons
    US-6953873-B2October 11, 2005Wisconsin Alumni Research FoundationLow-temperature hydrocarbon production from oxygenated hydrocarbons
    US-5600043-AFebruary 04, 1997The Geon CompanyOxychlorination process
    US-6888013-B2May 03, 2005Polimeri Europa S.P.A.Integrated process for the preparation of olefin oxides
    GB-991303-AMay 05, 1965British Hydrocarbon Chem LtdThe production of olefines by the dehydrochlorination of alkyl chlorides
    US-6958306-B2October 25, 2005Univation Technologies, LlcActivated catalyst systems from substituted dialuminoxane complexes
    US-6902602-B2June 07, 2005Questair Technologies Inc.Gas separation by combined pressure swing and displacement purge
    WO-2007050745-A1May 03, 2007Shell Internationale Research Maatschappij B.V.Internal olefins process
    US-4538015-AAugust 27, 1985Mobil Oil CorporationCatalysis over activated zeolites
    EP-1837320-A1September 26, 2007ETH ZürichVerfahren zur Herstellung von gesättigten C2 bis C5-Kohlenwasserstoffen
    US-5705712-AJanuary 06, 1998UopIntegrated process for producing diisopropyl ether, an isopropyl tertiary alkyl ether and isopropyl alcohol
    GB-1172002-ANovember 26, 1969Marathon Oil Co, Danford H OlsonLow Temperature Process for Halogenation of Hydrocarbons
    US-5185479-AFebruary 09, 1993Stauffer John EProcess for methyl alcohol
    US-5741949-AApril 21, 1998Great Lakes Chemical CorporationContinuous bromination process and products thereof
    US-7182871-B2February 27, 2007Global Biosciences, Inc.Wastewater treatment with alkanes
    EP-1312411-A2May 21, 2003Rohm And Haas CompanyElektroaktive katalyse
    US-2003125589-A1July 03, 2003Grt, Inc.Zone reactor
    US-2003120121-A1June 26, 2003Grt, Inc.Method and apparatus for synthesizing from alcohols and ethers from alkanes, alkenes, and aromatics
    US-5411641-AMay 02, 1995E. I. Du Pont De Nemours And CompanyElectrochemical conversion of anhydrous hydrogen halide to halogen gas using a cation-transporting membrane
    US-6797845-B1September 28, 2004Dow Global Technologies Inc.Process for vinyl chloride manufacture from ethane and ethylene with immediate HCl recovery from reactor effluent
    US-7273957-B2September 25, 2007Catalytic Distillation TechnologiesProcess for the production of gasoline stocks
    US-6090312-AJuly 18, 2000Ziaka; Zoe D., Vasileiadis; SavvasReactor-membrane permeator process for hydrocarbon reforming and water gas-shift reactions
    US-6620757-B2September 16, 2003Univation Technologies, LlcCatalyst systems and their use in a polymerization process
    GB-2095245-ASeptember 29, 1982Ici PlcChlorination of alkanes
    US-6002059-ADecember 14, 1999Mobil Oil CorporationProcess for upgrading natural gas
    WO-2005105709-A1November 10, 2005Shell Internationale Research Maatschappij B.V.Process to convert linear alkanes into alpha olefins
    US-6838576-B1January 04, 20053M Innovative Properties CompanyProcess for preparing functional group-containing olefinic compounds
    US-7267758-B2September 11, 2007Institut Francais Du PetroleFlexible method for producing oil bases and middle distillates with hydroisomerization-conversion followed by catalytic dewaxing
    WO-2006053345-A1May 18, 2006Velocys Inc.Procede utilisant la technologie de microcanal pour conduire une reaction d'alkylation ou d'acylation
    US-7148356-B2December 12, 2006Board Of Trustees Of Michigan State UniversityProcess for the catalytic synthesis of biaryls and polymers from aryl compounds
    US-3883651-AMay 13, 1975Boehringer Sohn IngelheimPharmaceutical compositions containing a 2-(aminoalkylamino)-4-amino-thieno{8 3,2-d{9 pyrimidine and method of use
    US-5708246-AJanuary 13, 1998Battelle Memorial InstituteMethod of photocatalytic conversion of C-H organics
    US-5026934-AJune 25, 1991Lyondell Petrochemical CompanyMethod for converting light hydrocarbons to olefins, gasoline and methanol
    WO-2009152403-A1December 17, 2009Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons
    GB-1212240-ANovember 11, 1970Kalk Chemische Fabrik GmbhMethod of preparing alkyl bromides (including substituted alkyl bromides)
    US-2005192468-A1September 01, 2005Sherman Jeffrey H., Mcfarland Eric W., Weiss Michael J., Lorkovic Ivan M., Laverman Leroy E., Shouli Sun, Schaefer Dieter J., Stucky Galen D., Ford Peter C., Philip Grosso, Breed Ashley W., Doherty Michael F.Hydrocarbon conversion process improvements
    US-2011218372-A1September 08, 2011Marathon Gtf Technology, Ltd.Processes and systems for the staged synthesis of alkyl bromides
    EP-0976705-A1February 02, 2000Ube Industries, Ltd.Method of producing a phenolalkylether compound
    US-7091387-B2August 15, 2006Shell Oil CompanyProcess to convert alkanes into primary alcohols
    US-2011218374-A1September 08, 2011Marathon Gtf Technology, Ltd.Processes and systems for the staged synthesis of alkyl bromides
    WO-2009152405-A1December 17, 2009Marathon Gtf Technology, Ltd.Hydrogénation d’alcanes multi-bromés
    US-3702886-ANovember 14, 1972Mobil Oil CorpCrystalline zeolite zsm-5 and method of preparing the same
    US-6552241-B1April 22, 2003Conocophillips CompanyAlkylation process
    US-5276242-AJanuary 04, 1994Phillips Petroleum CompanyAlkylation process
    WO-2006015824-A1February 16, 2006Exxonmobil Chemical Patents Inc., Exxonmobil Chemical LimitedProcede pour produire du sec-butylbenzene
    WO-2006071354-A1July 06, 2006Chevron U.S.A. Inc.Composition de matiere de tamis moleculaire ssz-70 et synthese de celui-ci
    GB-2191214-ADecember 09, 1987British Petroleum Co PlcProduction of higher molecular weight hydrocarbons from methane
    US-5675046-AOctober 07, 1997Showa Denko K.K.Process for producing perfluorocarbon
    US-7094936-B1August 22, 2006Great Lakes Chemical CorporationProcess for preparing halogenated alkanes
    US-6525230-B2February 25, 2003Grt, Inc.Zone reactor
    US-6068679-AMay 30, 2000Aga AktiebolagProcess of and a device for producing a gas, containing at least one component, from a gas mixture
    US-6406523-B1June 18, 2002Questair Technologies, Inc.Rotary pressure swing adsorption apparatus
    GB-796048-AJune 04, 1958Bataafsche PetroleumConversion of hydrocarbons
    US-2009312586-A1December 17, 2009Marathon Gtf Technology, Ltd.Hydrogenation of multi-brominated alkanes
    US-3246043-AApril 12, 1966Universal Oil Prod CoPreparation of olefinic hydrocarbons
    US-4543434-ASeptember 24, 1985Mobil Oil CorporationProcess for producing liquid hydrocarbon fuels
    US-5565092-AOctober 15, 1996Exxon Chemical Patents Inc.Halogen resistant hydrogenation process and catalyst
    US-7199083-B2April 03, 2007Self Generating Foam IncoporatedSelf-generating foamed drilling fluids
    WO-2006039354-A2April 13, 2006Ab-Cwt, LlcProcess for conversion of organic, waste, or low-value materials into useful products
    WO-2005105715-A1November 10, 2005Shell Internationale Research Maatschappij B.V.Procédé pour convertir des alcanes en alcools primaires
    WO-2007141295-A1December 13, 2007High Point Pharmaceuticals, LlcProcédé de préparation de dérivés acide phénoxyacétique
    US-5105046-AApril 14, 1992Amoco CorporationOxidative conversion of lower alkanes to higher hydrocarbons via fluorine-containing materials
    US-7169730-B2January 30, 2007Hyperion Catalysis International, Inc.Modified carbide and oxycarbide containing catalysts and methods of making and using thereof
    WO-2007001934-A2January 04, 2007Chevron U.S.A. Inc.Molecular sieve ssz-56 composition of matter and synthesis thereof
    US-4006169-AFebruary 01, 1977Smithkline CorporationEpoxidation of α,β-ethylenic ketones
    EP-1440939-A1July 28, 2004Humboldt-Universität zu BerlinVerfahren zur Herstellung von amorphen Metallfluoriden
    US-4642404-AFebruary 10, 1987Mobil Oil CorporationConversion of olefins and paraffins to higher hydrocarbons
    WO-2008157043-A1December 24, 2008Albemarle CorporationProcédés de production d'hydrocarbures supérieurs à partir du méthane
    WO-2006067155-A2June 29, 2006Albemarle Netherlands BvCatalyseur, son procede de preparation, et son application
    WO-2005090272-A1September 29, 2005University Of UtahReacteur cyclonique et procedes associes
    US-2003166973-A1September 04, 2003Grt, Inc.Integrated process for synthesizing alcohols, ethers, aldehydes, and olefins from alkanes
    US-3598876-AAugust 10, 1971Universal Oil Prod CoSelective halogenation of hydrocarbons
    WO-2006104909-A2October 05, 2006Shell Internationale Research Maatschappij B.V.Procede de distillation catalytique pour l'obtention d'haloalkanes primaires
    US-6797851-B2September 28, 2004Exxonmobil Chemical Patents Inc.Two catalyst process for making olefin
    US-2007142680-A1June 21, 2007Ayoub Paul M, Hendrik Dirkzwager, Murray Brendan D, Sumrow Steve CMethods of preparing branched aliphatic alcohols
    US-2007148067-A1June 28, 2007Chevron U.S.A. Inc.Treatment of engine exhaust using molecular sieve ssz-74
    WO-2006067193-A1June 29, 2006Solvay (Société Anonyme)Procede de fabrication de 1,2-dichloroethane
    US-6909024-B1June 21, 2005The Dow Chemical CompanyProcess for the conversion of ethylene to vinyl chloride and novel catalyst compositions useful for such process
    EP-1760057-A1March 07, 2007Tokuyama CorporationMethod for producing polyhalogenated diamantane and derivative thereof
    WO-2007111997-A2October 04, 2007Velocys Inc.Process for making styrene using microchannel process technology
    US-5770175-AJune 23, 1998Chevron U.S.A. Inc.Method of preparing zeolite SSZ-42
    US-5663465-ASeptember 02, 1997Evc Technology AgBy-product recycling in oxychlorination process
    US-4621164-ANovember 04, 1986Purdue Research FoundationHydrocarbon production
    US-4524228-AJune 18, 1985Mobil Oil CorporationProduction of durene and gasoline from synthesis gas
    US-7083714-B2August 01, 2006Chevron U.S.A. Inc.Hydrocarbon conversion using molecular sieve SSZ-65
    US-7053252-B2May 30, 2006AtofinaProcess for preparing 1,1,1-trifluoro-2,2-dichloroethane
    US-7026145-B2April 11, 2006Cargill, Incorporated, Csm NvProcess for producing a purified lactic acid solution
    GB-1253618-ANovember 17, 1971Perstorp AbProcess for the production of dry semi-formals
    US-6740146-B2May 25, 2004Edward L. SimondsOxygen concentrator
    US-2006229228-A1October 12, 2006Zachary John Anthony Komon, Weiss Michael JMethod of making alkoxylates
    US-2004188271-A1September 30, 2004Council Of Scientific And Industrial ResearchProcess for electrochemical oxidation of bromide to bromine
    US-6825383-B1November 30, 2004Council Of Scientific And Industrial ResearchCatalytic process for regiospecific chlorination of alkanes, alkenes and arenes
    US-2005245777-A1November 03, 2005Fong Howard L, Trevino Lizbeth O C, Murray Brendan D, Cano Manuel LProcess to convert linear alkanes into alpha olefins
    US-2009247796-A1October 01, 2009Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons
    WO-2007130054-A1November 15, 2007Exxonmobil Chemical Patents Inc.Improved catalyst composition
    US-6203712-B1March 20, 2001Institut Francais Du PetroleProcess for separation by settling in a plurality of distinct zones
    US-4973776-ANovember 27, 1990Energy, Mines & Resources - CanadaConversion of methane to gasoline-range hydrocarbons via isobutene
    WO-2011109244-A2September 09, 2011Marathon Gtf Technology, Ltd.Procédés et systèmes de synthèse en plusieurs étapes faisant appel à des bromures d'alkyle
    EP-1808227-A1July 18, 2007Toagosei Co., Ltd.Process for producing metal oxide catalyst
    US-2007213545-A1September 13, 2007Bolk Jeroen W, Bos Alouisius N R, Evans Wayne E, Lockemeyer John R, Mcallister Paul M, Marie Ramakers Bernardus F J, Rekers Dominicus M, Slapak Mathias J PMethod Of Installing An Epoxidation Catalyst In A Reactor, A Method Of Preparing An Epoxidation Catalyst, An Epoxidation Catalyst, A Process For The Preparation Of An Olefin Oxide Or A Chemical Derivable From An Olefin Oxide, And A Reactor Suitable For Such A Process
    US-6933417-B1August 23, 2005Dow Global Technologies Inc.Process for vinyl chloride manufacture from ethane and ethylene with partial CHl recovery from reactor effluent
    US-5107061-AApril 21, 1992Exxon Chemical Patents Inc.Removal of organochlorides from hydrocarbon feed streams
    US-5276240-AJanuary 04, 1994Board Of Regents, The University Of Texas SystemCatalytic hydrodehalogenation of polyhalogenated hydrocarbons
    US-5866735-AFebruary 02, 1999Phillips Petroleum CompanyHydrocarbon hydrogenation process
    US-6900363-B2May 31, 2005Basf AktiengesellschaftMethod for the production of 1,2-dichloroethane
    US-2004062705-A1April 01, 2004Philippe LeducProcess for lowering the content of organic matter and nitrogenous products contained in bromide-containing effluents
    US-7208641-B2April 24, 2007Tosoh F-Tech, Inc.Method for producing 2,2,2-trifluoroethanol
    US-2007078285-A1April 05, 2007Battelle Memorial InstituteDimethyl ether production from methanol and/or syngas
    US-RE38493-EApril 13, 2004Questair Technologies Inc.Flow regulated pressure swing adsorption system
    US-6984763-B2January 10, 2006Dow Global Technologies Inc.Oxidative halogenation and optional dehydrogenation of c3+hydrocarbons
    US-2007197801-A1August 23, 2007Bolk Jeroen W, Bos Alouisius Nicolaas R, Evans Wayne E, Lockemeyer John R, Mcallister Paul M, Ramakers Bernardus Franciscus, Rekers Dominicus M, Slapak Mathias Jozef PMethod of installing an epoxidation catalyst in a reactor, a method of preparing an epoxidation catalyst, an epoxidation catalyst, a process for the preparation of an olefin oxide or a chemical derivable from an olefin oxide, and a reactor suitables for such a process
    US-2003069452-A1April 10, 2003Sherman Jeffrey H., Mcfarland EricMethod and apparatus for synthesizing from alcohols and ethers from alkanes, alkenes, and aromatics
    WO-2008157047-A1December 24, 2008Albemarle CorporationProcesses for producing hydrogen from hydrocarbon feed sources
    US-2005171393-A1August 04, 2005Lorkovic Ivan M.Hydrocarbon synthesis
    US-8173851-B2May 08, 2012Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons
    US-7037358-B2May 02, 2006The Boc Group, Inc., Questair Technologies Inc.PSA with adsorbents sensitive to contaminants
    WO-2007046986-A2April 26, 2007Marathon Oil CompanyProcess for converting gaseous alkanes to olefins and liquid hydrocarbons
    WO-2008036563-A2March 27, 2008Albemarle CorporationProcédés de conversion de méthane en hydrocarbures utiles et catalyseurs à cet effet
    US-2003078456-A1April 24, 2003Aysen Yilmaz, Yilmaz Gurkan Atinc, Lorkovic Ivan M., Stucky Galen D., Ford Peter C., Mcfarland Eric, Sherman Jeffrey H.Integrated process for synthesizing alcohols, ethers, aldehydes, and olefins from alkanes
    US-2003065239-A1April 03, 2003Peter Zhu, Roberts Charles G., Harriet Chan-MyersNon-hazardous basic neutralization of aldehydes
    US-2008022717-A1January 31, 2008Toyo Engineering CorporationProcess and apparatus for separation of hydrocarbons from liquefied natural gas
    GB-586483-AMarch 20, 1947Standard Oil Dev CoProcess for the conversion of normally gaseous olefins to liquid hydrocarbons
    GB-930341-AJuly 03, 1963California Research CorpCatalytic oxidation of hydrobromic acid with air
    US-2006149116-A1July 06, 2006Slaugh Lynn H, Fenouil Laurent A, Fong Howard LProcess for separating olefins from saturated hydrocarbons
    US-6953868-B2October 11, 2005Dow Global Technologies Inc., Regents Of The University Of MinnesotaOxyfunctionalization of polyolefins
    US-7019182-B2March 28, 2006Grt, Inc.Method of hydrocarbon preservation and environmental protection
    GB-536491-AMay 16, 1941Bataafsche PetroleumA process for the production of aromatic hydrocarbons from unsaturated hydrocarbons
    US-2011071326-A1March 24, 2011Marathon Gtf Technology, Ltd.Process for converting gaseous alkanes to liquid hydrocarbons
    GB-1233299-AMay 26, 1971
    GB-402928-ADecember 14, 1933Bataafsche PetroleumA process for the halogenation of unsaturated hydrocarbons
    US-2004152929-A1August 05, 2004Clarke William D, Haymon Terry D, Henley John P, Hickman Daniel A, Jones Mark E, Miller Matt C, Morris Thomas E, Reed Daniel J, Samson Lawrence J, Smith Steven AProcess for vinyl chloride manufacture from ethane and ethylene with air feed and alternative hcl processing methods
    US-2009163749-A1June 25, 2009Microvast Technologies, Ltd.Conversion of methane into c3˜c13 hydrocarbons
    US-7084308-B1August 01, 2006Stauffer John EManufacture of formaldehyde from methyl bromide
    US-7176342-B2February 13, 2007Enitecnologie S.P.A.Method for the preparation of hydrogenated hydrocarbons
    WO-2006104914-A1October 05, 2006Grt, Inc.Hydrocarbon synthesis
    EP-1661620-A1May 31, 2006Rohm and Haas CompanyMehrstufiges katalytisches System zur Umsetzung von Alkanen zu Alkenen und zu den entsprechenden sauerstoffhaltigen Verbindungen
    GB-1133752-ANovember 20, 1968Monsanto CoProduction of vinyl chloride
    GB-995960-AJune 23, 1965Chimica Dell Aniene S P A SocMethod for producing chlorobromomethanes
    GB-294100-AJune 27, 1929Curt EpnerImprovements in and relating to the production of liquid polymerisation products from gases containing hydrocarbons
    GB-775590-AMay 29, 1957Standard Oil CoImprovements in or relating to production of ethyl toluenes
    GB-1015033-ADecember 31, 1965Shell Int ResearchPreparation of olefin oxides
    US-3294846-ADecember 27, 1966Dow Chemical CoProcess for preparing metaaryloxy phenols
    US-3865886-AFebruary 11, 1975Lummus CoProduction of allyl chloride
    US-6096932-AAugust 01, 2000E. I. Du Pont De Nemours And CompanyFluorocarbon manufacturing process
    US-4317800-AMarch 02, 1982Esmil B.V.Process for simultaneously processing of used metal and/or metal _scrap and scrap containing halogenated hydrocarbons

NO-Patent Citations (99)

    Title
    Abstract of BE812868, Aromatic hydrocarbons prodn. from chlorinated hydrocarbons, Publication date: Sep. 27, 1974, esp@cenet database-worldwide.
    Abstract of BE814900, Volatile aramatic cpds. prodn., Publication date: Sep. 2, 1974, esp@cenet database-worldwide.
    Abstract of CN100999680, Esterification reaction tech. of preparing biodiesel by waste oil, Publication date: Jul. 18, 2007, Inventor: Weiming, esp@cenet database-worldwide.
    Abstract of CN101016229, Refining method for bromomeoamyl alcohol, Publication date: Aug. 15, 2007, Inventor: Tian, esp@cenet database-worldwide.
    Abstract of CN1199039, Pentanol and its production process, Publication date: Nov. 18, 1998, Inventor: Kailun, esp@cenet database-worldwide.
    Abstract of CN1210847, Process for producing low carbon alcohol by directly hydrating low carbon olefines, Publication date: Mar. 17, 1999, Inventor: Zhenguo et al., esp@cenet database-worldwide.
    Abstract of CN1321728, Method for preparing aromatic hydrocarbon and hydrogen gas by using low-pressure gas, Publication date: Nov. 14, 2001, Inventor: Jie et al., esp@cenet database-worldwide.
    Abstract of CN1451721, Process for non-catalytic combustion deoxidizing coal mine gas for producing methanol, Publication date: Oct. 29, 2003, Inventor: Pengwan et al., esp@cenet database-worldwide.
    Abstract of CN1623969, Method for preparing 1, 4-benzene dimethanol, Publication date: Jun. 8, 2005, Inventor: Jiarong et al., esp@cenet database-worldwide.
    Abstract of CN1657592, Method for converting oil to multiple energy fuel product, Publication date: Aug. 24, 2005, Inventor: Li, esp@cenet database-worldwide.
    Abstract of CN1687316, Method for producing biologic diesel oil from rosin, Publication date: Oct. 26, 2005, Inventor: Jianchun et al., esp@cenet database-worldwide.
    Abstract of CN1696248, Method for synthesizing biologic diesel oil based on ion liquid, Publication date: Nov. 16, 2005, Inventor: Sun, esp@cenet database-worldwide.
    Abstract of CN1699516, Process for preparing bio-diesel-oil by using microalgae fat, Publication date: Nov. 23, 2005, Inventor: Miao, esp@cenet database-worldwide.
    Abstract of CN1704392, Process for producing alkylbenzene, Publication date: Dec. 7, 2005, Inventor: Gao, esp@cenet database-worldwide.
    Abstract of CN1724612, Biological diesel oil catalyst and method of synthesizing biological diesel oil using sai catalyst, Publication date: Jan. 25, 2006, Inventor: Gu, esp@cenet database-worldwide.
    Abstract of CN1986737, Process of producing biodiesel oil with catering waste oil, Publication date: Jun. 27, 2007, Inventor: Chen, esp@cenet database-worldwide.
    Abstract of DE3209964, Process for the preparation of chlorinated hydrocarbons, Publication date: Nov. 11, 1982, Inventor: Pyke et al., esp@cenet database-worldwide.
    Abstract of DE3210196, Process for the preparation of a monochlorinated olefin, Publication date: Jan. 5, 1983, Inventor: Pyke et al., esp@cenet database-worldwide.
    Abstract of DE3226028, Process for the preparation of monochlorinated olefin, Publication date: Feb. 3, 1983, Inventor: Pyke et al., esp@cenet database-worldwide.
    Abstract of DE3334225, Process for the preparation of 1, 2-dichloroethane, Publication date: Apr. 4, 1985, Inventor: Hebgen et al., esp@cenet database-worldwide.
    Abstract of DE4232056, 2,5-Di:methyl-hexane-2, 5-di:ol continuous prodn. from tert. butanol-by oxidative dimerisation in two phase system with vigorous stirring, using aq. phase with specified density to facilitate phase sepn., Publication date: Mar. 31, 1994, Inventor: Gnann et al., esp@cenet database-worldwide.
    Abstract of DE4434823, Continuous prodn. of hydroxy-benzyl alkyl ether, Publication date: Apr. 4, 1996, Inventor: Stein et al., esp@cenet database-worldwide.
    Abstract of EP0021497 (A1), Synthesis of polyoxyalkylene glycol monoalkyl ethers, Publication date: Jan. 7, 1981, Inventor: Gibson, esp@cenet database-worldwide.
    Abstract of EP0039471, Process for the preparation of 2-chloro-1,1,1,2,3,3,3-heptafluoropropane, Publication date: Nov. 11, 1981, Inventor: Von Halasz, esp@cenet database-worldwide.
    Abstract of EP0101337, Process for the production of methylene chloride, Publication date: Feb. 22, 1984, Inventor: Olah et al., esp@cenet database-worldwide.
    Abstract of EP0235110, Process for the stabilization of silicalite catalysts, Publication date: Sep. 2, 1987, Inventor: Debras et al., esp@cenet database-worldwide.
    Abstract of EP0407989, Method for the production of 1,1,1-trifluoro-2,2-dichloroethane by photochlorination, Publication date: Jan. 16, 1991, Inventor: Cremer et al., esp@cenet database-worldwide.
    Abstract of EP0442258, Process for the preparation of a polyunsaturated olefin, Publication date: Aug. 21, 1991, Inventor: Gaudin et al., esp@cenet database-worldwide.
    Abstract of EP0465294, Process for the preparation of unsaturated bromides, Publication date: Jan. 8, 1992, Inventor: Decaudin et al., esp@cenet database-worldwide.
    Abstract of EP0549387, Synthesis of n-perfluorooctylbromide, Publication date: Jun. 30, 1993, Inventor: Drivon et al., esp@cenet database-worldwide.
    Abstract of EP0850906, Process and apparatus for the etherification of olefinic hydrocarbon feedstocks, Publication date: Jul. 1, 1998, Inventor: Masson, esp@cenet database-worldwide.
    Abstract of EP0858987, Process for the conversion of lighter alkanes to higher hydrocarbons, Publication date: Aug. 19, 1998, Inventor: Amariglio et al., esp@cenet database-worldwide.
    Abstract of EP1404636, Integrated process for synthesizing alcohols and ethers from alkanes, Publication date: Apr. 7, 2004, Inventor: Zhou et al., esp@cenet database-worldwide.
    Abstract of FR2692259, Aromatisation of 2-4C hydrocarbons-using a fixed-mobile-catalytic bed process, Publication date: Dec. 17, 1993, Inventor: Alario et al., esp@cenet database-worldwide.
    Abstract of FR2880019, Manufacturing 1, 2-dichloroethane, comprises cracking core hydrocarbonated source, separating into fractions, sending into chlorination reaction chamber and oxychlorination reaction chamber and separating from chambers, Publication date: Jun. 30, 2006, Inventor: Strebelle et al., esp@cenet database-worldwide.
    Abstract of FR2883870, Formation of 1, 2-dichloroethane useful in manufacture of vinyl chloride involves subjecting mixture of cracking products obtained by cracking of hydrocarbon source, to a succession of aqueous quenching, alkaline washing, and oxidation steps, Publication date: Oct. 6, 2006, Inventor: Balthasart et al., esp@cenet database-worldwide.
    Abstract of FR2883871, Preparing 1, 2-dichloroethane comprises cracking hydrocarbon to form mixture, sending mixture into storage reservoir, supplying mixture into chlorination and/or oxychloration reactor, and separating 1, 2-dichloroethane from reactor, Publication date: Oct. 6, 2006, Inventor: Balthasart et al., esp@cenet database-worldwide.
    Abstract of IT1255246, Process for the preparation of dinitrodiphenylmethanes, Publication date: Oct. 20, 1995, Applicant: Enichem Spa et al., esp@cenet database-worldwide.
    Abstract of IT1255358, Process for the synthesis of 1, 4-butanediol, Publication date: Oct. 31, 1995, Inventor: Marco, esp@cenet database-worldwide.
    Abstract of JP2001031605, Production of 3-hydroxy-1-cycloalkene, Publication date: Feb. 6, 2001, Inventor: Hideo et al, esp@cenet database-worldwide.
    Abstract of JP2004075683, Method for producing optically active halogenohydroxypropyl compound and glycidyl compound, Publication date: Mar. 11, 2004, Inventor: Keisuke et al., esp@cenet database-worldwide.
    Abstract of JP2004189655, Method for fluorinating with microwave, Publication date: Jul. 8, 2004, Inventor: Masaharu et al., esp@cenet database-worldwide.
    Abstract of JP2005075798, Method for Producing adamantyl ester compound, Publication date: Mar. 24, 2005, Inventor: Norihiro et al., esp@cenet database-worldwide.
    Abstract of JP2005082563, Method for producing 1, 3-adamantanediol, Publication date: Mar. 31, 2005, Inventor: Norihiro et al., esp@cenet database-worldwide.
    Abstract of JP2005145977, Process for catalytically oxidizing olefin and cycloolefin for the purpose of forming enol, olefin ketone, and epoxide, Publication date: Jun. 9, 2005, Inventor: Cancheng et al., esp@cenet database-worldwide.
    Abstract of JP2007045756, Hydrogenation method using diaphragm type hydrogenation catalyst, hydrogenation reaction apparatus and diaphragm type hydrogenation catalyst, Publication date: Feb. 22, 2007, Inventor: Shuji et al., esp@cenet database-worldwide.
    Abstract of JP2007061594, Method for decomposing organohalogen compound and mobile decomposition system, Publication date: Mar. 15, 2007, Inventor: Koichi et al., esp@cenet database-worldwide.
    Abstract of JP2007099729, Method for producing alpha-methylstyrene or cumene, Publication date: Ap;r. 19, 2007, Inventor: Toshio, esp@cenet database-worldwide.
    Abstract of JP2142740, Production of fluoroalcohol, Publication date: May 31, 1990, Inventor: Tsutomu et al., esp@cenet database-worldwide.
    Abstract of JP2144150, Chemical process and catalyst used therefore, Publication date: Jun. 1, 1990, Inventor: Deidamusu et al., esp@cenet database-worldwide.
    Abstract of JP4305542, Production of halogenated hydrocarbon compounds, Publication date: Oct. 28, 1992, Inventor: Shinsuke et al., esp@cenet database-worldwide.
    Abstract of JP6172225, Method for fluorinating halogenated hydrocarbon, Publication date: Jun. 21, 1994, Inventor: Takashi et al., esp@cenet database-worldwide.
    Abstract of JP6206834, Production of tetrachloroethanes, Publication date: Jul. 26, 1994, Inventor: Toshiro et al., esp@cenet database-worldwide.
    Abstract of JP8266888, Method for decomposing aromatic halogen compound, Publication date: Oct. 15, 1996, Inventor: Yuuji et al., esp@cenet database-worldwide.
    Abstract of RO119778, Process for preparing perchloroethylene, Publication date: Mar. 30, 2005, Inventor: Horia et al., esp@cenet database-worldwide.
    Abstract of WO0105737, Method for preparing a carboxylic acid, Publication date: Jan. 25, 2001, Inventor: Pascal et al., esp@cenet database-worldwide.
    Abstract of WO0105738, Method for preparing a carboxylic acid, Publication date: Jan. 25, 2001, Inventor: Pascal et al., esp@cenet database-worldwide.
    Abstract of WO2004092099, Method for producing cyclic enols, Publication date: Oct. 28, 2004, Inventor: Marko et al., esp@cenet database-worldwide.
    Abstract of WO2006063852, Electroluminescent polymers and use thereof, Publication date: Jun. 22, 2006, Inventor: Arne et al., esp@cenet database-worldwide.
    Abstract of WO2006076942, Method for the production of synthetic fuels from oxygenates, Publication date: Jul. 27, 2006, Inventor: Rothaemel et al., esp@cenet database-worldwide.
    Abstract of WO2006136135, Method for decarboxylating C-C cross-linking of carboxylic acids with carbon electrophiles, Publication date: Dec. 28, 2006, Inventor: Goossen Lukas et al., esp@cenet database-worldwide.
    Abstract of WO2007028761, Method for chlorinating alcohols, Publication date: Mar. 15, 2007, Inventor: Rohde et al., esp@cenet database-worldwide.
    Abstract of WO2007128842, Catalytic transalkylation of dialkyl benzenes, Publication date: Nov. 15, 2007, Inventor: Goncalvesalmeida et al., esp@cenet database-worldwide.
    Abstract of WO2007137566, Method for catalytic conversion of organic oxygenated compounds from biomaterials, Publication date: Dec. 6, 2007, Inventor: Reschetilowski, esp@cenet database-worldwide.
    Abstract of WO9721656, Method for making fluoroalkanols, Publication date: Jun. 19, 1997, Inventor: Gillet, esp@cenet database-worldwide.
    Abstract of WO9950213, Method for producing dialkyl ethers, Publication date: Oct. 7, 1999, Inventor: Falkowski Juergen et al., esp@cenet database-worldwide.
    Adachi et al., Synthesis of Sialyl Lewis X Ganglioside Analogs Containing a Variable Length Spacer Between the Sugar and Lipophilic Moieties, J. Carbohydrate Chemistry, vol. 17, No. 4-5, 1998, pp. 595-607; XP009081720.
    Bakker et al., An Exploratory Study of the Addition Reactions of Ethyleneglycol, 2-Chloroethanol and 1,3-Dichloro-2-Propanol to 1-Dodecene, J. Am. Oil Chem. Soc., vol. 44, No. 9, 1967, pp. 517-521; XP009081570.
    Benizri et al., Study of the Liquid-Vapor Equilibrium in the Bromine-Hydrobromic Acid-Water System, Hydrogen Energy Vector, 1980, pp. 101-116.
    Bouzide et al., Highly Selective Silver (I) Oxide Mediated Monoprotection of Symmetrical Diols, Tetrahedron Letters, Elsevier, vol. 38, No. 34, 1997, pp. 5945-5948; XP004094157.
    Bradshaw et al., Production of Hydrobromic Acid from Bromine and Methane for Hydrogen Production, Proceedings of the 2001 DOE Hydrogen Program Review, NREL/CP-570-30535, 2001.
    Combined International Search Report and Written Opinion Dated Apr. 17, 2007 for PCT/US2006/13394, in the name of GRT, Inc.
    Gibson et al., Phase-Transfer Synthesis of Monoalkyl Ethers of Oligoethylene Glycols, J. Org. Chem., vol. 45, No. 6, 1980, pp. 1095-1098; XP002427776.
    Kirk-Othmer Encyclopedia of Chemical Technology, 4th Edition, vol. 1, A Wiley-Interscience Publication, John Wiley & Sons, 1991, pp. 946-997.
    Loiseau et al., Multigram Synthesis of Well-Defined Extended Bifunctional Polyethylene Glycol (PEG) Chains, J. Org. Chem., vol. 69, No. 3, 2004, pp. 639-647; XP002345040.
    Mihai et al., Application of Bronsted-Type LFER in the Study of the Phospholipase C Mechanism, J. Am. Chem. Soc., vol. 125, No. 11, 2003, pp. 3236-3242; XP002427777.
    Motupally et al., Recycling Chlorine from Hydrogen Chloride, The Electrochemical Society Interface, Fall 2008, pp. 32-36.
    Nishikawa et al., Ultrasonic Relaxations in Aqueous Solutions of Alcohols and the Balance between Hydrophobicity and Hydrophilicity of the Solutes, J. Phys. Chem., vol. 97, No. 14, 1993, pp. 3539-3544; XP002427775.
    Prelog et al., Chirale 2,2'-Polyoxaalkano-9,9'-Spirobifluorene, Helvetica Chimica ACTA, vol. 62, No. 7, 1979, pp. 2285-2302; XP002030901.
    Shimizu et al., Gas-Phase Electrolysis of Hydrobromic Acid Using PTFE-Bonded Carbon Electrode, Int. J. Hydrogen Energy, vol. 13, No. 6, pp. 345-349, 1988.
    U.S. Appl. No. 60/487,364, filed Jul. 15, 2003, Lorkovic et al.
    U.S. Appl. No. 60/559,844, filed Apr. 6, 2004, Sherman et al.
    U.S. Office Action from U.S. Appl. No. 10/365,346 dated Jun. 12, 2006.
    U.S. Office Action from U.S. Appl. No. 10/826,885 dated Apr. 19, 2006.
    U.S. Office Action from U.S. Appl. No. 10/826,885 dated Jan. 24, 2007.
    U.S. Office Action from U.S. Appl. No. 10/826,885 dated Jul. 27, 2006.
    U.S. Office Action from U.S. Appl. No. 10/826,885 dated Nov. 2, 2006.
    U.S. Office Action from U.S. Appl. No. 10/826,885 dated Oct. 31, 2005.
    U.S. Office Action from U.S. Appl. No. 10/893,418 dated Jan. 2, 2008.
    U.S. Office Action from U.S. Appl. No. 10/893,418 dated Jun. 14, 2007.
    U.S. Office Action from U.S. Appl. No. 11/091,130 dated Oct. 3, 2007.
    U.S. Office Action from U.S. Appl. No. 11/101,886 dated Jan. 24, 2007.
    U.S. Office Action from U.S. Appl. No. 11/254,438 dated Jan. 24, 2007.
    U.S. Office Action from U.S. Appl. No. 11/254,438 dated Nov. 1, 2007.
    U.S. Office Action from U.S. Appl. No. 12/112,926 dated Jan. 16, 2009.
    U.S. Office Action from U.S. Appl. No. 12/112,926 dated Sep. 14, 2009.
    Velzen et al., HBr Electrolysis in the Ispra Mark 13A Flue Gas Desulphurization Process: Electrolysis in a DEM Cell, J. of Applied Electrochemistry, vol. 20, pp. 60-68, 1990.
    Wauters et al., Electrolytic Membrane Recovery of Bromine from Waste Hydrogen Bromide Streams, AlChE Journal, Oct. 1998, vol. 44, No. 10, pp. 2144-2148.
    Whitesides et al., Nuclear Magnetic Resonance Spectroscopy. The Effect of Structure on Magnetic Nonequivalence Due to Molecular Asymmetry, J. Am. Chem. Soc., vol. 86, No. 13, 1964, pp. 2628-2634; XP002427774.

Cited By (9)

    Publication numberPublication dateAssigneeTitle
    US-8282810-B2October 09, 2012Marathon Gtf Technology, Ltd.Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery
    US-8436220-B2May 07, 2013Marathon Gtf Technology, Ltd.Processes and systems for demethanization of brominated hydrocarbons
    US-8642822-B2February 04, 2014Marathon Gtf Technology, Ltd.Processes for converting gaseous alkanes to liquid hydrocarbons using microchannel reactor
    US-8802908-B2August 12, 2014Marathon Gtf Technology, Ltd.Processes and systems for separate, parallel methane and higher alkanes' bromination
    US-8815050-B2August 26, 2014Marathon Gtf Technology, Ltd.Processes and systems for drying liquid bromine
    US-8829256-B2September 09, 2014Gtc Technology Us, LlcProcesses and systems for fractionation of brominated hydrocarbons in the conversion of natural gas to liquid hydrocarbons
    US-9133078-B2September 15, 2015Gtc Technology Us, LlcProcesses and systems for the staged synthesis of alkyl bromides
    US-9193641-B2November 24, 2015Gtc Technology Us, LlcProcesses and systems for conversion of alkyl bromides to higher molecular weight hydrocarbons in circulating catalyst reactor-regenerator systems
    US-9206093-B2December 08, 2015Gtc Technology Us, LlcProcess for converting gaseous alkanes to liquid hydrocarbons