WO2019095987A1 - Method for preparing paraxylene directly from synthesis gas and toluene - Google Patents
Method for preparing paraxylene directly from synthesis gas and toluene Download PDFInfo
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- WO2019095987A1 WO2019095987A1 PCT/CN2018/112425 CN2018112425W WO2019095987A1 WO 2019095987 A1 WO2019095987 A1 WO 2019095987A1 CN 2018112425 W CN2018112425 W CN 2018112425W WO 2019095987 A1 WO2019095987 A1 WO 2019095987A1
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- 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
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
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- 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
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
- B01J29/44—Noble metals
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- 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
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing iron group metals, noble metals or copper
- B01J29/46—Iron group metals or copper
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- 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
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
- B01J29/48—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively containing arsenic, antimony, bismuth, vanadium, niobium tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/03—Precipitation; Co-precipitation
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/30—Ion-exchange
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
- C07C15/02—Monocyclic hydrocarbons
- C07C15/067—C8H10 hydrocarbons
- C07C15/08—Xylenes
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- 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
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
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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
- the present invention relates to a process for the direct preparation of para-xylene from syngas and toluene.
- Para-xylene is an important basic chemical raw material, mainly used to prepare p-dibenzoic acid (PTA), and then to produce polyethylene terephthalate (PET).
- PTA p-dibenzoic acid
- PET polyethylene terephthalate
- para-xylene is mainly obtained from an aromatic hydrocarbon combination device, in which high-purity PX products are obtained from naphtha by reforming, aromatics extraction, aromatics fractionation, disproportionation and transalkylation, xylene isomerization and adsorption separation. Due to thermodynamic constraints, the proportion of p-xylene in three xylenes is less than 25%, the material circulation is large, energy consumption is high, and investment is high. The alkylation of toluene with methanol to produce p-xylene can break through thermodynamic constraints to obtain a high proportion of para-xylene, which is a promising PX production route.
- methanol is generally produced from syngas. If the syngas is reacted with toluene to produce p-xylene directly, such a method can shorten the reaction path, save energy, reduce sewage discharge and reduce fixed investment.
- WO 2004/043593 discloses a process for the selective production of para-xylene by reacting an aromatic hydrocarbon with a feed comprising carbon monoxide and hydrogen in the presence of a selectively activated catalyst, and a catalyst used in the process, said catalyst comprising an acidic silicate Base material and catalytically active metal or metal oxide.
- Chinese patent application CN104945219A discloses a process for the one-step preparation of toluene and p-xylene from benzene and synthesis gas and a catalyst used therein, the catalyst comprising a metal oxide component and a solid acid component.
- U.S. Patent No. 4,487,984 discloses the preparation of alkylaromatic compounds by reacting an aromatic compound with a synthesis gas under alkylation conditions in the presence of a bifunctional catalyst comprising copper, zinc and aluminum or chromium. Composite oxides and aluminosilicates.
- a catalyst comprising at least one of a highly dispersed metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, which are inert carrier-limited, is very suitable for directly preparing para-xylene from syngas and toluene.
- the method of directly preparing para-xylene from syngas and toluene using the catalyst can achieve high raw material conversion and para-xylene selectivity, and is environmentally friendly.
- the present invention has been completed on the basis of the above findings.
- the feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene;
- the catalyst comprises at least one of an inert carrier-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert carrier-limited high-dispersion metal oxide material
- the inert carrier is at least one of silica and alumina, and the metal oxide is present in an amount of less than or equal to 10% by mass based on the weight of the inert carrier-limited high-dispersion metal oxide material.
- the acidic molecule is selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
- the reaction zone contains a fixed bed reactor, or a plurality of fixed bed reactors in series and/or in parallel.
- the reaction conditions include: a reaction temperature of 300 to 450 ° C, a reaction pressure of 0.5 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in the synthesis gas of 1:9 to 9:1, 0.01 to 20 h - toluene weight hourly space velocity of 1, and the volume hourly space velocity of synthesis gas under the standard condition of 1000 ⁇ 20000h -1.
- the present invention provides a process for the direct preparation of para-xylene from syngas and toluene, the process comprising:
- the feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene;
- the catalyst comprises at least one of an inert carrier-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert carrier-limited high-dispersion metal oxide material
- the inert carrier is at least one of silica and alumina, and the metal oxide is present in an amount of less than or equal to 10% by mass based on the weight of the inert carrier-limited high-dispersion metal oxide material.
- the acidic molecule is selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
- the catalyst used in the process of the invention comprises at least one of an inert support-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert support is limited
- the inert carrier is at least one of silicon oxide and aluminum oxide, and the content of the metal oxide in terms of metal is less than or equal to 10% by mass, based on the high dispersion of the inert carrier.
- the weight of the metal oxide material, and wherein the acidic molecules are selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
- the metal oxide in the inert support-limited high dispersion metal oxide material is an oxide that removes at least one of aluminum and a metal other than the radioactive element.
- the metal oxide in the inert carrier-limited high-dispersion metal oxide material is an oxide of at least one of zinc, chromium, zirconium, copper, manganese, platinum, and palladium. More preferably, the metal oxide in the inert carrier-limited high-dispersion metal oxide material is an oxide of at least one of zinc, chromium, and zirconium.
- the metal oxide content of the metal oxide in the inert carrier-limited high-dispersion metal oxide material is less than or equal to 10% by weight; preferably less than or equal to 5% by weight; more preferably less than Or equal to 2% by weight, based on the weight of the inert carrier-limited high dispersion metal oxide material.
- content of metal oxide does not include the content of alumina unless otherwise specified, if alumina is present.
- the average particle size of the metal oxide in the inert carrier-limited highly dispersed metal oxide material is less than or equal to 100 nm, preferably less than or equal to 50 nm, more preferably less than or equal to 20 nm.
- the X-ray powder diffraction pattern of the inert support-limited high dispersion metal oxide material does not exhibit characteristic diffraction peaks of the metal oxide.
- the inert support limited high dispersion metal oxide material is different from conventional metal composite oxide materials known in the art.
- the former has a high metal oxide dispersion (characteristic XRD diffraction peak without metal oxide), a small metal oxide mass fraction (generally less than 10%), and a small metal oxide average particle size (generally less than 100 nm) And usually has a large specific surface area (generally greater than 400 m 2 /g).
- zirconium composite oxide material has a metal oxide mass fraction generally greater than 80%, has a significant metal oxide characteristic XRD diffraction peak, and has a specific surface area generally less than 100 m 2 /g.
- the inert carrier which is abundantly present in the highly dispersed metal oxide material of the inert carrier of the present invention can provide both a large specific surface area and stability due to the confinement effect. Acts as a metal oxide that catalyzes the active component.
- the inert carrier-limited high dispersion metal oxide material has an average particle size of less than or equal to 5 mm, preferably less than or equal to 1 mm, more preferably less than or equal to 0.5 mm, still more preferably less than or equal to 0.1 mm. Still more preferably less than or equal to 0.05 mm.
- the inert support limited high dispersion metal oxide material can be prepared by a coprecipitation-calcination process.
- the inert carrier-limited high-dispersion metal oxide material can be prepared as follows: a salt of a catalytically active metal and an aluminum salt are mixed into a mixed metal salt aqueous solution; The mixed metal salt aqueous solution is contacted with the aqueous solution of the precipitating agent to coprecipitate the metal ions in the mixed metal salt aqueous solution; aging; and the precipitate is washed, dried, and calcined.
- precipitating agents include, but are not limited to, sodium carbonate, potassium carbonate, ammonium carbonate, sodium hydrogencarbonate, potassium hydrogencarbonate, ammonium hydrogencarbonate, aqueous ammonia, sodium hydroxide, potassium hydroxide, and mixtures thereof.
- the temperature during the coprecipitation is from 0 ° C to 90 ° C
- the pH during the coprecipitation is from 7.0 to 8.5
- the aging time is not less than 1 hour
- the calcination temperature is from 300 ° C to 700 ° C.
- the inert carrier-limited high-dispersion metal oxide material is prepared by formulating a salt of an aluminum salt and a catalytically active metal to a total metal ion concentration of from 0.1 mol/L to 3.5 mol/L.
- the mixed metal salt aqueous solution is contacted with a precipitating aqueous solution having a molar concentration of 0.1 mol/L to 3.5 mol/L at a temperature of 0 ° C to 90 ° C under stirring to coprecipitate the metal salt
- the metal ions are then aged for a period of time, the pH of the solution during the coprecipitation may be 7.0 to 8.5, and the aging time is not less than 1 hour; the obtained precipitate is filtered and washed and calcined at a temperature of, for example, 300 ° C to 700 ° C.
- a highly dispersed metal oxide material having an inert carrier confinement is obtained.
- the kind of the aluminum salt and the salt of the catalytically active metal is water-soluble, for example, having a water solubility of more than 1 g/L at 25 °C.
- the aluminum salt and the salt of the catalytically active metal include, but are not limited to, hydrochloride, sulfate, and nitrate.
- the contacting can be accomplished by cocurrent, feed or reverse feed.
- the inert carrier-limited, highly dispersed metal oxide material can be prepared by a sol-gel process.
- the inert carrier-limited high-dispersion metal oxide material can be prepared as follows: an aqueous solution of a salt of a catalytically active metal is added to a silicon oxychloride together with an aqueous solution of a precipitant. In the alkyl compound, and allowing the coprecipitation and the sol-gel reaction to proceed, the obtained gel is washed, dried, and calcined to obtain an inert carrier-limited high-dispersion metal oxide material.
- the precipitating agent include, but are not limited to, one or more of ammonium carbonate, aqueous ammonia, ammonium hydrogencarbonate, ammonium dihydrogen phosphate, and urea.
- the siloxane-based compound is an alkyl orthosilicate, examples of which include, but are not limited to, methyl orthosilicate, tetraethyl orthosilicate, n-propyl orthosilicate, orthosilicate Propyl ester, n-butyl orthosilicate, isobutyl orthosilicate, tert-butyl orthosilicate, and mixtures thereof.
- the acidic molecular sieve component of the catalyst of the present invention is selected from the group consisting of modified acidic ZSM-5 molecular sieves, modified acidic ZSM-11 molecular sieves, and mixtures thereof.
- the modification of the acidic molecular sieve is one or more of phosphorus modification, boron modification, silicon modification, alkaline earth metal modification, and rare earth metal modification.
- the crystals of the acidic ZSM-5 and ZSM-11 molecular sieves are microscale or nanoscale, and the crystals contain a microporous structure or a mesoporous-microporous structure.
- the modified acidic molecular sieves are either commercially available or can be prepared by methods known per se. There is no particular limitation on the specific method of preparing the modified acidic molecular sieve.
- the modified acidic molecular sieve can be obtained by modifying a commercially available acidic ZSM-5 molecular sieve or an acidic ZSM-11 molecular sieve.
- the acidic molecular sieve may be impregnated with, for example, H 3 PO 4 , NH 4 H 2 PO 4 or an aqueous solution of (NH 4 ) 2 HPO 4 , and then the impregnated acidic molecular sieve is dried and then calcined.
- a phosphorus-modified acidic molecular sieve containing 0.5 to 10.0% by weight of phosphorus based on the weight of the modified molecular sieve is obtained.
- the acidic molecular sieve may be impregnated with, for example, an aqueous solution of H 3 BO 3 , and then the impregnated acidic molecular sieve is dried and then calcined to obtain 0.5 to 10.0% by weight based on the weight of the modified molecular sieve.
- Boron modified acidic molecular sieves of boron are examples of Boron modified acidic molecular sieves of boron.
- the silicon modified acidic molecular sieve can be prepared by treatment with a siloxane compound by liquid phase deposition and/or treatment with a silane compound by vapor deposition.
- the siloxane compound and the silane compound which can be used are respectively represented by the following structural formula:
- R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 and R 8 are each independently a C 1-10 alkyl group.
- An example of the siloxane compound is tetraethyl orthosilicate, and an example of the silane compound is tetramethylsilane.
- the liquid phase deposition process is carried out by dissolving a silicone compound in an inert organic solvent to provide a solution of the siloxane compound, then soaking or impregnating the acidic molecular sieve with the solution, drying and then calcining A silicon modified acidic molecular sieve is obtained.
- the silicon-modified acidic molecular sieve may have a silicon loading of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve, and the silicon loading does not include the original silicon in the acidic molecular sieve.
- the inert organic solvent may be any solvent which does not react with the siloxane compound and the molecular sieve, such as n-hexane, cyclohexane, n-heptane.
- the vapor deposition process is carried out by passing a silane compound gas through an acidic molecular sieve and then calcining the treated acidic molecular sieve to obtain a silicon-modified acidic molecular sieve.
- the silicon-modified acidic molecular sieve may have a silicon loading of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve. The silicon loading does not include the original silicon in the acidic molecular sieve.
- the acidic molecular sieve may be impregnated with an alkaline earth or a rare earth metal salt aqueous solution, and then the impregnated acidic molecular sieve is filtered, dried and calcined to obtain a weight of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve.
- Alkaline earth or rare earth metal modified acidic molecular sieve of alkaline earth or rare earth metal may be impregnated with an alkaline earth or a rare earth metal salt aqueous solution, and then the impregnated acidic molecular sieve is filtered, dried and calcined to obtain a weight of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve.
- Alkaline earth or rare earth metal modified acidic molecular sieve of alkaline earth or rare earth metal Alkaline earth or rare earth metal modified acidic molecular sieve of alkaline earth or rare earth metal.
- the acidic molecular sieve has an average particle size of less than or equal to 5 mm, preferably less than or equal to 0.5 mm, more preferably less than or equal to 0.1 mm, still more preferably less than or equal to 0.05 mm.
- the dispersing agent is selected from the group consisting of alumina, silica, and mixtures thereof.
- alumina, silica or alumina-silica which can be used as a dispersant, and they are commercially available from many suppliers.
- the graphite powders usable in the present invention there are no particular limitations on the graphite powders usable in the present invention, and they are commercially available from many suppliers.
- the graphite powder has an average particle size of from 0.05 to 5 microns.
- the catalyst used in the process of the invention may be prepared by a process comprising the following steps:
- the catalyst of the present invention comprises from 10 to 90% by weight of an inert carrier-limited, highly dispersed metal oxide material.
- the lower limit of the content of the highly dispersed metal oxide material limited by the inert carrier may be 12, 15, 18, 20, 22, 25, 28, 30, 32, 35, 38, 40, 42, 45, 48, or 50 weight. %, and the upper limit may be 88, 85, 82, 80, 78, 75, 72, 70, 68, 65, 62, 60, 58, 55, 52 or 50% by weight, based on the weight of the catalyst.
- the catalyst of the present invention comprises from 10 to 90% by weight of an acidic molecular sieve.
- the lower limit of the content of the acidic molecular sieve may be 12, 15, 18, 20, 22, 25, 28, 30, 32, 35, 38, 40, 42, 45, 48, or 50% by weight, and the upper limit may be 88, 85. , 82, 80, 78, 75, 72, 70, 68, 65, 62, 60, 58, 55, 52, or 50% by weight, based on the weight of the catalyst.
- the catalyst of the present invention comprises 0 to 10% by weight, such as 0 to 8% by weight, 0 to 7% by weight, 0 to 6% by weight, or 0 to 5% by weight, based on the weight of the catalyst. meter.
- the catalyst of the present invention comprises 0 to 40% by weight, such as 0 to 38% by weight, 0 to 35% by weight, 0 to 30% by weight, or 0 to 25% by weight, based on the weight of the catalyst. meter.
- the catalyst of the present invention comprises 10 to 90% by weight of an inert carrier-limited high-dispersion metal oxide material, 10 to 90% by weight of an acidic molecular sieve, 0 to 10% by weight of graphite powder, and 0 to 40% by weight of the dispersant, wherein the total content of the inert carrier-limited high-dispersion metal oxide material and the acidic molecular sieve is from 60 to 100% by weight, based on the total weight of the catalyst.
- the catalyst of the present invention comprises 20 to 80% by weight of an inert carrier-limited high-dispersion metal oxide material, 20 to 80% by weight of an acidic molecular sieve, 0 to 5% by weight of graphite powder, and 0 to 30% by weight of a dispersant, the weight percentage being based on the total weight of the catalyst.
- the particle shape of the catalyst may be spherical, strip, cylindrical, semi-cylindrical, prismatic, clover, ring, pellet, regular or irregular grain or sheet.
- the feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene.
- syngas is used as one of the raw materials.
- synthetic gas refers to a mixture of hydrogen and carbon monoxide.
- the molar ratio of hydrogen to carbon monoxide in the syngas feed may be from 1:9 to 9:1, preferably from 1:9 to 1:1.
- toluene is also used as one of the raw materials.
- the reaction zone may be one or more fixed bed reactors.
- the fixed bed reactor can be operated in a continuous mode.
- the plurality of reactors can be in series, parallel, or a combination of series and parallel.
- the reaction conditions include: a reaction temperature of 300 to 450 ° C, a reaction pressure of 0.5 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in a synthesis gas of 1:9 to 9:1, 0.01 to 20 h. -1 toluene weight hourly space velocity, and syngas volume hourly space velocity in a standard state of 1000 to 20000 h -1 .
- the reaction conditions include: a reaction temperature of 320 to 400 ° C, a molar ratio of hydrogen to carbon monoxide in a synthesis gas of 1:9 to 1:1, a reaction pressure of 5.0 to 10.0 MPa, 0.5 to toluene weight hourly space velocity of 3h -1, and 1000 ⁇ 4000h -1 standard state of the volume hourly space velocity of the synthesis gas.
- the oxygen atoms in the CO mainly enter the CO 2 , so the wastewater generated during the reaction process is small.
- the separation of the para-xylene product from the reaction effluent comprising para-xylene may be carried out in a manner known per se.
- the beneficial effects of the invention include: compared with the method for alkylating toluene with methanol to produce para-xylene, the method of the invention has long catalyst life, less waste water, low raw material cost, wide source of raw materials, and energy consumption. Low advantage.
- the inert carrier-limited high-dispersion metal oxide material used in the method of the invention has a large surface area, high catalytic activity, relatively expensive active metal oxide component content, and is prepared. The process has less heavy metal ion emissions and is easier to form into an industrial catalyst.
- Figure 1 shows an XRD pattern of material A in Example 1.
- Figure 2 shows an XRD pattern of material REF-1 in Comparative Example 1.
- automatic gas composition analysis was performed using two Agilent 7890 gas chromatographs with a gas autosampler, a TCD detector coupled to a TDX-1 packed column, and an FID detector coupled to an FFAP and PLOT-Q capillary column.
- Carbon monoxide conversion [( moles of carbon monoxide carbon in the feed) - (moles of carbon monoxide in the discharge)] ⁇ (moles of carbon monoxide in the feed) ⁇ 100%
- Toluene conversion [(mole toluene in feed) - (moles of toluene in the discharge)] ⁇ (moles of toluene in the feed) ⁇ 100%
- Xylene selectivity (mole carbon number in the discharge) ⁇ (carbon moles of all hydrocarbon products in the discharge - carbon moles of raw material toluene) ⁇ 100%
- Paraxylene ratio (p-xylene carbon moles in the discharge) ⁇ (carbon moles of all xylene in the discharge) ⁇ 100%
- a mixed nitrate aqueous solution containing 0.2 mol/L Zn 2+ and 0.2 mol/L Cr 3+ was prepared to prepare 100 mL of a 1.0 mol/L urea aqueous solution.
- the above two solutions were added dropwise to 1 mol of ethyl orthosilicate, and reacted at room temperature for 24 hours to obtain a gel.
- the gel was washed with deionized water, dried at 100 ° C, and calcined at 500 ° C for 4 h to obtain a highly dispersed zinc chromium oxide material having a silica as an inert carrier, numbered E.
- E contains 1.8% by mass of zinc and 1.5% by mass of chromium.
- a mixed nitrate aqueous solution containing 0.2 mol/L Zn 2+ and 0.2 mol/L Zr 4+ was prepared to prepare 100 mL of a 1.0 mol/L urea aqueous solution.
- the above two solutions were added dropwise to 1 mol of ethyl orthosilicate, and reacted at room temperature for 24 hours to obtain a gel.
- the gel was washed with deionized water, dried at 100 ° C, and calcined at 500 ° C for 4 h to obtain a highly dispersed zinc zirconium oxide material having a silica as an inert carrier confinement, numbered F.
- F contains 1.8% by mass of zinc and 2.5% by mass of zirconium.
- the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of (NH 4 ) 2 HPO 4 (the content of P in the aqueous solution was 5% by mass), and dried. Then, it was calcined at 550 ° C for 4 hours in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 4% by mass of P, and numbered G.
- the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of H 3 BO 3 (the content of B in the aqueous solution was 10% by mass), dried, and then Calcination at 550 ° C for 4 h in an air atmosphere gave an acidic ZSM-5 molecular sieve containing 8 mass% B, numbered H.
- the ammonium type ZSM-11 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of H 3 BO 3 (the content of B in the aqueous solution was 10% by mass), dried, and then Calcination at 550 ° C for 4 h in an air atmosphere gave an acidic ZSM-11 molecular sieve containing 8 mass % B, numbered I.
- the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 hours in an air atmosphere, and then treated with a cyclohexane solution of tetraethyl orthosilicate (the content of Si in the solution was 10% by mass) at 50 ° C for 4 hours.
- reaction mixture was evaporated to dryness, and then calcined at 550 ° C for 4 hr in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 8% by mass of Si (excluding the original Si of the molecular sieve), No. J.
- 500 g of the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then treated with 1 L/min of nitrogen to carry 5% by volume of tetramethylsilane at 200 ° C for 3 hours, and then calcined at 550 ° C in an air atmosphere.
- an acidic ZSM-5 molecular sieve containing 2% by mass of Si (excluding the original Si of the molecular sieve) was obtained, numbered K.
- the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then impregnated at room temperature with an aqueous solution of magnesium nitrate and cerium nitrate (contents of Mg and Ce in the aqueous solution were respectively 5% by mass and 1.3% by mass). After 24 hours, after drying, it was calcined at 550 ° C for 4 h in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 4% by mass of Mg and 1% by mass of Ce, numbered L.
- reaction temperature (T) 400 ° C
- reaction pressure (P) 7.0 MPa
- GHSV gas volumetric space velocity
- WHSV tonnage mass space velocity
- Example 25 was repeated, but the catalyst M in Example 25 was replaced with the catalyst N-R.
- the reaction results are shown in Table 2.
- Example 25 was repeated, but the catalyst M in Example 25 was replaced with the catalyst REF-2.
- the reaction results are shown in Table 2.
- Catalyst S 5g was placed in a stainless steel reaction tube having an inner diameter of 8 mm, and activated with 50 ml/min of hydrogen at 300 ° C for 4 h.
- the product was analyzed by gas chromatography, and the reaction results are shown in Table 3.
- reaction temperature (T) 400 ° C
- reaction pressure (P) 4.0 MPa
- GHSV syngas volume space velocity
- V(H 2 )% 40%
- WHSV toluene mass space velocity
- Example 25 The catalyst deactivated in Example 25 was treated at 550 ° C for 10 h with a mixture of 2 vol% oxygen and 98 vol% nitrogen to regenerate the catalyst for one round. The reaction was then carried out under the conditions of Example 25. A total of five rounds were regenerated in the same way. The catalytic activity data after 500 h of each reaction was selected for comparison. The results are shown in Table 4.
- Example 31 The catalyst deactivated in Example 31 was treated at 550 ° C for 10 h with a mixed gas consisting of 2 vol% oxygen and 98 vol% nitrogen to regenerate the catalyst for one round. Then, the reaction was carried out under the conditions of Example 31. A total of five rounds were regenerated in the same way. The catalytic activity data after 500 h of each reaction was selected for comparison. The results are shown in Table 5.
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Abstract
Disclosed is a method for preparing paraxylene directly from a synthesis gas and toluene. The method comprises: allowing a raw material comprising a synthesis gas and toluene to come into contact with a catalyst in a reaction area in reaction conditions sufficient for converting at least a portion of the raw material so as to produce a reaction effluent comprising paraxylene; separating paraxylene from the reaction effluent, where the catalyst comprises an inert carrier-confined highly dispersed metal oxide material, an acidic zeolite, and optionally at least one of graphite powder and a dispersant, and in the inert carrier-confined highly dispersed metal oxide material, the inert carrier is at least one of silicon oxide and aluminum oxide, the content of the metal oxide in terms of the metal is less than or equal to 10 mass%, calculated on the basis of the weight of the inert carrier-confined highly dispersed metal oxide material, and, the acidic zeolite is selected from a modified acidic ZSM-5 zeolite, a modified acidic ZSM-11 zeolite, and a mixture of them.
Description
本发明涉及一种由合成气与甲苯直接制取对二甲苯的方法。The present invention relates to a process for the direct preparation of para-xylene from syngas and toluene.
对二甲苯(PX)是重要的基本化工原料,主要用来制备对二苯甲酸(PTA),进而生产聚对苯二甲酸乙二醇酯(PET)。目前,对二甲苯主要由芳烃联合装置得到,其中由石脑油通过重整、芳烃抽提、芳烃分馏、歧化和烷基转移,二甲苯异构化以及吸附分离得到高纯度PX产品。因热力学限制,对二甲苯在三个二甲苯中比例不到25%,物料循环处理量大,能耗高,投资高。利用甲醇对甲苯进行烷基化制对二甲苯能够突破热力学限制得到高比例的对二甲苯,是一个有前景的PX生产路线。Para-xylene (PX) is an important basic chemical raw material, mainly used to prepare p-dibenzoic acid (PTA), and then to produce polyethylene terephthalate (PET). At present, para-xylene is mainly obtained from an aromatic hydrocarbon combination device, in which high-purity PX products are obtained from naphtha by reforming, aromatics extraction, aromatics fractionation, disproportionation and transalkylation, xylene isomerization and adsorption separation. Due to thermodynamic constraints, the proportion of p-xylene in three xylenes is less than 25%, the material circulation is large, energy consumption is high, and investment is high. The alkylation of toluene with methanol to produce p-xylene can break through thermodynamic constraints to obtain a high proportion of para-xylene, which is a promising PX production route.
众所周知,甲醇一般以合成气为原料进行生产。如果利用合成气与甲苯反应直接制取对二甲苯,这样的方法可以缩短反应路径、节约能耗、减少污水排放以及降低固定投资。It is well known that methanol is generally produced from syngas. If the syngas is reacted with toluene to produce p-xylene directly, such a method can shorten the reaction path, save energy, reduce sewage discharge and reduce fixed investment.
WO2004/043593公开了通过使芳烃与包含一氧化碳和氢气的进料在选择性活化的催化剂存在下反应来选择性生产对二甲苯的方法以及该方法中使用的催化剂,所述催化剂包含酸性硅酸盐基材料和有催化活性的金属或金属氧化物。WO 2004/043593 discloses a process for the selective production of para-xylene by reacting an aromatic hydrocarbon with a feed comprising carbon monoxide and hydrogen in the presence of a selectively activated catalyst, and a catalyst used in the process, said catalyst comprising an acidic silicate Base material and catalytically active metal or metal oxide.
中国专利申请CN104945219A公开了苯与合成气一步制备甲苯和对二甲苯的方法及其中使用的催化剂,所述催化剂包含金属氧化物组分和固体酸组分。Chinese patent application CN104945219A discloses a process for the one-step preparation of toluene and p-xylene from benzene and synthesis gas and a catalyst used therein, the catalyst comprising a metal oxide component and a solid acid component.
美国专利号4,487,984公开了通过使芳族化合物与合成气在烷基化条件下在双功能催化剂存在下反应制备烷基芳族化合物的方法,所述双功能催化剂包含铜、锌和铝或铬的复合氧化物和硅铝酸盐。U.S. Patent No. 4,487,984 discloses the preparation of alkylaromatic compounds by reacting an aromatic compound with a synthesis gas under alkylation conditions in the presence of a bifunctional catalyst comprising copper, zinc and aluminum or chromium. Composite oxides and aluminosilicates.
仍然需要开发新的合成气与甲苯直接制取对二甲苯的方法,该方法可 以实现高的原料转化率和对二甲苯选择性,并且是环境友好的。There is still a need to develop a new process for the direct production of para-xylene from toluene with toluene which achieves high feedstock conversion and para-xylene selectivity and is environmentally friendly.
发明内容Summary of the invention
为了克服现有技术中存在的问题,本发明人进行了勤勉的研究。结果发现,一种包含惰性载体限域的高分散金属氧化物材料、酸性分子筛、和任选的石墨粉和分散剂中至少之一的催化剂非常适合由合成气和甲苯直接制备对二甲苯的方法,使用所述催化剂的、由合成气和甲苯直接制备对二甲苯的方法可以实现高的原料转化率和对二甲苯选择性,并且是环境友好的。在上述发现基础上完成了本发明。In order to overcome the problems existing in the prior art, the inventors conducted diligent research. As a result, it has been found that a catalyst comprising at least one of a highly dispersed metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, which are inert carrier-limited, is very suitable for directly preparing para-xylene from syngas and toluene. The method of directly preparing para-xylene from syngas and toluene using the catalyst can achieve high raw material conversion and para-xylene selectivity, and is environmentally friendly. The present invention has been completed on the basis of the above findings.
因此,本发明的一个目的是提供一种由合成气和甲苯直接制备对二甲苯的方法,该方法包括:Accordingly, it is an object of the present invention to provide a process for the direct preparation of para-xylene from syngas and toluene, the process comprising:
使包含合成气和甲苯的原料与催化剂在反应区中在足以转化至少部分原料的反应条件下接触,以得到包含对二甲苯的反应流出物;和The feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene;
从所述反应流出物中分离对二甲苯,Separating para-xylene from the reaction effluent,
其中所述催化剂包含惰性载体限域的高分散金属氧化物材料、酸性分子筛、和任选的石墨粉和分散剂中至少之一,其中在所述惰性载体限域的高分散金属氧化物材料中,惰性载体为氧化硅和氧化铝中至少之一,并且所述金属氧化物以金属计的含量低于或等于10质量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计,和其中所述酸性分子筛选自经过改性的酸性ZSM-5分子筛、经过改性的酸性ZSM-11分子筛和它们的混合物。Wherein the catalyst comprises at least one of an inert carrier-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert carrier-limited high-dispersion metal oxide material The inert carrier is at least one of silica and alumina, and the metal oxide is present in an amount of less than or equal to 10% by mass based on the weight of the inert carrier-limited high-dispersion metal oxide material. And wherein the acidic molecule is selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
在一个实施方案中,所述反应区含有一个固定床反应器,或串联和/或并联的多个固定床反应器。In one embodiment, the reaction zone contains a fixed bed reactor, or a plurality of fixed bed reactors in series and/or in parallel.
在一个实施方案中,所述反应条件包括:300~450℃的反应温度,0.5~10.0MPa的反应压力,1:9~9:1的合成气中氢气与一氧化碳的摩尔比,0.01~20h
-1的甲苯重时空速,和1000~20000h
-1的标准状态下合成气体积小时空速。
In one embodiment, the reaction conditions include: a reaction temperature of 300 to 450 ° C, a reaction pressure of 0.5 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in the synthesis gas of 1:9 to 9:1, 0.01 to 20 h - toluene weight hourly space velocity of 1, and the volume hourly space velocity of synthesis gas under the standard condition of 1000 ~ 20000h -1.
优选实施方案的描述Description of the preferred embodiment
在第一方面,本发明提供了一种由合成气和甲苯直接制备对二甲苯的 方法,该方法包括:In a first aspect, the present invention provides a process for the direct preparation of para-xylene from syngas and toluene, the process comprising:
使包含合成气和甲苯的原料与催化剂在反应区中在足以转化至少部分原料的反应条件下接触,以得到包含对二甲苯的反应流出物;和The feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene;
从所述反应流出物中分离对二甲苯,Separating para-xylene from the reaction effluent,
其中所述催化剂包含惰性载体限域的高分散金属氧化物材料、酸性分子筛、和任选的石墨粉和分散剂中至少之一,其中在所述惰性载体限域的高分散金属氧化物材料中,惰性载体为氧化硅和氧化铝中至少之一,并且所述金属氧化物以金属计的含量低于或等于10质量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计,和其中所述酸性分子筛选自经过改性的酸性ZSM-5分子筛、经过改性的酸性ZSM-11分子筛和它们的混合物。Wherein the catalyst comprises at least one of an inert carrier-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert carrier-limited high-dispersion metal oxide material The inert carrier is at least one of silica and alumina, and the metal oxide is present in an amount of less than or equal to 10% by mass based on the weight of the inert carrier-limited high-dispersion metal oxide material. And wherein the acidic molecule is selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
用于对二甲苯生产的催化剂Catalyst for p-xylene production
如上所述,本发明方法中使用的催化剂包含惰性载体限域的高分散金属氧化物材料、酸性分子筛、和任选的石墨粉和分散剂中至少之一,其中在所述惰性载体限域的高分散金属氧化物材料中,惰性载体为氧化硅和氧化铝中至少之一,并且所述金属氧化物以金属计的含量低于或等于10质量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计,和其中所述酸性分子筛选自经过改性的酸性ZSM-5分子筛、经过改性的酸性ZSM-11分子筛和它们的混合物。As stated above, the catalyst used in the process of the invention comprises at least one of an inert support-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert support is limited In the highly dispersed metal oxide material, the inert carrier is at least one of silicon oxide and aluminum oxide, and the content of the metal oxide in terms of metal is less than or equal to 10% by mass, based on the high dispersion of the inert carrier. The weight of the metal oxide material, and wherein the acidic molecules are selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
在一个实施方案中,所述惰性载体限域的高分散金属氧化物材料中的金属氧化物是除去铝和放射性元素外的金属中至少一种的氧化物。优选地,所述惰性载体限域的高分散金属氧化物材料中的金属氧化物为锌、铬、锆、铜、锰、铂和钯中的至少一种的氧化物。更优选地,所述惰性载体限域的高分散金属氧化物材料中的金属氧化物为锌、铬、锆中的至少一种的氧化物。In one embodiment, the metal oxide in the inert support-limited high dispersion metal oxide material is an oxide that removes at least one of aluminum and a metal other than the radioactive element. Preferably, the metal oxide in the inert carrier-limited high-dispersion metal oxide material is an oxide of at least one of zinc, chromium, zirconium, copper, manganese, platinum, and palladium. More preferably, the metal oxide in the inert carrier-limited high-dispersion metal oxide material is an oxide of at least one of zinc, chromium, and zirconium.
在一个实施方案中,所述惰性载体限域的高分散金属氧化物材料中金属氧化物的以金属计的含量低于或等于10重量%;优选低于或等于5重量%;更优选低于或等于2重量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计。除非另外指明,本文中使用的术语“金属氧化物的 含量”不包括氧化铝的含量,如果存在氧化铝的话。In one embodiment, the metal oxide content of the metal oxide in the inert carrier-limited high-dispersion metal oxide material is less than or equal to 10% by weight; preferably less than or equal to 5% by weight; more preferably less than Or equal to 2% by weight, based on the weight of the inert carrier-limited high dispersion metal oxide material. The term "content of metal oxide" as used herein does not include the content of alumina unless otherwise specified, if alumina is present.
在一个实施方案中,所述惰性载体限域的高分散金属氧化物材料中金属氧化物的平均颗粒尺度小于或等于100nm,优选小于或等于50nm,更优选小于或等于20nm。In one embodiment, the average particle size of the metal oxide in the inert carrier-limited highly dispersed metal oxide material is less than or equal to 100 nm, preferably less than or equal to 50 nm, more preferably less than or equal to 20 nm.
在一个优选的实施方案中,所述惰性载体限域的高分散金属氧化物材料的X射线粉末衍射图不显示所述金属氧化物的特征衍射峰。In a preferred embodiment, the X-ray powder diffraction pattern of the inert support-limited high dispersion metal oxide material does not exhibit characteristic diffraction peaks of the metal oxide.
所述惰性载体限域的高分散金属氧化物材料与本领域已知的常规金属复合氧化物材料不同。例如,前者具有高的金属氧化物分散度(无金属氧化物的特征XRD衍射峰)、小的金属氧化物质量分数(一般小于10%)和小的金属氧化物平均颗粒尺寸(一般小于100nm),并且通常具有大的比表面积(一般大于400m
2/g)。常规复合金属氧化物材料如本领域已知的、用于低温甲醇合成的铜锌铝复合氧化物材料(CuZnAlO
x)、用于高温甲醇合成的锌铬铝复合氧化物材料(ZnCrAlO
x)以及锌锆复合氧化物材料(ZnZrO
x)具有一般大于80%的金属氧化物质量分数,具有显著的金属氧化物特征XRD衍射峰,并且具有一般低于100m
2/g的比表面积。
The inert support limited high dispersion metal oxide material is different from conventional metal composite oxide materials known in the art. For example, the former has a high metal oxide dispersion (characteristic XRD diffraction peak without metal oxide), a small metal oxide mass fraction (generally less than 10%), and a small metal oxide average particle size (generally less than 100 nm) And usually has a large specific surface area (generally greater than 400 m 2 /g). Conventional composite metal oxide materials such as copper zinc aluminum composite oxide material (CuZnAlO x ) for low temperature methanol synthesis, zinc chromium aluminum composite oxide material (ZnCrAlO x ) for high temperature methanol synthesis, and zinc known in the art The zirconium composite oxide material (ZnZrO x ) has a metal oxide mass fraction generally greater than 80%, has a significant metal oxide characteristic XRD diffraction peak, and has a specific surface area generally less than 100 m 2 /g.
不希望局限于任何特定的理论,据信在本发明的惰性载体限域的高分散金属氧化物材料中大量存在的惰性载体既能提供大的比表面积,又能因限域效应起到稳定用作催化活性组分的金属氧化物的作用。Without wishing to be bound by any particular theory, it is believed that the inert carrier which is abundantly present in the highly dispersed metal oxide material of the inert carrier of the present invention can provide both a large specific surface area and stability due to the confinement effect. Acts as a metal oxide that catalyzes the active component.
在一个实施方案中,所述惰性载体限域的高分散金属氧化物材料的平均粒径小于或等于5mm,优选小于或等于1mm,更优选小于或等于0.5mm,仍更优选小于或等于0.1mm,仍更优选小于或等于0.05mm。In one embodiment, the inert carrier-limited high dispersion metal oxide material has an average particle size of less than or equal to 5 mm, preferably less than or equal to 1 mm, more preferably less than or equal to 0.5 mm, still more preferably less than or equal to 0.1 mm. Still more preferably less than or equal to 0.05 mm.
在一些实施方案中,所述惰性载体限域的高分散金属氧化物材料可以通过共沉淀-煅烧方法制备。例如,在使用氧化铝作为载体的情况下,所述惰性载体限域的高分散金属氧化物材料可以如下所述制备:将催化活性金属的盐与铝盐配成混合金属盐水溶液;使所述混合金属盐水溶液和沉淀剂水溶液接触,以使所述混合金属盐水溶液中的金属离子共沉淀;老化;和将沉淀物洗涤、干燥后煅烧。所述的沉淀剂的实例包括但不限于碳酸钠、碳酸钾、碳酸铵、碳酸氢钠、碳酸氢钾、碳酸氢铵、氨水、氢氧化钠、氢氧化钾和它们的混合物。In some embodiments, the inert support limited high dispersion metal oxide material can be prepared by a coprecipitation-calcination process. For example, in the case of using alumina as a carrier, the inert carrier-limited high-dispersion metal oxide material can be prepared as follows: a salt of a catalytically active metal and an aluminum salt are mixed into a mixed metal salt aqueous solution; The mixed metal salt aqueous solution is contacted with the aqueous solution of the precipitating agent to coprecipitate the metal ions in the mixed metal salt aqueous solution; aging; and the precipitate is washed, dried, and calcined. Examples of such precipitating agents include, but are not limited to, sodium carbonate, potassium carbonate, ammonium carbonate, sodium hydrogencarbonate, potassium hydrogencarbonate, ammonium hydrogencarbonate, aqueous ammonia, sodium hydroxide, potassium hydroxide, and mixtures thereof.
在一个实施方案中,所述共沉淀过程中温度为0℃至90℃,共沉淀过 程中pH值为7.0至8.5,老化时间不低于1小时,煅烧温度为300℃至700℃。In one embodiment, the temperature during the coprecipitation is from 0 ° C to 90 ° C, the pH during the coprecipitation is from 7.0 to 8.5, the aging time is not less than 1 hour, and the calcination temperature is from 300 ° C to 700 ° C.
在一个具体的实施方案中,所述惰性载体限域的高分散金属氧化物材料如下制备:将铝盐和催化活性金属的盐配成总金属离子浓度为0.1mol/L至3.5mol/L的混合金属盐水溶液;然后使所述混合金属盐水溶液与摩尔浓度为0.1mol/L至3.5mol/L的沉淀剂水溶液在0℃至90℃的温度下在搅拌下接触以共沉淀金属盐中的金属离子并且然后老化一段时间,共沉淀过程中溶液pH值可以为7.0至8.5,老化时间不低于1小时;将所得到的沉淀物过滤和洗涤后在例如300℃至700℃的温度下煅烧,制得惰性载体限域的高分散金属氧化物材料。In a specific embodiment, the inert carrier-limited high-dispersion metal oxide material is prepared by formulating a salt of an aluminum salt and a catalytically active metal to a total metal ion concentration of from 0.1 mol/L to 3.5 mol/L. Mixing a metal salt aqueous solution; then, the mixed metal salt aqueous solution is contacted with a precipitating aqueous solution having a molar concentration of 0.1 mol/L to 3.5 mol/L at a temperature of 0 ° C to 90 ° C under stirring to coprecipitate the metal salt The metal ions are then aged for a period of time, the pH of the solution during the coprecipitation may be 7.0 to 8.5, and the aging time is not less than 1 hour; the obtained precipitate is filtered and washed and calcined at a temperature of, for example, 300 ° C to 700 ° C. A highly dispersed metal oxide material having an inert carrier confinement is obtained.
对所述铝盐和所述催化活性金属的盐的种类没有特殊的限制,只要它们是水溶性的,例如在25℃下具有大于1g/L的水溶解度。所述铝盐和所述催化活性金属的盐的实例包括但不限于盐酸盐、硫酸盐和硝酸盐。There is no particular restriction on the kind of the aluminum salt and the salt of the catalytically active metal as long as they are water-soluble, for example, having a water solubility of more than 1 g/L at 25 °C. Examples of the aluminum salt and the salt of the catalytically active metal include, but are not limited to, hydrochloride, sulfate, and nitrate.
对所述混合金属盐水溶液与所述沉淀剂水溶液的接触方式没有特殊的限制。在一个具体的实施方案中,所述接触可以采取并流加料、正加料或反加料的方式完成。There is no particular limitation on the manner in which the mixed metal salt aqueous solution is contacted with the aqueous precipitant solution. In a particular embodiment, the contacting can be accomplished by cocurrent, feed or reverse feed.
在另外一些实施方案中,所述惰性载体限域的高分散金属氧化物材料可以通过溶胶-凝胶方法制备。例如,在使用至少二氧化硅作为载体的情况下,所述惰性载体限域的高分散金属氧化物材料可以如下所述制备:将催化活性金属的盐的水溶液与沉淀剂水溶液一起加入到硅氧烷基化合物中,并允许共沉淀和溶胶凝胶反应进行,然后将所得到的凝胶洗涤、干燥后煅烧,制得惰性载体限域的高分散金属氧化物材料。所述的沉淀剂的实例包括但不限于碳酸铵、氨水、碳酸氢铵、碳酸二氢铵、尿素中的一种或多种。In other embodiments, the inert carrier-limited, highly dispersed metal oxide material can be prepared by a sol-gel process. For example, in the case of using at least silica as a carrier, the inert carrier-limited high-dispersion metal oxide material can be prepared as follows: an aqueous solution of a salt of a catalytically active metal is added to a silicon oxychloride together with an aqueous solution of a precipitant. In the alkyl compound, and allowing the coprecipitation and the sol-gel reaction to proceed, the obtained gel is washed, dried, and calcined to obtain an inert carrier-limited high-dispersion metal oxide material. Examples of the precipitating agent include, but are not limited to, one or more of ammonium carbonate, aqueous ammonia, ammonium hydrogencarbonate, ammonium dihydrogen phosphate, and urea.
在一个实施方案中,所述硅氧烷基化合物为正硅酸烷基酯,其实例包括但不限于正硅酸甲酯、正硅酸乙酯、正硅酸正丙酯、正硅酸异丙酯、正硅酸正丁酯、正硅酸异丁酯、正硅酸叔丁酯和它们的混合物。In one embodiment, the siloxane-based compound is an alkyl orthosilicate, examples of which include, but are not limited to, methyl orthosilicate, tetraethyl orthosilicate, n-propyl orthosilicate, orthosilicate Propyl ester, n-butyl orthosilicate, isobutyl orthosilicate, tert-butyl orthosilicate, and mixtures thereof.
本发明催化剂中的酸性分子筛组分选自经过改性的酸性ZSM-5分子筛、经过改性的酸性ZSM-11分子筛和它们的混合物。The acidic molecular sieve component of the catalyst of the present invention is selected from the group consisting of modified acidic ZSM-5 molecular sieves, modified acidic ZSM-11 molecular sieves, and mixtures thereof.
在一些实施方案中,酸性分子筛的改性是磷改性、硼改性、硅改性、碱土金属改性和稀土金属改性中的一种或多种。In some embodiments, the modification of the acidic molecular sieve is one or more of phosphorus modification, boron modification, silicon modification, alkaline earth metal modification, and rare earth metal modification.
在一些实施方案中,所述酸性ZSM-5和ZSM-11分子筛中硅和铝的原 子比为Si/Al=3~200,优选Si/Al=100~150。In some embodiments, the atomic ratio of silicon to aluminum in the acidic ZSM-5 and ZSM-11 molecular sieves is Si/Al = 3 to 200, preferably Si/Al = 100 to 150.
在一些实施方案中,所述酸性ZSM-5与ZSM-11分子筛的晶体是微米尺度或纳米尺度,晶体中含有微孔结构或介孔-微孔结构。所述改性的酸性分子筛可商购得到,或者可以通过本质上已知的方法制备。对制备所述改性的酸性分子筛的具体方法没有特殊的限制。例如,可以通过对可商购得到的上述酸性ZSM-5分子筛或酸性ZSM-11分子筛进行改性处理得到所述改性的酸性分子筛。In some embodiments, the crystals of the acidic ZSM-5 and ZSM-11 molecular sieves are microscale or nanoscale, and the crystals contain a microporous structure or a mesoporous-microporous structure. The modified acidic molecular sieves are either commercially available or can be prepared by methods known per se. There is no particular limitation on the specific method of preparing the modified acidic molecular sieve. For example, the modified acidic molecular sieve can be obtained by modifying a commercially available acidic ZSM-5 molecular sieve or an acidic ZSM-11 molecular sieve.
在一个具体实施方案中,可以通过用例如H
3PO
4,NH
4H
2PO
4或(NH
4)
2HPO
4水溶液浸渍酸性分子筛,然后将所述浸渍过的酸性分子筛烘干和然后煅烧,得到基于改性分子筛的重量计含0.5~10.0重量%的磷的磷改性酸性分子筛。
In a specific embodiment, the acidic molecular sieve may be impregnated with, for example, H 3 PO 4 , NH 4 H 2 PO 4 or an aqueous solution of (NH 4 ) 2 HPO 4 , and then the impregnated acidic molecular sieve is dried and then calcined. A phosphorus-modified acidic molecular sieve containing 0.5 to 10.0% by weight of phosphorus based on the weight of the modified molecular sieve is obtained.
在另一个具体实施方案中,可以通过用例如H
3BO
3水溶液浸渍酸性分子筛,然后将所述浸渍过的酸性分子筛烘干和然后煅烧,得到基于改性分子筛的重量计含0.5~10.0重量%的硼的硼改性酸性分子筛。
In another embodiment, the acidic molecular sieve may be impregnated with, for example, an aqueous solution of H 3 BO 3 , and then the impregnated acidic molecular sieve is dried and then calcined to obtain 0.5 to 10.0% by weight based on the weight of the modified molecular sieve. Boron modified acidic molecular sieves of boron.
在又一个具体实施方案中,可以通过用硅氧烷化合物经液相沉积法处理和/或用硅烷化合物经气相沉积法处理来制备硅改性的酸性分子筛。可以使用的硅氧烷化合物和硅烷化合物分别由以下结构式表示:In yet another embodiment, the silicon modified acidic molecular sieve can be prepared by treatment with a siloxane compound by liquid phase deposition and/or treatment with a silane compound by vapor deposition. The siloxane compound and the silane compound which can be used are respectively represented by the following structural formula:
其中R
1、R
2、R
3、R
4、R
5、R
6、R
7和R
8各自独立地为C
1-10烷基。所述硅氧烷化合物的一个实例为正硅酸乙酯,和所述硅烷化合物的一个实例为四甲基硅烷。
Wherein R 1 , R 2 , R 3 , R 4 , R 5 , R 6 , R 7 and R 8 are each independently a C 1-10 alkyl group. An example of the siloxane compound is tetraethyl orthosilicate, and an example of the silane compound is tetramethylsilane.
在一个具体实施方案中,所述液相沉积法如下进行:将硅氧烷化合物溶解到惰性有机溶剂中以提供硅氧烷化合物溶液,然后用所述溶液浸泡或浸渍酸性分子筛,干燥和然后煅烧,得到硅改性的酸性分子筛。基于改性分子筛的重量计,该硅改性的酸性分子筛中硅负载量可以为0.5~10.0重量%,所述硅负载量不包括酸性分子筛中原有的硅。所述的惰性有机溶剂可以是任何不与硅氧烷化合物以及分子筛反应的溶剂,例如正己烷、环己 烷、正庚烷。In a specific embodiment, the liquid phase deposition process is carried out by dissolving a silicone compound in an inert organic solvent to provide a solution of the siloxane compound, then soaking or impregnating the acidic molecular sieve with the solution, drying and then calcining A silicon modified acidic molecular sieve is obtained. The silicon-modified acidic molecular sieve may have a silicon loading of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve, and the silicon loading does not include the original silicon in the acidic molecular sieve. The inert organic solvent may be any solvent which does not react with the siloxane compound and the molecular sieve, such as n-hexane, cyclohexane, n-heptane.
在一个具体实施方案中,所述气相沉积法如下进行:使硅烷化合物气体通过酸性分子筛,然后煅烧处理过的酸性分子筛,得到硅改性的酸性分子筛。基于改性分子筛的重量计,该硅改性的酸性分子筛中硅负载量可以为0.5~10.0重量%。所述硅负载量不包括酸性分子筛中原有的硅。In a specific embodiment, the vapor deposition process is carried out by passing a silane compound gas through an acidic molecular sieve and then calcining the treated acidic molecular sieve to obtain a silicon-modified acidic molecular sieve. The silicon-modified acidic molecular sieve may have a silicon loading of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve. The silicon loading does not include the original silicon in the acidic molecular sieve.
在一个具体实施方案中,可以通过用碱土或稀土金属盐水溶液浸渍酸性分子筛,然后将浸渍过的酸性分子筛过滤、烘干和煅烧,得到基于改性分子筛的重量计含0.5~10.0重量的%的碱土或稀土金属的碱土或稀土金属改性酸性分子筛。In a specific embodiment, the acidic molecular sieve may be impregnated with an alkaline earth or a rare earth metal salt aqueous solution, and then the impregnated acidic molecular sieve is filtered, dried and calcined to obtain a weight of 0.5 to 10.0% by weight based on the weight of the modified molecular sieve. Alkaline earth or rare earth metal modified acidic molecular sieve of alkaline earth or rare earth metal.
在一个实施方案中,所述酸性分子筛的平均粒径小于或等于5mm,优选小于或等于0.5mm,更优选小于或等于0.1mm,仍更优选小于或等于0.05mm。In one embodiment, the acidic molecular sieve has an average particle size of less than or equal to 5 mm, preferably less than or equal to 0.5 mm, more preferably less than or equal to 0.1 mm, still more preferably less than or equal to 0.05 mm.
在一些实施方案中,所述分散剂选自氧化铝、二氧化硅和它们的混合物。对可用作分散剂的氧化铝、二氧化硅或氧化铝-二氧化硅没有特殊的限制,并且它们可从很多供应商处商购得到。In some embodiments, the dispersing agent is selected from the group consisting of alumina, silica, and mixtures thereof. There are no particular restrictions on alumina, silica or alumina-silica which can be used as a dispersant, and they are commercially available from many suppliers.
对于可用于本发明中的石墨粉没有特殊的限制,并且它们可从很多供应商处商购得到。在一些实施方案中,所述石墨粉具有0.05~5微米的平均颗粒大小。There are no particular limitations on the graphite powders usable in the present invention, and they are commercially available from many suppliers. In some embodiments, the graphite powder has an average particle size of from 0.05 to 5 microns.
在一个实施方案中,本发明方法中使用的所述催化剂可以通过包括以下步骤的方法制备:In one embodiment, the catalyst used in the process of the invention may be prepared by a process comprising the following steps:
(1)提供惰性载体限域的高分散金属氧化物材料;(1) providing a highly dispersed metal oxide material having an inert carrier confinement;
(2)提供改性的酸性分子筛;(2) providing a modified acidic molecular sieve;
(3)混合由步骤(1)得到的惰性载体限域的高分散金属氧化物材料、由步骤(2)得到的改性的酸性分子筛以及任选的石墨粉和分散剂中至少之一,并将所得到的混合物模制成型。(3) mixing at least one of the inert carrier-limited high-dispersion metal oxide material obtained in the step (1), the modified acidic molecular sieve obtained in the step (2), and optionally graphite powder and a dispersant, and The resulting mixture was molded into a shape.
在一些实施方案中,本发明的催化剂包含10~90重量%的惰性载体限域的高分散金属氧化物材料。惰性载体限域的高分散金属氧化物材料的含量的下限可以是12,15,18,20,22,25,28,30,32,35,38,40,42,45,48,或50重量%,并且上限可以是88,85,82,80,78,75,72,70,68,65,62,60,58,55,52或50重量%,基于催化剂的重量计。In some embodiments, the catalyst of the present invention comprises from 10 to 90% by weight of an inert carrier-limited, highly dispersed metal oxide material. The lower limit of the content of the highly dispersed metal oxide material limited by the inert carrier may be 12, 15, 18, 20, 22, 25, 28, 30, 32, 35, 38, 40, 42, 45, 48, or 50 weight. %, and the upper limit may be 88, 85, 82, 80, 78, 75, 72, 70, 68, 65, 62, 60, 58, 55, 52 or 50% by weight, based on the weight of the catalyst.
在一些实施方案中,本发明的催化剂包含10~90重量%的酸性分子筛。酸性分子筛的含量的下限可以是12,15,18,20,22,25,28,30,32,35,38,40,42,45,48,或50重量%,并且上限可以是88,85,82,80,78,75,72,70,68,65,62,60,58,55,52,或50重量%,基于催化剂的重量计。In some embodiments, the catalyst of the present invention comprises from 10 to 90% by weight of an acidic molecular sieve. The lower limit of the content of the acidic molecular sieve may be 12, 15, 18, 20, 22, 25, 28, 30, 32, 35, 38, 40, 42, 45, 48, or 50% by weight, and the upper limit may be 88, 85. , 82, 80, 78, 75, 72, 70, 68, 65, 62, 60, 58, 55, 52, or 50% by weight, based on the weight of the catalyst.
在一些实施方案中,本发明的催化剂包含0~10重量%,例如0~8重量%,0~7重量%,0~6重量%,或0~5重量%的石墨粉,基于催化剂的重量计。In some embodiments, the catalyst of the present invention comprises 0 to 10% by weight, such as 0 to 8% by weight, 0 to 7% by weight, 0 to 6% by weight, or 0 to 5% by weight, based on the weight of the catalyst. meter.
在一些实施方案中,本发明的催化剂包含0~40重量%,例如0~38重量%,0~35重量%,0~30重量%,或0~25重量%的分散剂,基于催化剂的重量计。In some embodiments, the catalyst of the present invention comprises 0 to 40% by weight, such as 0 to 38% by weight, 0 to 35% by weight, 0 to 30% by weight, or 0 to 25% by weight, based on the weight of the catalyst. meter.
在一些实施方案中,本发明的催化剂包含10~90重量%的惰性载体限域的高分散金属氧化物材料,10~90重量%的酸性分子筛,0~10重量%的石墨粉,和0~40重量%的分散剂,其中惰性载体限域的高分散金属氧化物材料和酸性分子筛的总含量为60~100重量%,所述重量百分数基于催化剂的总重量计。在一些优选的实施方案中,本发明的催化剂包含20~80重量%的惰性载体限域的高分散金属氧化物材料,20~80重量%的酸性分子筛,0~5重量%的石墨粉,和0~30重量%的分散剂,所述重量百分数基于催化剂的总重量计。In some embodiments, the catalyst of the present invention comprises 10 to 90% by weight of an inert carrier-limited high-dispersion metal oxide material, 10 to 90% by weight of an acidic molecular sieve, 0 to 10% by weight of graphite powder, and 0 to 40% by weight of the dispersant, wherein the total content of the inert carrier-limited high-dispersion metal oxide material and the acidic molecular sieve is from 60 to 100% by weight, based on the total weight of the catalyst. In some preferred embodiments, the catalyst of the present invention comprises 20 to 80% by weight of an inert carrier-limited high-dispersion metal oxide material, 20 to 80% by weight of an acidic molecular sieve, 0 to 5% by weight of graphite powder, and 0 to 30% by weight of a dispersant, the weight percentage being based on the total weight of the catalyst.
对所述催化剂的形状没有特殊的限制,只有其适合意图应用的工艺。在一个具体实施方案中,所述催化剂的颗粒形状可以为球形、条形、圆柱形、半圆柱形、棱柱形、三叶草形、环形、丸形、规则或不规则颗粒性或片状。There is no particular limitation on the shape of the catalyst, only that it is suitable for the process intended for application. In a specific embodiment, the particle shape of the catalyst may be spherical, strip, cylindrical, semi-cylindrical, prismatic, clover, ring, pellet, regular or irregular grain or sheet.
在本发明中,术语“粉末”、“颗粒”和“粉状颗粒”可以互换使用。In the present invention, the terms "powder", "particle" and "powdered particles" are used interchangeably.
由合成气和甲苯制备对二甲苯的方法Method for preparing p-xylene from syngas and toluene
如前所述,在本发明的方法中,包含合成气和甲苯的原料与催化剂在反应区中在足以转化至少部分原料的反应条件下接触,以得到包含对二甲苯的反应流出物。As previously mentioned, in the process of the present invention, the feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene.
在本发明的方法中,使用合成气作为原料之一。本文中使用的术语“合 成气”是指氢气与一氧化碳的混合气。在所述合成气原料中,氢气与一氧化碳的摩尔比可以为1:9-9:1,优选为1:9-1:1。In the process of the invention, syngas is used as one of the raw materials. The term "synthetic gas" as used herein refers to a mixture of hydrogen and carbon monoxide. The molar ratio of hydrogen to carbon monoxide in the syngas feed may be from 1:9 to 9:1, preferably from 1:9 to 1:1.
在本发明的方法中,还使用甲苯作为原料之一。In the process of the present invention, toluene is also used as one of the raw materials.
在本发明的方法中,所述反应区可以为一个或多个固定床反应器。所述固定床反应器可以采用连续模式操作。当采用多个固定床反应器时,所述多个反应器可以呈串联、并联、或者串联与并联相结合的构型。In the process of the invention, the reaction zone may be one or more fixed bed reactors. The fixed bed reactor can be operated in a continuous mode. When multiple fixed bed reactors are employed, the plurality of reactors can be in series, parallel, or a combination of series and parallel.
在本发明的方法中,所述反应条件包括:300~450℃的反应温度,0.5~10.0MPa的反应压力,1:9~9:1的合成气中氢气与一氧化碳的摩尔比,0.01~20h
-1的甲苯重时空速,和1000~20000h
-1的标准状态下合成气体积小时空速。
In the method of the present invention, the reaction conditions include: a reaction temperature of 300 to 450 ° C, a reaction pressure of 0.5 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in a synthesis gas of 1:9 to 9:1, 0.01 to 20 h. -1 toluene weight hourly space velocity, and syngas volume hourly space velocity in a standard state of 1000 to 20000 h -1 .
在一个优选的实施方案中,所述反应条件包括:320~400℃的反应温度,1:9~1:1的合成气中氢气与一氧化碳的摩尔比,5.0~10.0MPa的反应压力,0.5~3h
-1的甲苯重时空速,和1000~4000h
-1的标准状态下合成气体积小时空速。
In a preferred embodiment, the reaction conditions include: a reaction temperature of 320 to 400 ° C, a molar ratio of hydrogen to carbon monoxide in a synthesis gas of 1:9 to 1:1, a reaction pressure of 5.0 to 10.0 MPa, 0.5 to toluene weight hourly space velocity of 3h -1, and 1000 ~ 4000h -1 standard state of the volume hourly space velocity of the synthesis gas.
不希望局限于任何具体理论,据信合成气与甲苯反应制取对二甲苯的反应过程非常复杂,并且包括一系列的反应过程,例如:Without wishing to be bound by any particular theory, it is believed that the reaction of syngas with toluene to produce para-xylene is very complex and involves a series of reaction processes such as:
1)合成气直接制取芳烃反应,例如1) Syngas directly produces aromatic hydrocarbons, for example
2)合成气与甲苯的烷基化反应,例如2) Alkylation of syngas with toluene, for example
3)烷基转移反应,例如3) a transalkylation reaction, for example
CO中的氧原子主要进入了CO
2中,因此反应过程废水产生很少。
The oxygen atoms in the CO mainly enter the CO 2 , so the wastewater generated during the reaction process is small.
反应流出物的分离Separation of reaction effluent
在本发明的方法中,从所述包含对二甲苯的反应流出物中分离对二甲苯产物可以按照本质上已知的方法。In the process of the invention, the separation of the para-xylene product from the reaction effluent comprising para-xylene may be carried out in a manner known per se.
本发明能产生的有益效果包括:与用甲醇对甲苯进行烷基化制对二甲苯的方法相比,本发明的方法具有催化剂寿命长,产生废水少,原料成本低,原料来源广泛,能耗低的优点。与常规金属复合氧化物材料相比,本发明方法中使用的惰性载体限域的高分散金属氧化物材料具有比表面大、催化活性高、相对较贵的活性金属氧化物组分含量低、制备过程中重金属离子排放少和更容易成型为工业催化剂的优点。The beneficial effects of the invention include: compared with the method for alkylating toluene with methanol to produce para-xylene, the method of the invention has long catalyst life, less waste water, low raw material cost, wide source of raw materials, and energy consumption. Low advantage. Compared with the conventional metal composite oxide material, the inert carrier-limited high-dispersion metal oxide material used in the method of the invention has a large surface area, high catalytic activity, relatively expensive active metal oxide component content, and is prepared. The process has less heavy metal ion emissions and is easier to form into an industrial catalyst.
图1显示了实施例1中材料A的XRD图。Figure 1 shows an XRD pattern of material A in Example 1.
图2显示了对比例1中材料REF-1的XRD图。Figure 2 shows an XRD pattern of material REF-1 in Comparative Example 1.
下面结合实施例详述本发明,但本发明并不局限于这些实施例。The invention will be described in detail below with reference to examples, but the invention is not limited to the examples.
除非另外指明,本发明的实施例中的原料均通过商业途径购买。The raw materials in the examples of the present invention are all commercially available unless otherwise indicated.
在实施例中,利用带有气体自动进样器、连接TDX-1填充柱的TCD检测器以及连接FFAP与PLOT-Q毛细管柱的FID检测器的两台Agilent7890气相色谱仪进行气体组成自动分析。In the examples, automatic gas composition analysis was performed using two Agilent 7890 gas chromatographs with a gas autosampler, a TCD detector coupled to a TDX-1 packed column, and an FID detector coupled to an FFAP and PLOT-Q capillary column.
在实施例中,转化率和选择性基于碳摩尔数进行计算:In the examples, the conversion and selectivity are calculated based on the number of moles of carbon:
一氧化碳转化率=[(进料中的一氧化碳碳摩尔数)-(出料中的一氧 化碳碳摩尔数)]÷(进料中的一氧化碳碳摩尔数)×100%Carbon monoxide conversion = [( moles of carbon monoxide carbon in the feed) - (moles of carbon monoxide in the discharge)] ÷ (moles of carbon monoxide in the feed) × 100%
甲苯转化率=[(进料中的甲苯碳摩尔数)-(出料中的甲苯碳摩尔数)]÷(进料中的甲苯碳摩尔数)×100%Toluene conversion = [(mole toluene in feed) - (moles of toluene in the discharge)] ÷ (moles of toluene in the feed) × 100%
二甲苯选择性=(出料中的二甲苯碳摩尔数)÷(出料中的所有烃类产物的碳摩尔数-原料甲苯的碳摩尔数)×100%Xylene selectivity = (mole carbon number in the discharge) ÷ (carbon moles of all hydrocarbon products in the discharge - carbon moles of raw material toluene) × 100%
对二甲苯比例=(出料中的对二甲苯碳摩尔数)÷(出料中的所有二甲苯的碳摩尔数)×100%Paraxylene ratio = (p-xylene carbon moles in the discharge) ÷ (carbon moles of all xylene in the discharge) × 100%
惰性载体限域的高分散金属氧化物材料Inert carrier limited high dispersion metal oxide material
实施例1Example 1
配制含0.05mol/L Zn
2+与1.0mol/L Al
3+的混合硝酸盐水溶液1L,将0.5mol/L的氨水溶液缓慢加入其中,同时控制共沉淀反应温度为70℃和控制pH值为7.2,使金属离子共沉淀。反应结束后使反应混合物在70℃的温度下老化4h。将沉淀物过滤、用去离子水洗涤后干燥,500℃煅烧4h,得到氧化铝作为惰性载体限域的高分散锌氧化物材料,编号为A。A含8.3重量%的锌,XRD图如图1所示。
Prepare 1 L of mixed nitrate aqueous solution containing 0.05 mol/L Zn 2+ and 1.0 mol/L Al 3+ , slowly add 0.5 mol/L ammonia solution, and control the coprecipitation reaction temperature to 70 ° C and control the pH value. 7.2, coprecipitating metal ions. After the end of the reaction, the reaction mixture was aged at 70 ° C for 4 h. The precipitate was filtered, washed with deionized water, dried, and calcined at 500 ° C for 4 h to obtain alumina as an inert carrier-limited high-dispersion zinc oxide material, numbered A. A contains 8.3% by weight of zinc, and the XRD pattern is shown in Fig. 1.
实施例2Example 2
配制含0.02mol/L Zn
2+、0.02mol/L Cr
3+与1.0mol/L Al
3+的混合硝酸盐水溶液1L,将1.0mol/L的碳酸铵溶液缓慢加入其中,同时控制共沉淀反应温度为70℃和控制pH值为7.5,使金属离子共沉淀。反应结束后使反应混合物在70℃的温度下老化4h。将沉淀物过滤、用去离子水洗涤后干燥,500℃煅烧4h,得到氧化铝作为惰性载体限域的高分散锌铬氧化物材料,编号为B。B含3.1重量%的锌和2.5重量%的铬。
Prepare 1L of mixed nitrate solution containing 0.02mol/L Zn 2+ , 0.02mol/L Cr 3+ and 1.0mol/L Al 3+ , and slowly add 1.0mol/L ammonium carbonate solution to control the coprecipitation reaction. The metal ions were co-precipitated at a temperature of 70 ° C and a controlled pH of 7.5. After the end of the reaction, the reaction mixture was aged at 70 ° C for 4 h. The precipitate was filtered, washed with deionized water, dried, and calcined at 500 ° C for 4 h to obtain alumina as an inert carrier-limited high-dispersion zinc-chromium oxide material, numbered B. B contains 3.1% by weight of zinc and 2.5% by weight of chromium.
实施例3Example 3
配制含0.01mol/L Zn
2+、0.01mol/L Zr
4+与1.0mol/L Al
3+的混合硝酸盐水溶液1L,将1.2mol/L的碳酸钠溶液缓慢加入其中,同时控制共沉淀反应温度为70℃和控制pH值为7.3,使金属离子共沉淀。反应结束后使反应混合物在70℃的温度下老化4h。将沉淀物过滤、用去离子水洗涤后干燥,500℃煅烧4h,得到氧化铝作为惰性载体限域的高分散锌锆氧化物材料,编号为C。C含1.5质量%的锌和2.1质量%的锆。
Prepare 1L mixed nitrate solution containing 0.01mol/L Zn 2+ , 0.01mol/L Zr 4+ and 1.0mol/L Al 3+ , and slowly add 1.2mol/L sodium carbonate solution to control the coprecipitation reaction. The temperature was 70 ° C and the pH was controlled to 7.3 to coprecipitate the metal ions. After the end of the reaction, the reaction mixture was aged at 70 ° C for 4 h. The precipitate was filtered, washed with deionized water, dried, and calcined at 500 ° C for 4 h to obtain alumina as an inert carrier-limited high-dispersion zinc-zirconium oxide material, numbered C. C contains 1.5% by mass of zinc and 2.1% by mass of zirconium.
实施例4Example 4
配制含0.01mol/L Zn
2+、0.02mol/L Cu
2+与1.0mol/L Al
3+的混合硝酸盐水溶液1L,将1.5mol/L的碳酸钾溶液缓慢加入其中,同时控制共沉淀反应温度为70℃和控制pH值为7.9,使金属离子共沉淀。反应结束后使反应混合物在70℃的温度下老化4h。将沉淀物过滤、用去离子水洗涤后干燥,500℃煅烧4h,得到氧化铝作为惰性载体限域的高分散锌铜氧化物材料,编号为D。D含1.5质量%的锌和3.1质量%的铜。
Prepare 1L of mixed nitrate solution containing 0.01mol/L Zn 2+ , 0.02mol/L Cu 2+ and 1.0mol/L Al 3+ , and slowly add 1.5mol/L potassium carbonate solution to control the coprecipitation reaction. The metal ions were coprecipitated at a temperature of 70 ° C and a controlled pH of 7.9. After the end of the reaction, the reaction mixture was aged at 70 ° C for 4 h. The precipitate was filtered, washed with deionized water, dried, and calcined at 500 ° C for 4 h to obtain alumina as an inert carrier-limited high-dispersion zinc-copper oxide material, numbered D. D contains 1.5% by mass of zinc and 3.1% by mass of copper.
实施例5Example 5
配制含0.2mol/L Zn
2+与0.2mol/L Cr
3+的混合硝酸盐水溶液100mL,配制1.0mol/L的尿素水溶液100mL。将上述两种溶液滴加入1mol的正硅酸乙酯中,室温反应24h,获得凝胶。将所述凝胶用去离子水洗涤,在100℃干燥,500℃煅烧4h,得到二氧化硅作为惰性载体限域的高分散锌铬氧化物材料,编号为E。E含1.8质量%的锌和1.5质量%的铬。
100 mL of a mixed nitrate aqueous solution containing 0.2 mol/L Zn 2+ and 0.2 mol/L Cr 3+ was prepared to prepare 100 mL of a 1.0 mol/L urea aqueous solution. The above two solutions were added dropwise to 1 mol of ethyl orthosilicate, and reacted at room temperature for 24 hours to obtain a gel. The gel was washed with deionized water, dried at 100 ° C, and calcined at 500 ° C for 4 h to obtain a highly dispersed zinc chromium oxide material having a silica as an inert carrier, numbered E. E contains 1.8% by mass of zinc and 1.5% by mass of chromium.
实施例6Example 6
配制含0.2mol/L Zn
2+与0.2mol/L Zr
4+的混合硝酸盐水溶液100mL,配制1.0mol/L的尿素水溶液100mL。将上述两种溶液滴加入1mol的正硅酸乙酯中,室温反应24h,获得凝胶。将所述凝胶用去离子水洗涤,在100℃干燥,500℃煅烧4h,得到氧化硅作为惰性载体限域的高分散锌锆氧化物材料,编号为F。F含1.8质量%的锌和2.5质量%的锆。
100 mL of a mixed nitrate aqueous solution containing 0.2 mol/L Zn 2+ and 0.2 mol/L Zr 4+ was prepared to prepare 100 mL of a 1.0 mol/L urea aqueous solution. The above two solutions were added dropwise to 1 mol of ethyl orthosilicate, and reacted at room temperature for 24 hours to obtain a gel. The gel was washed with deionized water, dried at 100 ° C, and calcined at 500 ° C for 4 h to obtain a highly dispersed zinc zirconium oxide material having a silica as an inert carrier confinement, numbered F. F contains 1.8% by mass of zinc and 2.5% by mass of zirconium.
对比例1Comparative example 1
配制含1.0mol/L Zn
2+、0.50mol/L Cr
3+与0.20mol/L Al
3+的混合硝酸盐水溶液1L,将1.0mol/L的碳酸铵溶液缓慢加入其中,同时控制共沉淀反应温度为70℃和控制pH值为7.5,使金属离子共沉淀。反应结束后使反应混合物在70℃的温度下老化4h。将沉淀物过滤、用去离子水洗涤后干燥,500℃煅烧4h,得到锌铬铝复合氧化物,编号为REF-1。REF-1的XRD图如图2所示。
Prepare 1L of mixed nitrate solution containing 1.0mol/L Zn 2+ , 0.50mol/L Cr 3+ and 0.20mol/L Al 3+ , and slowly add 1.0mol/L ammonium carbonate solution to control the coprecipitation reaction. The metal ions were co-precipitated at a temperature of 70 ° C and a controlled pH of 7.5. After the end of the reaction, the reaction mixture was aged at 70 ° C for 4 h. The precipitate was filtered, washed with deionized water, dried, and calcined at 500 ° C for 4 h to obtain a zinc chromium aluminum composite oxide, numbered REF-1. The XRD pattern of REF-1 is shown in Figure 2.
改性酸性分子筛制备Modified acidic molecular sieve preparation
实施例7Example 7
将Si/Al=25(原子比)的钠型ZSM-5(得自南开大学催化剂厂)用0.8 mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1),得到铵型ZSM-5分子筛。将该铵型ZSM-5分子筛在空气气氛下550℃煅烧4h,然后利用(NH
4)
2HPO
4水溶液(水溶液中P的含量为5质量%)在室温下等体积浸渍24小时,烘干后,再在空气气氛下550℃煅烧4h,得到含4质量%P的酸性ZSM-5分子筛,编号为G。
A sodium type ZSM-5 (available from Nankai University Catalyst Factory) with Si/Al=25 (atomic ratio) was exchanged three times with a 0.8 mol/L aqueous solution of ammonium nitrate at 80 ° C (the ratio of ammonium nitrate aqueous solution to molecular sieve was 20: 1) An ammonium type ZSM-5 molecular sieve is obtained. The ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of (NH 4 ) 2 HPO 4 (the content of P in the aqueous solution was 5% by mass), and dried. Then, it was calcined at 550 ° C for 4 hours in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 4% by mass of P, and numbered G.
实施例8Example 8
将Si/Al=200(原子比)的钠型ZSM-5(得自南开大学催化剂厂)用0.8mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1),得到铵型ZSM-5分子筛。将该铵型ZSM-5分子筛在空气气氛下550℃煅烧4h,然后利用H
3BO
3水溶液(水溶液中B的含量为10质量%)在室温下等体积浸渍24小时,烘干后,再在空气气氛下550℃煅烧4h,得到含8质量%B的酸性ZSM-5分子筛,编号为H。
A sodium type ZSM-5 (available from Nankai University Catalyst Factory) having Si/Al=200 (atomic ratio) was exchanged three times with a 0.8 mol/L aqueous solution of ammonium nitrate at 80 ° C (the ratio of the aqueous ammonium nitrate solution to the molecular sieve was 20: 1) An ammonium type ZSM-5 molecular sieve is obtained. The ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of H 3 BO 3 (the content of B in the aqueous solution was 10% by mass), dried, and then Calcination at 550 ° C for 4 h in an air atmosphere gave an acidic ZSM-5 molecular sieve containing 8 mass% B, numbered H.
实施例9Example 9
将Si/Al=40(原子比)的钠型ZSM-11(得自奥科公司)用0.8mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1),得到铵型ZSM-11分子筛。将该铵型ZSM-11分子筛在空气气氛下550℃煅烧4h,然后利用H
3BO
3水溶液(水溶液中B的含量为10质量%)在室温下等体积浸渍24小时,烘干后,再在空气气氛下550℃煅烧4h,得到含8质量%B的酸性ZSM-11分子筛,编号为I。
A sodium type ZSM-11 (available from Aoke) having Si/Al = 40 (atomic ratio) was exchanged three times at 80 ° C with a 0.8 mol/L aqueous solution of ammonium nitrate (the ratio of the aqueous ammonium nitrate solution to the molecular sieve was 20:1). ), an ammonium type ZSM-11 molecular sieve was obtained. The ammonium type ZSM-11 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then immersed in an equal volume at room temperature for 24 hours using an aqueous solution of H 3 BO 3 (the content of B in the aqueous solution was 10% by mass), dried, and then Calcination at 550 ° C for 4 h in an air atmosphere gave an acidic ZSM-11 molecular sieve containing 8 mass % B, numbered I.
实施例10Example 10
将Si/Al=3(原子比)的钠型ZSM-5(得自奥科公司)用0.8mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1),得到铵型ZSM-5分子筛。将该铵型ZSM-5分子筛在空气气氛下550℃煅烧4h,然后利用正硅酸乙酯的环己烷溶液(溶液中Si的含量为10质量%)在50℃下处理4小时。将反应混合物蒸干后在空气气氛下550℃煅烧4h,得到含8质量%Si(不包括分子筛原有的Si)的酸性ZSM-5分子筛,编号为J。A sodium type ZSM-5 (available from Aoke Company) having Si/Al = 3 (atomic ratio) was exchanged three times at 80 ° C with a 0.8 mol/L aqueous solution of ammonium nitrate (the ratio of the aqueous ammonium nitrate solution to the molecular sieve was 20:1). ), an ammonium type ZSM-5 molecular sieve was obtained. The ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 hours in an air atmosphere, and then treated with a cyclohexane solution of tetraethyl orthosilicate (the content of Si in the solution was 10% by mass) at 50 ° C for 4 hours. The reaction mixture was evaporated to dryness, and then calcined at 550 ° C for 4 hr in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 8% by mass of Si (excluding the original Si of the molecular sieve), No. J.
实施例11Example 11
将Si/Al=80(原子比)的钠型ZSM-5(得自复旭公司)用0.8mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1), 得到铵型ZSM-5分子筛。将该铵型ZSM-5分子筛500g在空气气氛下550℃煅烧4h,然后利用1L/min氮气携带5%体积分数的四甲基硅烷在200℃下处理3小时,再在空气气氛下550℃煅烧4h,得到含2质量%Si(不包括分子筛原有的Si)的酸性ZSM-5分子筛,编号为K。The sodium type ZSM-5 (from Juxu) with Si/Al=80 (atomic ratio) was exchanged three times with 0.8 mol/L aqueous ammonium nitrate solution at 80 ° C (the ratio of ammonium nitrate aqueous solution to molecular sieve was 20:1). ), an ammonium type ZSM-5 molecular sieve was obtained. 500 g of the ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then treated with 1 L/min of nitrogen to carry 5% by volume of tetramethylsilane at 200 ° C for 3 hours, and then calcined at 550 ° C in an air atmosphere. 4h, an acidic ZSM-5 molecular sieve containing 2% by mass of Si (excluding the original Si of the molecular sieve) was obtained, numbered K.
实施例12Example 12
将Si/Al=60(原子比)的钠型ZSM-5(得自南开大学催化剂厂)用0.8mol/L的硝酸铵水溶液在80℃交换3次(硝酸铵水溶液与分子筛体积比为20:1),得到铵型ZSM-5分子筛。将该铵型ZSM-5分子筛在空气气氛下550℃煅烧4h,然后利用硝酸镁与硝酸铈混合水溶液(水溶液中Mg与Ce的含量分别为5质量%和1.3质量%)在室温下等体积浸渍24小时,烘干后,再在空气气氛下550℃煅烧4h,得到含4质量%Mg和1质量%Ce的酸性ZSM-5分子筛,编号为L。A sodium type ZSM-5 (available from Nankai University Catalyst Factory) having Si/Al=60 (atomic ratio) was exchanged three times with a 0.8 mol/L aqueous solution of ammonium nitrate at 80 ° C (the ratio of the aqueous ammonium nitrate solution to the molecular sieve was 20: 1) An ammonium type ZSM-5 molecular sieve is obtained. The ammonium type ZSM-5 molecular sieve was calcined at 550 ° C for 4 h in an air atmosphere, and then impregnated at room temperature with an aqueous solution of magnesium nitrate and cerium nitrate (contents of Mg and Ce in the aqueous solution were respectively 5% by mass and 1.3% by mass). After 24 hours, after drying, it was calcined at 550 ° C for 4 h in an air atmosphere to obtain an acidic ZSM-5 molecular sieve containing 4% by mass of Mg and 1% by mass of Ce, numbered L.
催化剂制备Catalyst preparation
实施例13Example 13
将20质量份得自实施例1的惰性载体限域的高分散金属氧化物材料A、70质量份得自实施例7的酸性分子筛G、5质量份石墨粉和5质量份作为分散剂的氧化硅均匀混合,然后用打片机打片成直径为4mm,高度为4mm的柱状催化剂,编号为M。制备方案汇总见表1。20 parts by mass of the highly dispersed metal oxide material A derived from the inert carrier of Example 1, 70 parts by mass of the acidic molecular sieve G obtained in Example 7, 5 parts by mass of graphite powder, and 5 parts by mass as a dispersing agent The silicon was uniformly mixed, and then punched into a columnar catalyst having a diameter of 4 mm and a height of 4 mm by a tableting machine, and numbered M. The preparation scheme is summarized in Table 1.
实施例14~18Examples 14-18
制备方法与实施例13相似,具体方案见表1。The preparation method is similar to that of Example 13, and the specific scheme is shown in Table 1.
对比例2Comparative example 2
将20质量份得自对比例1的金属复合氧化物REF-1、70质量份得自实施例7的酸性分子筛G、5质量份石墨粉和5质量份作为分散剂的氧化硅均匀混合,然后用打片机打片成直径为4mm,高度为4mm的柱状催化剂,编号为REF-2。20 parts by mass of the metal composite oxide REF-1 obtained in Comparative Example 1, 70 parts by mass of the acidic molecular sieve G obtained in Example 7, 5 parts by mass of graphite powder, and 5 parts by mass of silicon oxide as a dispersing agent were uniformly mixed, and then A columnar catalyst having a diameter of 4 mm and a height of 4 mm was punched by a tableting machine and numbered REF-2.
实施例19Example 19
将75质量份得自实施例1的惰性载体限域的高分散金属氧化物材料A与25质量份得自实施例7的酸性分子筛G均匀混合并碾碎成小于0.05mm的粉末,然后压片筛分制成1-2mm颗粒催化剂,编号为S,制备方案汇 总见表1。75 parts by mass of the highly dispersed metal oxide material A from the inert carrier of Example 1 was uniformly mixed with 25 parts by mass of the acidic molecular sieve G obtained in Example 7 and crushed into a powder of less than 0.05 mm, and then tableted. The sieve was prepared into a 1-2 mm particle catalyst, numbered S, and the preparation scheme is summarized in Table 1.
实施例20~24Examples 20-24
制备方法与实施例19相似,具体方案见表1。The preparation method is similar to that of Example 19, and the specific scheme is shown in Table 1.
对比例3Comparative example 3
将75质量份得自对比例1的金属复合氧化物REF-1与25质量份得自实施例7的酸性分子筛G均匀混合并碾碎成小于0.05mm的粉末,然后压片筛分制成1-2mm颗粒催化剂,编号为REF-3。75 parts by mass of the metal composite oxide REF-1 obtained from Comparative Example 1 and 25 parts by mass of the acidic molecular sieve G obtained in Example 7 were uniformly mixed and crushed into a powder of less than 0.05 mm, and then sieved into 1 - 2 mm particulate catalyst, numbered REF-3.
表1 催化剂制备方案Table 1 catalyst preparation scheme
催化剂性能测试Catalyst performance test
实施例25Example 25
将催化剂M 200g装入内径为28mm的不锈钢反应管内,用1000ml/min氢气在300℃下活化4h。然后将氢气流切换为合成气流并引入甲苯流,并在以下条件下反应:反应温度(T)=400℃,反应压力(P)=7.0MPa,标准状况下气体体积空速(GHSV)=6000h
-1,合成气中CO与H
2的体积比为1:1,甲苯质量空速(WHSV)=1.0h
-1。反应稳定后,用气相 色谱分析产物。反应结果见表2。
200 g of the catalyst M was placed in a stainless steel reaction tube having an inner diameter of 28 mm, and activated with 1000 ml/min of hydrogen at 300 ° C for 4 hours. The hydrogen stream is then switched to a syngas stream and a toluene stream is introduced and reacted under the following conditions: reaction temperature (T) = 400 ° C, reaction pressure (P) = 7.0 MPa, gas volumetric space velocity (GHSV) = 6000 h under standard conditions -1 , the volume ratio of CO to H 2 in the synthesis gas is 1:1, and the tonnage mass space velocity (WHSV) = 1.0 h -1 . After the reaction was stabilized, the product was analyzed by gas chromatography. The reaction results are shown in Table 2.
实施例26-30Example 26-30
重复实施例25,但是将实施例25中的催化剂M换成催化剂N-R。反应结果见表2。Example 25 was repeated, but the catalyst M in Example 25 was replaced with the catalyst N-R. The reaction results are shown in Table 2.
对比例4Comparative example 4
重复实施例25,但是将实施例25中的催化剂M换成催化剂REF-2。反应结果见表2。Example 25 was repeated, but the catalyst M in Example 25 was replaced with the catalyst REF-2. The reaction results are shown in Table 2.
表2 实施例25-30和对比例4中的催化反应结果Table 2 Results of catalytic reactions in Examples 25-30 and Comparative Example 4
实施例31Example 31
将催化剂S 5g装入内径为8mm的不锈钢反应管内,用50ml/min氢气在300在℃下活化4h。然后将氢气流切换为合成气流并引入甲苯流,并在以下条件下反应:反应温度(T)=400℃,反应压力(P)=4.0MPa,标准状况下合成气气体体积空速(GHSV)=4000h
-1,合成气中CO与H
2的体积比为1.5:1,甲苯质量空速(WHSV)=0.5h
-1。反应500h后,用气相色谱分析产物,反应结果见表3。
Catalyst S 5g was placed in a stainless steel reaction tube having an inner diameter of 8 mm, and activated with 50 ml/min of hydrogen at 300 ° C for 4 h. The hydrogen stream is then switched to a syngas stream and a toluene stream is introduced and reacted under the following conditions: reaction temperature (T) = 400 ° C, reaction pressure (P) = 4.0 MPa, syngas gas volumetric space velocity (GHSV) under standard conditions =4000h -1 , the volume ratio of CO to H 2 in the synthesis gas is 1.5:1, and the tonnage mass space velocity (WHSV) = 0.5h -1 . After the reaction for 500 hours, the product was analyzed by gas chromatography, and the reaction results are shown in Table 3.
实施例32-36Example 32-36
反应条件和反应结果见表3。其他操作同实施例31。The reaction conditions and reaction results are shown in Table 3. The other operations are the same as those in the embodiment 31.
对比例5Comparative example 5
将催化剂REF-3 5g装入内径为8mm的不锈钢反应管内,用50ml/min氢气在300在℃下活化4h,以下条件下反应:反应温度(T)=400℃,反应压力(P)=4.0MPa,标准状况下合成气体积空速(GHSV)=4000h
-1,合成气(CO与H
2混合气)中氢气的体积分数V(H
2)%=40%,甲苯质量空速(WHSV)=0.5h
-1。反应500h后,用气相色谱分析产物,反应结果见表3。
5 g of catalyst REF-3 was placed in a stainless steel reaction tube with an inner diameter of 8 mm, and activated with 50 ml/min of hydrogen at 300 ° C for 4 h under the following conditions: reaction temperature (T) = 400 ° C, reaction pressure (P) = 4.0 MPa, syngas volume space velocity (GHSV)=4000h -1 under standard conditions, volume fraction of hydrogen in synthesis gas (CO and H 2 mixture) V(H 2 )%=40%, toluene mass space velocity (WHSV) =0.5h -1 . After the reaction for 500 hours, the product was analyzed by gas chromatography, and the reaction results are shown in Table 3.
表3 实施例31-36和对比例5中的催化反应结果Table 3 Results of catalytic reactions in Examples 31-36 and Comparative Example 5
催化剂再生性能测试Catalyst regeneration performance test
实施例37Example 37
将实施例25中失活后的催化剂利用由2体积%氧气和98体积%氮气组成的混合气在550℃处理10h,使得催化剂再生一轮。然后在实施例25的条件下反应。按照同样的方式总共再生五轮。选取每轮反应500h后的催化活性数据进行比较,结果见表4。The catalyst deactivated in Example 25 was treated at 550 ° C for 10 h with a mixture of 2 vol% oxygen and 98 vol% nitrogen to regenerate the catalyst for one round. The reaction was then carried out under the conditions of Example 25. A total of five rounds were regenerated in the same way. The catalytic activity data after 500 h of each reaction was selected for comparison. The results are shown in Table 4.
表4 实施例37中的催化剂再生性能测
试结果
Table 4 Catalyst Regeneration Performance test results in 37 patients
实施例38Example 38
将实施例31中失活后的催化剂利用由2体积%氧气和98体积%氮气 组成的混合气在550℃处理10h,使得催化剂再生一轮。然后在实施例31的条件下反应。按照同样的方式总共再生五轮。选取每轮反应500h后的催化活性数据进行比较,结果见表5。The catalyst deactivated in Example 31 was treated at 550 ° C for 10 h with a mixed gas consisting of 2 vol% oxygen and 98 vol% nitrogen to regenerate the catalyst for one round. Then, the reaction was carried out under the conditions of Example 31. A total of five rounds were regenerated in the same way. The catalytic activity data after 500 h of each reaction was selected for comparison. The results are shown in Table 5.
表5 实施例38中的催化剂再生性能测试结果Table 5 Test results of catalyst regeneration performance in Example 38
以上所述,仅是本发明的几个实施例,并非对本发明做任何形式的限制,虽然本发明以较佳实施例揭示如上,然而并非用以限制本发明,任何熟悉本专业的技术人员,在不脱离本发明技术方案的范围内,利用上述揭示的技术内容做出些许的变动或修饰均等同于等效实施案例,均属于技术方案范围内。The above is only a few embodiments of the present invention, and is not intended to limit the present invention. The present invention is disclosed by the preferred embodiments, but is not intended to limit the present invention. It is within the scope of the technical solution to make a slight change or modification with the technical content disclosed above, which is equivalent to the equivalent embodiment, without departing from the scope of the present invention.
Claims (12)
- 一种由合成气与甲苯直接制备对二甲苯的方法,该方法包括:A method for directly preparing para-xylene from syngas and toluene, the method comprising:使包含合成气和甲苯的原料与催化剂在反应区中在足以转化至少部分原料的反应条件下接触,以得到包含对二甲苯的反应流出物;和The feedstock comprising synthesis gas and toluene is contacted with a catalyst in a reaction zone under reaction conditions sufficient to convert at least a portion of the feedstock to provide a reaction effluent comprising para-xylene;从所述反应流出物中分离对二甲苯,Separating para-xylene from the reaction effluent,其中所述催化剂包含惰性载体限域的高分散金属氧化物材料、酸性分子筛、和任选的石墨粉和分散剂中至少之一,其中在所述惰性载体限域的高分散金属氧化物材料中,惰性载体为氧化硅和氧化铝中至少之一,并且所述金属氧化物以金属计的含量低于或等于10质量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计,和其中所述酸性分子筛选自经过改性的酸性ZSM-5分子筛、经过改性的酸性ZSM-11分子筛和它们的混合物。Wherein the catalyst comprises at least one of an inert carrier-limited high-dispersion metal oxide material, an acidic molecular sieve, and optionally a graphite powder and a dispersant, wherein the inert carrier-limited high-dispersion metal oxide material The inert carrier is at least one of silica and alumina, and the metal oxide is present in an amount of less than or equal to 10% by mass based on the weight of the inert carrier-limited high-dispersion metal oxide material. And wherein the acidic molecule is selected from the modified acidic ZSM-5 molecular sieve, the modified acidic ZSM-11 molecular sieve, and mixtures thereof.
- 权利要求1所述的方法,该方法具有以下特征中至少之一:The method of claim 1 having at least one of the following features:-所述反应区包括一个固定床反应器,或者以串联和/或并联方式连接的多个固定床反应器;The reaction zone comprises a fixed bed reactor or a plurality of fixed bed reactors connected in series and / or in parallel;-所述反应条件包括:300~450℃的反应温度,0.5~10.0MPa的反应压力,1:9~9:1的合成气中氢气与一氧化碳的摩尔比,0.01~20h -1的甲苯重时空速,和1000~20000h -1的标准状态下合成气体积小时空速; - the reaction conditions include: a reaction temperature of 300 to 450 ° C, a reaction pressure of 0.5 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in a synthesis gas of 1:9 to 9:1, and a toluene weight hourly space of 0.01 to 20 h -1 Speed, and the hourly space velocity of the syngas at a standard state of 1000 to 20000 h -1 ;-所述金属氧化物是锌、铬、锆、铜、锰、铂和钯中的至少一种的氧化物;The metal oxide is an oxide of at least one of zinc, chromium, zirconium, copper, manganese, platinum and palladium;-所述惰性载体限域的高分散金属氧化物材料中金属氧化物以金属计的含量低于或等于5重量%,基于所述惰性载体限域的高分散金属氧化物材料的重量计;The content of the metal oxide in the inert carrier-limited high-dispersion metal oxide material in terms of metal is less than or equal to 5% by weight, based on the weight of the inert carrier-limited high-dispersion metal oxide material;-所述惰性载体限域的高分散金属氧化物材料中金属氧化物的颗粒尺度小于或等于100nm;The particle size of the metal oxide in the inert carrier-limited high-dispersion metal oxide material is less than or equal to 100 nm;-酸性分子筛的改性是磷改性、硼改性、硅改性、碱土金属改性和稀土金属改性中的一种或多种;- the modification of the acidic molecular sieve is one or more of phosphorus modification, boron modification, silicon modification, alkaline earth metal modification and rare earth metal modification;-所述酸性ZSM-5和ZSM-11分子筛中硅和铝的原子比为Si/Al=3~200;和- an atomic ratio of silicon to aluminum in the acidic ZSM-5 and ZSM-11 molecular sieves is Si/Al = 3 to 200;-所述催化剂的形状为球形、条形、圆柱形、半圆柱形、棱柱形、三叶 草形、环形、丸形、规则或不规则颗粒性或片状。- The shape of the catalyst is spherical, strip, cylindrical, semi-cylindrical, prismatic, clover, ring, pellet, regular or irregular grain or flake.
- 权利要求1所述的方法,其中所述催化剂包含10~90重量%的惰性载体限域的高分散金属氧化物材料,10~90重量%的酸性分子筛,0~10重量%的石墨粉,和0~40重量%的分散剂,其中惰性载体限域的高分散金属氧化物材料和酸性分子筛的总含量为60~100重量%,所述重量百分数基于催化剂的总重量计。The method of claim 1 wherein said catalyst comprises from 10 to 90% by weight of an inert carrier-limited, highly dispersed metal oxide material, from 10 to 90% by weight of an acidic molecular sieve, from 0 to 10% by weight of graphite powder, and 0 to 40% by weight of the dispersant, wherein the total content of the inert carrier-limited high-dispersion metal oxide material and the acidic molecular sieve is from 60 to 100% by weight, based on the total weight of the catalyst.
- 权利要求1所述的方法,其中所述催化剂包含20~80重量%的惰性载体限域的高分散金属氧化物材料,20~80重量%的酸性分子筛,0~5重量%的石墨粉,和0~30重量%的分散剂,所述重量百分数基于催化剂的总重量计。The method of claim 1 wherein said catalyst comprises from 20 to 80% by weight of an inert carrier-limited, highly dispersed metal oxide material, from 20 to 80% by weight of an acidic molecular sieve, from 0 to 5% by weight of graphite powder, and 0 to 30% by weight of a dispersant, the weight percentage being based on the total weight of the catalyst.
- 权利要求1所述的方法,其中所述惰性载体限域的高分散金属氧化物材料的平均粒径小于或等于5mm,并且所述酸性分子筛颗粒的平均粒径小于或等于5mm;优选所述惰性载体限域的高分散金属氧化物材料的平均粒径小于或等于0.05mm,并且所述酸性分子筛颗粒的平均粒径小于或等于0.05mm。The method of claim 1 wherein said inert support-limited high-dispersion metal oxide material has an average particle size of less than or equal to 5 mm and said acidic molecular sieve particles have an average particle size of less than or equal to 5 mm; preferably said inert The carrier-limited high-dispersion metal oxide material has an average particle diameter of less than or equal to 0.05 mm, and the acidic molecular sieve particles have an average particle diameter of less than or equal to 0.05 mm.
- 权利要求1所述的方法,其中所述催化剂通过包括以下步骤的方法制备:The method of claim 1 wherein said catalyst is prepared by a process comprising the steps of:(1)提供惰性载体限域的高分散金属氧化物材料;(1) providing a highly dispersed metal oxide material having an inert carrier confinement;(2)提供改性的酸性分子筛;(2) providing a modified acidic molecular sieve;(3)混合由步骤(1)得到的惰性载体限域的高分散金属氧化物材料、由步骤(2)得到的改性的酸性分子筛、以及任选的石墨粉和分散剂中至少之一,并将所得到的混合物模制成型。(3) mixing at least one of the inert carrier-limited high-dispersion metal oxide material obtained in the step (1), the modified acidic molecular sieve obtained in the step (2), and optionally the graphite powder and the dispersant, The resulting mixture was molded into shape.
- 权利要求6所述的方法,其中所述用于制备催化剂的方法具有以下特征中至少之一:The method of claim 6 wherein said method for preparing a catalyst has at least one of the following features:-在步骤(1)中,通过沉淀-煅烧方法制备所述惰性载体限域的高分散金属氧化物材料,或者通过溶胶-凝胶方法制备所述惰性载体限域的高分散金属氧化物材料;- in step (1), preparing the inert carrier-limited high-dispersion metal oxide material by a precipitation-calcination method, or preparing the inert carrier-limited high-dispersion metal oxide material by a sol-gel method;-所述改性的酸性分子筛选自磷改性、硼改性、硅改性、碱土金属改性和/或稀土金属改性的ZSM-5分子筛和ZSM-11分子筛;- the modified acidic molecule is screened from a ZSM-5 molecular sieve and a ZSM-11 molecular sieve modified by phosphorus modification, boron modification, silicon modification, alkaline earth metal modification and/or rare earth metal modification;-在步骤(3)中,采用挤出方法或模压方法将所述混合物模制成催化剂颗粒。- In the step (3), the mixture is molded into catalyst particles by an extrusion method or a molding method.
- 权利要求6所述的方法,其中在所述用于制备催化剂的方法的步骤(1)中,通过包括如下步骤的方法提供所述惰性载体限域的高分散金属氧化物材料:将催化活性金属的盐与铝盐配成混合金属盐水溶液;使所述混合金属盐水溶液和沉淀剂水溶液接触,以使所述混合金属盐水溶液中的金属离子共沉淀;老化;和将沉淀物洗涤、干燥后煅烧,制得惰性载体限域的高分散金属氧化物材料。The method of claim 6, wherein in the step (1) of the method for preparing a catalyst, the inert carrier-limited high-dispersion metal oxide material is provided by a method comprising the steps of: catalytically active metal a salt and an aluminum salt are mixed into a mixed metal salt solution; contacting the mixed metal salt aqueous solution with an aqueous solution of a precipitating agent to coprecipitate the metal ions in the mixed metal salt aqueous solution; aging; and washing and drying the precipitate Calcination produces a highly dispersed metal oxide material that is inert to the carrier.
- 权利要求8所述的方法,其具有以下特征中至少之一:The method of claim 8 having at least one of the following features:-所述催化活性金属的盐和所述铝盐选自盐酸盐、硫酸盐和硝酸盐;a salt of said catalytically active metal and said aluminum salt being selected from the group consisting of hydrochlorides, sulfates and nitrates;-所述沉淀剂选自碳酸钠、碳酸钾、碳酸铵、碳酸氢钠、碳酸氢钾、碳酸氢铵、氨水、氢氧化钠、氢氧化钾和它们的混合物;The precipitating agent is selected from the group consisting of sodium carbonate, potassium carbonate, ammonium carbonate, sodium hydrogencarbonate, potassium hydrogencarbonate, ammonium hydrogencarbonate, aqueous ammonia, sodium hydroxide, potassium hydroxide and mixtures thereof;-所述共沉淀在0℃至90℃下进行;- the coprecipitation is carried out at 0 ° C to 90 ° C;-所述共沉淀过程中pH值为7.0至8.5;- the pH value during the coprecipitation is 7.0 to 8.5;-所述老化时间不低于1小时;- the aging time is not less than 1 hour;-所述煅烧在300℃至700℃下进行。- the calcination is carried out at 300 ° C to 700 ° C.
- 权利要求6所述的方法,其中在所述用于制备催化剂的方法的步骤(1)中,通过包括如下步骤的方法提供所述惰性载体限域的高分散金属氧化物材料:将催化活性金属的盐的水溶液与沉淀剂水溶液一起加入到硅氧烷基化合物中,并允许共沉淀和溶胶凝胶反应进行,然后将所得到的凝胶洗涤、干燥后煅烧,制得惰性载体限域的高分散金属氧化物材料。The method of claim 6, wherein in the step (1) of the method for preparing a catalyst, the inert carrier-limited high-dispersion metal oxide material is provided by a method comprising the steps of: catalytically active metal The aqueous solution of the salt is added to the siloxane-based compound together with the aqueous solution of the precipitating agent, and the coprecipitation and the sol-gel reaction are allowed to proceed, and then the obtained gel is washed, dried, and calcined to obtain a high inert carrier. Disperse metal oxide materials.
- 权利要求10所述的方法,其具有以下特征中至少之一:The method of claim 10 having at least one of the following features:-所述沉淀剂选自碳酸铵、氨水、碳酸氢铵、碳酸二氢铵、尿素和它们的混合物;The precipitating agent is selected from the group consisting of ammonium carbonate, aqueous ammonia, ammonium hydrogencarbonate, ammonium dihydrogen phosphate, urea, and mixtures thereof;-所述硅氧烷基化合物为正硅酸烷基酯,优选选自正硅酸甲酯、正硅酸乙酯、正硅酸正丙酯、正硅酸异丙酯、正硅酸正丁酯、正硅酸异丁酯、正硅酸叔丁酯和它们的混合物。- the siloxane-based compound is an alkyl orthosilicate, preferably selected from the group consisting of methyl orthosilicate, ethyl orthosilicate, n-propyl orthosilicate, isopropyl orthosilicate, n-butyl orthosilicate Ester, isobutyl orthosilicate, tert-butyl orthosilicate, and mixtures thereof.
- 权利要求1所述的方法,其中所述反应条件包括:320~400℃的反应温度,5.0~10.0MPa的反应压力,1:9~1:1的合成气中氢气与一氧化碳的摩尔比,0.5~3h -1的甲苯质量空速,和1000~4000h -1的标准状态下合成气体积空速。 The method of claim 1 wherein said reaction conditions comprise: a reaction temperature of from 320 to 400 ° C, a reaction pressure of from 5.0 to 10.0 MPa, a molar ratio of hydrogen to carbon monoxide in the synthesis gas of from 1:9 to 1:1, 0.5 Toluene mass space velocity of ~3h -1 , and syngas volume space velocity in the standard state of 1000-4000h -1 .
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