Classifications

• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D301/00—Preparation of oxiranes
  • C07D301/02—Synthesis of the oxirane ring
  • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
  • C07D301/12—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with hydrogen peroxide or inorganic peroxides or peracids
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J29/00—Catalysts comprising molecular sieves
  • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
  • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
  • B01J29/80—Mixtures of different zeolites
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D301/00—Preparation of oxiranes
  • C07D301/02—Synthesis of the oxirane ring
  • C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
  • C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07D—HETEROCYCLIC COMPOUNDS
  • C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
  • C07D303/02—Compounds containing oxirane rings
  • C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
• • 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
• • 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
  • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

• the present invention relates to a process for preparing propylene oxide by reacting propylene and a peroxide compound, in the presence of a pretreated titanium silicalite epoxidation catalyst.
• a problem with the prior art propylene oxide production processes relates to the use of methanol as a solvent for the processes. While methanol is a necessary reaction component of the peroxide reaction to obtain high activity, the methanol is generally used in large excesses (for example, from 50 - 90 weight percent) to ensure that the reaction mixture remains as one liquid phase.
• Clerici et al. "Epoxidation of Lower Olefins with Hydrogen Peroxide and Titanium Silicalite," Journal of Catalysis, 1993, 140, 71-83, discloses a process that is representative of titanium silicalite hydrogen peroxide epoxidation processes, wherein the methanol level used in one example is approximately 97%.
• Zhang et al. disclose that replacing approximately 24% of the methanol in Zhang et al.'s system with other solvents such as CC1 4 , toluene, or 1 , 2-dichloroethane, results in increased selectivity and less clogging of the catalyst pores, as measured by thermogravimetric analysis (TGA) and pore volume analyses.
• TGA thermogravimetric analysis
• the present invention provides a propylene oxide production process which uses substantially no methanol as a solvent as compared to previously known processes.
• the present invention is directed to a process for preparing propylene oxide by epoxidizing propylene with an oxidant in the presence of a pretreated catalyst; wherein the catalyst comprises an activated titanium silicalite with MFI structure (TS-1 ) catalyst; and wherein the catalyst has been activated by pretreatment with methanol to form the pretreated catalyst.
• the pretreated TS-1 catalyst may be used in the epoxidation of propylene reaction with no additional methanol added as a solvent to the reaction mixture during the reaction of epoxidizing the propylene; and the pretreated catalyst of the present invention has equivalent activity compared to a non-pretreated TS-1 catalyst used in combination with large excesses of methanol as a solvent in accordance with the processes known in the prior art.
• the present invention includes a modified TS-1 catalyst comprising a TS-1 catalyst which has been treated with methanol, and optionally, air dried prior to the use of such modified catalyst.
• the catalyst is modified, i.e., treated with methanol, before the catalyst is used in the reaction of epoxidizing propylene to form propylene oxide.
• resulting pretreated TS-1 catalyst becomes activated and ready for use in a propylene epoxidation reaction process. No additional solvent is necessary in the propylene reaction composition, which promotes the formation of two liquid phases.
• the present invention is advantaged compared to those of the prior art which use 50 weight percent (wt%) or more methanol because the separation and isolation of the epoxide from the reaction mixture is facilitated.
• the removal of methanol as a solvent results in the formation of two liquid phases, which can be decanted after the reaction to obtain an epoxide-rich organic phase.
• the present invention is advantaged compared to the prior art processes because by pre-treating the catalyst with methanol and then using the modified catalyst in the process of the present invention, a higher selectivity of H 2 0 2 to propylene oxide, a higher propylene oxide yield, and a higher selectivity of propylene oxide versus byproducts can be achieved.
• the advantages of the system of the present invention include decreased losses of propylene oxide by solvolysis and decreased energy costs for separation, while maintaining fast reaction times.
• the present invention also presents an advantage over reactor compositions which use amounts of methanol of 50 wt% or higher as a solvent by decreasing by at least 80% the formation of byproduct in the reaction.
• Another advantage of the present invention is lower equipment cost and lower energy usage due to not having to separate out, recover and/or recycle methanol when used as a solvent in a reaction mixture.
• One broad embodiment of the present invention comprises a process for preparing propylene oxide comprising epoxidizing propylene with an oxidant in the presence of a pretreated catalyst; wherein the pretreated catalyst comprises an activated titanium silicalite with MFI structure (TS-1) catalyst; and wherein the catalyst has been activated by pretreatment with methanol in an effective amount to sufficiently activate the catalyst and form the pretreated catalyst.
• a pretreated catalyst comprises an activated titanium silicalite with MFI structure (TS-1) catalyst
• the process for preparing an activated catalyst for use in the present invention comprises pretreating a TS-1 catalyst with methanol.
• the pretreating step includes for example, the step of contacting a TS-1 catalyst with the methanol under conditions to have the methanol bond to the TS-1 catalyst prior to use of the catalyst.
• the catalyst useful in the process of the present invention includes known titanium silicalite catalysts.
• the TS-1 catalysts used in the present invention process may be selected from commercially available catalyst such as TS-1 from Sud Chemie, Polimeri Europa, or Clean Science, for example.
• the TS-1 catalysts can be manufactured by any of the known processes such as those described in U.S. Patent No. 4,410,501 , for example.
• titanium silicates may be used such as titanium-silicalites with a MEL or intermediate MFI MEL structure and titanium-silicalites from beta zeolites containing titanium and having a BEA structure.
• Other titanium containing zeolite catalysts generally known as TS-2, TS-3, Ti-MCM-22, Ti-MWW, ZSM-48 and ZMS-12 can also be used for preparing the catalyst of the present invention process.
• the concentration of the TS-1 catalyst used in the present invention is generally from about 0.1 weight percent (wt%) to about 50 wt%, preferably from about 0.1 wt% to about 25 wt% and more preferably from about 1 wt% to about 10 wt%.
• the methanol useful in the present invention includes known methanol compounds commercially available such as methanol from Fisher Scientific.
• the amount of methanol (MeOH) used to pretreat the TS-1 catalyst is generally at a mole ratio of MeOH to TS-1 catalyst of from about 0.1 : 1 MeOH:TS-l to about 100: 1 MeOH:TS-l , preferably, from about 1 : 1 MeOH:TS-l to about
• MeOH:TS-l 100: 1 MeOH:TS-l , more preferably from about 1 : 1 MeOH:TS-l to about 50: 1
• MeOH:TS-l and most preferably from about 5: 1 MeOH:TS- l to about 10: 1 MeOH:TS- l .
• the fraction (the at least a portion) of titanium that is chemically bonded with methanol in TS-1 catalyst generally is from about 50% to about 200%, preferably from about 100% to about 200% and more preferably from about 150% to about 200%; as determined by infrared (IR) spectroscopy and TGA; and based on the theory that each Ti molecule can bind two MeOH molecules.
• the process of pretreating the catalyst includes for example contacting a TS-1 catalyst with the methanol at a temperature of from about -20 °C to about 60 °C, preferably from about 0 °Qto about 60 °C, and more preferably from about 25 °C to about 60°C.
• the contacting step may be carried out by known methods and equipment such as mechanical stirring, flowing through a packed catalyst bed, or soaking in a container; and the like.
• the contacting step can be carried out for a pre-determined period of time sufficient to bond the methanol to the TS-1 catalyst, such as for example, generally for about 1 minute to about 24 hours, preferably from about 5 minutes to about 1 hour, and more preferably from about 30 minutes to about 1 hour.
• the pretreated catalyst may be separated from the excess methanol. Any separation method known in the art may be used such as filtering, centrifuging, evaporating, decantation, and the like.
• the isolated pretreated catalyst may be dried before or after filtering the catalyst.
• Any drying method known in the art may be used such as by flowing air, placement in a dessicator, or placement in an oven at temperatures below 65 °C with or without the presence of air.
• the pretreated catalyst may be used in the process of epoxidizing propylene to form propylene oxide.
• the pretreated catalyst product of the present invention preferably contains at least a portion of methanol chemically bonded to titanium atoms of the catalyst.
• the fraction of titanium that is chemically bonded with methanol in TS-1 catalyst generally is from about 50% to about 200%, preferably from about 100% to about 200% and more preferably from about 150% to about 200%; as determined by
• the chemisorption of MeOH onto Ti causes a shift in the frequency of the Ti-0 stretch to higher wavenumbers.
• the chemisorption is also evidenced by evolution of material in a TGA at approximately 400 °C.
• methanol that is not chemically bonded but is retained in the pores of the catalyst may be present as well. This is not seen in the IR spectrum at the indicated range, and evolves at approximately 65 °C in the TGA.
• the pretreated catalyst described above may be used in a process of the present invention for oxidizing propylene by reacting the propylene with an oxidant, such as hydrogen peroxide, under reaction conditions to prepare propylene oxide; wherein this oxidizing reaction (also referred to herein as an epoxidation reaction) is catalyzed by the methanol pretreated TS- 1 catalyst which has been activated by pretreatment with methanol as described above.
• an oxidant such as hydrogen peroxide
• the propylene useful in the epoxidation process of the present invention includes any propylene compound known in the art such as propylene commercially available from Sigma Aldrich. Alternatively, the propylene can be manufactured by known . processes.
• the concentration of the propylene used in the epoxidation process is generally from about 10 wt% to about 90 wt%, preferably from about 20 wt% to about 80. wt%, and more preferably from about 30 wt% to about 70 wt%.
• the oxidant useful in the propylene epoxidation process of the present invention includes known oxidant compounds such as peroxocompounds such as a hydroperoxide including for example hydrogen peroxide, commercially available from Fisher Scientific.
• oxidant compounds such as peroxocompounds such as a hydroperoxide including for example hydrogen peroxide, commercially available from Fisher Scientific.
• hydroperoxides include, but are not limited to, tert-butyl hydroperoxide, ethylbenzene hydroperoxide, acetyl peroxide, benzoyl peroxide, methyl ethyl ketone peroxide, cumene peroxide, and combinations thereof.
• the epoxidation of propylene may be carried out preferably using hydrogen peroxide.
• An advantage of this process is the avoidance of forming by-products and/or co-products.
• the concentration of the oxidant used in the epoxidation process is generally from about 1 wt% to about 30 wt%, preferably from about 1 wt% to about 15 wt%, and more preferably from about 1 wt% to about 7 wt%.
• the propylene epoxidation process includes for example mixing the propylene with an oxidant at a temperature of from about 0 °C to about 60 °C, preferably from about 10 °C to about 50 °C, and more preferably from about 25 °C to about 45 °C.
• the mixing step may be carried out by known methods and equipment such as a stirred batch reactor, a plug flow reactor, a continuously stirred tank reactor, a fluidized bed reactor, a loop reactor, or a tubular reactor, and the like.
• the resultant propylene oxide may be recovered from the reaction mixture. Any recovery method known in the art may be used such as decantation, extraction, evaporation, or distillation, and the like.
• the propylene oxide may be further used as an intermediate product in various processes such as for making coatings and composites.
• the process steps may include the following steps: addition of reactants, mixing the reactants in the presence of a catalyst, separation of the reactants from the catalyst, separation of propylene from the reaction mixture, and optionally, recycle of unreacted propylene and/or solvents.
• Some of the advantages of the process of the present invention includes for example, (1) no methanol is needed or used to prepare propylene oxide product; the use of no methanol facilitates separation and isolation of the desired propylene oxide product; (2) an increase in yield of propylene oxide product; the propylene oxide yield is preserved, while the losses of propylene oxide to byproducts is reduced; (3) a decrease in methanol byproducts production, thus providing a purer propylene oxide product; and (4) lower equipment cost and lower energy usage due to not having to separate out, recover and/or recycle methanol when used as a solvent in a reaction mixture.
• GC gas chromatography
• PO propylene oxide
• biphasic means two liquid phases which are present in addition to any solid or gas phases which may be present in a reaction mixture.
• GC Gas chromatography
• the amount of hydrogen peroxide is analyzed by iodometric titration using 0.01 normality (N) sodium thiosulfate.
• TS-1 catalyst (6.90 g) is stirred with MeOH (50 mL) at 25°C for 1 hour. The catalyst is vacuum filtered through a 0.45 ⁇ filter paper and air-dried in a dessicator. The resulting TS- 1 catalyst prepared this way will hereafter be referred to as the "pretreated TS- 1 catalyst".
• the reactor contents are drained equally into two 250 mL centrifuge tubes, and then centrifuged at 3000 rpm and 0 °C for 30 minutes.
• the liquid is decanted from the catalyst into a separatory funnel, where resultant organic and aqueous phases are collected separately.
• the organic and the aqueous phases are analyzed by GC and the amount of peroxide remaining is determined by titration with sodium thiosulfate.

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• 2011
  • 2011-03-16 TW TW100108896A patent/TWI523689B/zh not_active IP Right Cessation
  • 2011-03-22 WO PCT/US2011/000523 patent/WO2011119217A1/en not_active Ceased
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