Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
  • C07C2/66—Catalytic processes
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
  • C07C2/66—Catalytic processes
  • C07C2/70—Catalytic processes with acids
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
  • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/14—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of germanium, tin or lead
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
  • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • C07C2523/24—Chromium, molybdenum or tungsten
  • C07C2523/30—Tungsten
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • C07C2527/02—Sulfur, selenium or tellurium; Compounds thereof
  • C07C2527/053—Sulfates or other compounds comprising the anion (SnO3n+1)2-
  • C07C2527/054—Sulfuric acid or other acids with the formula H2Sn03n+1

Definitions

• the present invention relates to a catalyst and process for alkylation of non-oxygen-containing aromatic hydrocarbons, such as benzene, toluene, xylene, or mixtures thereof.
• Lewis or Br ⁇ nsted acid catalysts Typical commercial catalysts include phosphoric acid/kieselguhr, aluminum chloride, and hydrogen fluoride.
• the alkylations are done in the liquid phase, usually in the presence of hydrogen fluoride.
• Alkylations of benzene with higher olefins is especially difficult, and requires hydrogen fluoride treatment.
• Such a process is disclosed by Himes in U.S. Patent No. 4,503,277, entitled "HF Regeneration in Aromatic Hydrocarbon Alkylation Process," which is hereby incorporated by reference for all purposes.
• hydrogen fluoride is not environmentally attractive.
• a process for using solid catalysts to produce alkyl aromatics using lower olefins is disclosed by Vora et al. in U.S. Patent No. 5,012,021, entitled “Process for the Production of Alkylaromatic Hydrocarbons Using Solid Catalysts," which is hereby incorporated by reference for all purposes.
• the disclosed solid catalysts include amorphous silica-alumina, crystalline aluminosilicate materials, naturally occurring and man-made clays, and acidic polymer catalysts.
• Vora et al. does not mention sulfonated zirconia as a possible catalyst.
• activated solid acidic catalysts that have a metal oxide are good catalysts for alkylation of non-oxygen-containing aromatic hydrocarbons, such as benzene, toluene, xylene, or mixtures thereof, if the activated catalyst is used without exposure to atmospheric water.
• specific catalysts are zirconium oxide or tin oxide, such as Zr0 2 -H 2 S0 ; Zr0 2 -W0 3 ; and Sn0 2 -H 2 S0 4 .
• These catalysts are especially good for the alkylation of benzene, even when the olefins have sixteen or more carbon atoms per molecule.
• the prior art fails to recognize these metal oxide catalysts as good catalysts for this very difficult reaction.
• the olefins have from 16 to 28 carbon atoms per molecule. More preferably, the olefins are alpha olefins having from 20 to 24 carbon atoms per molecule.
• the present invention involves the alkylation of non-oxygen-containing aromatic hydrocarbons, such as benzene and alkyl benzenes.
• aromatics are reacted with olefins in the presence of a solid, acidic catalyst comprising a metal oxide. That catalyst is activated prior to use and the activated catalyst is used without exposure to atmospheric water.
• olefins having at least sixteen carbon atoms per molecule are reacted in the presence of a solid, acidic catalyst that has either zirconium oxide or tin oxide.
• the preferred catalyst compositions are mixed oxides.
• alkylation of benzene or alkyl benzenes does not take place as readily as alkylation of other aromatics, and alkylation of aromatics with higher olefins in the C. 6 to C 28 range does not take place as readily as with the lower olefins.
• the alkylation of benzene with higher olefins is especially difficult.
• the present invention is a solid, acid replacement for hydrogen fluoride.
• Solid, acidic catalysts have been used with low molecular weight olefins. They have not been used with higher molecular weight olefins, such as the C 20 -C 24 ⁇ -olefins of the present invention.
• the non-oxygen-containing aromatic hydrocarbon that is alkylated in the subject process is preferably benzene, but a higher molecular weight hydrocarbon may also be charged to the process.
• Benzene is less reactive than substituted aromatics, thereby it requires higher temperatures to get high conversion of product.
• the feed aromatic hydrocarbon may, therefore, be toluene, xylene, ethylbenzene, naphthalene, etc., as long as it doesn't contain oxygen.
• the feed olefinic hydrocarbons that are consumed in the process may have from about six to twenty-eight carbon atoms per molecule. Preferably, they have sixteen to twenty-eight carbon atoms per molecule. Most preferably, they are predominately alpha olefins having from twenty to twenty- four carbon atoms per molecule. In this most preferred embodiment, small amounts of C 18 and C 26 olefins can be present.
• the catalysts of the present invention are solid, acidic catalysts that have a metal oxide, preferably zirconium oxide or tin oxide.
• the catalyst is activated prior to use and the activated catalyst is used without exposure to atmospheric water.
• the preferred catalyst compositions are mixed oxides.
• the preferred catalysts are Zr0 2 -H 2 S0 4 ; Zr0 2 -W0 3 ; and Sn0 2 -H 2 S0 4 .
• the most preferred catalysts contain zirconium oxide, such as Zr0 2 -H 2 S0 4 .
• Catalysts are activated by:
• the inert material may be dried gases such as nitrogen, helium, argon or dried liquids, such as hexane and benzene.
• the inert material must not be capable of, or contain materials, producing water or protic materials when heated or brought in the presence of an acidic catalyst (e.g., alcohols, ethers, ammonia, amines, etc.).
• an acidic catalyst e.g., alcohols, ethers, ammonia, amines, etc.
• the activation temperature is at least 100° C, because that is the boiling point of water. More preferred is about 150° C, but activation temperature has to be determined by experiment. In our practice, we have used 100° or 150° C activation for batch reactions and 150° to 300° C for flow reactions.
• the catalyst can be bound by conventional means, such as disclosed by King in U.S. Patent No. 4,873,017 described above.
• Examples 1 and 2 are two different preparations of catalysts of the present invention used in two different alkylation examples.
• ZrOCI 2 « 8H 2 0 (150 g) was dissolved in 600 ml distilled water. To this solution was added concentrated ammonium hydroxide solution until the pH reached 10.0. As the ammonium hydroxide solution was added, a thick white precipitate formed. Additional water was added to aid mixing. The solids were collected on a filter and washed twice with distilled water. The solid material was dried for four days at 95-103° C. To the resulting hydrated zirconium hydroxide (9.661 g) from the previous step was added 151.8 ml 1 N (0.5 M) sulfuric acid. The mixture was stirred for half an hour and the solids were recovered by filtering through a fritted glass filter.
• the collected solids were washed twice with 100 ml of distilled water. The resulting solids were dried at 100° C for 18 hours. The dried solids were calcined in flowing air according to the following temperature schedule: Heat to 120° C at 10 m in Hold at 120° C for three hours Heat to 540° C at 2 min Hold at 540° C for five hours
• the solids were stirred for half an hour and collected by filtration. The collected solids were washed with 3000 ml of distilled water. The resulting solids were dried at 100° C for 18 hours. The dried solids were calcined in flowing air according to the temperature schedule given for Catalyst A.
• a 1/2" OD reactor was packed with 17.3g of Catalyst A (pelletized and crushed to 20/40 mesh) with alundum placed above and below the catalyst bed.
• the catalyst was activated at 300°C under flowing nitrogen (100 SCCM/min) at atmospheric pressure for four hours. After cooling to ambient temperature under nitrogen, the catalyst was heated to 50°C and a feed consisting of benzene/C 20 . 24 ⁇ -olefin (4:1 molar ratio) was introduced. After a pressure of 300 psig was obtained, the flow rate was set at 15 ⁇ l/min. Product samples were taken periodically and analyzed as described above. After 28.9 hours, the temperature was increased to 75°C and after 53.8 hours, temperature was again increased to 100°C.
• the catalyst from the previous experiment was removed from the reactor and calcined under flowing nitrogen according to the temperature schedule shown for the preparation of Catalyst A to remove organic residues and coke. It was then recharged to the reactor. It was activated at 300°C for three hours as described above. After cooling to ambient temperature, feed was introduced and pressure maintained at 300 psig. The feed rate was set at 5.7 ⁇ l/min and the reactor was heated stepwise to 100°C. Conversion was increased to greater than 90% after two days at this temperature. After 239 hours at 100°, the temperature was increased to 115°. For a period of 290 hours at 100° or higher temperature, the olefin conversion was at least 88%.
• Sulfated zirconia catalyst (1.784 g) was charged to a round-bottom flask equipped with a magnetic stirring bar and a reflux condenser. The condenser was air-cooled. To the round bottom flask were added 3.202 g of commercial C 20 - 2 alpha olefin and 3.907 g phenol. The molar ratio phenoholefin was 4 and the weight ratio of feed (phenol + olefin) to catalyst was 4. The phenol and alpha olefin were used as received. The round bottom flask was heated by an oil bath pre-heated to 155° C while the contents of the flask were stirred magnetically. Samples were taken periodically by syringe and were analyzed by SFC. Results showed 99.4% olefin conversion in one hour. This experiment showed that phenol is readily alkylated by C 20 . 24 alpha olefin without any activation or drying of the catalyst.

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• Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

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• 1995
  • 1995-12-29 EP EP95944407A patent/EP0748305B1/en not_active Expired - Lifetime
  • 1995-12-29 WO PCT/US1995/016931 patent/WO1996020905A1/en not_active Ceased
  • 1995-12-29 JP JP8521141A patent/JPH09509967A/ja not_active Abandoned
  • 1995-12-29 CA CA 2184157 patent/CA2184157A1/en not_active Abandoned
  • 1995-12-29 DE DE69518405T patent/DE69518405T2/de not_active Expired - Fee Related

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