EP0994834A1 - Complexe de catalyseurs renfermant des ligands et des metaux du groupe du platine et procede ameliore de conversion catalytique d'alcanes en esters et en leurs derives - Google Patents

Complexe de catalyseurs renfermant des ligands et des metaux du groupe du platine et procede ameliore de conversion catalytique d'alcanes en esters et en leurs derives

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Publication number
EP0994834A1
EP0994834A1 EP97925483A EP97925483A EP0994834A1 EP 0994834 A1 EP0994834 A1 EP 0994834A1 EP 97925483 A EP97925483 A EP 97925483A EP 97925483 A EP97925483 A EP 97925483A EP 0994834 A1 EP0994834 A1 EP 0994834A1
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EP
European Patent Office
Prior art keywords
catalyst
platinum group
group metal
ligand
lower alkane
Prior art date
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EP97925483A
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German (de)
English (en)
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EP0994834A4 (fr
Inventor
Roy A. Periana
Douglas J. Taube
Scott Gamble
Henry Taube
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Catalytica Inc
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Catalytica Inc
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Priority claimed from PCT/US1997/007772 external-priority patent/WO1998050333A1/fr
Publication of EP0994834A1 publication Critical patent/EP0994834A1/fr
Publication of EP0994834A4 publication Critical patent/EP0994834A4/fr
Withdrawn legal-status Critical Current

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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • This invention relates to an improved process for converting lower alkanes into their corresponding esters using ligand-assisted noble or platinum group metal catalysts and to novel ligated platinum group metal catalysts which are useful in catalyzing the alkane conversion reaction.
  • the process of the invention also includes additional and optional conversion steps whereby the ester product may be converted to other intermediates or derivatives, such as an alcohol or alkyl halide, which, in turn, can be converted to liquid hydrocarbons such as gasoline.
  • the invention is directed to an improved process for the selective oxidation of lower alkane starting materials into their corresponding esters and, optionally, into various derivatives (such as methanol) in oxidizing acidic media using a stable platinum group metal ligand catalyst complex at elevated temperatures and to a class of novel platinum group metal ligand complexes which are sufficiently stable in the oxidizing acidic media at elevated temperatures to be effective catalysts in the alkane conversion reaction.
  • a threshold problem in devising a catalytic process for the partial oxidation of alkanes is the non-reactive nature of the alkane C-H bond and the difficulty in finding a catalytic substance which will promote activation of, and subsequent reaction at, one or more of the C-H bonds of the alkane reactant without also catalyzing complete oxidation of the alkane in question — e.g., methane to CO2.
  • This threshold problem has been solved, to at least some degree, by the catalytic process described in U.S. Patent Nos.
  • Hg(II) is the most effective catalyst for the oxidation of methane to methanol in oxidizing, strongly acidic media.
  • the issue of loss of metal ion by reduction to bulk metal is mitigated because the bulk metal form of Hg is not noble and the cationic state is thermodynamically favored over the metallic state.
  • this metal suffers from disadvantages that in sulfuric acid solvents containing free SO3, a major side product, methane sulfonic acid is produced.
  • the noble metals do not suffer these disadvantages, but have not been used because of the issues of catalyst deactivation and poor selectivity, as discussed above. Thus, it would be advantageous to address the issue of bulk metal formation in the use of the noble metals.
  • One possibility for allowing the use of noble metals in the alkane oxidation reaction is to modify the reaction system to permit dissolution and reoxidation of the metallic form of the noble metal, and/or to prevent the formation of the metallic metal. In certain cases, this can be accomplished by the use of ligands that stabilize the ionic forms of the metals.
  • ligands that stabilize the ionic forms of the metals.
  • chloride ions are added to stabilize the Pd catalysts in the active, cationic state.
  • Other ligands have been investigated in that system, but in general chloride has been found to be the most ideal ligand because of the resulting stability and high efficiency of the catalytic system.
  • Organic-type ligands such as amines, phosphines, thiols, alcohols, bromides, iodides, cyanides, etc., are not used because they are not as efficient as chloride and can be destroyed by the oxidizing or acidic conditions of the reaction.
  • platinum group metal catalysis of the partial oxidation of a lower alkane reactant to form an ester in oxidizing, strongly acidic media can be substantially enhanced by employing a platinum group metal-ligand complex wherein the ligand employed is a heteroatom-containing ligand which forms a mono-dentate or poly-dentate complex with the platinum group metal and the complex so formed is stable in the strong acid reaction media for at least ten minutes at temperatures of at least about 180°C.
  • Stability in this case refers to kinetic stability in the acidic reaction media in that the platinum group metal catalyst complex continues to exist in its catalytically active form in sufficient amounts to catalyze the partial oxidation reaction at useful reaction rates rather than becoming unavailable to catalyze the reaction through a combination of insolubility in the reaction media or loss of structure through protonation and/or oxidation resulting in decomposition of the catalytically active species.
  • the invention is an improved process for partial oxidation of a lower alkane to form an ester which comprises contacting the lower alkane, an oxidizing agent, a strong acid and a catalyst comprising a catalytic amount of a platinum group metal stabilized with a heteroatom-containing ligand, which forms a mono-dentate or poly-dentate ligand complex with the platinum group metal, said complex being stable in the strong acid for at least about ten minutes at temperatures of about 180°C and said contacting occurring at esterification conditions to produce a lower alkyl ester of the acid in a molar amount greater than the molar amount of catalytic metal present.
  • the process of the invention includes subsequent process steps where the alkyl ester product of the partial oxidation is reacted with a nucleophile, such as H2O or HC1, to yield a functionalized derivative, e.g., an alcohol or alkyl chloride, of the lower alkane starting material and where, optionally, the functionalized derivative of the lower alkane is catalytically converted into a higher molecular weight hydrocarbon.
  • a nucleophile such as H2O or HC1
  • An additional aspect of the invention is directed to a novel class of ligated platinum group metal catalyst complexes which exhibit high levels of catalytic activity in the acidic, oxidizing reaction media employed in the process of the invention.
  • These novel catalyst compositions comprise a catalytically-active, platinum group metal/ligand complex of the formula ML m X n wherein M is a platinum group metal, L is a bidiazine ligand, optionally substituted with one or more hydrocarbyl groups or substituted hydrocarbyl groups, or a substituent selected from -SO3H and fluoride or any mixture thereof, X is an oxidation resistant anion selected from halide, hydroxide, sulfate, bisulfate, nitrate and phosphate or the conjugate anion base of the strong acid reactant, m is 1 or 2 and n is an integer of 1 to 8 depending on the oxidation state of the platinum group metal. DESCRIPTION OF THE INVENTION
  • the process of the invention essentially parallels the step- wise process disclosed in U.S. Patent Nos. 5, 233,113 and/or 5,306,855, both of which are herewith incorporated by reference, with the exception of the catalyst employed in the first (or ester-forming) step of the process described therein.
  • the first step of the process involves contacting a lower alkane with an acid and an oxidizing agent in the presence of a catalyst, in this case a ligated platinum group metal catalyst complex, at elevated temperatures to afford the alkyl ester product.
  • the catalyst employed in the first or ester-forming step of the process of the invention is suitably a platinum group metal stabilized with a heteroatom-containing ligand which forms a mono-dentate or poly-dentate ligand complex with the platinum group metal, said complex being stable in the strong acid employed as the solvent for the ester-forming step for at least about ten minutes at temperatures of about 180°C.
  • platinum group metal ligand complexes which exhibit substantial instability and loss of catalytic activity in the presence of the strong acid at about 180°C (which is typically the low end of the temperature range for the ester-forming reaction) in less than about 10 minutes of contact time do not afford a sufficient space-time yield of ester product to be useful in industrial scale processes.
  • the catalyst complex is stable in the strong acid for at least about 30 minutes and most preferably for greater than two hours.
  • the mono-dentate or poly-dentate, preferably bi-dentate, ligand employed in the catalyst complex is suitably a heteroatom-containing ligand which binds the platinum group metal through one or more nitrogen, sulfur or phosphorus atoms or mixtures thereof — e.g., phosphines, organo-phosphorus compounds, amines and heterocyclic organic compounds containing ring nitrogens and/or sulfur atoms.
  • the stabilizing ligand for the catalyst complex is a heteroatom-containing ligand where the heteroatom is nitrogen which forms a bi-dentate ligand complex with the platinum group metal.
  • any platinum group metal may be employed in the catalyst complex used in the ester-forming reaction — e.g., Pt, Pd, Rh, Ir, Rh and Os or mixtures thereof — it is preferred that the platinum group metal be selected from Pd and Pt or mixtures thereof with Pt being most preferred from a catalytic activity standpoint.
  • the catalyst complex employed in the ester-forming reaction is a platinum group metal ligand complex of the formula ML m X n wherein M is a platinum group metal, L is a bidiazine ligand, optionally substituted with one or more hydrocarbyl groups or substituted hydrocarbyl groups, or a substituent selected from -SO3H and fluoride or any mixture thereof, X is an oxidation-resistant anion selected from halide, hydroxide, sulfate, bisulfate, nitrate and phosphate or the conjugate anion base of the strong acid reactant, m is 1 or 2 and n is an integer of 1 to 8 depending on the oxidation state of the platinum group metal employed.
  • M is platinum
  • X is preferably 1, 2, 3 or 4 and, most preferably, 1 or 2.
  • Y, Y', Z and Z' are nitrogen or carbon with the proviso that one of Y, Y', Z and Z' must be nitrogen and the remainder of Y, Y', Z and Z' must be carbon
  • R and R' are hydrogen, hydrocarbyl, substituted hydrocarbyl, fluoride or -SO3H and m' and n' are 0, 1,
  • bidiazine ligands of the above formula possess unique stability in the strong acid media at 180°C or higher with essentially no loss of catalytic activity being observed in residence times ranging from greater than two hours to several days.
  • exemplary of suitable bidiazine ligand compounds in this preferred class are the following bidiazine compounds (which may be optionally substituted as set forth above):
  • M represents platinum in the formula given above
  • L is a 2,2'-bipyrimidine (preferably unsubstituted) and
  • X is a halide selected from chloride, bromide and iodide.
  • m is 1 and n is 2.
  • the catalyst complexes of the invention can be prepared by any conventional method for preparing such metal ligand complexes.
  • the catalyst complexes are separately prepared by mixing, in appropriate molar ratios, a platinum group metal (in compound or bulk metal form); a ligand compound and an inorganic salt containing the oxidation-resistant anion in an aqueous or weakly acidic media to form the complex which can then be added to the acidic oxidizing reaction media used in the ester-forming reaction.
  • the platinum group metal in addition to bulk metal form which is suitably a finely divided dispersion of metal, the platinum group metal may be added in the form of a soluble salt compound — e.g., a halide or nitrate, or as an oxide or hydroxide.
  • a soluble salt compound e.g., a halide or nitrate, or as an oxide or hydroxide.
  • the inorganic salt employed is suitably an alkali or alkaline earth metal salt or other salt containing a basic cation — e.g., an ammonium salt.
  • platinum group metal in the form of a salt where the anion is one of the oxidation resistant anions set forth for X in the formula given above — e.g, halide, hydroxide, sulfate, bisulfate, nitrate or phosphate and thereby avoid the need for separate addition of an inorganic salt component.
  • the preferred platinum group metal ligand complex can be most conveniently prepared by adding the catalyst components directly to the strong acid media employed in the ester-forming reaction and allowing the catalyst to form in situ in the reaction zone or vessel used to partially oxidize the lower alkane to the corresponding ester. That is, in this preferred aspect, the active catalyst is prepared in situ in the oxyester-forming reaction zone by mixing the platinum group metal in bulk or compound form, preferably a compound of platinum, a bidiazine compound and an inorganic salt containing the oxidation resistant anion in the strong acid employed as the reaction media for the ester-forming reaction prior to introduction of this lower alkane reactant.
  • the molar ratios of platinum group metal: bidiazine ligand: inorganic salt components suitably used in the preparation are about 1-2:0.5-1:1-2 dependent on the concentration of strong acid in the reaction zone temperatures and the nature of the ligand employed.
  • the optimum molar ratio of Pt: Ligand: Cl is about 1:0.75:2 for highest catalytic activity in 100% H2SO4 at 220°C in the partial oxidation of methane.
  • the catalytic activity of the platinum group metal catalyst complex in the ester-forming reaction can be enhanced by the addition of a co-catalyst or oxidation synergist comprising a halide ion or an inorganic salt of tellurium or antimony or mixtures thereof.
  • a co-catalyst or oxidation synergist comprising a halide ion or an inorganic salt of tellurium or antimony or mixtures thereof.
  • the platinum group metal catalyst operates in two distinct steps — i.e., a C-H bond activation step which is rapid and an oxidation step which appears to be rate limiting — and the presence of the co-catalyst increases the rate of oxidation of the oxidation step and therefore the rate of the catalytic cycle increases.
  • the co-catalyst should be selected from tellurium and antimony salts to maximize the benefit obtained from the co-catalyst.
  • co-catalysts include Te(IV) and Te(VI) salts, most preferably, Te halide salts — e.g., TeCl4, TeCl5 and TeBr
  • Te halide salts e.g., TeCl4, TeCl5 and TeBr
  • the amount of co-catalyst which is suitably employed relative to the amount of catalyst complex present can vary over wide limits depending on the other reaction conditions used but typically ranges between about 0.5 to 4 moles of co-catalyst per mole of platinum group metal catalyst complex present.
  • the co-catalyst is present at from about 1 to about 2 moles per mole of catalyst complex employed in the reaction zone.
  • Lower alkanes which may be suitably employed as starting materials for the ester-forming reaction include C ⁇ to Cg straight or branched-chain alkanes — e.g., methane, ethane, propane, isobutane, hexane and heptane.
  • the lower alkane starting material is a straight chained alkane of 1 to 4 carbon atoms, that is, methane, ethane, propane or butane, and, most preferably, the alkane starting material is methane including impure forms of methane such as that found in natural gas reservoirs.
  • the oxidizing agent employed in the ester-forming reaction may be a strong oxidant such as those disclosed in the referenced U.S. Patent Nos. 5,233,113 and 5,306,855 — e.g., HNO3, perchloric acid, peroxy compounds (H2O2, CH3CO3H,
  • K2S2 ⁇ g hypochlorites (such as NaOCl), O2, O3, SO3, NO2, and cyanogen, as well as a variety of other oxidizing substances having redox potentials greater than 0.3 volts — e.g., quinones, halogens, selenium cations, tellurium cations and the like.
  • Preferred oxidants from a cost of materials, availability and effectiveness standpoints include SO3, H2SO4 and O2 while oxidants which can be recycled with O2 — e.g., SO3, H2O2, quinone and cations of selenium and/or tellurium — are also advantageous.
  • the oxidant can be added to the ester reaction zone before, or after, or during the addition of the alkane starting material.
  • the amount of oxidizing agent employed is typically at least stoichiometric with the amount of alkane starting material added to the reaction zone.
  • the acid employed as the reaction medium or solvent in the ester-forming reaction may be any of the acids described in the referenced U.S. patents (see above), including organic or inorganic acids such as HNO3, H2SO4, CF3CO2H, CF3SO3H,
  • the preferred acids are strong acids haying pK a s of less than 2.0 with H2SO4 and CF3SO3H being particularly preferred.
  • the function of the acid is to generate an alkyl compound containing an electron withdrawing group such as -OSO3H, -OSO2CF3 or -OH2 + .
  • an electron withdrawing group such as -OSO3H, -OSO2CF3 or -OH2 + .
  • the function of the electron withdrawing group is to
  • the acid is desirably used in excess since it can act both as the reaction medium and as a reactant in the process, that is, the acid contributes the anion to form the ester on oxidation of the alkane.
  • the acid employed is desirably oxidation-resistant in that it is not itself oxidized by the platinum group metal complex in the noted reaction medium.
  • H2SO4 is employed as the reaction medium together with an oxidizing agent selected from SO3, O2 and H2SO4.
  • H2SO4 functions both as the acid and the oxidant.
  • the ester-forming reaction can be carried out either batchwise or continuously using processing methods or techniques which are well known in the art.
  • the amount of catalyst complex employed must be at least a catalytic amount with amounts ranging between about 50 ppm and 1.0% by mole of the total liquid present being effective.
  • the temperatures of the ester-forming reaction is typically above 50°C and preferably between 95°C and 250°C with temperatures in the range of about 180° to 230°C being most preferred.
  • methane is the alkane reactant, it is added at a pressure above about 50 psig, preferably, above about 450 psig.
  • a nucleophile is reacted with the ester to form a functionalized derivative of the lower alkane and the functionalized derivative is then catalytically converted to a comparatively higher molecular weight hydrocarbon.
  • the ester may be reacted directly with a nucleophilic substance or, optionally, the ester may be recovered from the ester-forming reaction by flashing or distillation and then reacted with a nucleophilic substance such as water or a hydrogen halide to produce the functionalized derivative of the alkane starting material.
  • the functionalized derivative is methanol if this nucleophile is H2O; methyl halide, if the nucleophile is a hydrogen halide such as
  • nucleophile HC1, HBr, or HI
  • methyl amine if the nucleophile is NH3
  • a methyl thiol if the nucleophile is H2S or acetonitrile if the nucleophile is HCN.
  • other functionalized derivatives can be generated from the original methyl ester by reaction with other nucleophiles, e.g., other esters such as methyl triflouroacetate if the nucleophile is triflouroacetic acid.
  • nucleophile is used generally in this context and to one skilled in the art many such exchange reactions can be considered. These reactions proceed readily to completion. An excess of the nucleophile is desirable.
  • the preferred nucleophile is H2O since it may also be produced in the ester-forming reaction.
  • the product methanol may be used directly, or may be converted to a variety of hydrocarbons in the subsequent optional step.
  • the subsequent optional process step includes conversion of the functionalized alkane derivative — e.g., methanol to a longer chain or higher molecular weight hydrocarbon.
  • the functionalized alkane derivative e.g., methanol
  • Butter shows the production of olefinic and aromatic compounds by contacting the methyl intermediate with an aluminosilicate catalyst, preferably HZSM-5, at a temperature between 650°-1000°F.
  • an aluminosilicate catalyst preferably HZSM-5
  • Butter suggests a process using a preferable catalyst of antimony oxide and HZSM-5 at a temperature between 250°-700°C.
  • the ZSM-5 zeolite has been disclosed as a suitable molecular sieve catalyst for converting methyl alcohol into gasoline range hydrocarbons. See, for instance, U.S. Patent Nos. 3,702,886 to Argauer et al. and 3,928,483 to Chang et al.
  • the reaction products were analyzed by gas chromatography (GC), high-pressure liquid chromatography (HPLC), and nuclear magnetic resonance spectroscopy (NMR).
  • GC gas chromatography
  • HPLC high-pressure liquid chromatography
  • NMR nuclear magnetic resonance spectroscopy
  • the gas phase of the reactions of methane with platinum compounds in sulfuric acid were analyzed by gas chromatography on a Hewlett-Packard 5880 GC fitted with a HayeSep ⁇ D packed column and a thermal conductivity detector.
  • the response factors for the gases, Ne, CH4, CO2, CO, SO2, and CH3CI were obtained by the injection of a calibration gas mixture (Alphagaz). Neon was added to the feed methane (3 mole %) as an internal standard.
  • the liquid phase of the reaction was analyzed by both HPLC and NMR.
  • the reaction solution was hydrolyzed by the addition of 1 mL reaction solution to 3 mL distilled water and heated to 95 °C for 2 hours.
  • the hydrolyzed solution was injected onto a Hewlett-Packard 1050 HPLC equipped with a Aminex ⁇ HPX87H ion exclusion column and a refractive index detector.
  • the eluant was 0.01% H2SO4 in water.
  • reaction solutions were also analyzed by multinuclear NMR ( ⁇ H and ⁇ C).
  • the concentration of the products in the neat reaction solutions were measured by NMR using acetic acid as an internal standard.
  • the catalysts including Pt(bpym)Cl2 were synthesized according to general literature procedures (Kiernan, P.M., Ludi, A., J.C.S. Dalton, 1978, 1127). In short, K2PtCl4 and the appropriate ligand added in a stoichiometric ratio, were added to distilled water and allowed to stir for several hours. During this time, the initially orange solution became cloudy and a precipitate formed. When the solution had become void of color, the reaction was filtered giving a powder. In most cases the solid was air dried and used. In the case of Pt(bpym)Cl2, the solid formed a hydrate, Pt(bpym)Cl2'0.5 H2O. The solid was dehydrated by adding the dark green solid to acetone resulting in an orange solid. C. Reaction Procedures
  • the 300 cc autoclave (Autoclave Engineers) was constructed of Hasteloy C.
  • the internal parts were tantalum (stir shaft, impeller and baffle) or covered with glass.
  • the reaction was stirred by an external Magna drive stirrer connected to an impeller.
  • the reaction solution was loaded into a glass liner which fit snugly into the reactor body.
  • Methane was fed into the reactor using a high-pressure feed cylinder.
  • the amount of methane fed into the reactor was measured by the pressure drop in the feed cylinder.
  • the ester-forming reactions in sulfuric acid were run at reaction temperatures between 180°-220 °C for 1 to 6 hours. Reactions conducted in the 300 cc autoclave were typically run in the batch mode. At the end of the reaction, the reactor was cooled to room temperature by the use of a water jacket, and the gas phase bled to an evacuated cylinder. The gas was analyzed by GC. A second venting of the reactor head space into an evacuated cylinder was conducted so that the final reactor pressure was less than 500 torr.
  • the second venting was performed to remove most of the soluble gases from the reaction solution.
  • the gases from the second venting were also analyzed by GC.
  • the reaction solution was analyzed by HPLC and NMR.
  • the carbon mass balance of the reaction was measured in two separate ways, by the use of neon as an internal standard, and by measuring the amount of the exit gases using the ideal gas law. Typically, both methods gave carbon mass balance values of greater than 95%.
  • reactions were also run on a smaller scale in 100 cc Parr bombs. These reactions were heated by an external oil bath and stirred by using a Teflon® stir-bar driven by an external magnetic stirrer. The reaction solution volumes, typically 5 ml, were added to a glass vial equipped with a weep hole. Analysis of the gas phase was by GC, and the solution phase by HPLC and NMR. Carbon mass balance values were not obtained in the
  • This example describes the oxidation of methane at high pressure using a platinum 2,2'-bipyrimidine iodide catalyst complex (Pt(bpym)l2) in 100.5% H2SO4.
  • the experiment was conducted in a 300 cc autoclave using the procedure described above.
  • reaction solution and reactor wash solutions were analyzed by removing 1 mL aliquots of each, diluting in 3 mL H2O, sealing in sample vials which were placed in a heater block at 95°C for 120 mins. After hydrolysis, the solutions were cooled, centrifuged, and analyzed by HPLC.
  • HPLC traces indicated a methanol concentration of 860.4 mM in the original reaction solution, and a total of 103.252 mmol methanol.
  • the selectivity to methanol was 80.04%, with a methanol yield of 71.17% based on a methane conversion of 88.92%.
  • the carbon mass balance was 92.53%.
  • Selectivity is defined as percent selectivity to methanol product determined by dividing the moles of methanol found in the final reaction product by the moles of methane consumed in the reaction times 100. Percent conversion is calculated as moles of methane consumed divided by moles of methane charged times 100 and percent yield is determined by multiplying selectivity times conversion.
  • Example 2 Using the procedure described in Example 1, a series of experiments were conducted comparing the mercury catalyst of the prior art with the ligated catalyst of the invention in the oxidation of methane to methanol. These experiments were conducted in a 300 cc autoclave. The concentration of the catalysts were 50 mM for the platinum catalysts and 100 mM for HgSO4. The concentration of methanol produced in the experiment in which the catalyst was generated in situ (H2Pt(OH)g + bpym + TeCl4) was
  • This example describes the oxidation of methane at high pressure using a platinum 2,2'-bipyrimidine bromide catalyst complex (Pt(bpym)Br2) in 96% H2SO4.
  • the reaction was conducted in a 100 mL Parr reactor.
  • reaction solution A 1 mL aliquot of the reaction solution was diluted in 3 mL H2O, and sealed in a sample vial which was placed in a heater block at 95° C for 120 mins. After hydrolysis, the solution was cooled, centrifuged, and analyzed by HPLC. The HPLC trace indicated methanol at a concentration of 487.0 mM (2.435 mmole) in the original reaction solution.
  • This example describes the oxidation of methane at high pressure using a platinum ammine chloride catalyst complex (c-Pt(NH3)2Cl2) in 96% H2SO4.
  • Example 2 Using the procedure described in Example 1, a series of experiments were conducted comparing the mercury catalyst of the prior art with the ligated catalyst of the invention, PtCl2, and H2Pt(OH)g in the oxidation of methane to methanol. These experiments were conducted in a Parr bomb using the procedure described in Example 3. The concentration of the catalysts were 25 mM except for PtCl2 which was 100 mM. The concentration of methanol produced in the experiment in which the catalyst was generated in situ (H2Pt(OH)g + bpym + TeCl4) was 1.05 M. The results are given in Table 2 below where percent selectivity (to methanol) is determined by dividing the moles of methanol found in the final reaction product by the moles of methane consumed in the reaction times 100.
  • This example describes the oxidation of methane at high pressure using a platinum triethyl-phosphine hydrochloride catalyst complex (Pt(PEt3)2HCl) in 96% H2SO4.
  • Pt(PEt3)2HCl platinum triethyl-phosphine hydrochloride catalyst complex
  • This example describes the oxidation of ethane at high pressure using a platinum
  • This example describes the oxidation of ethane at high pressure using a platinum 2,2'-bipyrimidine sulfate catalyst complex (Pt(bpym)SO4) in 102% H2SO4.
  • Pt(bpym)SO4 platinum 2,2'-bipyrimidine sulfate catalyst complex
  • Example 3 Using the procedure of Example 3, an additional series of platinum catalysts (complexed and uncomplexed) were tested in the oxidation of methane to methanol. The results are given in Table 4 below where the ligands used include en or ethylene diamine, bpy or 2,2'-bipyridine, bpym or 2,2'-bipyrimidine, bpym' or 4,4'-bipyrimidine, bpyz or 2,2'-bypyrazine, bpdz or 3,3'-bipyridazine. The selectivities were determined as described above in Example 9.
  • Example 2 Using the reaction procedure described in Example 1, a comparison was made of a preformed catalyst complex and a catalyst complex formed in situ in the catalytic oxidation of methane to methanol.
  • the catalyst complex used was Pt(bpym)Cl2 preformed as described above or formed in situ from the catalyst components bypyrimidine, chloride and platinum or bypyrimidine, sulfate and platinum. The results are shown in Table 5. These reactions were conducted in the 300 cc autoclave. The platinum concentration for these experiments was 50 mM. The reactions were run for 90 minutes at 215°C under 500 psig CH /Ne.
  • the "Pt(bpym)(Cl)(OSO 3 H)" catalyst stoichiometry was prepared by adding 25 mM each of Pt(bpym)Cl2 and Pt(bpym)SO4.
  • Table 9 lists several experiments investigating the selective oxidation of ethane to ethanol, 1,2-ethane diol, and halide-substituted analogs using the general procedure of Example 7. These experiments were conducted in a Parr bomb using 300 psig CH3CH3/ e (2.99 mol% Ne). The sulfuric acid concentrations, reaction temperatures, and.times are listed in the table. The gases, including Ne, O2, N2, CH3CH3, CO2, and
  • CH3CH2CI were collected and analyzed by GC as in the methane experiments.
  • the liquid phase was diluted 1 :3 with distilled water, heated to 95°C for 2 hours to hydrolyze bisulfate esters to alcohols, and analyzed by HPLC.
  • the HPLC was calibrated for ethanol, 1,2-ethane diol, acetic acid, l-chloro-2-ethanol, and acetaldehyde.
  • This example describes the oxidation of methane at high pressure using Pt(NH CSCSNH 2 )Cl2 in 96% H2SO4.
  • reaction solution A 1 mL aliquot of the reaction solution was diluted in 3 mL H2O, and sealed in a sample vial which was placed in a heater block at 95°C for 120 min. After hydrolysis, the solution was cooled, centrifuged, and analyzed by HPLC. The HPLC trace indicated methanol at a concentration of 98.4 mM (0.492 mmole) in the original reaction solution.
  • reaction solution A 1 mL aliquot of the reaction solution was diluted in 3 mL H2O, and sealed in a sample vial which was placed in a heater block at 95 °C for 120 min. After hydrolysis, the solution was cooled, centrifuged, and analyzed by HPLC. The HPLC trace indicated methanol at a concentration of 69 mM (0.345 mmole) in the original reaction solution.

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Abstract

L'invention concerne un procédé amélioré d'oxydation sélective de matières de départ à base d'alcane inférieur (tel que le méthane) pour les transformer en esters et, éventuellement, en différents dérivés (tels que le méthanol) en milieux acides oxydants, à l'aide d'un complexe stable de catalyseurs renfermant des ligands et des métaux du groupe du platine, à des températures élevées. L'invention concerne également une classe de nouveaux complexes renfermant des ligands et des métaux du groupe du platine utilisant des ligands à base de bidiazine qui sont suffisamment stables en milieux acides oxydants à des températures élevées pour former des catalyseurs efficaces dans la réaction de conversion d'alcanes.
EP97925483A 1997-05-06 1997-05-06 Complexe de catalyseurs renfermant des ligands et des metaux du groupe du platine et procede ameliore de conversion catalytique d'alcanes en esters et en leurs derives Withdrawn EP0994834A4 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/US1997/007772 WO1998050333A1 (fr) 1996-04-24 1997-05-06 Complexe de catalyseurs renfermant des ligands et des metaux du groupe du platine et procede ameliore de conversion catalytique d'alcanes en esters et en leurs derives

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EP0994834A1 true EP0994834A1 (fr) 2000-04-26
EP0994834A4 EP0994834A4 (fr) 2004-12-29

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EP97925483A Withdrawn EP0994834A4 (fr) 1997-05-06 1997-05-06 Complexe de catalyseurs renfermant des ligands et des metaux du groupe du platine et procede ameliore de conversion catalytique d'alcanes en esters et en leurs derives

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EP (1) EP0994834A4 (fr)
JP (1) JP2001524125A (fr)
AU (1) AU3060997A (fr)
CA (1) CA2287300A1 (fr)

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AU2008282659A1 (en) * 2007-07-27 2009-02-05 Dow Global Technologies Inc. Process for selective, partial, substantially solvent-free, oxidation of methane to methanol and/or a methanol derivative with a heterogeneous catalyst and sulfur trioxide
KR101825158B1 (ko) * 2016-12-27 2018-02-06 한국과학기술연구원 메탄올 전구체 생성용 촉매 조성물, 이를 이용하여 생성된 메탄올 전구체 및 메탄올
KR102137669B1 (ko) * 2019-08-05 2020-07-27 한국과학기술연구원 메탄올 또는 그 전구체 합성용 촉매, 이의 제조방법 및 이를 이용한 메탄올 또는 그 전구체의 제조방법
KR102405065B1 (ko) * 2020-01-31 2022-06-07 한국과학기술연구원 메탄 활성화 촉매, 이를 이용한 메틸에스테르 제조방법

Non-Patent Citations (3)

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Title
DATABASE CAPLUS [Online] CHEMICAL ABSTRACTS SERVICE, COLUMBUS, OHIO, US; KOSAKADA, KOTARO: "Oxidation of methane to methanol derivatives by platinum complex catalysts" retrieved from STN Database accession no. 1999:649302 XP002301868 & ORGANOMETALLIC NEWS , (3), 88 CODEN: ORGNE8; ISSN: 0917-1274, 1995, *
KIERNAN, PATRICK M. ET AL: "Complexes of platinum(II) with 2.2'-bipyrimidine: the effect of hydrogen bonding on intermetallic interactions" JOURNAL OF THE CHEMICAL SOCIETY, DALTON TRANSACTIONS: INORGANIC CHEMISTRY (1972-1999) , (9), 1127-30 CODEN: JCDTBI; ISSN: 0300-9246, 1978, XP001194470 *
See also references of WO9850333A1 *

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CA2287300A1 (fr) 1998-11-12
EP0994834A4 (fr) 2004-12-29
JP2001524125A (ja) 2001-11-27
AU3060997A (en) 1998-11-27

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