CA2088939A1 - Low temperature conversion of alkanes - Google Patents
Low temperature conversion of alkanesInfo
- Publication number
- CA2088939A1 CA2088939A1 CA002088939A CA2088939A CA2088939A1 CA 2088939 A1 CA2088939 A1 CA 2088939A1 CA 002088939 A CA002088939 A CA 002088939A CA 2088939 A CA2088939 A CA 2088939A CA 2088939 A1 CA2088939 A1 CA 2088939A1
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- Canada
- Prior art keywords
- transition metal
- metal halide
- halogen source
- added halogen
- group
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/09—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis
- C07C29/12—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of esters of mineral acids
- C07C29/124—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrolysis of esters of mineral acids of halides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/093—Preparation of halogenated hydrocarbons by replacement by halogens
- C07C17/10—Preparation of halogenated hydrocarbons by replacement by halogens of hydrogen atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
- C07B2200/00—Indexing scheme relating to specific properties of organic compounds
- C07B2200/05—Isotopically modified compounds, e.g. labelled
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
The invention relates to a process for selectively producing alkyl halides from alkanes, such as methane and ethane at low tempera-tures and low pressures. Optional hydrolysis to the corresponding alcohols may follow. The process involves adding an alkane and an added halogen source to an aqueous solution in a homogeneous system in the presence of a transition metal halide containing complex, for a time, under conditions and in effective amounts that will permit the formation of alkyl monohalides.
The invention relates to a process for selectively producing alkyl halides from alkanes, such as methane and ethane at low tempera-tures and low pressures. Optional hydrolysis to the corresponding alcohols may follow. The process involves adding an alkane and an added halogen source to an aqueous solution in a homogeneous system in the presence of a transition metal halide containing complex, for a time, under conditions and in effective amounts that will permit the formation of alkyl monohalides.
Description
BACKGROUND OF THE INVENTION
Field of the Invention The invention relates to a process for the selective mono-halogenation of alkanes to alkyl monohalides in a homogeneous (sup-ported or unsupported) liquid phase system under mild conditions of temperature and pressure. The halogenation may be followed by hydrol-ysis to produce alcohols.
Description of Related Art Selective halogenation of alkanes to alkyl halides, parti-cularly chlorination to alkyl chlorides under relatively mild tempera-ture and pressure offers the possibility for development of simple, low cost means for producing alkyl halides. Alkyl halides are known to those having ordinary skill in the art to have utility as a feed-stock for more valuable commercial reactions. For example, methyl chloride and other alkyl halides have utility as an intermediate for product;on of alcohols, such as methanol, which itself is useful as an alternative, less environmentally damaging, fuel source. Additional-ly, methanol can be used as a feedstock for chemical reactions; for example, it can be used in reactions to yield gasoline or other hydro-carbons. More importantly, alcohol can be used as a transportation fuel source or as an additive to transportation fuels, particularly gasoline, to reduce hydrocarbon emissions and produce a more environ-mentally safe fuel.
The literature describes a number of processes for monohalo-genating alkanes. However, unlike the processes described in the literature, applicants' monohalogenate alkanes in a process that uses a homogeneous liquid phase/transition metal complex system that uses no metal-bound halogen sources operates in the presence of the transi-tion metal halide complexes, shows no evidence of metallic platinum formation during the reaction until the added halogen source is depleted, and is highly selective for monohalogenated products and their hydrolysis products.
SUMMARY OF THE INVENTION
The present invention relates to a process for selectively producing alkyl monohalides, particularly alkyl chlorides, at rela-tively mild conditions of temperature and pressure in a homogeneous system from alkanes, particularly methane and ethane and mixtures thereof, by combining the alkane and an added halogen source in an aqueous solution, preferably water, in the presence of a soluble transition metal halide complex. The alkyl monohalides may be con-verted via hydrolysis to alcohols.
DESCRIPTION OF THE INVENTION
Alkyl halides, particularly alkyl chlorides such as methyl chloride, can be produced selectively by a process which comprises adding an alkane or mixtures of alkanes, and an added halogen source to an aqueous solution in the presence of a transition metal halide complex. The alkanes suitably may be methane, ethane or higher alkanes. The halogens are preferably chlorine, fluorine or bromine.
The corresponding alcohol(s) may be produced during the reaction from the hydrolysis of the resulting alkyl halides or in a separate hydrol-ysis step.
The transition metal halide complex can be added to the system or may be produced by one ordinarily skilled in the art, in situ, from a compound consisting of a transition metal and a ligand capable of reacting to form the complex provided that the resulting complex is homogeneous with the system. Particularly useful transi-tion metal halide complexes are those in which the transition metal is platinum, palladium, and nickel or mixtures thereof or, more prefera-bly, platinum; and the halide is fluoride, chloride, bromide, or iodide or mixtures thereof, preferably chloride. The preferable combination of transition metal and halide is that of platinum and chloride; for example, as (PtC14)-2/(PtC16)-2 or as (PtC14)-2 alone.
Field of the Invention The invention relates to a process for the selective mono-halogenation of alkanes to alkyl monohalides in a homogeneous (sup-ported or unsupported) liquid phase system under mild conditions of temperature and pressure. The halogenation may be followed by hydrol-ysis to produce alcohols.
Description of Related Art Selective halogenation of alkanes to alkyl halides, parti-cularly chlorination to alkyl chlorides under relatively mild tempera-ture and pressure offers the possibility for development of simple, low cost means for producing alkyl halides. Alkyl halides are known to those having ordinary skill in the art to have utility as a feed-stock for more valuable commercial reactions. For example, methyl chloride and other alkyl halides have utility as an intermediate for product;on of alcohols, such as methanol, which itself is useful as an alternative, less environmentally damaging, fuel source. Additional-ly, methanol can be used as a feedstock for chemical reactions; for example, it can be used in reactions to yield gasoline or other hydro-carbons. More importantly, alcohol can be used as a transportation fuel source or as an additive to transportation fuels, particularly gasoline, to reduce hydrocarbon emissions and produce a more environ-mentally safe fuel.
The literature describes a number of processes for monohalo-genating alkanes. However, unlike the processes described in the literature, applicants' monohalogenate alkanes in a process that uses a homogeneous liquid phase/transition metal complex system that uses no metal-bound halogen sources operates in the presence of the transi-tion metal halide complexes, shows no evidence of metallic platinum formation during the reaction until the added halogen source is depleted, and is highly selective for monohalogenated products and their hydrolysis products.
SUMMARY OF THE INVENTION
The present invention relates to a process for selectively producing alkyl monohalides, particularly alkyl chlorides, at rela-tively mild conditions of temperature and pressure in a homogeneous system from alkanes, particularly methane and ethane and mixtures thereof, by combining the alkane and an added halogen source in an aqueous solution, preferably water, in the presence of a soluble transition metal halide complex. The alkyl monohalides may be con-verted via hydrolysis to alcohols.
DESCRIPTION OF THE INVENTION
Alkyl halides, particularly alkyl chlorides such as methyl chloride, can be produced selectively by a process which comprises adding an alkane or mixtures of alkanes, and an added halogen source to an aqueous solution in the presence of a transition metal halide complex. The alkanes suitably may be methane, ethane or higher alkanes. The halogens are preferably chlorine, fluorine or bromine.
The corresponding alcohol(s) may be produced during the reaction from the hydrolysis of the resulting alkyl halides or in a separate hydrol-ysis step.
The transition metal halide complex can be added to the system or may be produced by one ordinarily skilled in the art, in situ, from a compound consisting of a transition metal and a ligand capable of reacting to form the complex provided that the resulting complex is homogeneous with the system. Particularly useful transi-tion metal halide complexes are those in which the transition metal is platinum, palladium, and nickel or mixtures thereof or, more prefera-bly, platinum; and the halide is fluoride, chloride, bromide, or iodide or mixtures thereof, preferably chloride. The preferable combination of transition metal and halide is that of platinum and chloride; for example, as (PtC14)-2/(PtC16)-2 or as (PtC14)-2 alone.
The cation portion of the complex may be a Group IA or IIA element, preferably H+, K+, or Na+. The particular complex may be prepared by methods known to ones ordinarily skilled in the art or obtained from commercial sources. The complex should be homogeneous with the aqueous solution in the system.
The complex useful in the process of the present invention and the aqueous solution also may be supported in a solid hydrophilic support. In general, the support will be a porous solid material.
For example, materials having a pore volume relative to solid weight of from about 0.1 to 1.5 cubic centimeters per gram, with a preferred range of from about 0.4 to 1.0 are especially useful supports. The macropore volume of the porous support should be at least 10% of the total pore volume. By macropore volume is meant pores having diame-ters greater than 100 Angstroms.
Specific examples of such materials useful as a support for the homogeneous liquid phase system in the practice of the process of the present invention are silica, clay, alumina, silica/alumina, acid treated clay and titania. Indeed, it is particularly preferred in the practice of the present invention to use acidic porous support materi-als such as silica/alumina, clay and, even more particularly, acid treated clay.
In a supported homogeneous liquid phase system, the transi-tion metal complex used in the process of the present invention is dissolved in a supported aqueous ac;d phase; i.e., an aqueous acid phase that does not circulate or flow as a liquid, but is immobile and supported by the porous solid support. Typical supported aqueous acid liquid phase materials that may be used in the practice of the present invention include aqueous solutions of HCl, HF, CH3COOH, CF3COOH, H3P04, H2S04, CH3S03H, CF3S03H, BF3 and mixtures thereof, preferably HCl, HF and mixtures thereof.
The volume of the supported aqueous phase will generally be a predetermined maximum amount that can be supported without causing the particles of the support to stick together, which amount may readily be determined by one ordinarily skilled in the art. The amount of aqueous phase should be less than that of the pore volume of the specific support employed. Indeed, it is preferred that the amount of aqueous phase will be about 10% less than the pore volume of the support. Thus, for example, about 1.3 cc of aqueous phase will be used with a support having a pore volume of 1.5 cc/gm.
Finally, in the homogeneous liquid phase system used in the process of the present invention, there is included a transition metal halide complex which is dissolved in the aqueous phase. The transition metals that may be employed herein include cobalt, rhodium, iridium, palladium, platinum, ruthenium, rhenium and mixtures thereof, but prefe~rred is platinum.
In preparing a supported homogeneous liquid phase system, the transition metal complex is first dissolved in the aqueous phase, then the solution is impregnated into the porous support material by any appropriate means known to one skilled in the art, for example, by the incipient wetness technique.
The added halogen source used in the practice of the present invention should be additional to any halide contained in the transi-tion metal halide complex having the transition metal halide. The source may be any Group VIIA element or compound, any Group VIIA-containing compound, and any other Group VIIA-containing species that exist(s) as an equilibrium product of the reaction of the Group VIIA
element, compound or Group VIIA-containing species in water in the presence of the complex and mixtures thereof. The added halogen source may be in elemental, molecular, ionic, free radical, other form or species, or mixtures thereof that are consistent with the chemical composition of the source. It may be introduced into the system in gaseous, liquid or other form that is or becomes soluble or dissolves in whole or in part in water, or it may be present in the system as an equilibrium product of the reactions involved in the particular system. The added halogen source is preferably a halogen, halide and hypohalide, or mixtures thereof, more preferably chlorine, a chloride and a hypochloride; even more preferably, Cl2 and HOCl, most prefera-bly Cl2-In the process of the present invention, monohalogenation ofthe alkanes is carried out under relatively mild conditions. ~uitable monohalogenations may be carried out at a temperature range from about 20C to about 315C, preferably from about 20C to about 200C, more preferably from about 25 to about 150C; and hydrolysis to the corresponding alcohols may be accomplished at temperatures from about 20C to about 315C, preferably from about 100C to about 250C, more preferably from about 100C to about 150C. The total pressure selected will vary based on the form in which the alkane and added halogen source are introduced into the system (e.g. liquid, gas), but generally for gaseous sources should be from about 1 atm to about 300 atm. Where, for example, the reaction is carried out using gaseous Cl2 at about 20C to about 25C, the preferable pressure range is from about 1 to about 6 atm. Halogenation of alkanes to alkyl monohalides, according to the process of the present invention, may be carried out selectivelyS using the ratio of added halogen source to alkane of greater than or equal to about 1:1, preferably from about 1:1 to about 1:10, more preferably from about 1:1 to about 1:100.
If a significant amount of alcohol production is desired the reaction should be permitted to progress for a sufficient time to produce alcohol, but should not be allowed to proceed to the point that the added halogen source is depleted. The reactants should be used in effective amounts for the production of the alkyl halide.
Where the added halogen source is Cl2 or ~IOCl and the complex contain-ing the transition metal halide is Na2PtCl4/Na2PtCl6 or Na2PtCl4 alone, the process produces alkyl chlorides, particularly methyl chloride and ethyl chloride in high selectivity at pressures as low as about 5 atm, and at temperatures as low as about 100C almost immedi-ately. The reaction may be expected to proceed slowly, even at pressures as low as 1 atm.
In all cases, the pressure and temperature of the reaction and concentrations of reactants should be such that the flash point of 208~39 the gaseous reactants is not exceeded. Due regard should be given to the corrosive nature of the particular Group VIIA reactants used.
Particularly in the case of fluorinati~n of alkanes, reactions should be performed in high dilution, preferably in the presence of an inert gas, to minimize handling problems. For processes known to those ordinarily skilled in the art for carrying out reactions using halo-gens, see e.g., F. Cotton and G. Wilkinson, Advanced Inorqanic ChemistrY. A Comprehensive Text, 4th ed., Part 2, Ch. 17, p.p.
542-576 "The Group VII Elements, Fluorine, Chlorine, Bromine, Iodine and Astatine".
The process of the present invention may be run in batch or may be operated continuously. The latter may be accomplished by removing on an ongoing basis the alkyl monohalides (or the alcohol, if the reaction is allowed to proceed under conditions which result in the hydrolysis to alcohol), recycling the complex containing the transition metal halide and regenerating the halogen source by oxida-tion of the halogen cnntaining by-products of the reaction.
Reaction times for the process of the present invention will depend on the particular combination of reagents used, the sample size, and the type of process (batch or continuous), but should be sufficient to permit the synthesis of alkyl monohalides, and, if alcohol production is desired, the hydrolysis of the alkyl monohalides to alcohol. In order to maintain the selectivity of the reaction toward the production of alkyl monohalides, care should be taken such that the added halogen source is not depleted.
Subject to the foregoing limitations, reaction times gener-ally needed to produce alcohol in quantities that are equal to or greater than those of, for example, alkyl chloride, are from about 15 minutes to about 16 hours at from about 100C to about 150C and from about 20 atm to about 80 atm, the more preferable time being from about 30 minutes to about 8 hours.
The selection of the particular reaction times, conditions and combination and concentrations of reagents will be readily 208~39 apparent to one ordinarily skilled in the art given parameters estab-lished by the the teachings herein. General background concerning, for example, the conditions necessary for the chlorination of methane can be found in J. S. Sconce, Chlorine. Its Manufacture. Properties and Uses, R. Landau and S. Fox, Chapter 12, "Chlorinated Methanes", pp. 334 to 375. Other halogenation reactions may be carried out simi-larly by one ordinarily skilled in the art.
In order to maintain the high selectivity for alcohol production that is a characteristic of the present invention, it is important that the added halogen source not be depleted during the reaction. This may be accomplished by oxidizing the halide and oxyhalide by-products of the reaction to regenerate gaseous halogen and recycling them back into the system, or by adding additional halogen source to the reaction. Otherwise, at the point at which the added halogen source is depleted, the reaction may continue for a time and is identified by the formation of the metallic (zero valence) form of the transition metal portion of the complex (e.g., metallic plati-num for the Na2PtCl4/Na2PtCl6 complex). It should be emphasized that in order to carry out chlorination, the platinum complex is required in a concentration of from about 0.001 mole/liter to about mole/liter, preferably from about 0.01 mole/liter to about mole/liter, more preferably from about 0.1 mole/liter to about 0.5 mole/liter. However, in order to carry out the hydrolysis step, the platinum complex in a concentration of from about 0.01 mole/liter to about 1 mole/liter is required.
The following examples are illustrative and not intended to limit the scope of the invention.
Example 1 Commercially available chlorine, methane, Na2PtCl4 and Na2PtCl6 were used without further purification. The reaction was performed at 125C for 2 hours in an 8 ml sapphire high pressure nuclear magnetic resonance ("NMR") tube with 3 g of a D20 solution containing 1.2 mmol Na2PtCl6 and 0.16 mmol Na2PtCl4 at 72 psi Cl2 and 208~939 392 psi 13CH4. For an illustration of a sapphire NMR tube assembly, see I. T. Horvath and E. Ponce, "New Valve Design for High Pressure Sapphire Tubes for NMR Measurements", Review of Scientific Instru-ments, Vol. 62, No. 4, pp. 1104-1105 (1991). After 2 hours, the high pressure NMR spectrum showed the selective formation of methanol (approximately 40%, in the form of CH30D) as evidenced by the peak at about 49.5 ppm. NMR indicates the formation of trace amounts of C02, with a peak at about 125 ppm; CH2(0D)2 (approximately 2%), with a peak at about 85 ppm; CH2Cl2 (approximately 2%) with a peak at about 56 ppm; CH3Cl, (approximately 5%) with a peak at about 26 ppm; and un-reacted methane (approximately 50%), with a peak at about -4 ppm.
Formation of metallic platinum was not observed upon visual inspection of the transparent NMR tube under pressure. HCl that is formed as a by-product during the formation of methanol may be treated with 2 to recover the chlorine. Methanol may be separated by distillation by processes known to one having ordinary skill in the art.
Example 2 Commercially available methyl chloride was used without further purification. Hydrolysis was carried out in a sapphire high pressure NMR tube with 39 of a D20 solution containing 1.2 mmol Na2PtCl6 and 0.16 mmole Na2PtCl4 at 50 psi CH3Cl and heated to 125C
for 1 hour. High pressure ~3C NMR spectrum showed the selective formation of methanol ~in the form of CH30D). The spectrum had the following characteristics: a peak at about 49.5 ppm, representing CH30D (approximately 49%); a peak at about 26 ppm for CH3Cl (approxi-mately 50%).
The complex useful in the process of the present invention and the aqueous solution also may be supported in a solid hydrophilic support. In general, the support will be a porous solid material.
For example, materials having a pore volume relative to solid weight of from about 0.1 to 1.5 cubic centimeters per gram, with a preferred range of from about 0.4 to 1.0 are especially useful supports. The macropore volume of the porous support should be at least 10% of the total pore volume. By macropore volume is meant pores having diame-ters greater than 100 Angstroms.
Specific examples of such materials useful as a support for the homogeneous liquid phase system in the practice of the process of the present invention are silica, clay, alumina, silica/alumina, acid treated clay and titania. Indeed, it is particularly preferred in the practice of the present invention to use acidic porous support materi-als such as silica/alumina, clay and, even more particularly, acid treated clay.
In a supported homogeneous liquid phase system, the transi-tion metal complex used in the process of the present invention is dissolved in a supported aqueous ac;d phase; i.e., an aqueous acid phase that does not circulate or flow as a liquid, but is immobile and supported by the porous solid support. Typical supported aqueous acid liquid phase materials that may be used in the practice of the present invention include aqueous solutions of HCl, HF, CH3COOH, CF3COOH, H3P04, H2S04, CH3S03H, CF3S03H, BF3 and mixtures thereof, preferably HCl, HF and mixtures thereof.
The volume of the supported aqueous phase will generally be a predetermined maximum amount that can be supported without causing the particles of the support to stick together, which amount may readily be determined by one ordinarily skilled in the art. The amount of aqueous phase should be less than that of the pore volume of the specific support employed. Indeed, it is preferred that the amount of aqueous phase will be about 10% less than the pore volume of the support. Thus, for example, about 1.3 cc of aqueous phase will be used with a support having a pore volume of 1.5 cc/gm.
Finally, in the homogeneous liquid phase system used in the process of the present invention, there is included a transition metal halide complex which is dissolved in the aqueous phase. The transition metals that may be employed herein include cobalt, rhodium, iridium, palladium, platinum, ruthenium, rhenium and mixtures thereof, but prefe~rred is platinum.
In preparing a supported homogeneous liquid phase system, the transition metal complex is first dissolved in the aqueous phase, then the solution is impregnated into the porous support material by any appropriate means known to one skilled in the art, for example, by the incipient wetness technique.
The added halogen source used in the practice of the present invention should be additional to any halide contained in the transi-tion metal halide complex having the transition metal halide. The source may be any Group VIIA element or compound, any Group VIIA-containing compound, and any other Group VIIA-containing species that exist(s) as an equilibrium product of the reaction of the Group VIIA
element, compound or Group VIIA-containing species in water in the presence of the complex and mixtures thereof. The added halogen source may be in elemental, molecular, ionic, free radical, other form or species, or mixtures thereof that are consistent with the chemical composition of the source. It may be introduced into the system in gaseous, liquid or other form that is or becomes soluble or dissolves in whole or in part in water, or it may be present in the system as an equilibrium product of the reactions involved in the particular system. The added halogen source is preferably a halogen, halide and hypohalide, or mixtures thereof, more preferably chlorine, a chloride and a hypochloride; even more preferably, Cl2 and HOCl, most prefera-bly Cl2-In the process of the present invention, monohalogenation ofthe alkanes is carried out under relatively mild conditions. ~uitable monohalogenations may be carried out at a temperature range from about 20C to about 315C, preferably from about 20C to about 200C, more preferably from about 25 to about 150C; and hydrolysis to the corresponding alcohols may be accomplished at temperatures from about 20C to about 315C, preferably from about 100C to about 250C, more preferably from about 100C to about 150C. The total pressure selected will vary based on the form in which the alkane and added halogen source are introduced into the system (e.g. liquid, gas), but generally for gaseous sources should be from about 1 atm to about 300 atm. Where, for example, the reaction is carried out using gaseous Cl2 at about 20C to about 25C, the preferable pressure range is from about 1 to about 6 atm. Halogenation of alkanes to alkyl monohalides, according to the process of the present invention, may be carried out selectivelyS using the ratio of added halogen source to alkane of greater than or equal to about 1:1, preferably from about 1:1 to about 1:10, more preferably from about 1:1 to about 1:100.
If a significant amount of alcohol production is desired the reaction should be permitted to progress for a sufficient time to produce alcohol, but should not be allowed to proceed to the point that the added halogen source is depleted. The reactants should be used in effective amounts for the production of the alkyl halide.
Where the added halogen source is Cl2 or ~IOCl and the complex contain-ing the transition metal halide is Na2PtCl4/Na2PtCl6 or Na2PtCl4 alone, the process produces alkyl chlorides, particularly methyl chloride and ethyl chloride in high selectivity at pressures as low as about 5 atm, and at temperatures as low as about 100C almost immedi-ately. The reaction may be expected to proceed slowly, even at pressures as low as 1 atm.
In all cases, the pressure and temperature of the reaction and concentrations of reactants should be such that the flash point of 208~39 the gaseous reactants is not exceeded. Due regard should be given to the corrosive nature of the particular Group VIIA reactants used.
Particularly in the case of fluorinati~n of alkanes, reactions should be performed in high dilution, preferably in the presence of an inert gas, to minimize handling problems. For processes known to those ordinarily skilled in the art for carrying out reactions using halo-gens, see e.g., F. Cotton and G. Wilkinson, Advanced Inorqanic ChemistrY. A Comprehensive Text, 4th ed., Part 2, Ch. 17, p.p.
542-576 "The Group VII Elements, Fluorine, Chlorine, Bromine, Iodine and Astatine".
The process of the present invention may be run in batch or may be operated continuously. The latter may be accomplished by removing on an ongoing basis the alkyl monohalides (or the alcohol, if the reaction is allowed to proceed under conditions which result in the hydrolysis to alcohol), recycling the complex containing the transition metal halide and regenerating the halogen source by oxida-tion of the halogen cnntaining by-products of the reaction.
Reaction times for the process of the present invention will depend on the particular combination of reagents used, the sample size, and the type of process (batch or continuous), but should be sufficient to permit the synthesis of alkyl monohalides, and, if alcohol production is desired, the hydrolysis of the alkyl monohalides to alcohol. In order to maintain the selectivity of the reaction toward the production of alkyl monohalides, care should be taken such that the added halogen source is not depleted.
Subject to the foregoing limitations, reaction times gener-ally needed to produce alcohol in quantities that are equal to or greater than those of, for example, alkyl chloride, are from about 15 minutes to about 16 hours at from about 100C to about 150C and from about 20 atm to about 80 atm, the more preferable time being from about 30 minutes to about 8 hours.
The selection of the particular reaction times, conditions and combination and concentrations of reagents will be readily 208~39 apparent to one ordinarily skilled in the art given parameters estab-lished by the the teachings herein. General background concerning, for example, the conditions necessary for the chlorination of methane can be found in J. S. Sconce, Chlorine. Its Manufacture. Properties and Uses, R. Landau and S. Fox, Chapter 12, "Chlorinated Methanes", pp. 334 to 375. Other halogenation reactions may be carried out simi-larly by one ordinarily skilled in the art.
In order to maintain the high selectivity for alcohol production that is a characteristic of the present invention, it is important that the added halogen source not be depleted during the reaction. This may be accomplished by oxidizing the halide and oxyhalide by-products of the reaction to regenerate gaseous halogen and recycling them back into the system, or by adding additional halogen source to the reaction. Otherwise, at the point at which the added halogen source is depleted, the reaction may continue for a time and is identified by the formation of the metallic (zero valence) form of the transition metal portion of the complex (e.g., metallic plati-num for the Na2PtCl4/Na2PtCl6 complex). It should be emphasized that in order to carry out chlorination, the platinum complex is required in a concentration of from about 0.001 mole/liter to about mole/liter, preferably from about 0.01 mole/liter to about mole/liter, more preferably from about 0.1 mole/liter to about 0.5 mole/liter. However, in order to carry out the hydrolysis step, the platinum complex in a concentration of from about 0.01 mole/liter to about 1 mole/liter is required.
The following examples are illustrative and not intended to limit the scope of the invention.
Example 1 Commercially available chlorine, methane, Na2PtCl4 and Na2PtCl6 were used without further purification. The reaction was performed at 125C for 2 hours in an 8 ml sapphire high pressure nuclear magnetic resonance ("NMR") tube with 3 g of a D20 solution containing 1.2 mmol Na2PtCl6 and 0.16 mmol Na2PtCl4 at 72 psi Cl2 and 208~939 392 psi 13CH4. For an illustration of a sapphire NMR tube assembly, see I. T. Horvath and E. Ponce, "New Valve Design for High Pressure Sapphire Tubes for NMR Measurements", Review of Scientific Instru-ments, Vol. 62, No. 4, pp. 1104-1105 (1991). After 2 hours, the high pressure NMR spectrum showed the selective formation of methanol (approximately 40%, in the form of CH30D) as evidenced by the peak at about 49.5 ppm. NMR indicates the formation of trace amounts of C02, with a peak at about 125 ppm; CH2(0D)2 (approximately 2%), with a peak at about 85 ppm; CH2Cl2 (approximately 2%) with a peak at about 56 ppm; CH3Cl, (approximately 5%) with a peak at about 26 ppm; and un-reacted methane (approximately 50%), with a peak at about -4 ppm.
Formation of metallic platinum was not observed upon visual inspection of the transparent NMR tube under pressure. HCl that is formed as a by-product during the formation of methanol may be treated with 2 to recover the chlorine. Methanol may be separated by distillation by processes known to one having ordinary skill in the art.
Example 2 Commercially available methyl chloride was used without further purification. Hydrolysis was carried out in a sapphire high pressure NMR tube with 39 of a D20 solution containing 1.2 mmol Na2PtCl6 and 0.16 mmole Na2PtCl4 at 50 psi CH3Cl and heated to 125C
for 1 hour. High pressure ~3C NMR spectrum showed the selective formation of methanol ~in the form of CH30D). The spectrum had the following characteristics: a peak at about 49.5 ppm, representing CH30D (approximately 49%); a peak at about 26 ppm for CH3Cl (approxi-mately 50%).
Claims (10)
1. A process of selectively making alkyl monohalides, which process comprises: forming liquid phase containing water, an alkane, a transition metal halide complex and an added halogen source in addi-tion to that contained in the transition metal halide complex; react-ing the alkane, added halogen source and transition metal halide complex mixture at a temperature and for a sufficient time and in amounts that are effective to produce the corresponding alkyl mono-halide and wherein the added halogen source is not completely deplet-ed.
2. The process of claim 1 wherein the ratio of added halogen source to alkane is greater than or equal to about 1:1.
3. The process of claim 1 wherein the added halogen source is selected from the group consisting of a Group VIIA element, a Group VIIA compound and Group VIIA-containing species that exists as an equilibrium product in water of the reaction of the Group VIIA ele-ment, compound or other Group VIIA-containing species and the transi-tion metal halide complex.
4. The process of claim 1 wherein the alkyl monohalide is alkyl chloride.
5. The process of claim 1 wherein the added halogen source is selected from the group consisting of a halogen, a halide, a hypohalide and mixtures thereof.
6. The process of claim 1 wherein the added halogen source is a gas.
7. The process of claim 1 wherein the transition metal halide contains platinum, palladium, nickel and mixtures thereof.
8. The process of claim 1 wherein the transition metal halide is selected from the group consisting of (PtCl4)-2 and (PtCl6)-2 in combination, and (PtCl4)-2 alone.
9. The process of claim 1 wherein the transition metal halide is (PtCl4)-2/(PtCl6)-2.
10. The process of claim 1 wherein the liquid phase is supported on a solid, porous support.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US84881492A | 1992-03-10 | 1992-03-10 | |
| US848,814 | 1992-03-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2088939A1 true CA2088939A1 (en) | 1993-09-11 |
Family
ID=25304350
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002088939A Abandoned CA2088939A1 (en) | 1992-03-10 | 1993-02-05 | Low temperature conversion of alkanes |
Country Status (3)
| Country | Link |
|---|---|
| EP (1) | EP0560546A1 (en) |
| JP (1) | JPH069446A (en) |
| CA (1) | CA2088939A1 (en) |
Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7838708B2 (en) | 2001-06-20 | 2010-11-23 | Grt, Inc. | Hydrocarbon conversion process improvements |
| AU2004268935B2 (en) | 2003-07-15 | 2010-12-02 | Grt, Inc. | Hydrocarbon synthesis |
| US20050171393A1 (en) | 2003-07-15 | 2005-08-04 | Lorkovic Ivan M. | Hydrocarbon synthesis |
| US8642822B2 (en) | 2004-04-16 | 2014-02-04 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons using microchannel reactor |
| US7674941B2 (en) | 2004-04-16 | 2010-03-09 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons |
| US8173851B2 (en) | 2004-04-16 | 2012-05-08 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons |
| US7244867B2 (en) | 2004-04-16 | 2007-07-17 | Marathon Oil Company | Process for converting gaseous alkanes to liquid hydrocarbons |
| US20060100469A1 (en) | 2004-04-16 | 2006-05-11 | Waycuilis John J | Process for converting gaseous alkanes to olefins and liquid hydrocarbons |
| US20080275284A1 (en) | 2004-04-16 | 2008-11-06 | Marathon Oil Company | Process for converting gaseous alkanes to liquid hydrocarbons |
| JP2007108046A (en) * | 2005-10-14 | 2007-04-26 | Idemitsu Kosan Co Ltd | Two-layer separating temperature measuring device and measuring technique thereof |
| MY153001A (en) | 2006-02-03 | 2014-12-31 | Grt Inc | Continuous process for converting natural gas to liquid hydrocarbons |
| ZA200807230B (en) | 2006-02-03 | 2009-11-25 | Grt Inc | Separation of light gases from halogens |
| KR20100027141A (en) | 2007-05-24 | 2010-03-10 | 지알티, 인코포레이티드 | Zone reactor incorporating reversible hydrogen halide capture and release |
| US8282810B2 (en) | 2008-06-13 | 2012-10-09 | Marathon Gtf Technology, Ltd. | Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery |
| CA2730934C (en) | 2008-07-18 | 2017-07-04 | Grt, Inc. | Continuous process for converting natural gas to liquid hydrocarbons |
| US8198495B2 (en) | 2010-03-02 | 2012-06-12 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
| US8367884B2 (en) | 2010-03-02 | 2013-02-05 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
| EP3859017A1 (en) | 2010-06-26 | 2021-08-04 | Virdia, Inc. | Methods for production of sugar mixtures |
| IL206678A0 (en) | 2010-06-28 | 2010-12-30 | Hcl Cleantech Ltd | A method for the production of fermentable sugars |
| IL207329A0 (en) | 2010-08-01 | 2010-12-30 | Robert Jansen | A method for refining a recycle extractant and for processing a lignocellulosic material and for the production of a carbohydrate composition |
| IL207945A0 (en) | 2010-09-02 | 2010-12-30 | Robert Jansen | Method for the production of carbohydrates |
| US8815050B2 (en) | 2011-03-22 | 2014-08-26 | Marathon Gtf Technology, Ltd. | Processes and systems for drying liquid bromine |
| EP3401322B1 (en) | 2011-04-07 | 2022-06-08 | Virdia, LLC | Lignocellulose conversion processes and products |
| US8436220B2 (en) | 2011-06-10 | 2013-05-07 | Marathon Gtf Technology, Ltd. | Processes and systems for demethanization of brominated hydrocarbons |
| US8829256B2 (en) | 2011-06-30 | 2014-09-09 | Gtc Technology Us, Llc | Processes and systems for fractionation of brominated hydrocarbons in the conversion of natural gas to liquid hydrocarbons |
| US8802908B2 (en) | 2011-10-21 | 2014-08-12 | Marathon Gtf Technology, Ltd. | Processes and systems for separate, parallel methane and higher alkanes' bromination |
| US9193641B2 (en) | 2011-12-16 | 2015-11-24 | Gtc Technology Us, Llc | Processes and systems for conversion of alkyl bromides to higher molecular weight hydrocarbons in circulating catalyst reactor-regenerator systems |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6035766Y2 (en) * | 1981-03-16 | 1985-10-24 | 三菱自動車工業株式会社 | clamp device |
| JPS61139377U (en) * | 1985-02-20 | 1986-08-29 |
-
1993
- 1993-02-05 CA CA002088939A patent/CA2088939A1/en not_active Abandoned
- 1993-03-04 JP JP5043678A patent/JPH069446A/en active Pending
- 1993-03-08 EP EP93301717A patent/EP0560546A1/en not_active Withdrawn
Also Published As
| Publication number | Publication date |
|---|---|
| JPH069446A (en) | 1994-01-18 |
| EP0560546A1 (en) | 1993-09-15 |
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