JP2022048658A - Method for recycling catalyst for alcohol production - Google Patents

Abstract

To provide a method for stably producing alcohol for a long time, capable of reusing a degraded catalyst for alcohol production with reduced activity or alcohol selectivity in the production of alcohol by hydration reaction of an olefin with a solid acid catalyst having heteropoly acid or a salt thereof supported on a carrier.SOLUTION: A catalyst for alcohol production with reduced activity or alcohol selectivity is recycled with a recycling gas containing water vapor in a temperature range of 150-350°C.SELECTED DRAWING: None

Description

The present invention relates to a method for regenerating a catalyst for producing an alcohol by a hydration reaction of an olefin.

Industrial ethanol is an important industrial chemical product widely used as an intermediate for organic solvents, organic synthetic raw materials, disinfectants, chemicals and the like. Industrial ethanol is a liquid acid such as sulfuric acid or sulfonic acid, a zeolite catalyst, a metal oxide catalyst containing tungsten, niobium, tungstic acid or the like, or a heteropolyacid or phosphoric acid such as phosphotungstic acid or silicotungstic acid as a silica carrier. It is known that it can be obtained by a hydration reaction of ethylene in the presence of a solid acid catalyst supported on a diatomaceous earth carrier or the like. In particular, a process using a solid catalyst in which phosphoric acid is supported on a carrier is industrially carried out. However, it has been reported that the yield or selectivity of alcohol gradually decreases with the reaction time in catalysts such as zeolite and heteropolyacid, and the short catalyst life has become a problem (Non-Patent Documents 1 and 2). ). Patent Documents 1 and 2 describe improved heteropolyacidic catalysts, but their lifetimes have not been sufficiently evaluated, and these catalysts have not reached the level of industrial use.

Japanese Unexamined Patent Publication No. 8-192047 Japanese Patent Application Laid-Open No. 8-225473

Industrial Chemistry Magazine Vol. 69, No. 10, pp. 32-32, 1966 Journal of the Petroleum Society, April 1963, pp. 336-341

When the yield of the target alcohol decreases, it is generally practiced to gradually raise the reaction temperature for the purpose of maintaining the catalytic activity. However, the acid catalyst used as a catalyst for producing alcohol is sensitive to heat, and if the reaction temperature is set too high, the catalyst is decomposed, resulting in rapid deterioration of the catalyst. Therefore, from the viewpoint of extending the life of the catalyst and stable reaction over a long period of time, an effective regeneration method of the catalyst is strongly desired.

As a method for regenerating a catalyst, a method of burning and removing a carbon component adhering to a deteriorated catalyst at a high temperature using an oxygen-containing gas is generally known. However, this method is not suitable because the catalyst for alcohol production has low thermal stability. Further, in the industrial process, it is not practical to change the temperature from the reaction temperature every time the regeneration process is performed, because it takes time and effort, a loss of operating time occurs, and additional equipment is required. A regeneration process that can be performed at a temperature that is the same as the reaction temperature is desirable in an actual industrial process.

The present invention reuses a deteriorated alcohol production catalyst having reduced activity or alcohol selectivity in the production of alcohol by a hydration reaction of an olefin using a solid acid catalyst in which a heteropolyacid or a salt thereof is supported on a carrier. It is possible and an object of the present invention is to provide a method for stably producing alcohol over a long period of time.

As a result of diligent studies, the present inventors have found that in the production of alcohol by the hydration reaction of olefins performed in the gas phase, the catalyst deteriorates due to the adhesion of the carbon component to the catalyst surface, and the activity of the catalyst and the alcohol The present invention has been completed by finding that the selectivity can be restored by treating a catalyst deteriorated with a regenerating gas containing water vapor under temperature and pressure conditions close to the reaction conditions.

That is, the present invention relates to the following [1] to [7].
[1]
A method for regenerating an alcohol production catalyst, which comprises treating an alcohol production catalyst having reduced activity or alcohol selectivity with a regeneration gas containing water vapor within a temperature range of 150 to 350 ° C., wherein the alcohol is produced. The production catalyst is used for producing alcohol by supplying water and an olefin having 2 to 5 carbon atoms to a reactor and hydrating them in the gas phase, and the heteropolyacid or a salt thereof is used. A method for regenerating a catalyst for producing alcohol, which is a solid acid catalyst supported on a carrier.
[2]
The method for regenerating an alcohol production catalyst according to [1], wherein the regenerating gas is a mixed gas containing an inert gas and water vapor.
[3]
The method for regenerating an alcohol-producing catalyst according to any one of [1] or [2], wherein the partial pressure of water vapor in the regenerating gas is 0.01 to 1 MPa.
[4]
The method for regenerating an alcohol-producing catalyst according to any one of [1] to [3], wherein the treatment with the regenerating gas is performed in the reactor without removing the alcohol-producing catalyst from the reactor.
[5]
The heteropolyacid is at least one compound selected from the group consisting of silicotungstic acid, phosphotungstic acid, phosphomolybdic acid, phytomolybdic acid, cavanadotungstic acid, limbanadotungstic acid and limbanadomolybdic acid [1]. The method for regenerating a catalyst for producing alcohol according to any one of [4].
[6]
The method for regenerating an alcohol-producing catalyst according to any one of [1] to [5], wherein the carrier is silica.
[7]
The method for regenerating an alcohol-producing catalyst according to any one of [1] to [6], wherein the olefin having 2 to 5 carbon atoms is ethylene and the alcohol is ethanol.

According to the present invention, in the production of alcohol by a hydration reaction of an olefin using a solid acid catalyst in which a heteropolyacid or a salt thereof is supported on a carrier, a deteriorated catalyst for alcohol production having reduced activity or alcohol selectivity can be used. It is reusable and can stably produce alcohol for a long period of time.

It is a graph which shows the time-dependent change of the ethylene conversion rate in Example 1 and Comparative Example 1. It is a graph which shows the time-dependent change of the ethanol selectivity in Example 1 and Comparative Example 1.

Hereinafter, preferred embodiments of the present invention will be described, but it should be understood that the present invention is not limited to these embodiments and can be applied in various ways within the spirit and practice thereof.

(Catalyst for alcohol production)
In one embodiment, a solid acid catalyst in which a heteropolyacid or a salt thereof (also referred to as “heteropolylate” in the present disclosure) is supported on a carrier is used as a catalyst for alcohol production.

(Heteropolyacid, heteropolyate)
Heteropolyacids are composed of a central element and peripheral elements to which oxygen is bound. The central element is usually silicon or phosphorus, but can consist of any one selected from a variety of Group 1 to Group 17 elements in the Periodic Table of the Elements. Specifically, for example, ferric ion; divalent beryllium, zinc, cobalt or nickel ion; trivalent boron, aluminum, gallium, iron, cerium, arsenic, antimony, phosphorus, bismuth, chromium or rhodium. Ions; tetravalent silicon, germanium, tin, titanium, zirconium, vanadium, sulfur, tellurium, manganese, nickel, platinum, thorium, hafnium, cerium ions and other rare earth ions; pentavalent phosphorus, arsenic, vanadium, antimony Ions; hexavalent tellurium ions; and arsenic iodine ions can be mentioned, but are not limited thereto. Specific examples of peripheral elements include, but are not limited to, tungsten, molybdenum, vanadium, niobium, tantalum and the like.

Such heteropolyacids are also known as "polyoxoanions", "polyoxometal salts" or "metal oxide clusters". Some of the well-known structures of anions are named after the researchers in this field, for example, Keggin-type structures, Wells-Dawson-type structures. And Anderson-Evans-Perloff type structures are known. Details are described in "Chemistry of Polyacids" (edited by The Chemical Society of Japan, Quarterly Chemistry Review No. 20, 1993). Heteropolyacids usually have a high molecular weight, eg, a molecular weight in the range of 700-8500, and include not only their monomers but also dimeric complexes.

The heteropolyate is not particularly limited as long as it is a metal salt or an onium salt in which a part or all of the hydrogen atom of the heteropolyacid is substituted. Specific examples thereof include, but are not limited to, metal salts of lithium, sodium, potassium, cesium, magnesium, barium, copper, gold and gallium, and onium salts such as ammonia.

Heteropolyacids have a relatively high solubility in polar solvents such as water or other oxygenated solvents, especially if the heteropolyacid is a free acid and some salts. Their solubility can be controlled by selecting the appropriate counterion.

Examples of heteropolyacids that can be used as catalysts are silicate tungstic acid H ₄ [SiW ₁₂ O ₄₀ ] · xH ₂ O.
Phosphor Tungstic Acid H ₃ [PW ₁₂ O ₄₀ ] · xH ₂ O
Phosphomolybic acid H ₃ [PMo ₁₂ O ₄₀ ] · xH ₂ O
Molybdate molybdate H ₄ [SiMo ₁₂ O ₄₀ ] · xH ₂ O
Keibanado Tungstic Acid H _{4 + n} [SiV _n W _12-n O ₄₀ ] · xH ₂ O
Limbanad Tungstic Acid H _{3 + n} [PV _n W _12-n O ₄₀ ] · xH ₂ O
Limbanado molybdic acid H _{3 + n} [PV _n Mo _12-n O ₄₀ ] · xH ₂ O
Keibanado molybdic acid H _{4 + n} [SiV _n Mo _12-n O ₄₀ ] · xH ₂ O
Keimoribdo Tungstic Acid H ₄ [SiMon W _{12-n O 40} ] · xH ₂ O
Phosphoribd Tungstic Acid H ₃ [PMon W _{12-n O 40} ] · xH ₂ O
(In the formula, n is an integer of 1 to 11 and x is an integer of 1 or more.)
However, it is not limited to these.

The heteropolyacid is preferably silicotung acid, phosphotungnic acid, phosphomolybdic acid, phytomolybdic acid, cayvanadotungstate, limbanadotungstate, or limbanadomolybdic acid, and is preferably phytonicic acid, phosphotungnic acid, or caiba. More preferably, it is nadtungstate or limbanadtungnic acid.

The method for synthesizing such a heteropolyacid is not particularly limited, and any method may be used. For example, a heteropolyacid can be obtained by heating an acidic aqueous solution (about pH1 to pH2) containing a salt of molybdenum acid or tungsten acid and a simple oxygen acid of a heteroatom or a salt thereof. The heteropolyacid compound can be isolated by crystallization separation as a metal salt from, for example, the produced heteropolyacid aqueous solution. A specific example of the production of heteropolyacids is 1413 of "New Experimental Chemistry Course 8 Synthesis of Inorganic Compounds (III)" (edited by The Chemical Society of Japan, published by Maruzen Co., Ltd., August 20, 1984, 3rd edition). It is described on the page, but is not limited to this. The structure of the synthesized heteropolyacid can be confirmed by X-ray diffraction, UV, or IR measurement in addition to chemical analysis.

Preferred examples of the heteropolylate salt include lithium salt, sodium salt, potassium salt, cesium salt, magnesium salt, barium salt, copper salt, gold salt, gallium salt, ammonium salt and the like of the above-mentioned preferred heteropolyacid.

Specific examples of the heteropolymate include lithium silicate of silicate, sodium salt of silicate, cesium salt of cesium, copper salt of silicate, gold salt of silicate, and gallium salt of silicate. Lithium salt of phosphotung acid, sodium salt of phosphotung acid, cesium salt of phosphotung acid, copper salt of phosphotung acid, gold salt of phosphotung acid, gallium salt of phosphotung acid; lithium salt of phosphomolydic acid, Sodium salt of phosphomolybdic acid, cesium salt of phosphomolybdic acid, copper salt of phosphomolybdic acid, gold salt of phosphomolybdic acid, gallium salt of phosphomolybdic acid; lithium salt of silicate molybdic acid, sodium salt of silicate molybdic acid, kay. Cesium salt of molybdenum acid, copper salt of silicate molybdenum acid, gold salt of silicate molybdic acid, gallium salt of silicate molybdic acid; lithium salt of keibanado tungstate, sodium salt of keibanado tungstate, cesium salt of keibanado tungstate , Copper salt of cavanado tungsten acid, gold salt of cavanado tungsten acid, gallium salt of cavanado tungsten acid; lithium salt of limbanado tungstate, sodium salt of limbanado tungstate, cesium salt of limbanado tungstate, limba Copper salt of nadtungstate, gold salt of limbanadotungstate, gallium salt of limbanadotungstate; lithium salt of limbanadomolybdic acid, sodium salt of limbanadomolybdenum, cesium salt of limbanadomolybdenum, limbanadomolybdenum Copper salt of acid, gold salt of limbanado molybdenum acid, gallium salt of limbanado molybdenum acid; lithium salt of keibanado molybdenum acid, sodium salt of keibanado molybdenum acid, cesium salt of keibanado molybdenum acid, cesium salt of keibanado molybdenum acid Examples thereof include a copper salt, a gold salt of cayvanado molybdenum acid, and a gallium salt of cavanado molybdic acid.

Heteropolylates are lithium salt of siltytung acid, sodium salt of caytungic acid, cesium salt of caytung acid, copper salt of caytungic acid, gold salt of caytung acid, gallium salt of caytung acid; phosphotung acid. Lithium salt, sodium phosphotung acid salt, cesium salt of phosphotung acid, copper salt of phosphotung acid, gold salt of phosphotung acid, gallium salt of phosphotung acid; lithium salt of phosphomolydic acid, phosphomolybdic acid Sodium salt, cesium salt of phosphomolybdic acid, copper salt of phosphomolybdic acid, gold salt of phosphomolybdic acid, gallium salt of phosphomolybdic acid; lithium salt of silicate molybdic acid, sodium salt of silicate molybdic acid, cesium of silicate molybdic acid Salt, copper salt of cay molybdic acid, gold salt of cay molybdic acid, gallium salt of cay molybdic acid; lithium salt of cayvanado tung acid, sodium salt of cavanado tung acid, cesium salt of cavanado tung acid, cay vanado tungsten Copper salt of acid, gold salt of cayvanado tungstate, gallium salt of cavanado tungstate; lithium salt of limbanado tungstate, sodium salt of limbanado tungstate, cesium salt of limbanado tungstate, limbanado tungstate Copper salt, gold salt of limbanado tungstate, gallium salt of limbanado tungstate; lithium salt of limbanado molybdic acid, sodium salt of limbanado molybdenum, cesium salt of limbanado molybdenum, copper salt of limbanado molybdenum , Gold salt of limbanado molybdenum acid, gallium salt of limbanado molybdenum acid; lithium salt of cybanado molybdenum acid, or sodium salt of cyvanado molybdenum acid is preferable.

Heteropolylates are lithium salt of siltytung acid, sodium salt of caytung acid, cesium salt of caytung acid, copper salt of caytungic acid, gold salt of caytung acid, gallium salt of caytung acid; phosphotung acid. Lithium salt, sodium phosphotung acid salt, cesium salt of phosphotung acid, copper salt of phosphotung acid, gold salt of phosphotung acid, gallium salt of phosphotung acid; lithium salt of cayvanado tung acid, cayvanado tungsten Sodium acid salt, cesium salt of cayvanado tung acid, copper salt of cavanado tung acid, gold salt of cavanado tung acid, gallium salt of cavanado tung acid; lithium salt of limbanado tung acid, of limbanado tung acid More preferably, it is a sodium salt, a cesium salt of limbanado tungstate, a copper salt of limbanado tungstate, a gold salt of limbanado tungstate, or a gallium salt of limbanado tungstate.

It is particularly preferable to use a lithium salt of silicotungstic acid or a cesium salt of phosphotungstic acid as the heteropolymate.

(Carrier)
Heteropolyacids or heteropolylates are used by supporting them on a carrier. The carrier is preferably at least one selected from the group consisting of silica, diatomaceous earth, titania, activated carbon, alumina, and silica-alumina, and more preferably silica.

(Silica carrier)
Generally, synthetic amorphous silica is produced by either a dry method or a wet method. The combustion method of burning silicon tetrachloride in a hydrogen flame in the presence of oxygen is classified as a dry method, and the growth of primary particles is suppressed by advancing the neutralization reaction of sodium silicate and mineral acid in the acidic pH range. A gel method that causes aggregation in the state of being in the state, a sol-gel method that hydrolyzes alkoxysilane, and ion exchange of sodium silicate to prepare active silicic acid, and then particle growth in a seed particle-containing aqueous solution whose pH is adjusted under heating. The water glass method for hydrolyzing is classified as a wet method. The silica obtained by the combustion method is fumed silica gel, the silica obtained by the gel method is silica gel, and the silica obtained by dispersing the silica particles obtained by the sol-gel method and the water glass method in a medium such as water is colloidal silica, respectively. It is commonly called.

The silica carrier of one embodiment is obtained by kneading fumed silica obtained by a combustion method, silica gel obtained by a gel method, and colloidal silica obtained by a sol-gel method or a water glass method to form a kneaded product. Then, it can be obtained by firing the molded product.

When fumed silica, silica gel, and colloidal silica are kneaded, molded, and fired, the size of the primary and secondary particles of the silica carrier after firing depends on the mixing ratio of each component, kneading method, firing conditions, and the like. Since the internal state of the porous body changes, the higher-order structure of the silica carrier cannot be specified. The composition formula of the silica carrier is SiO ₂ .

There are no restrictions on fumed silica, and general fumed silica can be used. Examples of commercially available fumed silica include Aerosil (trademark) manufactured by Nippon Aerosil Co., Ltd., Leolosil (trademark) manufactured by Tokuyama Corporation, CAB-O-SIL (trademark) manufactured by Cabot Corporation, and the like. Can be done. There are hydrophilic and hydrophobic grades of fumed silica on the market, but any of them can be used. A typical fumed silica has, for example, a primary particle diameter of 7 to 40 nm and a specific surface area of 50 to 500 m ² / g as physical properties, is not porous but has no internal surface area and is amorphous, and has purity as silicon oxide. Is as high as 99% or more, and has a feature that it contains almost no metal or heavy metal.

There are no restrictions on silica gel, and general silica gel can be used. Examples of commercially available silica gel include NIPGEL manufactured by Tosoh Silica Co., Ltd., MIZUKASIL manufactured by Mizusawa Industrial Chemical Ltd., CARiACT manufactured by Fuji Silysia Chemical Ltd., and Sunsphere manufactured by AGC SI-Tech Co., Ltd. Can be done. Generally, silica gel is prepared by using sodium silicate obtained by dissolving silica gel (SiO ₂ ) and soda ash (Na ₂ CO ₃ ) in water and dissolving sodium silicate glass (cullet) in water. It is produced by gelling the entire reaction solution by reacting with a mineral acid such as silica gel under acidic conditions and causing aggregation while suppressing the growth of primary particles. The physical characteristics of silica gel are not particularly limited, but silica gel has the characteristics that the primary particles are small, the specific surface area is high, and the secondary particles are hard. As examples of specific physical properties of silica gel, the BET specific surface area is 200 to 1000 m ² / g, the secondary particle diameter is 1 to 30 μm, and the pore volume by the nitrogen gas adsorption method (BJH method) is 0.3 to 2. It is mentioned that it is 5 mL / g. The higher the purity of silica gel, the more preferable, and the preferable purity is 95% by mass or more, more preferably 98% by mass or more.

Colloidal silica is not particularly limited, and general colloidal silica can be used. Examples of commercially available colloidal silica include Snowtex (trademark) manufactured by Nissan Chemical Industries, Ltd., silica doll manufactured by Nippon Chemical Industrial Co., Ltd., Adeleite manufactured by ADEKA Co., Ltd., and CAB-O-SIL manufactured by Cabot Corporation. (Trademark) TG-C colloidal silica, Quattron (trademark) manufactured by Fuso Chemical Industries, Ltd. and the like can be mentioned. Colloidal silica is silica fine particles dispersed in a medium such as water. As a method for producing colloidal silica, there are a water glass method and a sol-gel method by hydrolysis of alkoxysilane, and colloidal silica produced by either method can be used. Colloidal silica produced by the water glass method and colloidal silica produced by the sol-gel method may be used in combination. Typical physical properties of colloidal silica include a particle size of 4 to 80 nm and a solid content concentration of silica dispersed in water or an organic solvent of 5 to 40% by mass. The concentration of impurities in colloidal silica may affect the catalytically active component carried, so a lower concentration is desirable. The silica purity in the solid content is preferably 99% by mass or more, more preferably 99.5% by mass or more.

The silica carrier can be obtained by kneading fumed silica, silica gel, and colloidal silica, molding the obtained kneaded product, and then firing the molded product. Appropriate additives may be added during kneading. The blending ratio of fumed silica, silica gel, and colloidal silica is preferably 5 to 50 parts by mass of fumed silica, 40 to 90 parts by mass of silica gel, and 5 to 30 parts by mass of solid content of colloidal silica. More preferably, it is 15 to 40 parts by mass of fumed silica, 45 to 70 parts by mass of silica gel, and 5 to 15 parts by mass of solid content of colloidal silica.

When mixing fumed silica, silica gel, and colloidal silica, water or additives can be added for the purpose of improving moldability, improving the strength of the final silica carrier, and the like. The additive is not particularly limited, and an additive used in producing a general ceramic molded product can be used. Depending on the purpose, a binder, a plasticizer, a dispersant, a lubricant, a wetting agent, an antifoaming agent and the like can be used.

Examples of the binder include wax emulsion, arabic rubber, lignin, dextrin, polyvinyl alcohol, polyethylene oxide, starch, methyl cellulose, Na-carboxymethyl cellulose, hydroxyethyl cellulose, sodium alginate, argin ammonium, tragant rubber and the like. Since the viscosity of the kneaded product changes greatly depending on the type and concentration of the binder, select the type and amount of the binder so that the viscosity is suitable for the molding method to be used.

Examples of the plasticizer include glycerin, polyethylene glycol, dibutyl phthalate and the like, and the flexibility of the kneaded product can be enhanced.

As the dispersant, in an aqueous system, ammonium carboxymethyl cellulose (CMC-NH ₄ ), an oligomer of acrylic acid or an ammonium salt thereof, an anionic surfactant, ammonium polycarboxylate, wax emulsion, various amines such as monoethylamine, pyridine, etc. Examples thereof include piperidin and tetramethylammonium hydroxide, and examples of non-aqueous systems include fatty acids, fatty acid esters, phosphate esters, synthetic surfactants, and benzenesulfonic acids. By adding these dispersants, it is possible to obtain a silica carrier having a uniform fine structure after firing while avoiding the formation of aggregated particles.

Examples of the lubricant include liquid paraffin, paraffin wax, chlorinated hydrocarbon and the like in the hydrocarbon type, and fatty acid amide type and the like in the fatty acid type such as stearic acid, lauric acid and metal salts thereof. .. By adding the lubricant, the friction between the powders can be reduced, the fluidity can be improved, the molding can be facilitated, and the molded product can be easily removed from the mold.

Wetting agents can be added to improve the wetting properties of the powder and the dispersant. Examples of the wetting agent include nonionic surfactants, alcohols, glycols and the like as water-based agents, and polyethylene glycol ethyl ether, polyoxyethylene ester and the like as non-aqueous systems. These substances are easily adsorbed on the solid-liquid interface and reduce the interfacial tension to improve the wetting of the solid.

When handling a slurry-based kneaded product, a defoaming agent such as a nonionic surfactant, a polyalkylene glycol-based derivative, or a polyether-based derivative can be added.

These additives can be used alone or in combination of two or more at the same time, but they are effective and inexpensive when added in as little as possible, do not react with powder, and are soluble in water or solvent. Complete decomposition in an oxidizing or non-oxidizing atmosphere, for example at a relatively low temperature of 400 ° C or less, no ash, especially alkali metals and heavy metals, remaining after decomposition explosion, decomposition gas is non-toxic and non-corrosive, product It is desirable not to interfere with the recycling of the debris that did not become.

The shape of the silica carrier is not particularly limited. For example, a spherical shape, a columnar shape, a hollow columnar shape, a plate shape, an elliptical shape, a sheet shape, a honeycomb shape and the like can be mentioned. It is preferably spherical, cylindrical, hollow cylindrical, or elliptical, and more preferably spherical or cylindrical, which facilitates filling into the reactor and carrying the catalytically active component.

The method for molding the silica carrier is not particularly limited. It is molded from a kneaded product containing fumed silica, silica gel, and colloidal silica by any convenient method such as cast molding, extrusion molding, rolling granulation, spray drying and the like. General die-in molding involves putting the kneaded material in a metal mold, filling it well while hitting it with a mallet, pressing it with a piston, and then removing it from the mold. It is also called stamp molding. .. Extrusion molding generally involves packing the kneaded product into a press, extruding it from a die, cutting it to an appropriate length, and forming it into a desired shape. Rolling granulation involves dropping the kneaded material onto a rotating disk placed at an angle and rolling the granules on the disk to grow them into a spherical shape. Spray drying generally involves spraying a thick slurry into hot air to obtain porous particles, although it does not result in very large particles.

The size of the silica carrier is not particularly limited. Since it affects the handling at the time of manufacturing or filling the catalyst carrying the catalytically active component, the differential pressure after filling in the reactor, the reaction performance of the catalytic reaction, etc., it is desirable to make the size in consideration of them. .. Since the silica carrier shrinks when the molded product is fired, the size of the silica carrier is determined by the firing conditions. When the silica carrier is spherical, the size of the silica carrier (after firing) is preferably 0.5 mm to 12 mm, more preferably 1 mm to 10 mm, and further preferably 2 mm to 8 mm. preferable. When the silica carrier has a non-spherical shape, the size of the silica carrier (after firing) is preferably 0.5 mm to 12 mm, which is the maximum dimension when the size is measured, and is preferably 1 mm to 1 mm. It is more preferably 10 mm, further preferably 2 mm to 8 mm. When the particle size of the silica carrier is 0.5 mm or more, it is possible to prevent a decrease in productivity during carrier production and an increase in pressure loss when used as a catalyst. When the particle size of the silica carrier is 12 mm or less, it is possible to prevent a decrease in the reaction rate due to the rate-determining diffusion in the carrier and an increase in by-products.

The shape of the silica carrier can also be adjusted by performing a treatment using Malmölizer (registered trademark) (Fuji Powder Co., Ltd.) or the like before or after firing, if necessary. For example, a columnar molded body before firing can be formed into a spherical shape by treating it with the Malmö riser (registered trademark).

The calcination method is not particularly limited, but there is an appropriate calcination temperature range from the viewpoint of decomposing additives and preventing structural destruction of silica. The firing temperature is preferably 300 ° C to 1000 ° C, more preferably 500 ° C to 900 ° C. When the calcination temperature is in this range, the additive is completely decomposed and the performance of the silica carrier is not adversely affected. It also improves the specific surface area of the silica carrier. The firing treatment can be carried out under either oxidizing or non-oxidizing conditions. For example, the firing treatment may be performed in an air atmosphere or in an inert gas atmosphere such as nitrogen gas. The time of the firing treatment is also not particularly limited, and can be appropriately determined depending on the shape and size of the molded product, the type and amount of the additive used, and the like.

The silica carrier of one embodiment has mesopores having a pore diameter of 2 to 50 nm and macropores having a pore diameter of more than 50 nm and 1000 nm or less in the measurement of pore size distribution. The presence of mesopores can be confirmed by the gas adsorption method (BJH method). The presence of macropores can be confirmed by the mercury intrusion method. Generally, a mercury intrusion method and a gas adsorption method (BJH method) are widely used for measuring the pore size distribution of a porous substance such as silica. Looking at the classification of pores by the IUPAC (International Union of Pure and Applied Chemistry), some of the macropores of 50 nm or more and the mesopores of 2 nm to less than 50 nm are classified as mesopores by the gas adsorption method. Micropores of 2 nm or less can be measured. When the silica carrier has macropores of the above size, the diffusion rate of the substance in the pores is further improved. When such a silica carrier is used as a catalyst, it can be expected that the activity is improved with an increase in the main reaction rate and the selectivity is improved with the sequential suppression of side reactions of the target product. By having mesopores of the above size in combination with the macropores, the supported components can be highly dispersed, and it is expected that the catalytic activity will be improved as the reaction active sites increase.

In the silica carrier, the distribution ratio of each pore is not particularly limited, and an appropriate pore diameter distribution ratio can be selected depending on the type of reaction using the silica carrier. The pore size distribution ratio can be adjusted by the mixing ratio of fumed silica, silica gel, and colloidal silica when producing the silica carrier, the type and amount of the additive used, the firing temperature, the molding method, and the like.

In the pore size distribution by the mercury intrusion method, the pore volume (integral value of the total macropore volume) of the macropores of the silica carrier is preferably 0.05 to 0.50 cc / g. The pore volume of the macropores of the silica carrier is more preferably 0.07 to 0.40 cc / g, still more preferably 0.10 to 0.30 cc / g. When the pore volume of the macropores of the silica carrier is in the range of 0.05 to 0.50 cc / g, the diffusion rate of the substance and the strength of the carrier can be compatible with each other.

The specific surface area (BET specific surface area) of the silica carrier by the BET method is preferably 200 to 500 m ² / g. The BET specific surface area of the silica carrier is more preferably 220 to 400 m ² / g, still more preferably 240 to 400 m ² / g. When the BET specific surface area of the silica carrier is in the range of 200 to 500 m ² / g, a sufficient reaction rate can be obtained when catalyzed.

The bulk density of the silica carrier is preferably 300 to 700 g / L. The bulk density of the silica carrier is more preferably 400 to 650 g / L, still more preferably 450 to 600 g / L. When the bulk density of the silica carrier is in the range of 300 to 700 g / L, a required amount of the active ingredient can be supported and the strength of the carrier can be maintained.

The average pore diameter of the mesopores obtained by the gas adsorption method (BJH method) of the silica carrier is preferably 3 to 16 nm. The average pore diameter of the mesopores obtained by the gas adsorption method (BJH method) of the silica carrier is more preferably 4 to 14 nm, still more preferably 5 to 12 nm. When the average pore diameter of the mesopores by the gas adsorption method (BJH method) of the silica carrier is in the range of 3 to 16 nm, the specific surface area by the BET method becomes a sufficient value.

The carrier may have any shape, and the shape is not particularly limited. The carrier may be, for example, powdery, spherical, pellet-shaped, or the like, and is preferably spherical or pellet-shaped. The particle size of the carrier is also not particularly limited. The particle size of the carrier varies depending on the form of the reaction, but when used in the fixed bed method, it is preferably 2 mm to 10 mm, more preferably 3 mm to 7 mm.

There is no particular limitation on the method of supporting the heteropolyacid or a salt thereof on the carrier. Generally, it can be carried out by allowing a carrier to absorb a solution or suspension obtained by dissolving or suspending a heteropolyacid or a salt thereof in a solvent and evaporating the solvent.

As a method of supporting the heteropolyrate on the carrier, a method of supporting the heteropolyacid on the carrier and then supporting the raw material of the element forming the salt, and a method of supporting the carrier together with the raw material of the heteropolyacid and the element forming the salt. Examples thereof include, but are not limited to, a method of supporting a heteropolyacid prepared in advance on a carrier, and a method of supporting a raw material of an element forming a salt on the carrier and then carrying a heteropolyacid. In any of the above methods, the heteropolyacid, its salt, and the raw material of the element forming the salt can be dissolved or suspended in a suitable solvent and supported on the carrier. The solvent may be any one that can dissolve or suspend the heteropolyacid, its salt, or the raw material of the element forming the salt, and water, an organic solvent or a mixture thereof, etc. are used, and water, alcohol or a mixture thereof is preferable. A mixture is used.

Specifically, the amount of the heteropolyacid or its salt carried on the carrier is adjusted by, for example, dissolving the heteropolyacid or its salt in distilled water corresponding to the amount of water absorption liquid of the carrier and impregnating the carrier with the solution. be able to. In another embodiment, the amount of heteropolyacid or salt carried on the carrier is such that the carrier is immersed in a solution of excess heteropolyacid or salt thereof with moderate movement and then filtered to result in excess heteropolyacid or salt thereof. It can also be adjusted by removing the salt. The volume of the solution or suspension varies depending on the carrier used, the supporting method, and the like. A solid acid catalyst supported on a carrier can be obtained by evaporating the solvent of a carrier impregnated with a heteropolyacid or a salt thereof in a heating oven for several hours. The drying method is not particularly limited, and various methods such as a stationary type and a belt conveyor type can be used. In addition, the amount of the heteropolyacid or its salt supported on the carrier can be accurately measured by chemical analysis such as ICP and XRF.

The amount of the heteropolyacid or its salt supported on the carrier is preferably 10 to 150 parts by mass, preferably 30 to 100 parts by mass, based on 100 parts by mass of the carrier. More preferred.

(Method for producing alcohol by hydration reaction of olefin)
As the alcohol, a solid acid catalyst (hereinafter referred to as "catalyst for alcohol production") in which a heteropolyacid or a heteropolylate is supported on a carrier is used, and water and an olefin having 2 to 5 carbon atoms are used as a reactor. It can be obtained by supplying it to the gas phase and allowing it to undergo a hydration reaction in the gas phase.

（式中、Ｒ^１～Ｒ^４はそれぞれ独立して水素原子又は炭素原子数１～３のアルキル基を表し、Ｒ^１～Ｒ^４の合計の炭素原子数は０～３である。） A specific example of the alcohol production reaction by the hydration reaction of an olefin having 2 to 5 carbon atoms is shown in the formula (1).

(In the formula, R ¹ to R ⁴ each independently represent a hydrogen atom or an alkyl group having 1 to 3 carbon atoms, and the total number of carbon atoms of R ¹ to R ⁴ is 0 to 3).

The olefin having 2 to 5 carbon atoms that can be used in the hydration reaction of the olefin using the alcohol production catalyst is not particularly limited. Examples of the olefin having 2 to 5 carbon atoms include ethylene, propylene, n-butene, isobutene, pentene, or a mixture thereof, and more preferably ethylene. There is no limit to the ratio of olefin and water used, but the molar ratio of olefin to water is high because the concentration of olefin depends on the reaction rate and the energy cost of the alcohol production process increases when the water concentration is high. Is preferably water: olefin = 0.01 to 2.0, and more preferably water: olefin = 0.1 to 1.0.

There is no limitation on the type of hydration reaction of the olefin using the catalyst for alcohol production, and any reaction type can be used. Preferred types include a fixed bed type, a fluidized bed type, a suspended bed type, and the like from the viewpoint of ease of separation from the catalyst and reaction efficiency, and more preferably, separation from the catalyst is most preferable. It is a fixed floor type that does not require energy.

The gas space velocity when the fixed bed type is used is not particularly limited, but is preferably 500 to 15,000 / hr, more preferably 1000 to 10000 / hr from the viewpoint of energy and reaction efficiency. If the gas space velocity is 500 / hr or more, the amount of catalyst used can be effectively reduced, and if it is 15,000 / hr or less, the gas circulation amount can be reduced. Therefore, alcohol is used within the above range. Can be manufactured more efficiently.

There is no limitation on the reaction pressure in the hydration reaction of the olefin using the catalyst for alcohol production. Since the hydration reaction of olefin is a reaction in which the number of molecules is reduced, it is generally advantageous to carry out the hydration reaction at high pressure. The reaction pressure is preferably 0.5 to 7.0 MPaG, more preferably 1.5 to 4.0 MPaG. "G" means gauge pressure. If the reaction pressure is 0.5 MPaG or more, a sufficient reaction rate can be obtained, and if it is 7.0 MPaG or less, equipment for olefin condensation measures and olefin evaporation is installed, equipment for high pressure gas safety measures, and equipment for high pressure gas safety measures. The cost related to energy can be further reduced.

The reaction temperature of the hydration reaction of the olefin using the alcohol production catalyst is not particularly limited and can be carried out in a wide range of temperatures. The preferred reaction temperature is 100 to 550 ° C, more preferably 150 to 350 ° C, considering the thermal stability of the heteropolyacid or heteropolyate and the temperature at which water, which is one of the raw materials, does not condense.

The hydration reaction of the olefin using the catalyst for alcohol production is an equilibrium reaction, and the conversion rate of the olefin is the equilibrium conversion rate at the maximum. For example, the equilibrium conversion rate in the production of ethanol by hydration of ethylene is calculated to be 7.5% at a temperature of 200 ° C. and a pressure of 2.0 MPaG. Therefore, in the method for producing alcohol by hydration of olefin, the maximum conversion rate is determined by the equilibrium conversion rate, and as seen in the example of ethylene, the hydration reaction of olefin tends to have a small equilibrium conversion rate. Industrially, there is a strong demand for highly efficient olefin hydration reactions under mild conditions.

In the olefin hydration reaction using an alcohol production catalyst, the loss of the olefin can be reduced by recycling the unreacted olefin to the reactor. There is no limitation on the method of recycling the unreacted olefin to the reactor, and the olefin may be isolated and recycled from the process fluid coming out of the reactor, or may be recycled together with other inert components. Industrial grade ethylene usually contains very small amounts of ethane. Therefore, when recycling unreacted ethylene to a reactor using ethylene containing ethane, a part of the recovered ethylene gas should be purged to the outside of the system in order to prevent the concentration and accumulation of ethane. Is desirable.

In the hydration reaction of an olefin using a catalyst for alcohol production, the produced alcohol may be dehydrated and an ether compound may be produced as a by-product. For example, when ethanol is obtained by hydration of ethylene, diethyl ether is by-produced. This diethyl ether is considered to be produced by a dehydration reaction from two molecules of ethanol, and when ethanol is produced by a hydration reaction of ethylene, the yield of the reaction is significantly reduced, but by-produced diethyl ether. Diethyl ether is converted to ethanol by recycling it into a reactor, and ethanol can be produced from ethylene with extremely high efficiency. The method of recycling the by-produced ether compound into the reactor is not particularly limited, but for example, a method of isolating the ether compound from the components distilled from the reactor and recycling it into the reactor, and reacting as a gas component together with the unreacted olefin. There is a method of recycling to a vessel.

(Catalyst regeneration)
The present inventors treat a catalyst that has deteriorated due to the production of alcohol, specifically that the activity or alcohol selectivity has decreased, with a regeneration gas containing water vapor, so that a part of the carbon component adhering to the catalyst is partially removed. It was desorbed and found that the catalyst was regenerated. The regenerating gas used for regenerating the catalyst is not particularly limited as long as it contains water vapor, but the regenerating gas is preferably a mixed gas of water vapor and an inert gas such as nitrogen. Examples of the inert gas include nitrogen gas and noble gases such as helium and argon, and nitrogen gas is preferable from the viewpoint of cost. The treatment of the catalyst using the regenerating gas is not particularly limited and can be carried out by any known method. For example, without removing the catalyst from the reactor with the catalyst filled in the reactor, the introduction of olefins, water, etc., which are reaction raw materials, is stopped to stop the reaction, and an inert gas is circulated and adsorbed on the catalyst. , Alcohol and the like may be completely desorbed, and then a regenerating gas may be introduced into the reactor to treat the catalyst in the reactor. Instead, similarly, the introduction of olefins, water, etc., which are reaction raw materials, is stopped to stop the reaction, the catalyst layer is sufficiently cooled, the catalyst is withdrawn from the reactor, and the catalyst is filled in another container. The catalyst may be treated in the container. From the viewpoint of the labor of refilling the catalyst and the cost of the container for regeneration, it is preferable to carry out the treatment in the reactor without removing the catalyst from the reactor, thereby shortening the reaction stop time and economically. The processing can be performed advantageously.

The pressure of the regenerating gas may be normal pressure or pressurized, and is not particularly limited. When the regenerating gas is pressurized, a higher water pressure can be obtained, so that the catalyst can be regenerated more effectively. The pressure of the regenerating gas is preferably 0.01 to 4 MPaG, more preferably 1 to 3 MPaG.

The partial pressure of water vapor in the regenerating gas may be about the same as in the hydration reaction, preferably 0.01 to 1 MPaA, and more preferably 0.2 to 0.6 MPaA. "A" means absolute pressure.

The treatment time is preferably 1 to 100 hours, more preferably 3 to 30 hours. The specific catalyst load (WHSV; 1 gram of catalyst and the number of grams of water at room temperature per hour) is preferably 0.05 to 2 h ^-1 , more preferably 0.2 to 1.0 h ^-1 .

The treatment temperature is 150 to 350 ° C, preferably 180 to 250 ° C. If the temperature is lower than the dew point of water vapor, the supported components of the catalyst may dissolve, so it is desirable that the temperature is higher than that.

The present invention will be further described with reference to the following examples and comparative examples, but these examples show the outline of the present invention, and the present invention is not limited to these examples.

1. 1. Manufacture of silica carrier Aerosil ™ 300 (manufactured by Nippon Aerosil Co., Ltd.) 40 parts by mass as fumed silica, CARiACT G6 (manufactured by Fuji Silysia Chemical Ltd.) 60 parts by mass as silica gel, and Snowtex O (Nissan Chemical Co., Ltd.) as colloidal silica. After kneading 40 parts by mass of (manufactured by Co., Ltd.) with a kneader, water and additives (methyl cellulose: SM-4000 manufactured by Shin-Etsu Chemical Industry Co., Ltd., resin binder: Celander (registered trademark) YB-132A manufactured by Yuken Kogyo Co., Ltd. ) Was added to a kneader in an appropriate amount and further kneaded to prepare a kneaded product. Next, the kneaded product was put into an extrusion molding machine equipped with a die having a circular hole of 3 mmφ at the tip. A columnar pre-baking molded product was obtained while cutting the intermediate material extruded from the extrusion molding machine with a cutter so as to have a length of 3 mm. The pre-baked molded body was formed into a spherical shape with Malmöllizer (registered trademark), pre-dried at 70 ° C., and then calcined at a temperature of 820 ° C. in an air atmosphere to obtain silica carrier A.

The water absorption rate of the carrier means a numerical value measured by the following measuring method.
(1) Weigh about 5 g of the carrier with a balance (W1 g) and put it in a 100 mL beaker.
(2) Add about 15 mL of pure water (ion-exchanged water) to the beaker so as to completely cover the carrier.
(3) Leave it for 30 minutes.
(4) Empty the carrier and pure water on the wire mesh and drain the pure water.
(5) Lightly press the water adhering to the surface of the carrier with a paper towel until the surface loses its luster to remove it.
(6) The weight of the carrier + pure water is measured (W2g).
(7) The water absorption rate of the carrier is calculated from the following formula.
Water absorption rate (g / g-carrier) = (W2-W1) / W1
Therefore, the water absorption amount (g) of the carrier is calculated by multiplying the water absorption rate (g / g) of the carrier by the mass (g) of the carrier used.

2. 2. Preparation of catalyst for alcohol production in which silicate tungstic acid is supported on a silica carrier 150 g of commercially available Keggin type silicate tungstic acid 26 hydrate (H ₄ SiW ₁₂ O ₄₀・ 26H ₂ O; manufactured by Nippon Inorganic Chemical Industry Co., Ltd.) Weighed, charged into a eggplant-shaped flask, distilled water was added to a volume corresponding to 95% of the water absorption of the silica carrier A, and silicotungstic acid was dissolved. Next, 300 mL of silica carrier A was weighed and placed in an eggplant-shaped flask containing a solution of silicotungstic acid. After charging, the eggplant-shaped flask was stirred so that the liquid was in contact with the silica carrier A, and the silica tungstic acid was supported on the silica carrier A. The silica carrier A carrying the silicotungstic acid was taken out from the eggplant-shaped flask, spread on a vat, and air-dried for 1 hour. Next, the silica carrier carrying the air-dried silica-tung acid was placed on a bat and placed in a dryer, dried under 130 ° C. conditions for 5 hours, then removed from the dryer and transferred into a dried desiccator. After cooling to room temperature, an alcohol production catalyst A in which the silica tung acid acid was supported on the silica carrier A was obtained.

3. 3. Ethylene hydration reaction (gas recycling evaluation)
After filling the alcohol production catalyst A with a vertical gas phase fixed bed reactor made of SUS, the temperature rise and pressure increase are controlled, and water vaporized from the evaporator and a predetermined amount of ethylene are introduced into the reactor from the mass flow controller. did. The reaction gas after passing through the reactor was cooled, and the condensed liquid and the reaction gas from which the condensed product was removed were sampled for a certain period of time. A part of the reaction gas from which the condensate was removed was purged so that inert gas such as ethane did not accumulate, and the remaining gas was introduced into a compressor as recycled gas, pressurized, and recycled to the reactor. The sampled liquid (reaction liquid) and reaction gas were analyzed using a gas chromatophy analyzer and a Karl Fischer analyzer, and the reaction results were calculated.

4. Analysis of reaction gas The sampled reaction gas was analyzed by a system program using multiple columns and two detectors using a gas chromatography device (device name: 7890) manufactured by Agilent Technologies, Inc.
・ Gas chromatography conditions Oven: Hold at 40 ° C for 3 minutes, then heat up to 200 ° C at 20 ° C / min Carrier gas: Helium Split ratio: 10: 1
-Column used (manufactured by Agilent Technologies Co., Ltd.)
HP-1 (2m) + GasPro (30m) 32m x 320μm x 0μm
DB-624 60m x 320μm x 1.8μm
-Detector Front detector: FID (heater 230 ° C, hydrogen flow rate 40 mL / min, air flow rate 400 L / min)
Back detector: FID (heater 230 ° C, hydrogen flow rate 40 mL / min, air flow rate 400 L / min)
Aux detector: TCD (heater 230 ° C, reference flow rate 45 mL / min, make-up flow rate 2 mL / min)

5. Analysis of Reaction Solution The sampled reaction solution was analyzed using a gas chromatography device (device name: 6850) manufactured by Agilent Technologies, Inc. The water concentration in the reaction solution was analyzed with a Karl Fischer analyzer manufactured by Mitsubishi Chemical Corporation.
Column used: PoraBONDQ 25m x 0.53mm ID x 10μm
Oven temperature: 100 ° C for 2 minutes, then temperature rises to 240 ° C at 5 ° C / min Injection temperature: 250 ° C
Detector temperature: 300 ° C

The ethylene conversion rate, ethanol selectivity, and acetaldehyde selectivity were calculated by the following formulas.
Ethylene conversion rate (mol%) = (number of moles of reacted ethylene / number of moles of supplied ethylene) x 100
Ethanol selectivity (mol%) = (number of moles of produced ethanol / number of moles of supplied ethylene) x 100
Acetaldehyde selectivity (mol%) = (number of moles of acetaldehyde produced / number of moles of ethylene supplied) x 100

6. Regeneration treatment of catalyst After stopping the supply of raw material gas and purging the reactor with nitrogen gas instead, a predetermined amount of water vaporized from the evaporator and a predetermined amount of nitrogen gas from the mass flow controller were introduced into the reactor. At this time, the catalyst was regenerated without changing the temperature and pressure from the time of the hydration reaction.

<Example 1>
300 mL of the alcohol production catalyst A was weighed, filled in a tube-type reactor (SUS316, inner diameter 34 mm, length 1500 mm), replaced with nitrogen gas, and then pressurized to 2.0 MPaG. Next, the reactor was heated to 190 ° C., and when the temperature became stable, the reactor was charged with water and ethylene in an amount such that GHSV (gas phase space velocity) was 3000 / hr and the molar ratio of water to ethylene was 0.3. Ethylene was produced by a hydration reaction of ethylene. After feeding water and ethylene, the temperature of the heat source of the reactor was adjusted so that the temperature of the catalyst layer became 194 ° C. after the temperature became stable. Since the acetaldehyde selectivity increased to 0.10% when 3200 hours had passed from the start of the hydration reaction, the supply of raw materials was stopped, and the reactor was charged with a flow rate of GHSV (gas phase space velocity) of 3000 / hr using nitrogen gas. Was purged for 3 hours. Then, a mixed gas composed of 78% by volume of nitrogen gas and 22% by volume of water vapor was introduced into the reactor at GHSV3000 / hr, and the catalyst was regenerated for 3 hours. The temperature during the regeneration treatment was 190 ° C., the pressure was 2.0 MPaG, and the partial pressure of steam was 0.46 MPa.

When the reaction was started again after the regeneration treatment, the acetaldehyde selectivity decreased to 0.07%. Further, after 900 hours (4100 hours after the start of the hydration reaction) and 1500 hours (4700 hours after the start of the hydration reaction), the reaction was similarly stopped and the catalyst was regenerated while the ethanol was added. Manufactured. Even after 5000 hours had passed from the start of the hydration reaction, the ethylene conversion was maintained at 4.1% and the ethanol selectivity was 99.6%. The results are shown in Table 1.

<Comparative Example 1>
Table 2 shows the results of continuing the hydration reaction without performing the regeneration treatment under the same catalyst and reaction conditions as those used in Example 1. After 5000 hours from the start of the hydration reaction, the ethylene conversion rate decreased to 3.8%, the ethanol selectivity decreased to 98.9%, and the acetaldehyde selectivity increased to 0.44%. The results are shown in Table 2.

The changes over time in the ethylene conversion rates of Example 1 and Comparative Example 1 are shown in graphs in FIG. 1, and the changes in ethanol selectivity over time are shown in FIG. 2, respectively.

From the above results, it can be seen that the ethylene conversion rate and the ethanol selectivity can be maintained even if the reaction is carried out for a long time by performing the catalyst regeneration treatment.

Since the ethylene conversion rate is low in a commercial ethanol plant, the difference in conversion rate of 0.3% has a large effect on productivity and cost. If the annual production volume is 50,000 tons, the conversion rate of 0.3% corresponds to about 3700 tons. Assuming that the price of absolute ethanol is 120 yen / kg, the cost-effectiveness of catalyst regeneration is estimated to be over 400 million yen per year.

According to the present invention, a deteriorated catalyst for alcohol production having reduced activity or alcohol selectivity can be reused, and alcohol can be stably produced for a long period of time.

Claims (7)

A method for regenerating an alcohol production catalyst, which comprises treating an alcohol production catalyst having reduced activity or alcohol selectivity with a regeneration gas containing water vapor within a temperature range of 150 to 350 ° C., wherein the alcohol is produced. The production catalyst is used for producing alcohol by supplying water and an olefin having 2 to 5 carbon atoms to a reactor and hydrating them in a gas phase, and the heteropolyacid or a salt thereof is used. A method for regenerating a catalyst for producing alcohol, which is a solid acid catalyst supported on a carrier. The method for regenerating an alcohol production catalyst according to claim 1, wherein the regenerating gas is a mixed gas containing an inert gas and water vapor. The method for regenerating an alcohol-producing catalyst according to claim 1 or 2, wherein the partial pressure of water vapor in the regenerating gas is 0.01 to 1 MPa. The method for regenerating an alcohol-producing catalyst according to any one of claims 1 to 3, wherein the treatment with the regenerating gas is performed in the reactor without removing the alcohol-producing catalyst from the reactor. Claim 1 in which the heteropolyacid is at least one compound selected from the group consisting of silicotungstic acid, phosphotungstic acid, phosphomolybdic acid, phytomolybdic acid, cavanadotungstic acid, limbanadotungstic acid and limbanadomolybdic acid. The method for regenerating a catalyst for producing alcohol according to any one of 4 to 4. The method for regenerating an alcohol-producing catalyst according to any one of claims 1 to 5, wherein the carrier is silica. The method for regenerating an alcohol-producing catalyst according to any one of claims 1 to 6, wherein the olefin having 2 to 5 carbon atoms is ethylene and the alcohol is ethanol.

Images