WO2005075072A1 - α,β−不飽和カルボン酸製造用触媒及びその製造方法、並びに、α,β−不飽和カルボン酸の製造方法 - Google Patents
α,β−不飽和カルボン酸製造用触媒及びその製造方法、並びに、α,β−不飽和カルボン酸の製造方法 Download PDFInfo
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- WO2005075072A1 WO2005075072A1 PCT/JP2005/001804 JP2005001804W WO2005075072A1 WO 2005075072 A1 WO2005075072 A1 WO 2005075072A1 JP 2005001804 W JP2005001804 W JP 2005001804W WO 2005075072 A1 WO2005075072 A1 WO 2005075072A1
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- Prior art keywords
- catalyst
- producing
- carboxylic acid
- unsaturated carboxylic
- pore volume
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Classifications
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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
- B01J29/064—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing iron group metals, noble metals or copper
- B01J29/068—Noble metals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/44—Palladium
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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
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
- B01J35/391—Physical properties of the active metal ingredient
- B01J35/393—Metal or metal oxide crystallite size
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
- B01J37/10—Heat treatment in the presence of water, e.g. steam
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- B01J37/16—Reducing
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
- C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
- C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
- C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C57/00—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms
- C07C57/02—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
- C07C57/03—Monocarboxylic acids
- C07C57/04—Acrylic acid; Methacrylic acid
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- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/18—Carbon
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/617—500-1000 m2/g
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
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- B01J35/635—0.5-1.0 ml/g
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- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/63—Pore volume
- B01J35/638—Pore volume more than 1.0 ml/g
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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
- B01J37/0201—Impregnation
- B01J37/0203—Impregnation the impregnation liquid containing organic compounds
Definitions
- the present invention relates to a catalyst for producing ⁇ -unsaturated carboxylic acid from liquid olefin or ⁇ / 3-unsaturated aldehyde by liquid phase oxidation, a method for producing the same, and a, ⁇ using the catalyst.
- the present invention relates to a method for producing a monounsaturated carboxylic acid.
- Acrylic acid ⁇ methacrylic acid is used in extremely large amounts for applications such as synthetic resin raw materials.
- methacrylic acid there are gas-phase oxidation method, liquid-phase oxidation method of isobutene, and method via acetone cyanohydrin, but these methods are not particularly advantageous. It is produced industrially.
- Catalysts and methods for obtaining ⁇ -unsaturated carboxylic acids by liquid phase oxidation of olefins or j3_unsaturated aldehydes with molecular oxygen have been actively studied.
- a method using a catalyst carrying gold Patent Document 1
- a method using a palladium metal catalyst Patent Documents 2-6)
- a method using a molybdenum compound and a palladium catalyst Patent Document 7
- Patent Documents 2 to 7 contain palladium as a catalyst component, but do not describe the particle diameter of nodium. Some of the catalysts described in Patent Documents 117 are supported on a carrier such as activated carbon, alumina, and silica. Regarding the physical properties of these carriers, Patent Document 1 only states that "hydrophobic carriers or those obtained by subjecting ordinary carriers to hydrophobizing treatment are preferred", and there is no reference to the physical properties of other carriers. Rena,
- Patent Document 1 JP 2001-172222 A
- Patent Document 2 JP-A-60-155148
- Patent Document 3 JP-A-60-139341
- Patent Document 4 JP-A-60-139643
- Patent Document 5 US Pat. No. 4,435,598
- Patent Document 6 International Publication No. 02/083299 pamphlet
- Patent Document 7 JP-A-56-59722
- Patent Literature 17 does not capture these polymers and oligomers, and the actual selectivity and yield of acrylic acid, including these by-products, are described in Examples of Patent Literature 117. It was found to be lower than what was done. As described above, the reaction results in the method for producing, -unsaturated carboxylic acids are not yet satisfactory, and further improvement has been desired.
- the present invention provides a catalyst capable of producing ⁇ -unsaturated carboxylic acid with good reaction performance from an olefin or a // 3-unsaturated aldehyde by liquid phase oxidation, a method for producing the same, and the catalyst. It is an object of the present invention to provide a method for producing ⁇ -unsaturated carboxylic acid. Means for solving the problem
- the present inventors have found that the catalyst properties are greatly affected by the physical properties of the carrier used in producing the catalyst, particularly the pore volume, and have reached the present invention. Further, the present inventors have found that particularly when palladium is used as a catalyst component, the catalytic performance is greatly affected by the particle size of palladium in the produced catalyst, and have reached the present invention.
- the catalyst for producing j3-unsaturated carboxylic acid according to the present invention is a catalyst for producing ⁇ -unsaturated carboxylic acid by liquid-phase oxidation from olefins or / 3-unsaturated aldehydes. Then, it is as follows.
- the method for producing a catalyst for producing an ⁇ , ⁇ -unsaturated carboxylic acid according to the present invention is the method for producing a catalyst for producing an ⁇ , ⁇ -unsaturated carboxylic acid according to the above [1], wherein the catalyst is used in the presence of the carrier.
- This is a method for producing a catalyst for producing ⁇ -unsaturated carboxylic acids by reducing metal compounds with a reducing agent.
- the method for producing a catalyst for producing a ⁇ -unsaturated carboxylic acid according to the present invention is the method for producing a catalyst for producing a ⁇ -unsaturated carboxylic acid according to the above [2], wherein This is a method for producing a catalyst for producing ⁇ -unsaturated carboxylic acids by reducing a palladium compound with a reducing agent.
- the process for producing j3-unsaturated carboxylic acid according to the present invention is characterized in that, in the presence of the catalyst for producing ⁇ -unsaturated carboxylic acid according to the above [1] or [2], This is a method for producing monounsaturated carboxylic acids in which aldehydes are oxidized in the liquid phase by molecular oxygen.
- a catalyst capable of producing an ⁇ , i3-unsaturated carboxylic acid from an olefin or an ⁇ , ⁇ -unsaturated aldehyde by liquid phase oxidation with good reaction results, a method for producing the same, and the catalyst And a method for producing ⁇ -unsaturated carboxylic acid using the same.
- the catalyst for the production of mono-unsaturated carboxylic acids of the present invention (hereinafter sometimes simply referred to as "catalyst") is an ⁇ , ⁇ -unsaturated carboxylic acid obtained by liquid phase oxidation from olefin or ⁇ , ⁇ monounsaturated aldehyde.
- a catalyst for producing an acid which is as follows.
- a catalyst for producing monounsaturated carboxylic acids characterized in that palladium having an average particle diameter in the range of 118 nm is supported on a carrier.
- an ⁇ , ⁇ -unsaturated carboxylic acid can be produced with good reaction results from olefins or ⁇ , ⁇ -unsaturated aldehydes by liquid phase oxidation.
- the catalysts of the present invention are, among other olefins, propylene and isobutylene, It is particularly effective in the liquid phase oxidation of acrolein and methacrolein among aldehydes.
- the catalyst of the present invention is a supported catalyst in which a metal is supported on a carrier.
- a metal is supported on a carrier.
- the support and the metal that can be used as the catalyst of the present invention will be described.
- activated carbon is a power produced by processes of carbonization, sizing, activation, washing, drying and pulverization.
- the production process is not particularly limited.
- Various raw materials such as coconut shell, coal, wood, and synthetic resin, which are not particularly limited, can also be used for the carbonaceous material that is the raw material of the activated carbon.
- the activation method is not particularly limited, and it can be activated using steam, carbon dioxide, oxygen, phosphoric acid, phosphate, zinc chloride, or the like.
- the activated carbon after activation is washed with a mineral acid, hydrochloric acid, water or the like, if necessary, dried, and then used.
- a mineral acid, hydrochloric acid, water or the like if necessary, dried, and then used.
- chlorine is likely to have an adverse effect on the catalytic performance, so it is preferable that chlorine is as small as possible. Therefore, it is preferable that the activated carbon produced using zinc chloride or hydrochloric acid be sufficiently washed to remove chlorine contained as much as possible.
- the shape of the activated carbon is not particularly limited, and various activated carbons such as powder, spherical, pellet, and fiber can be used.
- BET specific surface area of activated carbon is, 300 meters 2 / g or more preferably tool 600 meters 2 / g or more and particularly preferably les. Also, 4000 m 2 / g or less is preferred, and 2500 m 2 / g or less is particularly preferred.
- a carrier having a total pore volume of 0.4 to 1.5 cc / g measured by a nitrogen gas adsorption method is selected and used.
- the use of such a carrier makes it possible to produce highly unsaturated carboxylic acids from olefins or ⁇ -unsaturated aldehydes by liquid phase oxidation with high selectivity and high productivity.
- the configuration and the manufacturing method will be described.
- a carrier having a total pore volume of 0.40 to 0.80 cc / g it is more preferably 0.47 ccZg or more, more preferably 0.70 cc / g or less, and still more preferably 0.67 ccZg or less.
- acrylic acid and metal it is possible to obtain a target product such as vac acid with a good selectivity. It seems that by setting the total pore volume to a smaller range in the above range, by-products such as oligomers are suppressed, and the selectivity of the target product is further improved.
- the ratio of the pore volume of the mesopores having a pore diameter of 2 nm or more and 50 nm or less is preferably 40% or less of the total pore volume, more preferably 35% or less, and still more preferably 30% or less. It is particularly preferably at most 20%.
- the ratio of the pore volume of the mesopores is preferably 5% or more of the total pore volume, more preferably 7% or more, and further preferably 9% or more. In particular, in this case, if the pore volume is the same, the lower the ratio of the mesopore pores, the more difficult it is to produce by-products such as oligomers, so that the selectivity may be further improved.
- the BET specific surface area of the support is preferably 600 m 2 Zg or more, more preferably 800 m 2 / g or more, more preferably 2000 m 2 / g or less, and more preferably 1500 m 2 Zg or less.
- a carrier having a total pore volume of 0.70 to 1.50 cc / g it is more preferably 0.80 cc / g or more, still more preferably 0.90 cc / g or more, more preferably 1.4 cc / g or less, and still more preferably 1.3 cc / g or less.
- a carrier that satisfies such conditions it is possible to obtain target products having high catalytic activity, such as acrylic acid and methacrylic acid, with good productivity.
- the ratio of the pore volume of the mesopores having a pore diameter of 2 nm or more and 50 nm or less is preferably 10% or more of the total pore volume, more preferably 20% or more, and still more preferably 30% or more. It is particularly preferably at least 40%. Further, it is preferably at most 65%, more preferably at most 60%, further preferably at most 55%. In particular, in this case, if the pore volume is the same, the higher the ratio of the mesopores, the easier the diffusion in the pores becomes, so that the production efficiency may be further improved.
- the BET specific surface area force of the carrier is preferably 100 m 2 Zg or more, more preferably 300 m 2 Zg or more, more preferably 5000 m 2 Zg or less, more preferably 4000 m 2 / g or less.
- the total pore volume of the carrier, the pore volume of mesopores having a pore diameter of 2 nm or more and 50 nm or less, and the BET specific surface area are measured, for example, by an automatic specific surface area Z pore distribution measurement manufactured by Micromeritics. It can be measured by TriStar3000 (trade name) or the like.
- the metal supported on the carrier is not particularly limited as long as it functions as a catalyst for liquid phase oxidation, but palladium, which is preferably a noble metal, or palladium, which is more preferably gold, is particularly preferable.
- the metal may be one kind or two or more kinds. Further, it may contain a metal that does not function as a catalyst for liquid phase oxidation. From the viewpoint of catalytic activity, the amount of metal that does not function as a catalyst for liquid phase oxidation is preferably 50 atomic% or less.
- the catalyst of the present invention there is a catalyst in which palladium having an average particle diameter in a range of 118 nm is supported on a carrier.
- a catalyst capable of producing a / 3_unsaturated carboxylic acid from an a, j3_unsaturated aldehyde in a high yield can be obtained.
- the average particle diameter is preferably 1.2 nm or more, more preferably 1.4 nm or more.
- the average particle size is preferably 7 nm or less, more preferably 6 nm or less.
- the activity of the catalyst containing the same tends to decrease, and the yield of a, monounsaturated carboxylic acid tends to decrease.
- the catalyst may contain a metal other than palladium, but from the viewpoint of catalytic activity, the content of the metal other than nodium is preferably 50 atomic% or less.
- the above average particle size of palladium is a value obtained by measuring palladium in the catalyst by a transmission electron microscope, and is specifically a value calculated as follows.
- An observation image of a transmission electron microscope is printed out at the same magnification, and 50 points of palladium in the visual field are randomly picked up and each particle diameter is measured. Since the shape of the palladium area is almost circular, the measurement is performed by approximating that all areas are circular. Perform this operation for three fields of view and average the measured values to obtain the average particle size.
- the observation with a transmission electron microscope should be performed at an observation magnification that allows measurement of the particle size of palladium.
- the average particle diameter of palladium in the catalyst is determined by the type of the carrier used and the BET specific surface area, the type of the solvent used for preparing the catalyst and the mixing ratio in the case of the mixed solvent, Kind and concentration, temperature and time for reducing palladium compound, etc. Varies depending on various conditions. In the present invention, it is necessary that these conditions are appropriately selected and set, and that the average particle diameter of palladium in the obtained catalyst be within the above range.
- the method for producing the catalyst of the present invention is not particularly limited, but it is preferable to employ a method of reducing a metal compound with a reducing agent in the presence of a carrier.
- a solution of a metal compound in which a carrier is dispersed is prepared, and a reducing agent is added thereto to reduce the solution
- a liquid phase reduction method, a solution in which the solution of the metal compound is impregnated into the carrier is dried, It can be produced by a gas phase reduction method in which reduction is performed in a reducing atmosphere.
- the liquid phase reduction method is preferred.
- a method for producing a catalyst by the liquid phase reduction method will be described.
- metal compound to be used chloride, oxide, acetate, nitrate, sulfate, tetraammine complex, acetylacetonato complex or the like of a metal serving as a catalyst, Metals, oxides, acetates, nitrates or sulfates are more preferred, and chlorides, acetates or nitrates are more preferred. These can be used alone or in combination of two or more.
- the chlorine in the metal compound is preferably 100 ppm or less. That is, it is preferable to use a metal compound containing no chlorine, such as an acetate, a nitrate, and a bisacetyl acetonate complex.
- a metal compound containing no chlorine such as an acetate, a nitrate, and a bisacetyl acetonate complex.
- palladium is selected as the metal, for example, palladium acetate, palladium nitrate, bisacetylacetonato palladium can be suitably used.
- the solvent for dissolving the metal compound is appropriately selected depending on the solubility of the metal compound and the reducing agent, the dispersibility of the carrier, and the like, and includes water, alcohols, ketones, organic acids, hydrocarbons, or a mixture thereof. Two or more mixed solvents selected from the group can be used. As the solvent, one or more organic solvents selected from the group consisting of alcohols, ketones, and organic acids are preferred.
- a mixed solvent of an organic solvent and water is also preferably used because a catalyst with higher performance can be produced.
- a mixed solvent of an organic solvent and water a mixed solvent of one or more organic solvents selected from the group consisting of alcohols, ketones, and organic acids and water is preferred.
- a mixed solvent of water and one or more solvents selected from organic acids is preferred.
- the organic acids are preferably at least one selected from the group consisting of acetic acid, propionic acid, n-butyric acid, iso-butyric acid, n-valeric acid and iso-valeric acid.
- n-valeric acid or acetic acid is particularly preferred.
- the amount of water at that time is not particularly limited, but is preferably 5% by mass or more, more preferably 8% by mass or more, based on the mass of the mixed solvent. Further, the amount of water is preferably 60% by mass or less, more preferably 50% by mass or less, and still more preferably 40% by mass or less. In the case of a mixed solvent, it is desirable to be in a uniform state, but an uneven state is acceptable.
- the carrier and the metal compound are added to the solvent in a desired order or simultaneously in the solvent to prepare a solution of the metal compound in which the carrier is dispersed.
- the concentration of the metal compound is preferably at least 0.1% by mass, more preferably at least 0.2% by mass, and particularly preferably at least 0.5% by mass.
- the concentration of the metal compound is preferably 20% by mass or less, more preferably 10% by mass or less, further preferably 7% by mass or less, and particularly preferably 4% by mass or less.
- the metal compound solution in which the carrier is dispersed is reduced by adding a reducing agent to obtain a catalyst in which a metal is supported on the carrier.
- the reducing agent used is not particularly limited, as long as it has the ability to reduce the metal in the oxidized state in the metal compound.
- hydrazine, formaldehyde, sodium borohydride, hydrogen, formic acid, formic acid salts, alcohols, and olefins can be used.
- formaldehyde, propylene or isopropylene which is preferably at least one selected from the group consisting of honolemunorehdehyde, propylene, isobutylene, 1-butene and 2-butene, is more preferable.
- a metal compound solution in which the carrier is dispersed is charged into a pressurizing device such as an autoclave and the inside is pressurized with the reducing agent. It is preferable to adopt a method of performing reduction by The pressure is preferably 0.1- 1. OMPa (gauge pressure; hereinafter, all pressures are expressed as gauge pressures).
- the reduction can be performed by adding the reducing agent to a metal compound solution in which a carrier is dispersed.
- the amount of the reducing agent to be used is preferably about 115 mol per 1 mol of the metal compound.
- the temperature and reduction time of the system at the time of reduction vary depending on the reduction method, the carrier used, the metal compound, the solvent, the reducing agent and the like.
- the temperature is preferably 5 ° C or more, more preferably 0 ° C or more, and still more preferably 15 ° C or more.
- the reduction temperature is preferably 150 ° C. or less, more preferably 100 ° C. or less, and further preferably 80 ° C. or less.
- the reduction time is preferably 0.1 hour or more, more preferably 0.25 hour or more, and even more preferably 0.5 hour or more.
- the reduction time is preferably 24 hours or less, more preferably 4 hours or less, further preferably 3 hours or less, and particularly preferably 2 hours or less.
- the catalyst in which the metal is supported on the carrier is separated from the dispersion.
- this method is not particularly limited, for example, methods such as filtration and centrifugation can be used.
- the separated catalyst is appropriately dried.
- the drying method is not particularly limited, and various methods can be used.
- the concentration of the metal contained in the solution separated from the catalyst after the reduction is preferably 10 mg / l or less. This amount can be adjusted by the concentration of the metal compound before reduction, reduction conditions, and the like.
- the presence or absence of a metal in the solution can be easily confirmed by adding a reducing agent such as hydrazine, and the amount of the metal in the solution can be quantified by elemental analysis such as ICP.
- the metal loading of the catalyst is preferably 0.1% by mass or more, more preferably 0.5% by mass or more, and still more preferably 1% by mass or more, based on the carrier before being supported. Particularly preferably, it is at least 4% by mass.
- the metal loading of the catalyst is preferably 40% by mass or less, more preferably 30% by mass or less, still more preferably 20% by mass or less, and particularly preferably 15% by mass or less, based on the mass of the carrier before being supported. % By mass or less.
- the loading ratio can be determined from the mass of the carrier used for preparing the catalyst, the mass of the metal in the metal compound, and the mass of the metal contained in the solution separated from the catalyst after reduction.
- the catalyst thus produced may be used for the reaction in the form of a dispersion after washing with a solvent, or may be used for the reaction after separation by centrifugation or filtration.
- the catalyst may be activated before being subjected to the liquid phase oxidation.
- the method of activation is not particularly limited, and various methods can be used. As a method of activation, a method of heating under a reducing atmosphere in a hydrogen stream is preferable.
- ⁇ -unsaturated carboxylic acid is obtained by liquid phase oxidation from olefin or ⁇ -unsaturated aldehyde. A method for manufacturing the will be described.
- Examples of the olefin as a raw material for the liquid phase oxidation include propylene, isobutylene, 2-butene and the like.
- Examples of the ⁇ -unsaturated aldehyde as a raw material include acrolein, methacrolein, crotonaldehyde ( ⁇ -methylacrolein), cinnamaldehyde ( ⁇ -phenylacrolein) and the like.
- the raw material olefin or ⁇ , ⁇ -unsaturated aldehyde may contain a small amount of a saturated hydrocarbon and / or a lower saturated aldehyde as impurities.
- the ⁇ , ⁇ -unsaturated carboxylic acid produced by liquid phase oxidation is an ⁇ , ⁇ -unsaturated carboxylic acid having the same carbon skeleton as olefin when the raw material is olefin.
- the raw material is an ⁇ , ⁇ monounsaturated aldehyde
- it is an ⁇ , ⁇ monounsaturated carboxylic acid in which the aldehyde group of the ⁇ , ⁇ monounsaturated aldehyde is changed to a carboxy group.
- the catalyst of the present invention is suitable for liquid phase oxidation for producing acrylic acid, isobutylene or methacrolein methacrylic acid from propylene or acrolein.
- Air is economical as the molecular oxygen source used in the reaction, but pure oxygen or a mixed gas of pure oxygen and air can also be used. If necessary, air or pure oxygen can be replaced with nitrogen or nitrogen. A mixed gas diluted with carbon oxide, steam, or the like can also be used.
- the solvent used for the liquid phase oxidation is not particularly limited, but, for example, water; alcohols such as tert-butanol, cyclohexanol; ketones such as acetone, methyl ethyl ketone and methyl isobutyl ketone; Organic acids such as acetic acid, propionic acid, ⁇ -butyric acid, iso-butyric acid, n-valeric acid and iso-valeric acid; organic acid esters such as ethyl acetate and methyl propionate; Hydrocarbons such as xane, cyclohexane, and toluene, or a mixed solvent of two or more selected from these groups can be used. Among them, one or more solvents selected from the group consisting of alcohols, ketones, organic acids and organic acid esters are preferred, and C-C organic acids, tertiary butanol, and C-C Consists of ketones
- one selected from the group or a mixture thereof contains any of the more preferred tertiary butanol, acetic acid and n-valeric acid.
- the performance of the liquid phase oxidation reaction is further improved by using a mixed solvent of water with one or more solvents selected from the group consisting of alcohols, ketones, organic acids, and organic acid esters. Is preferred.
- the amount of water at this time is not particularly limited, but is preferably 2% by mass or more, more preferably 5% by mass or more, and preferably 70% by mass or less, more preferably 50% by mass, based on the mass of the mixed solvent. % By mass or less.
- the solvent is desirably uniform, but it may be used in a non-uniform state.
- the liquid phase oxidation reaction may be carried out in any of a continuous system and a batch system, but in view of productivity, the continuous system is industrially preferable.
- the amount of olefin or ⁇ , ⁇ monounsaturated aldehyde used as a raw material is usually at least 0.1 part by mass, preferably at least 0.5 part by mass, per 100 parts by mass of the solvent. Further, it is usually at most 20 parts by mass, preferably at most 10 parts by mass.
- the amount of molecular oxygen to be used is preferably at least 0.1 mol, more preferably at least 0.3 mol, per mol of olefin or ⁇ , ⁇ -unsaturated aldehyde as a raw material, Particularly preferably, it is at least 0.5 mol.
- the amount of the molecular oxygen used is preferably 30 mol or less, more preferably 25 mol or less, further preferably 20 mol or less, particularly preferably 15 monoles or less, and most preferably 10 mol or less. It is less than monole.
- the catalyst is used in a state of being suspended in a reaction solution for performing liquid phase oxidation, but may be used in a fixed bed.
- the amount of the catalyst used is preferably at least 0.1 part by mass, more preferably at least 0.5 part by mass, as the catalyst present in the reactor, based on 100 parts by mass of the solution present in the reactor, Particularly preferably, it is at least 1 part by mass.
- the amount of the catalyst used is preferably 30 parts by mass or less, more preferably 20 parts by mass or less, and particularly preferably 15 parts by mass or less.
- the reaction temperature and the reaction pressure are appropriately selected depending on the solvent and the reaction raw materials used.
- the reaction temperature is preferably 30 ° C. or higher, more preferably 50 ° C.
- the reaction temperature is preferably 200 ° C or lower, more preferably 150 ° C or lower.
- the reaction pressure is preferably at least atmospheric pressure (OMPa), more preferably at least 0.5 MPa, even more preferably at least 2 MPa, and preferably at most 10 MPa, more preferably at most 7 MPa, even more preferably at most 5 MPa. It is as follows.
- the raw materials and products were analyzed using gas chromatography.
- the reaction rate of the olefin or ⁇ -unsaturated aldehyde, the selectivity of the formed ⁇ -unsaturated aldehyde, the selectivity of the formed polymer 'oligomer, the formed , Selectivity, yield, and productivity are defined as follows.
- A is the number of moles of supplied olefin or ⁇ , ⁇ -unsaturated aldehyde
- ⁇ is the number of moles of reacted olefin or ⁇ , ⁇ -unsaturated aldehyde
- C is the number of ⁇ , ⁇ -unsaturated aldehydes formed.
- the number of moles, D is the number of moles of ⁇ , ⁇ -unsaturated carboxylic acid formed
- ⁇ is the olefin or ⁇ , ⁇ -unsaturated ⁇ , which supplied the total mass (unit: g) of the polymer and oligomer.
- Molecules of polymers and oligomers calculated as olefin or ⁇ -unsaturated aldehyde calculated by dividing by the molecular weight of aldehyde F is the mass of ⁇ , ⁇ -unsaturated carboxylic acid formed (unit: g), G is used The mass (unit: g) of the metal contained in the obtained catalyst, and H is the reaction time (unit: h).
- C / B 0 in the case of liquid-phase oxidation reaction of , / 3-unsaturated aldehyde.
- the pore volume and pore distribution of the carrier were measured by a constant volume method based on a nitrogen gas adsorption method using an automatic specific surface area Z pore distribution measuring device TriStar3000 (trade name) manufactured by Micromeritics.
- the pore diameter measurable by this method is in the range of about 11 lOOnm, and all pore volumes and pore distributions described in the present invention increase relative pressure (adsorption equilibrium pressure Z saturated vapor pressure). Calculated based on the change in the amount of nitrogen adsorption (adsorption isotherm)
- the total pore volume per unit mass of the carrier and the BET specific surface area were measured using the t-plot method.
- the pore volume of pores having a pore diameter of 2 nm or more and 50 nm or less was calculated using the BJH method, and the ratio to the total pore volume was calculated.
- the average particle diameter of palladium in the supported palladium-containing catalyst was measured by a transmission electron microscope. Specifically, the calculation was performed as follows. Observed images of the transmission electron microscope were printed out at the same magnification, and 50 points of palladium particles in the visual field were randomly picked up to measure the particle diameter of each. Since the shape of the palladium particles was almost circular, the measurement was performed by approximating that all of the particles were circular. This operation was performed for three visual fields, and the average of the measured values was taken as the average particle diameter.
- the temperature was raised to 50 ° C in 30 minutes, and reduction was performed for 30 minutes. After the reduction was completed, the resulting supported palladium catalyst was filtered, washed and replaced with an 88% by mass aqueous acetic acid solution, and filtered to obtain a supported palladium-containing catalyst having a loading of 10% by mass.
- Kuraray Chemical's coconut shell raw activated carbon (total pore volume is 0.49 cc / g, BE
- the catalyst was prepared in the same manner as in Example 1 except that the T specific surface area was 988 m 2 / g, and the ratio of the pore volume of mesopores having a pore diameter of 2 nm to 50 nm was 10% of the total pore volume. The reaction was evaluated.
- Total pore volume is 0.46 cc Zg, BET specific surface area is 753 m 2 Zg, and the ratio of pore volume of mesopore pores with a pore diameter of 2 nm to 50 nm is 33% of the total pore volume
- Catalyst preparation and reaction evaluation were performed in the same manner as in Example 1 except that) was used.
- activated carbon activated by Kuraray Chemical Co., Ltd. As a carrier, activated carbon activated by Kuraray Chemical Co., Ltd. (Total pore volume is 0.75 cc / g, BET specific surface area is 1613 m 2 / g, and the ratio of the pore volume of mesopores with a pore diameter of 2 nm to 50 nm is all pores. Catalyst preparation and reaction evaluation were performed in the same manner as in Example 1 except that 4.0% of the volume was used.
- activated carbon from Dainen Co., Ltd. As a carrier, activated carbon from Dainen Co., Ltd. (total pore volume is 0.92 cc / g, BET specific surface area is 1345 m 2 Zg, and the ratio of the pore volume of mesopores with a pore diameter of 2 nm or more and 50 nm or less is the percentage of the total pore volume.
- Catalyst preparation and reaction evaluation were carried out in the same manner as in Example 1 except that the reaction time was 11 minutes.
- Kuraray Chemical's synthetic raw material activated carbon As a carrier, Kuraray Chemical's synthetic raw material activated carbon (total pore volume is 1.27 cc / g, BET specific surface area is 2587 m 2 / g, and the percentage of the pore volume of mesopores with a pore diameter of 2 nm to 50 nm is all pores
- the catalyst was prepared and the reaction was evaluated in the same manner as in Example 1 except that the reaction time was 11 minutes.
- Activated charcoal made of Norit Co. as a carrier (Total pore volume is 1.30 cc / g, BET specific surface area is 1692 m 2 Zg, and the ratio of the pore volume of mesopore pores with a pore diameter of 2 nm to 50 nm is the total pore volume.
- the catalyst was prepared and the reaction was evaluated in the same manner as in Example 1 except that the reaction time was 15 minutes.
- Activated carbon from Coal Co., Ltd. manufactured by Kansai Thermochemical Co., Ltd. Total pore volume is 1.61 cc / g, BET specific surface area is 3174 m 2 / g, and the ratio of the pore volume of mesopore pores with a pore diameter of 2 nm to 50 nm is all pores.
- Catalyst preparation and reaction evaluation were performed in the same manner as in Example 1 except that 35% of the volume) was used.
- Total pore volume is 1.61 cc / g
- BET specific surface area is 1680 m 2 Zg
- the ratio of the pore volume of mesopore pores with a pore diameter of 2 nm or more and 50 nm or less is the percentage of the total pore volume.
- Activated carbon manufactured by Kuraray Chemical Co., Ltd. (with a total pore volume of 0.37 cc / g, a BET specific surface area of 690 m 2 / g, and a percentage of the pore volume of mesopores with a pore diameter of 2 nm or more and 50 nm or less A catalyst was prepared and reacted in the same manner as in Example 1 except that 2.7% of the volume) was used.
- Table 1 shows a list of physical properties and reaction results of the carriers used in Example 17 and Comparative Examples 13 to 13.
- Example 17 using a carrier having a total pore volume of 0.40 to 1.50 cc / g it was found that the selectivity and productivity of methacrylic acid were good.
- Examples 14 to 14 using a carrier having a small total pore volume it was found that methacrylic acid selectivity was particularly good.
- Example 57 using a carrier having a large total pore volume it was found that the productivity of methacrylic acid was particularly good.
- Total pore volume 0. 68ccZg BET specific surface area of 450m 2 Zg, 100% of the percentage total pore volume of the pore volume of pore diameter 2nm or 50nm or less mesopore pore) Caro forte acetic acid solution to 1 000 parts After shaking, evaporation was performed. Thereafter, baking was performed in air at 450 ° C. for 3 hours. The obtained catalyst precursor was added to 13 parts of a 37% by mass aqueous formaldehyde solution.
- the mixture was heated to 70 ° C., stirred and maintained for 2 hours, suction-filtered, and filtered and washed with water and a 75% by mass / butanol aqueous solution to obtain a supported palladium-containing catalyst having a loading of 5% by mass.
- the total amount of the catalyst (10.5 parts) obtained by the above method 100 parts of a 75% by mass aqueous solution of t-butanol, and 0.02 parts of p-methoxyphenol were placed in an autoclave, and the autoclave was sealed. Next, 2.75 parts of isobutylene were introduced, stirring was started (rotation speed: 100 rpm), and the temperature was raised to 90 ° C. After the temperature was raised, nitrogen was introduced into the autoclave to an internal pressure of 2.3 MPa, and then compressed air was introduced to an internal pressure of 4.6 MPa. When the internal pressure dropped to 0. IMPa during the reaction, the operation of introducing oxygen to raise the internal pressure to 0. IMPa was repeated 10 times.
- the reaction was terminated when the internal pressure decreased by 0. IMPa.
- the reaction time at this time was 56 minutes.
- the amount of molecular oxygen used in the oxidation reaction was 3.48 mol per 1 mol of isobutylene.
- the inside of the autoclave was ice-cooled in an ice bath.
- a gas collection bag was attached to the gas outlet of the autoclave, the gas outlet was opened, and the pressure inside the reactor was released while recovering gas coming out.
- the reaction solution containing the catalyst was taken out of the autoclave, the catalyst was separated by a membrane filter, and the reaction solution was recovered.
- the collected reaction solution and the collected gas were analyzed by gas chromatography, and the reaction rate and selectivity were calculated.
- the carrier used is a Y-type zeolite (silica / alumina (Si ⁇ / Al 2 O 3) molar ratio 200)
- Example 8 except that the total pore volume was changed to 0.50 cc Zg, the BET specific surface area was 629 m 2 Zg, and the ratio of the pore volume of mesopores having a pore diameter of 2 nm to 50 nm was 42% of the total pore volume.
- a palladium metal-supported Y-type zeolite-supported palladium-containing catalyst was obtained.
- the reaction was carried out in the same manner as in Example 8 except that the reaction time was 38 minutes using the catalyst obtained above. At this time, the conversion of isobutylene was 75.2%, the selectivity of methacrolein was 49.9%, the selectivity of methacrylic acid was 19.0%, and the productivity of methacrylic acid was 1.9 g / (g′h).
- the carrier used is H_ZSM_5 type with a silica / alumina (Si ⁇ / Al 2 O 3) molar ratio of 485.
- Table 2 shows a list of physical properties and reaction results of the carriers used in Examples 8 and 9 and Comparative Example 4. In Examples 8 and 9 using a carrier having a total pore volume of 0.40 to 1.50 cc / g, it was found that the selectivity and the productivity of methacrylic acid were good. [0093] [Table 2]
- the average particle diameter of palladium in the obtained palladium-containing supported catalyst was 1.5 nm (transmission electron microscope observation magnification: 1,000,000 times).
- An autoclave equipped with a stirrer was charged with 69 parts of an aqueous 88% by mass acetic acid solution containing 200 ppm of P-methoxyphenol and 3 parts of the above-mentioned supported catalyst containing palladium. Further, 2.5 parts of methacrolein were added to the mixture. After sealing the autoclave, stirring was started at a stirring rotation speed of 820 rpm, and the temperature was raised to 90 ° C by a heater. When the temperature reached 90 ° C., air was introduced to 3.2 MPa, and the air was maintained for 20 minutes (reaction time). The amount of molecular oxygen used in the oxidation reaction was 0.77 mol per 1 mol of methacrolein.
- the resultant was cooled to 20 ° C.
- an absorption tube containing cold water and a gas collection bag were installed in this order. Open the gas outlet and recover the gas pressure while Was released.
- the reaction solution was transferred to a centrifuge tube, and the catalyst was precipitated by centrifugation. The supernatant was collected by passing through a PTFE membrane filter (pore size: 0.5 / im).
- the methacrolein conversion was 93.6%
- the methacrylic acid selectivity was 79.9%
- the polymer oligomer selectivity was 8.5%
- the methacrylic acid yield was 74.8%.
- Activated carbon produced from coconut shell raw material (Total pore volume is 0.49 cc / g, BET specific surface area is 9
- a catalyst was prepared in the same manner as in Example 10, except that the ratio of the pore volume of mesopores having a pore size of 88 m 2 / g and a pore size of 2 nm to 50 nm was 10% of the total pore volume).
- the average particle size of palladium in the obtained palladium-containing supported catalyst (supporting rate: 10% by mass) was 2.6 nm (observation magnification of transmission electron microscope: 300,000 times).
- a catalyst was prepared in the same manner as in Example 10, except that a 96% by mass aqueous acetic acid solution was used as a catalyst preparation solvent.
- the average particle size of palladium in the obtained palladium-containing supported catalyst was 8.4 nm (observation magnification of transmission electron microscope: 300,000 times).
- a catalyst was prepared in the same manner as in Example 10 except that n-valeric acid was used as a catalyst preparation solvent.
- the average particle diameter of palladium in the obtained palladium-containing supported catalyst was 10.1 nm (observation magnification of transmission electron microscope: 300,000 times).
- Example 7 A catalyst was prepared in the same manner as in Example 10, except that the amount of palladium acetate was 0.11 part, the reduction temperature was 25 ° C, and the reduction time was 18 hours.
- the average particle diameter of palladium in the obtained palladium-containing supported catalyst (loading rate: 10% by mass) was 0.8 nm (transmission electron microscope observation magnification: 1,000,000 times).
- the reaction was evaluated in the same manner as in Example 10 except that the methacrolein reaction time was changed to 3 hours. As a result, the methacrolein reaction rate was 42.5%, the methacrylic acid selectivity was 59.8%, and the polymer 'oligomer' was used. The selectivity was 29.6% and the methacrylic acid yield was 25.4%.
- Table 3 shows a list of average particle diameters and reaction results of palladium in the catalysts used in Examples 10 and 11 and Comparative Examples 5-7. In Examples 10 and 11 using a catalyst having an average particle diameter of palladium of 118 nm, it was found that the yield of methacrylic acid was high.
- ⁇ -unsaturated carboxylic acid can be produced with good reaction results from orefin or / 3 / unsaturated aldehyde by liquid phase oxidation. I understood.
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KR1020117026712A KR101264031B1 (ko) | 2004-02-10 | 2005-02-08 | α,β-불포화 카복실산 제조용 촉매 및 그의 제조방법, 및 α,β-불포화 카복실산의 제조방법 |
US10/588,973 US20070173662A1 (en) | 2004-02-10 | 2005-02-08 | Catalyst for producing alpha, beta-unsaturated carboxylic acid and method for preparation thereof, and method for producing alpha, beta-unsaturated carboxylic acid |
CN200580004222XA CN1917956B (zh) | 2004-02-10 | 2005-02-08 | α,β-不饱和羧酸制造用催化剂及其制造方法,以及α,β-不饱和羧酸的制造方法 |
KR1020067018400A KR101154764B1 (ko) | 2004-02-10 | 2005-02-08 | α,β-불포화 카복실산 제조용 촉매 및 그의 제조방법, 및α,β-불포화 카복실산의 제조방법 |
US12/388,917 US7884239B2 (en) | 2004-02-10 | 2009-02-19 | Catalyst for producing α,β-unsaturated carboxylic acid and method for preparation thereof, and method for producing α,β-unsaturated carboxylic acid |
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US12/388,917 Division US7884239B2 (en) | 2004-02-10 | 2009-02-19 | Catalyst for producing α,β-unsaturated carboxylic acid and method for preparation thereof, and method for producing α,β-unsaturated carboxylic acid |
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KR101183773B1 (ko) * | 2005-02-18 | 2012-09-17 | 미츠비시 레이온 가부시키가이샤 | 팔라듐 함유 촉매, 그 제조 방법 및 α,β-불포화카르복실산의 제조 방법 |
KR101489010B1 (ko) * | 2006-12-28 | 2015-02-02 | 미츠비시 레이온 가부시키가이샤 | 팔라듐 함유 금속 담지 촉매의 재생 처리 방법, 팔라듐 함유 금속 담지 촉매 및 그 제조방법 |
WO2013017904A1 (en) * | 2011-07-29 | 2013-02-07 | Arkema France | Improved process of dehydration reactions |
KR20140053209A (ko) * | 2011-07-29 | 2014-05-07 | 닛뽄 가야쿠 가부시키가이샤 | 글리세린의 탈수 반응에 의한 아크롤레인 및 아크릴산의 제조용 촉매와, 그의 제조법 |
DE102012008170A1 (de) * | 2012-04-26 | 2013-10-31 | Entex Rust & Mitschke Gmbh | Planetwalzenextruder mit Planetspindeln und Anlaufring |
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- 2005-02-08 KR KR1020067018400A patent/KR101154764B1/ko active IP Right Grant
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US7884239B2 (en) | 2011-02-08 |
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