WO1998029370A1 - Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts - Google Patents

Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts Download PDF

Info

Publication number
WO1998029370A1
WO1998029370A1 PCT/US1997/024125 US9724125W WO9829370A1 WO 1998029370 A1 WO1998029370 A1 WO 1998029370A1 US 9724125 W US9724125 W US 9724125W WO 9829370 A1 WO9829370 A1 WO 9829370A1
Authority
WO
WIPO (PCT)
Prior art keywords
metal
catalyst
range
preceeding
sapo
Prior art date
Application number
PCT/US1997/024125
Other languages
French (fr)
Inventor
Hsiang-Ning Sun
Original Assignee
Exxon Chemical Patents Inc.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Exxon Chemical Patents Inc. filed Critical Exxon Chemical Patents Inc.
Priority to AU57258/98A priority Critical patent/AU5725898A/en
Priority to EP97953529A priority patent/EP0960089A1/en
Publication of WO1998029370A1 publication Critical patent/WO1998029370A1/en
Priority to NO993162A priority patent/NO993162D0/en

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/32—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen
    • C07C1/321—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen the hetero-atom being a non-metal atom
    • C07C1/323—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen the hetero-atom being a non-metal atom the hetero-atom being a nitrogen atom
    • 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
    • B01J29/82—Phosphates
    • B01J29/84—Aluminophosphates containing other elements, e.g. metals, boron
    • B01J29/85—Silicoaluminophosphates [SAPO compounds]
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C07C1/207—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms from carbonyl compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/26—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only halogen atoms as hetero-atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/32—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen
    • C07C1/321—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen the hetero-atom being a non-metal atom
    • C07C1/322—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from compounds containing hetero-atoms other than or in addition to oxygen or halogen the hetero-atom being a non-metal atom the hetero-atom being a sulfur atom
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/36—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon by splitting of esters
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • B01J21/063—Titanium; Oxides or hydroxides thereof
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/12—After treatment, characterised by the effect to be obtained to alter the outside of the crystallites, e.g. selectivation
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/82—Phosphates
    • C07C2529/84—Aluminophosphates containing other elements, e.g. metals, boron
    • C07C2529/85—Silicoaluminophosphates (SAPO compounds)

Definitions

  • the invention relates to a process for converting oxygenated organic material, such as methanol and dimethyl ether, to olefins using small pore non-zeolitic catalysts comprising a metal selected from the group consisting of lanthanide metals, actinide metals, scandium, yttrium,
  • Group IVB metals Group IVB metals, and Group VB metals.
  • Light olefins such as ethylene serve as feeds for the production of numerous chemicals. Olefins traditionally are produced by petroleum cracking. Because of the limited supply and/or the high cost of petroleum sources, the cost of producing olefins from petroleum sources has increased steadily.
  • Alternative feedstocks for the production of light olefins are oxygenates, such as alcohols, particularly methanol, dimethyl ether, and ethanol.
  • Alcohols may be produced by fermentation, or from synthesis gas derived from natural gas, petroleum liquids, carbonaceous materials, including coal, recycled plastics, municipal wastes, or any organic material. Because of the wide variety of sources, alcohol, alcohol derivatives, and other oxygenates have promise as an economical, non- petroleum source for olefin production.
  • Small pore catalysts such as SAPO-34
  • SAPO-34 Small pore catalysts
  • the conversion stability has been better using medium pore molecular sieves which have been ion-exchanged with metal ions.
  • the present invention provides a method for converting an organic starting material to olefins comprising contacting a feed comprising said organic starting material with a small pore non-zeolitic catalyst at a temperature, a pressure, and a weight hourly space velocity effective to produce olefins; wherein said molecular sieve catalyst comprises at least one metal selected from the group consisting of a lanthanide metal, an actinide metal, scandium, yttrium, Group IVB metals, and Group VB metals, and combinations thereof.
  • the invention involves the conversion of oxygenates to olefins using small pore non-zeolitic molecular sieve catalysts comprising certain metals.
  • Suitable small pore non-zeolitic molecular sieve catalysts include, but are not necessarily limited to, small pore silicoaluminophosphates (SAPOs) and small pore aluminophospho oxides (ALPO's).
  • SAPOs small pore silicoaluminophosphates
  • APO's small pore aluminophospho oxides
  • suitable small pore ALPO's include, but are not necessarily limited to
  • Preferred molecular sieve catalysts are SAPOs, such as SAPO-34, SAPO 17, SAPO-18, SAPO-43, and SAPO-44, and others which may be synthesized according to US-A-4,440,871 , incorporated herein by reference, and Zeolites, Vol. 17, pp. 512-522 (1996), incorporated herein by reference. Most preferred catalysts are
  • SAPO-17, SAPO-18, and SAPO-34 are examples of SAPO-17, SAPO-18, and SAPO-34.
  • Standard pore molecular sieve catalysts are defined as catalysts with pores having a diameter or pore size of less than about 5.0 Angstroms. Suitable catalysts have a pore size ranging from about 3.5 to about 5.0 Angstroms, preferably from about 4.0 to about 5.0 Angstroms, and most preferably from about 4.3 to about 5.0 Angstroms.
  • SAPO's have a three-dimensional microporous crystal framework of PO + , AIO 2 " and SiO 2 tetrahedral units.
  • the chemical composition (anhydrous) is: mR:(Si ⁇ Al y P z )02 wherein "R” represents at least one organic templating agent present in the intracrystalline pore system: "m” represents the moles of ARE present per mole of (Si x Al y Pz)O2 and has a value of from zero to 0.3, the maximum value in each case depending upon the molecular dimensions of the templating agent and the available void volume in the pore system of the particular SAPO species involved, and "x", "y”.
  • d "z” represent the mole fractions of silicon, aluminum and phosphorus, respectively. "R” may be removed at elevated temperatures.
  • Preferred metals for incorporation into the molecular sieve catalysts are selected from the group consisting of the lanthanide series, the actinide series, scandium, yttrium, Group IVB metals, Group VB metals (referring to Group IVB and VB of the Periodic Table of the Elements, as defined by the CAS Version, inside front cover, CRC Handbook of Chemistry and Physics, 76th Ed., CRC Press, 1995-96), and combinations thereof.
  • Such metals include, but are not necessarily limited to lanthanum, actinium, cerium, praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, thorium, protactinium, uranium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, and combinations thereof.
  • the metals may be derived from various compounds, i.e. in the form of the corresponding halide, sulfate, acetate, formate, propionate, oxalate, maleate, fumarate, other carboxylate, alkoxide, carbonyl, nitrate, or mixtures thereof.
  • the desired catalyst comprises SAPO-34 and the metal is ytterbium
  • the desired catalyst comprises SAPO-34 and the metal is titanium
  • titanium tetrabutoxide as the metal containing compound.
  • the process of incorporating the metal into the non-zeolitic catalyst may be accomplished using any of the standard methods well known to those skilled in the art. Examples are the incipient wetness method, mechanical mixing, and others. Ion exchange also is a suitable method for metals having a valence of less than about three. It is very difficult, if not impossible, to use ion exchange methods to incorporate ions having valences of three or higher.
  • a solution of the desired metal is first made by dissolving a desired amount of the metal-containing compound in water under mild conditions.
  • the water is de-ionized.
  • the temperature of mixing is dependent upon the solubility of the metal compound in water, or whatever other solvent is selected. Suitable solvents are organic, inorganic, and aqueous.
  • the process may be conducted under pressure, at reduced pressure, or at atmospheric pressure.
  • the solution is added to a predetermined amount of the non-zeolitic catalyst.
  • the resulting mixture is stirred as required. In some cases, stirring is not required and the mixture may be left undisturbed for a time adequate to permit the desired level of metal incorporation.
  • the catalyst product then is filtered, optionally washed, dried, and calcined by methods well known to those skilled in the art.
  • the amount of metal incorporated into the catalyst may vary over a wide range depending, at least in part, on the selected catalyst and the incorporation method. Preferably, the amount of metal incorporated should be at least about 0.0001 wt%, more preferably in the range of from about 0.0001 wt% and about 10 wt%.
  • the conversion process employs a starting material (feedstock) preferably comprising "oxygenates".
  • oxygenates is defined to include, but is not necessarily limited to aliphatic alcohols, ethers, carbonyl compounds (aldehydes, ketones, carboxylic acids, carbonates, and the like), and also compounds containing hetero-atoms, such as, halides, mercaptans, sulfides, amines, and mixtures thereof.
  • the aliphatic moiety preferably should contain in the range of from about 1 - 10 carbon atoms and more preferably in the range of from about 1 - 4 carbon atoms.
  • Representative oxygenates include, but are not necessarily limited to, lower straight chain or branched aliphatic alcohols, their unsaturated counterparts, and their nitrogen, halogen and sulfur analogues.
  • Suitable compounds include, but are not necessarily limited to: methanol; ethanol; n-propanol; isopropanol; C4 - C10 alcohols; methyl ethyl ether; dimethyl ether; diethyl ether; di-isopropyl ether; methyl mercaptan; methyl sulfide; methyl amine; ethyl mercaptan; diethyl sulfide; diethyl amine; ethyl chloride; formaldehyde; dimethyl carbonate; dimethyl ketone; acetic acid; n-alkyl amines, n-alkyl halides, n-alkyl sulfides having n-alkyl groups of in the range of from about 3 - 10 carbon atoms; and mixtures thereof.
  • oxygenate designates only the organic material used as the feed.
  • the total charge of feed to the reaction zone may contain additional compounds such as d
  • the conversion of feed to olefins preferably should be carried out in the vapor phase.
  • the feedstock should be contacted in the vapor phase in a reaction zone with the defined molecular sieve catalyst at effective process conditions so as to produce the desired olefins, i.e., an effective temperature, pressure, WHSV (Weight Hourly Space Velocity) and, optionally, an effective amount of diluent, correlated to produce olefins.
  • the process may be carried out in a liquid phase. When the process is carried out in the liquid phase, different conversion rates and selectivities of feedstock-to-product may result depending upon the composition of the liquid.
  • the temperature employed in the conversion process may vary over a wide range depending, at least in part, on the selected catalyst. Although not limited to a particular temperature, best results will be obtained if the process is conducted at temperatures in the range of from about 200 - 700 °C, preferably in the range of from about 250 -600 °C, and most preferably in the range of from about 300 - 500 °C. Lower temperatures generally result in lower rates of reaction, and the formation of the desired light olefin products may become markedly slow. However, at higher temperatures, the process may not form an optimum amount of light olefin products, and the coking rate may become too high.
  • Light olefin products will form-although not necessarily in optimum amounts-at a wide range of pressures, including but not limited to autogeneous pressures and pressures in the range of from about 0.1 kPa to about 100 MPa,.
  • a preferred pressure is in the range of from about 6.9 kPa to about 34 Mpa, most preferably in the range of from about 48 kPa to about 0.34 MPa.
  • the foregoing pressures are exclusive of diluent, if any is present, and refer to the partial pressure of the feedstock as it relates to oxygenate compounds and/or mixtures thereof. Pressures outside of the stated ranges may operate and are not excluded from the scope of the invention.
  • WHSV weight hourly space velocity
  • the WHSV generally should be in the range of from about 0.01 hr “1 to about 500 hr “1 , preferably in the range of from about 0.1 hr “1 to about 200 hr “1 , and most preferably in the range of from about 0.5 hr " to about 100 hr “1 .
  • the catalyst may contain other materials which act as inerts, fillers, or binders; therefore, the WHSV is calculated on the weight basis of methanol or dimethyl ether and non-zeolitic catalyst.
  • the feed may contain one or more diluents in an amount in the range of from about 1 and 99 molar percent, based on the total number of moles of all feed and diluent components fed to the reaction zone (or catalyst).
  • Diluents which may be employed in the process include, but are not necessarily limited to, helium, argon, nitrogen, carbon monoxide, carbon dioxide, hydrogen, water, paraffins, other hydrocarbons (such as methane), aromatic compounds, and mixtures thereof.
  • Preferred diluents are water and nitrogen.
  • the process may be carried out in a batch, semi-continuous, or continuous fashion.
  • the process may use a single reaction zone or a number of reaction zones arranged in series or in parallel.
  • the process may be intermittent or continuous in an elongated tubular zone or a number of such zones.
  • one or more of the non-zeolitic catalysts advantageously may be used in series to provide for a desired product mixture.
  • a dynamic bed system or any system that includes a variety of transport beds rather than fixed beds, may be desirable. If regeneration of the catalyst is required, such a system would permit introduction of the catalyst as a moving bed to a regeneration zone where, e.g., carbonaceous material could be removed or oxidized. Preferably, the catalyst should be regenerated by burning off carbonaceous deposits that accumulate during the process.
  • the following examples illustrate, but do not limit, the present invention.
  • ytterbium-containing solution was prepared by dissolving 0.42g of ytterbium (III) acetate tetrahydrate in 6ml of de-ionized water at room temperature. This solution was added to 3.5 grams of SAPO-34 calcined for 16 hours at 550 °C and the mixture was allowed to stand at room
  • the control and the ytterbium-modified catalysts were tested using the following procedure. 5.0 cc (approximately 2.7 grams) of each catalyst was mixed with 15 cc of quartz beads and loaded into a 3/4 inch outer diameter 316 stainless steel tubular reactor which was heated by a three-zone electric furnace. The first zone, acting as the preheating zone, vaporized the feed. The temperature of the center zone of the furnace was adjusted to 4501 °C and the pressure was maintained at 1 atm. The reactor was purged first with nitrogen at 50 cc/min flow rate for 30 minutes. The feed, a 4:1 (molar ratio) of water and methanol, was pumped into the reactor and calibrated to give a flow rate of about 0.7 hr "1 WHSV.
  • the effluent was analyzed at pre-determined intervals by an on-line gas chromatograph fitted with both a thermal conductivity detector and a flame ionization detector. The results are shown in the following table.
  • a titanium-containing solution was prepared by dissolving 0.449 g of titanium tetrabutoxide in 5cc of cyclohexane at room temperature. This solution was added to 3.0 grams of calcined SAPO-34 and the mixture was allowed to stand at room temperature overnight. The mixture was then dried at 110 °C for 2 hours, and calcined at 6501 °C overnight, to result in titanium-SAPO-34.
  • Example V The control and the titanium-modified catalysts were tested using the following procedure. 5.0 cc (approximately 2.7 grams) of each catalyst was diluted with 15 cc of glass beads and loaded into a 3/4 inch outer diameter 316 stainless steel tubular reactor which was heated by a three-zone electric furnace. The first zone, acting as the preheating zone, vaporized the feed. The temperature of the center zone of the furnace was adjusted to give a reaction temperature of 4501 °C and the pressure was maintained at 1 atm. The reactor was purged first with nitrogen at 50 cc/min flow rate for 30 minutes.
  • the feed a 4:1 (molar ratio) of water and methanol, was pumped into the reactor and calibrated to give a flow rate of about 0.7 hr "1 WHSV calculated on the basis of methanol and catalyst only.
  • the effluent was analyzed at pre-determined intervals by an on-line gas chromatograph fitted with both a thermal conductivity detector and a flame ionization detector.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)

Abstract

The present invention provides a method for converting an organic starting material to olefins comprising contacting a feed comprising said organic starting material with a small pore non-zeolitic catalyst at a temperature, a pressure, and a weight hourly space velocity effective to produce olefins; wherein said molecular sieve catalyst comprises at least one metal selected from the group consisting of a lanthanide metal, an actinide metal, scandium, yttrium, Group IVB metals, Group VB metals, and combinations thereof.

Description

Oxygenate Conversions Using Small Pore Non-Zeolitic Molecular Sieve Catalysts
This application claims priority to U.S. Provisional Patent Application No. 60/034,054, filed December 31 , 1996.
Field of the Invention
The invention relates to a process for converting oxygenated organic material, such as methanol and dimethyl ether, to olefins using small pore non-zeolitic catalysts comprising a metal selected from the group consisting of lanthanide metals, actinide metals, scandium, yttrium,
Group IVB metals, and Group VB metals.
Background of the Invention
Light olefins, such as ethylene, serve as feeds for the production of numerous chemicals. Olefins traditionally are produced by petroleum cracking. Because of the limited supply and/or the high cost of petroleum sources, the cost of producing olefins from petroleum sources has increased steadily.
Alternative feedstocks for the production of light olefins are oxygenates, such as alcohols, particularly methanol, dimethyl ether, and ethanol. Alcohols may be produced by fermentation, or from synthesis gas derived from natural gas, petroleum liquids, carbonaceous materials, including coal, recycled plastics, municipal wastes, or any organic material. Because of the wide variety of sources, alcohol, alcohol derivatives, and other oxygenates have promise as an economical, non- petroleum source for olefin production.
Small pore catalysts, such as SAPO-34, have been used to convert methanol and dimethyl ether to olefins. However, the conversion stability has been better using medium pore molecular sieves which have been ion-exchanged with metal ions.
Small pore catalysts which will convert oxygenates to olefins with a high conversion stability are needed. SUMMARY OF THE INVENTION
The present invention provides a method for converting an organic starting material to olefins comprising contacting a feed comprising said organic starting material with a small pore non-zeolitic catalyst at a temperature, a pressure, and a weight hourly space velocity effective to produce olefins; wherein said molecular sieve catalyst comprises at least one metal selected from the group consisting of a lanthanide metal, an actinide metal, scandium, yttrium, Group IVB metals, and Group VB metals, and combinations thereof.
DETAILED DESCRIPTION OF THE INVENTION
The invention involves the conversion of oxygenates to olefins using small pore non-zeolitic molecular sieve catalysts comprising certain metals. Suitable small pore non-zeolitic molecular sieve catalysts include, but are not necessarily limited to, small pore silicoaluminophosphates (SAPOs) and small pore aluminophospho oxides (ALPO's). Examples of suitable small pore ALPO's include, but are not necessarily limited to
ALPO-20 and ALPO-25. Preferred molecular sieve catalysts are SAPOs, such as SAPO-34, SAPO 17, SAPO-18, SAPO-43, and SAPO-44, and others which may be synthesized according to US-A-4,440,871 , incorporated herein by reference, and Zeolites, Vol. 17, pp. 512-522 (1996), incorporated herein by reference. Most preferred catalysts are
SAPO-17, SAPO-18, and SAPO-34.
"Small pore" molecular sieve catalysts are defined as catalysts with pores having a diameter or pore size of less than about 5.0 Angstroms. Suitable catalysts have a pore size ranging from about 3.5 to about 5.0 Angstroms, preferably from about 4.0 to about 5.0 Angstroms, and most preferably from about 4.3 to about 5.0 Angstroms.
SAPO's have a three-dimensional microporous crystal framework of PO+, AIO2 " and SiO2 tetrahedral units. The chemical composition (anhydrous) is: mR:(SiχAlyPz)02 wherein "R" represents at least one organic templating agent present in the intracrystalline pore system: "m" represents the moles of ARE present per mole of (SixAlyPz)O2 and has a value of from zero to 0.3, the maximum value in each case depending upon the molecular dimensions of the templating agent and the available void volume in the pore system of the particular SAPO species involved, and "x", "y". ar|d "z" represent the mole fractions of silicon, aluminum and phosphorus, respectively. "R" may be removed at elevated temperatures. Preferred metals for incorporation into the molecular sieve catalysts are selected from the group consisting of the lanthanide series, the actinide series, scandium, yttrium, Group IVB metals, Group VB metals (referring to Group IVB and VB of the Periodic Table of the Elements, as defined by the CAS Version, inside front cover, CRC Handbook of Chemistry and Physics, 76th Ed., CRC Press, 1995-96), and combinations thereof. Such metals include, but are not necessarily limited to lanthanum, actinium, cerium, praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, thorium, protactinium, uranium, scandium, yttrium, titanium, zirconium, hafnium, vanadium, niobium, tantalum, and combinations thereof.
The metals may be derived from various compounds, i.e. in the form of the corresponding halide, sulfate, acetate, formate, propionate, oxalate, maleate, fumarate, other carboxylate, alkoxide, carbonyl, nitrate, or mixtures thereof. When the desired catalyst comprises SAPO-34 and the metal is ytterbium, it is preferable to use ytterbium (III) acetate tetrahydrate as the metal containing compound. When the desired catalyst comprises SAPO-34 and the metal is titanium, it is preferable to use titanium tetrabutoxide as the metal containing compound. The process of incorporating the metal into the non-zeolitic catalyst may be accomplished using any of the standard methods well known to those skilled in the art. Examples are the incipient wetness method, mechanical mixing, and others. Ion exchange also is a suitable method for metals having a valence of less than about three. It is very difficult, if not impossible, to use ion exchange methods to incorporate ions having valences of three or higher.
In one embodiment, a solution of the desired metal is first made by dissolving a desired amount of the metal-containing compound in water under mild conditions. Preferably the water is de-ionized. The temperature of mixing is dependent upon the solubility of the metal compound in water, or whatever other solvent is selected. Suitable solvents are organic, inorganic, and aqueous. The process may be conducted under pressure, at reduced pressure, or at atmospheric pressure. After adequate mixing, the solution is added to a predetermined amount of the non-zeolitic catalyst. The resulting mixture is stirred as required. In some cases, stirring is not required and the mixture may be left undisturbed for a time adequate to permit the desired level of metal incorporation. The catalyst product then is filtered, optionally washed, dried, and calcined by methods well known to those skilled in the art.
The amount of metal incorporated into the catalyst may vary over a wide range depending, at least in part, on the selected catalyst and the incorporation method. Preferably, the amount of metal incorporated should be at least about 0.0001 wt%, more preferably in the range of from about 0.0001 wt% and about 10 wt%. The conversion process employs a starting material (feedstock) preferably comprising "oxygenates". As used herein, the term "oxygenates" is defined to include, but is not necessarily limited to aliphatic alcohols, ethers, carbonyl compounds (aldehydes, ketones, carboxylic acids, carbonates, and the like), and also compounds containing hetero-atoms, such as, halides, mercaptans, sulfides, amines, and mixtures thereof. The aliphatic moiety preferably should contain in the range of from about 1 - 10 carbon atoms and more preferably in the range of from about 1 - 4 carbon atoms. Representative oxygenates include, but are not necessarily limited to, lower straight chain or branched aliphatic alcohols, their unsaturated counterparts, and their nitrogen, halogen and sulfur analogues. Examples of suitable compounds include, but are not necessarily limited to: methanol; ethanol; n-propanol; isopropanol; C4 - C10 alcohols; methyl ethyl ether; dimethyl ether; diethyl ether; di-isopropyl ether; methyl mercaptan; methyl sulfide; methyl amine; ethyl mercaptan; diethyl sulfide; diethyl amine; ethyl chloride; formaldehyde; dimethyl carbonate; dimethyl ketone; acetic acid; n-alkyl amines, n-alkyl halides, n-alkyl sulfides having n-alkyl groups of in the range of from about 3 - 10 carbon atoms; and mixtures thereof. As used herein, the term "oxygenate" designates only the organic material used as the feed. The total charge of feed to the reaction zone may contain additional compounds such as diluents.
The conversion of feed to olefins preferably should be carried out in the vapor phase. Preferably, the feedstock should be contacted in the vapor phase in a reaction zone with the defined molecular sieve catalyst at effective process conditions so as to produce the desired olefins, i.e., an effective temperature, pressure, WHSV (Weight Hourly Space Velocity) and, optionally, an effective amount of diluent, correlated to produce olefins. Alternately, the process may be carried out in a liquid phase. When the process is carried out in the liquid phase, different conversion rates and selectivities of feedstock-to-product may result depending upon the composition of the liquid.
The temperature employed in the conversion process may vary over a wide range depending, at least in part, on the selected catalyst. Although not limited to a particular temperature, best results will be obtained if the process is conducted at temperatures in the range of from about 200 - 700 °C, preferably in the range of from about 250 -600 °C, and most preferably in the range of from about 300 - 500 °C. Lower temperatures generally result in lower rates of reaction, and the formation of the desired light olefin products may become markedly slow. However, at higher temperatures, the process may not form an optimum amount of light olefin products, and the coking rate may become too high.
Light olefin products will form-although not necessarily in optimum amounts-at a wide range of pressures, including but not limited to autogeneous pressures and pressures in the range of from about 0.1 kPa to about 100 MPa,. A preferred pressure is in the range of from about 6.9 kPa to about 34 Mpa, most preferably in the range of from about 48 kPa to about 0.34 MPa. The foregoing pressures are exclusive of diluent, if any is present, and refer to the partial pressure of the feedstock as it relates to oxygenate compounds and/or mixtures thereof. Pressures outside of the stated ranges may operate and are not excluded from the scope of the invention. Lower and upper extremes of pressure may adversely affect selectivity, conversion, coking rate, and/or reaction rate; however, light olefins such as ethylene still may form. The process should be continued for a period of time sufficient to produce the desired olefin products. The reaction time may vary from tenths of seconds to a number of hours. The reaction time is largely determined by the reaction temperature, the pressure, the catalyst selected, the weight hourly space velocity, the phase (liquid or vapor), and the selected process design characteristics. A wide range of weight hourly space velocity (WHSV) for the feedstock will function in the present invention. The WHSV generally should be in the range of from about 0.01 hr"1 to about 500 hr"1, preferably in the range of from about 0.1 hr"1 to about 200 hr"1, and most preferably in the range of from about 0.5 hr" to about 100 hr"1. The catalyst may contain other materials which act as inerts, fillers, or binders; therefore, the WHSV is calculated on the weight basis of methanol or dimethyl ether and non-zeolitic catalyst.
The feed may contain one or more diluents in an amount in the range of from about 1 and 99 molar percent, based on the total number of moles of all feed and diluent components fed to the reaction zone (or catalyst). Diluents which may be employed in the process include, but are not necessarily limited to, helium, argon, nitrogen, carbon monoxide, carbon dioxide, hydrogen, water, paraffins, other hydrocarbons (such as methane), aromatic compounds, and mixtures thereof. Preferred diluents are water and nitrogen.
The process may be carried out in a batch, semi-continuous, or continuous fashion. The process may use a single reaction zone or a number of reaction zones arranged in series or in parallel. The process may be intermittent or continuous in an elongated tubular zone or a number of such zones. When multiple reaction zones are used, one or more of the non-zeolitic catalysts advantageously may be used in series to provide for a desired product mixture.
A dynamic bed system, or any system that includes a variety of transport beds rather than fixed beds, may be desirable. If regeneration of the catalyst is required, such a system would permit introduction of the catalyst as a moving bed to a regeneration zone where, e.g., carbonaceous material could be removed or oxidized. Preferably, the catalyst should be regenerated by burning off carbonaceous deposits that accumulate during the process. The following examples illustrate, but do not limit, the present invention.
Example I
A sample of SAPO-34, received from UOP, Des Plaines, Illinois, as disclosed in US-A-4,440,871 , incorporated herein by reference, was used to act as a control for each experiment.
Example II
An ytterbium-containing solution was prepared by dissolving 0.42g of ytterbium (III) acetate tetrahydrate in 6ml of de-ionized water at room temperature. This solution was added to 3.5 grams of SAPO-34 calcined for 16 hours at 550 °C and the mixture was allowed to stand at room
1 ° temperature for one hour, and then dried at 110 C for 2 hours. The resulting dried catalyst was then calcined at 5001 °C for 16 hours, to result in ytterbium-SAPO-34. Example III
The control and the ytterbium-modified catalysts were tested using the following procedure. 5.0 cc (approximately 2.7 grams) of each catalyst was mixed with 15 cc of quartz beads and loaded into a 3/4 inch outer diameter 316 stainless steel tubular reactor which was heated by a three-zone electric furnace. The first zone, acting as the preheating zone, vaporized the feed. The temperature of the center zone of the furnace was adjusted to 4501 °C and the pressure was maintained at 1 atm. The reactor was purged first with nitrogen at 50 cc/min flow rate for 30 minutes. The feed, a 4:1 (molar ratio) of water and methanol, was pumped into the reactor and calibrated to give a flow rate of about 0.7 hr"1 WHSV.
The effluent was analyzed at pre-determined intervals by an on-line gas chromatograph fitted with both a thermal conductivity detector and a flame ionization detector. The results are shown in the following table.
Figure imgf000011_0001
An increase of approximately 10% in the ethylene yield is seen using the Yb-SAPO-34 catalyst, as compared to the untreated SAPO-34 catalyst.
Example IV
A titanium-containing solution was prepared by dissolving 0.449 g of titanium tetrabutoxide in 5cc of cyclohexane at room temperature. This solution was added to 3.0 grams of calcined SAPO-34 and the mixture was allowed to stand at room temperature overnight. The mixture was then dried at 110 °C for 2 hours, and calcined at 6501 °C overnight, to result in titanium-SAPO-34.
Example V The control and the titanium-modified catalysts were tested using the following procedure. 5.0 cc (approximately 2.7 grams) of each catalyst was diluted with 15 cc of glass beads and loaded into a 3/4 inch outer diameter 316 stainless steel tubular reactor which was heated by a three-zone electric furnace. The first zone, acting as the preheating zone, vaporized the feed. The temperature of the center zone of the furnace was adjusted to give a reaction temperature of 4501 °C and the pressure was maintained at 1 atm. The reactor was purged first with nitrogen at 50 cc/min flow rate for 30 minutes. The feed, a 4:1 (molar ratio) of water and methanol, was pumped into the reactor and calibrated to give a flow rate of about 0.7 hr"1 WHSV calculated on the basis of methanol and catalyst only. The effluent was analyzed at pre-determined intervals by an on-line gas chromatograph fitted with both a thermal conductivity detector and a flame ionization detector.
The results demonstrated a reduction in methane and ethane production, as shown in the following table.
Figure imgf000012_0001
Persons of ordinary skill in the art will recognize that many modifications may be made to the present invention without departing from the spirit and scope of the present invention. The embodiments described herein are meant to be illustrative only and should not be taken as limiting the invention, which is defined in the following claims.

Claims

Claims:
1. A method for converting an organic starting material to olefins comprising: contacting a feed comprising the organic starting material with a small pore non-zeolitic molecular sieve catalyst at a temperature, a pressure, and a weight hourly space velocity effective to produce olefins; wherein the catalyst comprises a non-zeolitic framework and a metal consisting of a lanthanide metal, an actinide metal, scandium, yttrium, a Group IVB metal, a Group VB metal, or combinations thereof.
2. A catalyst for converting an organic starting material to olefins comprising a non-zeolitic framework; and at least 0.0001 wt% of a metal consisting of lanthanide metals, actinide metals, scandium, yttrium, Group IVB metals, Group VB metals, or combinations thereof.
3. The method of Claim 1 or the catalyst of Claim 2 wherein the metal consists of a lanthanide metal, an actinide metal, scandium, yttrium, or combinations thereof, and preferably consists of lanthanum, actinium, cerium praseodymium, neodymium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, thorium, protactinium, uranium, scandium, yttrium, or combinations thereof.
4. The method of Claim 1 or the catalyst of Claim 2 wherein the metal is a Group IVB metal, a Group VB metal, or combinations thereof.
5. The method or the catalyst of any of the preceeding claims wherein the catalyst is a silicoaluminophosphate catalyst, and preferably is SAPO-17, SAPO-18, SAPO-34, and SAPO-44.
6. The method or the catalyst of any of the preceeding claims wherein the catalyst comprises pores having a diameter greater than 3.5 Angstroms and less than 5.0 Angstroms.
7. The method or the catalyst of any of the preceeding claims wherein the metal is derived from a compound consisting of halides, sulfates, acetates, formates, propionates, oxalates, maleates, fumarates, carboxylates, alkoxides, carbonyls, nitrates, or mixtures thereof.
8. The method or the catalyst of any of the preceeding claims wherein the catalyst comprises at least 0.0001 wt% of the metal, and preferably comprises in the range of from 0.0001 wt% to 10 wt%.
9. The method of any of the preceeding claims wherein the temperature is in the range of from 200 ┬░C to 600 ┬░C, preferably in the range of 250┬░ to 600┬░ C, and most preferably in the range of 300┬░ to 500┬░ C.
10. The method of any of the preceeding claims wherein the organic starting material consists of a halide, a mercaptan, a sulfide, or an amine, methanol, ethanol, n-propanol, isopropanol, C4 - C10 alcohols, methyl ethyl ether, dimethyl ether, diethyl ether, di- isopropyl ether, dimethyl carbonate, carbonyl compounds, or
11. The method of any of the preceeding claims wherein the organic starting material further comprises a diluent wherein the diluent consists of water, nitrogen, hydrogen, paraffins, olefins, aromatics, or mixtures thereof, and preferably is water and/or nitrogen.
12. The method of any of the preceeding claims wherein said pressure is in the range of from 0.1 kPa to 100 Mpa, preferably in the range of from 6.9 kPa to 34 Mpa, and most preferably in the range of from 48 kPa to 0.34 MPa.
13. The method of any of the preceeding claims wherein the weight hourly space velocity is in the range of from 0.01 to about 500 hr"1, preferably in the range of 0.1 hr"1 to 200 hr"1, and most preferably in the range of 0.5 hr"1 to 100 hr"1.
PCT/US1997/024125 1996-12-31 1997-12-31 Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts WO1998029370A1 (en)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU57258/98A AU5725898A (en) 1996-12-31 1997-12-31 Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts
EP97953529A EP0960089A1 (en) 1996-12-31 1997-12-31 Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts
NO993162A NO993162D0 (en) 1996-12-31 1999-06-25 Oxygen atom formation using non-zeolite molecular sieve catalysts with small pores

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US3405496P 1996-12-31 1996-12-31
US60/034,054 1996-12-31

Publications (1)

Publication Number Publication Date
WO1998029370A1 true WO1998029370A1 (en) 1998-07-09

Family

ID=21874015

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1997/024125 WO1998029370A1 (en) 1996-12-31 1997-12-31 Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts

Country Status (6)

Country Link
EP (1) EP0960089A1 (en)
AU (1) AU5725898A (en)
NO (1) NO993162D0 (en)
TW (1) TW412510B (en)
WO (1) WO1998029370A1 (en)
ZA (1) ZA9711646B (en)

Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001064340A1 (en) * 2000-03-01 2001-09-07 Exxonmobil Chemical Patents Inc. Thorium-containing sapo molecular sieve for producing olefins
WO2003074177A2 (en) * 2002-02-28 2003-09-12 Exxonmobil Chemical Patents Inc. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
US6710218B1 (en) 1997-10-02 2004-03-23 Casale Chemicals Sa Catalytic process for the preparation of light olefins from methanol in fluidized bed reactor
US6844291B2 (en) 2002-02-28 2005-01-18 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalyst thereof, their making and use in conversion processes
US6906232B2 (en) 2002-08-09 2005-06-14 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
US6951830B2 (en) 2003-08-05 2005-10-04 Exxonmobil Chemical Patents Inc. Molecular sieve catalyst compositions, their production and use in conversion processes
US6995111B2 (en) 2002-02-28 2006-02-07 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
WO2006038949A1 (en) * 2004-07-30 2006-04-13 Exxonmobil Chemical Patents Inc. Conversion of oxygenates to olefins
US7074739B2 (en) * 2002-11-19 2006-07-11 Exxonmobil Chemical Patents Inc. Multi-component molecular sieve catalyst compositions and their use in aromatics reactions
US7119242B2 (en) 2002-03-29 2006-10-10 Exxonmobil Chemical Patents Inc. Interior surface modifications of molecular sieves with organometallic reagents and the use thereof for the conversion of oxygenates to olefins
US7199277B2 (en) * 2004-07-01 2007-04-03 Exxonmobil Chemical Patents Inc. Pretreating a catalyst containing molecular sieve and active metal oxide
US7199278B2 (en) * 2004-07-30 2007-04-03 Exxonmobil Chemical Patents Inc. Conversion of oxygenates to olefins
US7208442B2 (en) 2002-02-28 2007-04-24 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalyst thereof, their making and use in conversion processes
US7319178B2 (en) 2002-02-28 2008-01-15 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
EP2082803A1 (en) 2008-01-25 2009-07-29 Total Petrochemicals Research Feluy Process for obtaining catalyst composites comprising MeAPO and their use in conversion of organics to olefins
US7638453B2 (en) * 2004-09-08 2009-12-29 Exxonmobile Research And Engineering Company Molecular sieve containing hydrodewaxing catalysts
US7700816B2 (en) 2005-08-18 2010-04-20 Exxonmobil Chemical Patents Inc. Catalytic conversion of oxygenates to olefins
US8080700B2 (en) 2008-12-15 2011-12-20 Exxonmobil Chemical Patents Inc. System and method for reducing decomposition byproducts in a methanol to olefin reactor system
WO2015050939A1 (en) 2013-10-04 2015-04-09 Exxonmobil Research And Engineering Company Methanol conversion process
EP3140036A4 (en) * 2014-07-03 2018-04-11 SABIC Global Technologies B.V. Stable catalyst for conversion of alkyl halide to olefins
WO2018096171A1 (en) 2016-11-28 2018-05-31 Basf Se Catalyst composite comprising an alkaline earth metal containing cha zeolite and use thereof in a process for the conversion of oxygenates to olefins
CN115231591A (en) * 2021-04-22 2022-10-25 中国石油化工股份有限公司 Pure-phase small-crystal-grain SAPO-44 molecular sieve and preparation method and application thereof
CN115672394A (en) * 2022-11-02 2023-02-03 万华化学集团股份有限公司 Preparation method of Cs/Eu-AFN molecular sieve catalyst and preparation method of 1,2-di-n-propoxybenzene

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0249915A1 (en) * 1986-06-16 1987-12-23 Uop Production of light olefins

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0249915A1 (en) * 1986-06-16 1987-12-23 Uop Production of light olefins

Cited By (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6710218B1 (en) 1997-10-02 2004-03-23 Casale Chemicals Sa Catalytic process for the preparation of light olefins from methanol in fluidized bed reactor
WO2001064340A1 (en) * 2000-03-01 2001-09-07 Exxonmobil Chemical Patents Inc. Thorium-containing sapo molecular sieve for producing olefins
CN1327964C (en) * 2002-02-28 2007-07-25 埃克森美孚化学专利公司 Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
US7208442B2 (en) 2002-02-28 2007-04-24 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalyst thereof, their making and use in conversion processes
WO2003074176A3 (en) * 2002-02-28 2003-12-18 Exxonmobil Chem Patents Inc Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
WO2003074177A3 (en) * 2002-02-28 2003-12-31 Exxonmobil Chem Patents Inc Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
WO2003074175A2 (en) 2002-02-28 2003-09-12 Exxonmobil Chemical Patents Inc. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
US6844291B2 (en) 2002-02-28 2005-01-18 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalyst thereof, their making and use in conversion processes
EA007872B1 (en) * 2002-02-28 2007-02-27 Эксонмобил Кемикэл Пейтентс Инк. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
WO2003074176A2 (en) 2002-02-28 2003-09-12 Exxonmobil Chemical Patents Inc. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
US6995111B2 (en) 2002-02-28 2006-02-07 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
WO2003074177A2 (en) * 2002-02-28 2003-09-12 Exxonmobil Chemical Patents Inc. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
US7319178B2 (en) 2002-02-28 2008-01-15 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
EA007871B1 (en) * 2002-02-28 2007-02-27 Эксонмобил Кемикэл Пейтентс Инк. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
AU2003225560B2 (en) * 2002-02-28 2008-05-08 Exxonmobil Chemical Patents Inc. Catalyst compositions comprising molecular sieves, their preparation and use in conversion processes
CN1298427C (en) * 2002-02-28 2007-02-07 埃克森美孚化学专利公司 Molecular sieve compositions, catalyst thereof, their making and use in conversion processes
US7195746B2 (en) 2002-03-29 2007-03-27 Exxon Mobil Chemical Patents Inc. Interior surface modifications of molecular sieves with organometallic reagents and the use thereof for the conversion of oxygenates to olefins
US7119242B2 (en) 2002-03-29 2006-10-10 Exxonmobil Chemical Patents Inc. Interior surface modifications of molecular sieves with organometallic reagents and the use thereof for the conversion of oxygenates to olefins
US7378563B2 (en) 2002-08-09 2008-05-27 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
US6906232B2 (en) 2002-08-09 2005-06-14 Exxonmobil Chemical Patents Inc. Molecular sieve compositions, catalysts thereof, their making and use in conversion processes
US7074739B2 (en) * 2002-11-19 2006-07-11 Exxonmobil Chemical Patents Inc. Multi-component molecular sieve catalyst compositions and their use in aromatics reactions
US7276638B2 (en) 2002-11-19 2007-10-02 Exxonmobil Chemical Patents Inc. Multi-component molecular sieve catalyst compositions and their use in aromatics reactions
US6951830B2 (en) 2003-08-05 2005-10-04 Exxonmobil Chemical Patents Inc. Molecular sieve catalyst compositions, their production and use in conversion processes
US7238845B2 (en) 2003-08-05 2007-07-03 Exxonmobil Chemical Patents Inc. Molecular sieve catalyst compositions, their production and use in conversion processes
US7199277B2 (en) * 2004-07-01 2007-04-03 Exxonmobil Chemical Patents Inc. Pretreating a catalyst containing molecular sieve and active metal oxide
US7199278B2 (en) * 2004-07-30 2007-04-03 Exxonmobil Chemical Patents Inc. Conversion of oxygenates to olefins
US7166757B2 (en) 2004-07-30 2007-01-23 Exxonmobil Chemical Patents Inc. Conversion of oxygenates to olefins
WO2006038949A1 (en) * 2004-07-30 2006-04-13 Exxonmobil Chemical Patents Inc. Conversion of oxygenates to olefins
US7638453B2 (en) * 2004-09-08 2009-12-29 Exxonmobile Research And Engineering Company Molecular sieve containing hydrodewaxing catalysts
US7700816B2 (en) 2005-08-18 2010-04-20 Exxonmobil Chemical Patents Inc. Catalytic conversion of oxygenates to olefins
EP2082803A1 (en) 2008-01-25 2009-07-29 Total Petrochemicals Research Feluy Process for obtaining catalyst composites comprising MeAPO and their use in conversion of organics to olefins
US8080700B2 (en) 2008-12-15 2011-12-20 Exxonmobil Chemical Patents Inc. System and method for reducing decomposition byproducts in a methanol to olefin reactor system
WO2015050939A1 (en) 2013-10-04 2015-04-09 Exxonmobil Research And Engineering Company Methanol conversion process
EP3140036A4 (en) * 2014-07-03 2018-04-11 SABIC Global Technologies B.V. Stable catalyst for conversion of alkyl halide to olefins
WO2018096171A1 (en) 2016-11-28 2018-05-31 Basf Se Catalyst composite comprising an alkaline earth metal containing cha zeolite and use thereof in a process for the conversion of oxygenates to olefins
US11529618B2 (en) 2016-11-28 2022-12-20 Basf Se Catalyst composite comprising an alkaline earth metal containing CHA zeolite and use thereof in a process for the conversion of oxygenates to olefins
CN115231591A (en) * 2021-04-22 2022-10-25 中国石油化工股份有限公司 Pure-phase small-crystal-grain SAPO-44 molecular sieve and preparation method and application thereof
CN115231591B (en) * 2021-04-22 2023-08-04 中国石油化工股份有限公司 Pure-phase small-grain SAPO-44 molecular sieve, and preparation method and application thereof
CN115672394A (en) * 2022-11-02 2023-02-03 万华化学集团股份有限公司 Preparation method of Cs/Eu-AFN molecular sieve catalyst and preparation method of 1,2-di-n-propoxybenzene
CN115672394B (en) * 2022-11-02 2024-02-02 万华化学集团股份有限公司 Preparation method of Cs/Eu-AFN molecular sieve catalyst and preparation method of 1, 2-di-n-propoxybenzene

Also Published As

Publication number Publication date
AU5725898A (en) 1998-07-31
TW412510B (en) 2000-11-21
EP0960089A1 (en) 1999-12-01
ZA9711646B (en) 1998-12-07
NO993162L (en) 1999-06-25
NO993162D0 (en) 1999-06-25

Similar Documents

Publication Publication Date Title
EP0960089A1 (en) Oxygenate conversions using small pore non-zeolitic molecular sieve catalysts
US6051746A (en) Oxygenate conversions using modified small pore molecular sieve catalysts
US6004898A (en) Alkaline earth metal containing small pore non-zeolitic molecular sieve catalysts
EP1036051B1 (en) Modification of molecular sieve catalysts for reduced methane production during conversion of oxygenates to olefins
US5962762A (en) Use of transition metal containing small pore molecular sieve catalysts in oxygenate conversion
JP2715186B2 (en) Production method of high purity olefin
US5925800A (en) Conversion of oxygenates to hydrocarbons with monolith supported non-zeolitic molecular sieve catalysts
US5932512A (en) Fluorination of synthesized molecular sieve catalysts for increased selectivity to ethylene during conversion of oxygenates to olefins
US6051745A (en) Silicoaluminophosphate material, a method of making such improved material and the use thereof in the conversion of oxygenated hydrocarbons to olefins
US6046371A (en) Silicoaluminophosphate material, a method of making such improved material and the use thereof in the conversion of oxygenated hydrocarbons to olefins
JPH067928B2 (en) Chemical conversion method
WO2000076944A1 (en) Process for increasing the selectivity of a reaction to convert oxygenates to olefins
AU5620798A (en) Use of short contact time in oxygenate conversion
WO2003084660A2 (en) Organometallic treated molecular sieves and the use thereof for the conversion of oxygenates to olefins
WO2000063144A1 (en) An improved silicoaluminophosphate material and use thereof
WO2001062382A2 (en) Catalyst pretreatment in an oxygenate to olefins reaction system
AU726688B2 (en) Oxygenate conversions using modified small pore molecular sieve catalysts

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AL AM AT AU AZ BA BB BG BR BY CA CH CN CU CZ DE DK EE ES FI GB GE GH HU ID IL IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MD MG MK MN MW MX NO NZ PL PT RO RU SD SE SG SI SK TJ TM TR TT UA UG UZ VN YU AM AZ BY KG KZ MD RU TJ TM

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW SD SZ UG ZW AT BE CH DE DK ES FI FR GB GR IE IT LU MC NL PT

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 1997953529

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWP Wipo information: published in national office

Ref document number: 1997953529

Country of ref document: EP

WWW Wipo information: withdrawn in national office

Ref document number: 1997953529

Country of ref document: EP