KR20100084131A

KR20100084131A - Process for producing pure butanol

Info

Publication number: KR20100084131A
Application number: KR1020100003741A
Authority: KR
Inventors: 장종산; 이정호; 황영규; 하종욱; 이승환; 김형록; 황동원
Original assignee: 한국화학연구원
Priority date: 2009-01-15
Filing date: 2010-01-15
Publication date: 2010-07-23
Also published as: KR101177565B1; WO2010082772A3; WO2010082772A2

Abstract

The present invention, (1) fermenting the biomass using a microorganism, (2) separating n-butanoic acid from the fermentation broth obtained in (1), (3) n-part separated in (2) High purity butanol exhibiting high selectivity and high productivity, including directly gas phase reduction by hydrogen over a ruthenium-based hydrogenation catalyst or copper-based nanocomposite catalyst, and (4) butanol purification by distillation of butanol obtained by hydrogenation It is to provide a method for producing and a hydrogenation catalyst for implementing the same.

Description

High Purity Butanol Manufacturing Process {PROCESS FOR PRODUCING PURE BUTANOL}

The present invention, (1) fermenting the biomass (Biomass) using a microorganism, (2) separating n-butanoic acid from the fermentation broth obtained in (1), (3) (2) high selectivity comprising the direct gas phase reduction of n-butanoic acid by hydrogen over a ruthenium-based hydrogenation catalyst or a copper-based nanocomposite catalyst and (4) a purification of butanol by distillation of butanol obtained by hydrogenation. It relates to a high-purity n-butanol production method showing a high productivity and a hydrogenation catalyst for the same.

Since the mid-20th century, the oil-based chemical industry has been greatly developed, but oil, gas, and coal, which are represented by fossil raw materials, are continuously increasing in price due to their limited resources. Competition is heating up. Moreover, chemical products produced from fossil raw materials generate a large amount of global warming gases and wastes as by-products in the manufacturing process, causing a serious environmental crisis for mankind, which is rapidly reducing the existing chemical industry. Therefore, there is a need for the development of a new environmentally friendly biochemical process using biomass as a raw material that can replace the chemical process based on fossil raw materials.

Industrial BT (Industrial biotechnology) is a technology that uses biotechnological technology for industrial production. Biorefinery is the core of the technology. Biorefining is an integrated process corresponding to existing petroleum refineries. It refers to a technology for making biofuels and chemical products using biomass and biotechnology as raw materials and a comprehensive plant system for realizing them.

Biorefinery based biofuels include bioethanol, biobutanol and biodiesel. In recent years, research on the deoiling of automobile fuels has been continuously conducted, and due to concerns about high oil prices and petroleum depletion, eco-friendly bioethanol has emerged as an alternative fuel for gasoline. The application of eco-friendly bioethanol continues to expand. In particular, the plant resources obtained by photosynthesis of carbon dioxide are the only carbon sources among renewable energy sources and have neutral characteristics for carbon dioxide emissions. As a result, the global issues of carbon dioxide emissions and global warming due to the use of fossil fuels have emerged as serious international issues. There is more interest than ever before. On the other hand, biobutanol has a lower polarity than bioethanol, so there is no problem of corrosion or low boiling point of bioethanol, and it is easy to mix gasoline due to low volatility than bioethanol. It is easy to store and store, and can be used without special modification of a petroleum-based automobile system, and has a number of advantages such as higher volumetric fuel efficiency than bioethanol. However, the biobutanol manufacturing process is far lower in yield and productivity than the bioethanol manufacturing process, and a bioprocess that is economically manufactured has not been developed. Until now, n-butanol has been produced in large quantities through hydrogenation after preparing butylaldehyde (Butyraldehyde) by hydroformylation reaction of propylene in petrochemical process, solvent, plasticizer, amino resin, butylamine, etc. It is used for the manufacture of. The n-butanol produced by the petrochemical process is difficult to use as a fuel because propylene, which is more expensive than fuel, is obtained as a raw material. Therefore, development of economic mass production technology of biobutanol derived from biomass is very important in the field of biorefinery because it can secure economic feasibility as an alternative fuel and can bring environmental effects due to reduction of greenhouse gas emission. In this regard, as an alternative to the biobutanol production process, n-butanoic acid is prepared from a raw material using biomass, a natural circulation resource, by bioprocessing, and n-butanol is reduced by catalytic chemical method to prepare n-butanol. Convergence bio-chemical techniques can be considered. This fusion bio-chemical technology is advantageous for supplying hydrogen required for the two-stage hydrogenation reaction because two moles of biohydrogen are produced together with the equivalent ratio of n-butanoic acid during fermentation of n-butanoic acid from raw materials as biomass. It implies

It is a chemically easy reaction to produce monohydric alcohols such as n-butanol by reduction reaction of monocarboxylic acids such as n-butanoic acid. However, such chemical reduction reactions require the use of expensive and powerful reducing agents such as lithium aluminum hydride (LiAlH ₄ ), so that reduction reactions using such reducing agents produce large quantities of general purpose monohydric alcohols such as n-butanol on an industrial scale. Not suitable for On the other hand, a hydrogenation reaction using hydrogen as a reducing agent on a hydrogenation catalyst is used to produce monohydric alcohol on an industrial scale. However, such a hydrogenation reaction is not usually applied to direct hydrogenation of carboxylic acid, which is generally used because the hydrogenation catalyst is dissolved in the reactant carboxylic acid to maintain the catalytic activity in the presence of carboxylic acid for a long time, Or because the catalyst component causes decarboxylation of the carboxylic acid, thereby degrading the selectivity of the direct hydrogenation reaction of the carboxylic acid.

Accordingly, most of the carboxylic acid hydrogenation processes are prepared by a two-step process in which a carboxylic acid is esterified with methanol or ethanol and the esterified product is hydrogenated to produce a monohydric alcohol. For example, 1,4-butanediol is prepared by hydrogenation of esterified products of maleic acid or maleic anhydride with methanol or ethanol [USP 6,100,410, USP 6,077,964, USP 5,981,769, USP 5,414,159, USP 5,334,779]. However, such a process requires the addition of an esterification step, recovery of alcohol used for the esterification reaction, and purification step for hydrogenation of the carboxylic acid, and recovery and purification of unreacted esterified product after the hydrogenation reaction. There are problems such as complexity and disadvantages in terms of production cost.

Because of these problems, much research is being conducted to shorten the reaction process in producing monohydric alcohols.

For example, US Pat. No. 6,495,730 and the patent cited in the patent disclose the preparation of 1,4-butanediol by direct hydrogenation of maleic acid or succinic acid under reaction conditions in which excess water is supplied relative to carboxylic acids. Hydrogenation catalyst systems are known [ruthenium-tin / activated carbon; Ruthenium-iron oxide; Ruthenium-tin / titanium or alumina; Ruthenium-tin and a component selected from alkali metals or alkaline earth metals; A component selected from tin-ruthenium, platinum and rhodium; Ruthenium-tin-platinum / active carbon].

On the other hand, US Pat. No. 4,443,639 discloses ARuDEOx (A = Zn, Cd and mixtures thereof, D = Co, Ni and mixtures thereof, E = Fe, Cu, Rh, Pd, Os, Ir, Pt as a hydrogenation catalyst of n-butanoic acid). And ruthenium-based catalysts of the mixtures thereof, and n-butanol is obtained when water is present, but n-butyl butyrate is obtained when there is no water.

In other words, the prior art requires the use of excess water to produce monohydric alcohols from carboxylic acids (using USP 4,443,639: 10 wt% aqueous acid solution), resulting in high waste water generation, high energy use costs and low productivity (e.g., LHSV). : 0.1 hr ^-1 or less) There are problems such as a hydrogenation reaction pressure requiring a high pressure of 60 atm or higher. Therefore, it is necessary to develop a hydrogenation catalyst that can be utilized irrespective of the water content, and to develop an economical manufacturing process technology for the industrial production of n-butanol by hydrogenation of n-butanoic acid.

Accordingly, an object of the present invention is to separate high-purity n-butanoic acid from fermentation broth obtained by fermenting biomass using microorganisms, and then to use n-butanoic acid using a specific catalyst having excellent thermal stability, chemical stability, and reaction activity. The present invention provides a highly available and economical process capable of producing n-butanol stably for a long time with high yield and selectivity by directly hydrogenating in a gas phase, and a hydrogenation catalyst therefor.

In order to achieve the object of the present invention, the present invention is the gas phase hydrogenation of n-butanoic acid on a ruthenium-based catalyst or a copper-based catalyst satisfying specific conditions after fermentation of biomass using microorganisms and separation of n-butanoic acid. It provides a method for producing high-purity n-butanol, characterized in that the by-products are separated by distillation of butanol.

A schematic process of the present invention is shown in FIG.

The fermentation process of the first-stage biomass-derived monosaccharides is by fermentation of bacterial microorganisms, and Clostridium-based microorganisms may be mainly used. In this fermentation process, monosaccharides may include glucose and xylose, and after the fermentation process, ammonium butyrate or alkali butane may be produced. During the fermentation process, biohydrogen and carbon dioxide are by-produced, and the obtained hydrogen can be recycled to the gas phase hydrogenation process.

In the second step, butanoic acid may be obtained by acidifying the butane produced in order to perform the separation and purification process of n-butanoic acid, and the butanoic acid purified liquid may be obtained by extractive distillation, reaction extraction, or the like.

In the third gas phase hydrogenation process of butanoic acid, the butanoic acid purified liquid obtained in step 2 is converted to high yield and high selectivity butanol using a ruthenium catalyst or a copper nanocomposite catalyst.

In the final fourth step, a small amount of unreacted products and by-products are separated and purified from the butanol obtained in step 3 by distillation to prepare high purity butanol. The final four-stage distillation process can be almost omitted or simplified depending on the intended use of butanol if the conversion yields close to 100% and more than 98% butanol selectivity in three steps.

As an aspect for achieving the object of the present invention, the third step is to directly hydrogenate n-butanoic acid in the presence of a ruthenium-based catalyst having a composition represented by the following formula (1) containing Ru, Sn, Zn as an essential component: Provided is a process for preparing n-butanol characterized by the following:

[Formula 1]

Ru (a) Sn (b) Zn (d) Ox

Where

(a), (b) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) is 1-20, preferably 2-10, (b) Represents 1 to 40, preferably 2 to 20;

x is the number of atoms of oxygen, which is determined by the valence and composition ratio of other components.

In addition, the catalyst of Formula 1 may additionally include at least one component A selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir, and Pt, and Si, Ti, and Al. It may further comprise one or more B selected.

Specifically, the present embodiment is represented by Formula 2, wherein the catalyst of Formula 1 may further include one or more components A selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir, and Pt. Provided is a process for preparing n-butanol, characterized in that:

[Formula 2]

Ru (a) Sn (b) A (c) Zn (d) Ox

Where

-(a), (b), (c) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) is 1-20, preferably 2-10 (b) represents 1 to 40, preferably 2 to 20, and (c) represents more than 0 to 20, preferably more than 0 to 10;

In addition, the present embodiment is a method for producing n-butanol, characterized in that the catalyst of formula (2) is represented by the following formula (3) further comprises at least one component B selected from the group consisting of Si, Ti and Al to provide:

(3)

Ru (a) Sn (b) A (c) Zn (d) B (e) Ox

Where

A represents at least one component selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir and Pt;

B represents at least one component selected from the group consisting of Si, Ti and Al;

-(a), (b), (c), (d) and (e) are the component ratios based on the number of atoms of each component, based on the case where (d) + (e) is 100,

(a) is 1-20, preferably 2-10;

(b) is 1-40, preferably 2-20;

(c) is greater than 0-20, preferably greater than 0-10;

(d) is 50 or more, preferably 80 to 100;

(e) represents greater than 0 to 50 or less, preferably greater than 0 to 20;

x is the number of atoms of oxygen, determined by the valence and composition ratios of the other components.

That is, the catalyst of the present embodiment is a catalyst composed of Ru and Sn components having a zinc oxide (ZnO) as a carrier, or an inorganic binder such as silica, alumina, or titanium oxide to impart moldability in the catalyst composed of the above components. At least one selected from the group consisting of reducing components, such as Co, Ni, Cu, Ag, Rh, Pd, Re, Ir, and Pt, in order to improve the catalyst's reducing ability It is a catalyst modified by adding the above improvement component further.

As another aspect for achieving the object of the present invention, the copper-based catalyst in the third step means all catalysts based on copper, such as copper-silica, copper-alumina, copper-titania, copper-zinc oxide, etc. . Specifically, the embodiment is a method for producing n-butanol comprising directly gas-phase reduction of n-butanoic acid by hydrogen on a reduced copper-based catalyst, the reduced copper-based catalyst is silica, alumina, titania and oxidation A copper catalyst obtained by reducing a complex oxide of at least one diluent selected from the group consisting of zinc and a copper oxide component, wherein the copper oxide component is 40 to 95 wt% and manufactured to have a copper oxide particle size of 50 nm or less. Catalyst. The copper-based catalyst may be modified by further including one or more refined components selected from the group consisting of cobalt, zinc, manganese, ruthenium, rhenium, palladium, platinum, silver, tellurium, selenium, magnesium and calcium.

In the fourth step, a butanol compound having a desired purity is obtained through a distillation step for separating and purifying butanic acid butyl ester, butanoic anhydride, water, and the like from the butanol product obtained in the three-step hydrogenation process. This distillation process may be omitted when the butanol selectivity in the three stages is very high, and may be used in combination with the distillation apparatus of the four stages with the distillation apparatus used in the two-stage extraction distillation process.

The present inventors have found and found that it is possible to economically produce n-butanol through a series of steps of fermentation of biomass feedstock, separation and purification of butanoic acid from fermentation, and gas phase hydrogenation of butanoic acid on the catalyst as described above in a fixed bed reaction. The invention has been completed.

In the n-butanol production method of the present invention, when the ruthenium-based catalyst of the formula (1) is used, it is possible to prepare n-butanol in high yield regardless of whether n-butanoic acid is contained, and is much milder than the known catalyst of the present invention. It can be operated under the reaction conditions, but can be produced in a high-selectivity and high productivity economical method n-butanol can be produced, and the long-term reaction stability of the catalyst is excellent, it can be an advantageous method for producing n-butanol commercial application. In addition, in the case of using a specific copper-based nanocomposite catalyst, n-butanoic acid alone is directly hydrogenated even under a reaction condition in which the n-butanoic acid reactant does not contain water, thereby suppressing side reactions while maintaining high selectivity and high space yield. Butanol can be produced, and thus n-butanol can be produced in an economical way.

1 shows a schematic of a biorefinary butanol preparation process.
2 is a mixture of 500 g / L glucose solution concentration and 1.5 g / L K ₂ HPO ₄ aqueous solution concentration was added 200 ml each during the fermentation process using Clostridium tyrobutyricum. It is a graph showing the glucose fermentation results of the case.
3 is a mixture of 300 ml and 200 ml of a total concentration of 500 g / L and a K ₂ HPO ₄ aqueous solution concentration of 1.5 g / L, respectively, in the middle of the fermentation process using Clostridium tyrobutyricum. It is a graph which shows the result of glucose fermentation in case of 500 ml addition.
4 shows the HPLC chromatogram of butanoic acid obtained by extractive distillation.
5 is a schematic diagram of a process for producing butanol by converting ammonium butyrate salt to butanoic acid using sulfuric acid and performing butanoic acid extraction, distillation and butanoic acid hydrogenation in an organic solvent.
6 is a schematic diagram of a process for producing butanol by converting ammonium butyrate salt to butanoic acid using hydrogen generated in the fermentation process and hydrogenating butanoic acid.
7 is a schematic diagram of a process of pyrolyzing an ammonium butyrate salt in an organic solvent to convert it to butanoic acid, and hydrogenating butanoic acid to produce butanol.

(Step 1: Fermentation process of biomass)

Biomass in the present invention means a renewable plant resources such as corn, soybeans, sugar cane, wood. In the fermentation process of the present invention, the parent strain is heat-treated and then inoculated into the medium, followed by incubation under anaerobic conditions, and then inoculated into a larger medium to carry out the seed culture. The seed culture solution is inoculated in a medium containing carbohydrates, yeast extracts, and the like to carry out fermentation. On a fermentor, the anaerobic conditions are maintained with nitrogen gas and the pH is adjusted with ammonia water and stirred.

In the fermentation process, as the parent strain, microorganisms that produce butanoic acid through fermentation are used, and any microorganism that generates butanoic acid is not particularly limited, but Clostridium , Butyrivibrio , Butyri Microorganisms in the genus Butyribacterium , Sarcina , Eubacterium , Fusobacterium and Megasphera can be used (Journal of Industrial Microbiology & Biotechnology 2000, 24: 153 -160), recombinant E. coli and recombinant Clostridium may be used (Appl. Microbiol. Biotechnol., 2008, 77: 1305-1316; Biotechnol. Bioeng., 2005, 90: 154-166). Preferably, Clostridium tyrobutyricum is used.

Clostridium tyrobutyricum, which has been widely used in butanoic acid production studies, is a gram-positive, rod-shaped, spore-forming, and obligate anaerobic bacterium. And butyric acid, acetic acid (CH ₃ COOH), hydrogen gas, and carbon dioxide are produced as main fermentation products from various carbohydrates, including xylose, and incubated under anaerobic conditions at 37 ° C. Clostridium tyrobutyricum is also called butyric acid bacteria because of its high yield and purity of butanoic acid production.

The fermenter used is not particularly limited, but it is preferable to use a fixed fibrous bed bioreactor (FBB) because the productivity can be increased.

(Second step: n-butanoic acid separation process)

Bio-derived chemical production by microbial fermentation, such as butanoic acid, typically consists of seed cultivation, fermentation, product recovery, concentration and purification. In fermentation-based processes, the purification cost is known to be approximately 60% or more of the total production cost. Therefore, the development of economical separation process is important, and in the case of butanoic acid purification, separation of by-products such as acetic acid is important. In the first stage, butanoic acid fermentation products are mainly obtained in the form of ammonium salts, alkali salts, or alkaline earth metal salts, and the fermentation broth containing butanoic acid is subjected to centrifugation or ultrafiltration. Before the butanoic acid is purified in step 2, acidic acid or acid gas is added to acidify the butanoic acid, followed by a separation and purification process, and pretreatment of centrifugation or ultrafiltration may be performed at any stage before or after acidification. Acids used for acidification of butane can be sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, acetic acid, and the like, and acidic gases can be carbon dioxide gas, hydrochloric acid gas, nitrogen oxides, sulfur oxides, and the like.

In the extraction distillation method using an organic solvent, in selecting an organic solvent (extractant), any organic solvent which is phase separated from water as an organic solvent used to recover butanoic acid from a fermentation broth may be considered. For example, aromatic solvents such as benzene, toluene, xylene, aromatic solvents partially substituted with chlorine or fluorine, organic solvents including halogen elements such as dichloromethane, chloroform, dichloroethane, methyl ethyl ketone, methyl isobutyl ketone Aliphatic alcohol solvents, such as ketone solvent, butanol, pentanol, hexanol, heptanol, and octanol, etc. can be used. It is preferable to use an organic solvent having a lower boiling point than the butanoic acid to be extracted in the solvent, and to select an organic solvent having high extraction selectivity for butanoic acid and by-product acetic acid as the extractant.

(Step 3: n-butanol manufacturing process)

(1) n-butanol production process using Ru / Sn / Zn catalyst

The inventors of the present invention have problems with the prior art using Ru-based catalysts for hydrogenation of carboxylic acids (e.g., a high reaction pressure is required as described above, the need to simultaneously supply more water than necessary to the reactants, and the productivity is low. N-butanoic acid in the case of a catalyst using zinc oxide (ZnO) as a carrier in a catalyst containing Ru at an appropriate concentration and reforming it with Sn during research to improve industrial production, etc.). It has been found that the hydrogenation reaction activity and selectivity of is significantly improved.

Hydrogenation of n-butanoic acid to produce n-butanol on Ru-Sn-ZnOx catalysts with a combination of Ru, Sn, and Zn components is possible even when pure n-butanoic acid or n-butanoic acid contains water. It exhibited high activity, high activity even at very low reaction pressures, and high productivity of sufficiently converting the reactants even at high space velocities.

In the catalyst of the present invention, Ru is a key main catalyst component exhibiting hydrogenation activity. When the number of atoms of the carrier component including the Zn component is 100, the number of Ru atoms is 1-20, preferably 2-10. When lower than this, the hydrogenation activity is low, and higher than this is not preferable considering the high price of Ru compared to the increase in activity.

The Sn component serves as a promoter of the Ru component and the number of atoms has a value in the range of 1 to 40, preferably 2 to 20. When it is lower or higher than this value, the effect is not high. Zn as a carrier mainly exists in an oxide state such as ZnO, and ZnO alone plays a sufficient role. However, in the catalyst of the present invention, when the extrusion molding method is used to use it as an industrial catalyst, an inorganic binder is added as necessary as a molding aid to have mechanical strength, and the inorganic binder (B) used is silica or At least one component selected from alumina and titanium dioxide may be further added. At this time, the addition amount of the inorganic binder B is added within a range of 50 or less (for example, when B is 50; Zn50-B50), preferably 20 or less, based on silicon, aluminum, and titanium elements. When the addition amount of the inorganic binder B is large, the catalytic activity is lowered, but the butanol selectivity during the hydrogenation reaction is lowered due to the increase in the dehydration capacity of the catalyst.

Meanwhile, the Ru component alone is sufficient as the main catalyst for the hydrogenation reaction, but Co, Ni, Cu, Ag, Rh, Pd, It may further comprise one or more components, A, selected from the group Re, Ir and Pt. At this time, the addition amount of the said component (A) is 1/2 or less with respect to Ru component. That is, it is added so as to have a value of 10 or less, preferably 5 or less. When the amount is large, the activity decreases due to the formation of an alloy or mixture with the Ru component, or the selectivity decreases due to decarboxylation.

In preparing the catalyst of Formula 1 of the present invention, a supporting method in which a component such as Ru, Sn is supported on a carrier including ZnO, or Sn and Zn oxide particles are first prepared, and at this time, other inorganic carrier components may be included. It can be manufactured by coprecipitation method or supporting method) or by the method of supporting reducing metal component including Ru component, or by any method such as coprecipitation method or sol-gel method that all catalyst components are coprecipitated at one time. It is possible.

The water-soluble salts necessary for the preparation of the catalyst may be chloride or nitrate, and the coprecipitation agent (or precipitant) may be any one selected from aqueous ammonia, sodium hydroxide, sodium carbonate and sodium bicarbonate. The shape of the catalyst molded body is not particularly limited, such as spherical shape, rod shape, and ring shape, and the molding method can be produced by any method such as extrusion molding, tablet molding, or supporting method.

The catalyst of the present invention prepared by the above-described method is subjected to a calcination process. The firing process is usually performed at 300 to 800 ° C, preferably at 350 to 600 ° C, under an air atmosphere.

The oxide catalyst of the formula (1) undergoes an activation process before the hydrogenation of n-butanoic acid, and the activation process is performed at 200 to 600 ° C., preferably at 250 to 400 ° C. using H ₂ / N ₂ mixed gas. To perform.

The hydrogenation conditions of n-butanoic acid are as follows. The hydrogenation reaction temperature is 150 ~ 400 ℃, and preferably 170 ~ 300 ℃, the reaction pressure is 0-50 atmospheric pressure, preferably the reaction pressure is from 1 to 50 atmospheres, more preferably 1 to 30 atm, H ₂ / n The molar ratio of butanoic acid is 10 to 200: 1, preferably 20 to 100: 1 and the feed rate of n-butanoic acid is supplied in the range of 0.05 to 5 hr ⁻¹ , preferably 0.2 to 3 hr ⁻¹ . The present invention is not limited to the water content of n-butanoic acid.

(2) n-butanol production process using copper catalyst

In general, in the reaction of producing an alcohol by hydrogenation of an organic carboxylic acid or anhydrides or esterified substances thereof, it is advantageous to obtain an appropriate reaction rate by increasing the reaction pressure, and to keep the reaction temperature as low as possible. This is because the selectivity decreases because the alcohol, which is a product, is dehydrated on the catalyst at a high temperature. Therefore, it is necessary to keep the reaction temperature low in order to suppress such dehydration reaction and obtain the target compound in high yield. However, in the case of the hydrogenation of esterification, since the hydrogenation proceeds at a reaction temperature of 140-200 ° C., the above-mentioned meaning is meaningful. However, in the case of hydrogenation of n-butanoic acid, which is the target reaction of the present invention, n-butanoic acid Due to the strong interaction between the carboxyl group and the metal as a reducing catalyst component, the reaction temperature at which the carboxylic acid is reduced is much higher than that of the esterified product. In addition, in order to obtain an appropriate reaction rate, it is necessary to keep the reaction pressure high. The n-butanoic acid should always be in contact with the catalyst in a gaseous state to avoid n-butanoic acid contacting the catalyst in liquid phase to liberate the catalyst component or cause particle growth to deactivate the catalyst. Therefore, in order for n-butanoic acid to exist in the gas state under high pressure conditions, it is necessary to maintain excess hydrogen flow conditions compared to n-butanoic acid, which means that hydrogenation of n-butanoic acid can be achieved within a short contact time. To satisfy this, the catalyst must have high activity. On the other hand, in order to reduce the energy cost and obtain the desired product in high yield, the reaction temperature and the pressure will be as low as possible.

In order to produce n-butanol in high yield and high productivity by gas phase reduction of n-butanoic acid under the above-described preconditions, the copper-based catalyst of the present invention has a content of copper oxide (precursor of copper component) in the catalyst composition. 40 to 95 wt%, preferably 50 to 90 wt%, and a catalyst prepared to have a particle size of copper oxide of 50 nm or less, preferably 30 nm or less, more preferably 20 nm or less. Should be In addition, silica, alumina, titania, zinc, etc. are used as the diluent together with the copper component, which is not a carrier in a conventional catalyst and is itself complexed with the copper component as nano-sized microparticles to form a nanocomposite. As a result, particle migration of the fine copper nanoparticles is suppressed, thereby helping the catalyst to have thermal stability.

The hydrogenation of n-butanoic acid is carried out at a reaction temperature of 200 to 350 ° C., preferably 220 to 300 ° C., whereas the particle migration of the microcopper particles, which is the main component of the catalyst, starts at about 180 ° C. [Topic in Catalysis 8 (1999) 259]. Therefore, the catalyst used in the present invention is less efficient when prepared by a general supporting method, it is efficient to prepare by the co-precipitation method or sol-gel method in order to obtain a compounding effect. In the case of gas phase hydrogenation of n-butanoic acid on a copper-based catalyst having the above-described properties, unlike the use of water in the above-mentioned patent documents, it is necessary to directly hydrogenate n-butanoic acid without using water. Butanol can be obtained with high productivity and high yield.

In the present invention, the gaseous hydrogenation conditions of n-butanoic acid on the catalyst are carried out under a reaction pressure of 5 to 70 atm, preferably 15 to 40 atm, in addition to the above reaction temperature, and when the pressure is low, the conversion rate is low and high. It is not preferable to use excess hydrogen to maintain the gaseous state of n-butanoic acid. In addition, the molar ratio of H ₂ / n-butanoic acid is 10 to 200: 1, preferably 20 to 150: 1, and when it is lower than this, it is difficult to maintain the gaseous state of n-butanoic acid, and when higher than this, excess hydrogen is recovered. This is undesirable because it must be reused. The feed rate (LHSV) of n-butanoic acid is 0.05-5 hr ⁻¹ , preferably 0.2-2 hr ⁻¹ .

In the present invention, the preferred catalyst is a catalyst for obtaining high selectivity by inhibiting dehydration reaction of the product n-butanol, considering that the hydrogenation reaction of n-butanoic acid is carried out at 200 ℃ or more, specifically 220 ~ 300 ℃ It is desirable to have weighting properties, and in this regard, a copper-silica composite catalyst in which the diluent is composed of silica nanoparticles in the above copper-based catalyst is effective in achieving the object of the present invention.

More preferably, cobalt, zinc, manganese, ruthenium, rhenium, palladium, platinum, silver, tellurium, selenium, magnesium as an improvement component in order to increase the hydrogenation capacity and to inhibit decarboxylation together with the copper component And catalysts modified with at least one or more of the components, such as calcium, are more effective. The promoter component is based on the copper oxide content It is preferable to use it at 20 wt% or less, and the catalyst performance is rather poor when used in excess. In the n-butanol production method of the present invention, the catalyst is usually prepared in the form of an oxide and filled in the reactor, and the activation is reduced by raising the temperature to 250-300 ° C. under a stream of hydrogen gas diluted with nitrogen before carrying out the reduction reaction. Go through the process.

(Step 4: High Purity Butanol Purification Process)

Butanol obtained in the three-stage hydrogenation process has a selectivity in the range of 90 to 99.9% when the reaction conditions are optimized, and the by-products include butanoic acid butyl ester, butanoic anhydride and water. Therefore, a butanol compound having a desired purity can be obtained through a general distillation process. This distillation process may be omitted when the butanol selectivity in the three stages is obtained very high, and may be used by sharing the distillation process of the four stages with the distillation column used in the two-stage extraction distillation process.

Hereinafter, the present invention will be described in more detail with reference to Examples. However, the scope of the present invention is not limited to the following examples.

Example 1

The mother strain Clostridium tyrobutyricum ATCC 25755 cells stored in spores at 4 ° C. were heat treated at 80 ° C. for 10 minutes, and then inoculated in 5 ml of RCM medium (manufactured by DIFCO) for 30 hours at 37 ° C. anaerobic conditions. After inoculating 1 ml into 100 ml of RCM medium prepared in a 500 ml flask, the resultant was incubated for about 12 hours. 100 ml of the seed culture solution, 50 g / L of glucose, 5 g / L of yeast extract, 1.5 g / L of K ₂ HPO ₄ , 5 g / L of Trypticase, (NH ₄ ) ₂ SO ₄ 3 g / L, Fermentation is performed by inoculating 2 L of medium containing 0.6 g / L of MgSO ₄ · 7H ₂ O and 0.03 g / L of FeSO ₄ · 7H ₂ O. Nitrogen gas is added at a rate of 100 ml / min and cultured under agitation conditions of pH 6.0, 37 ° C. and 200 rpm on a fermenter (bioflo 310, manufactured by NBS) maintaining an anaerobic state. pH adjustment was made into 14% ammonia water. In order to add the depleted glucose, the fermentation process was performed while adding in two patterns. In the first pattern, 200 ml of a mixed solution of 500 g / L of aqueous glucose solution and 1.5 g / L of aqueous K ₂ HPO ₄ solution was added at 17, 28, 41 and 48 hours, respectively. In the second pattern, 300 ml, 200 ml, and 500 ml of a mixed solution of 500 g / L and a K ₂ HPO ₄ aqueous solution concentration of 1.5 g / L were added three times at 17, 21 and 25 hours, respectively. The fermentation broth thus obtained is subjected to centrifugation or ultrafiltration to remove inorganics and insoluble suspended solids. 32 mL of H ₂ SO ₄ (98%) was added per 1 L of fermentation broth in order to convert the butyrate in the form of ammonium salt contained in the fermentation broth obtained through the above process into butanoic acid. At this time, the pH of the fermentation broth decreased from 6.6 to 2.7.

HPLC pumps (P1000, manufactured by spectrasystem), HPLC columns (Zorbax SB-Aq, 4.6 mm ID> 150 mm> 5 μm, manufactured by Agilent technology) and UV detectors (ACME 9000, Younglin instrument) to analyze the concentrations of butanoic and acetic acid Corp.) was used. The mobile phase flowed a 0.1 wt% H ₃ PO ₄ solution at a flow rate of 1 ml / min, with a sample injection volume of 20 μl. As shown in FIG. 2, the fermentation broth obtained by fermentation of 112 hours following the injection of the glucose solution of the first pattern, yielding 68.4 g / L butanate and 13.1 g / L acetate. 3 shows 62.4 g / L butanate and 10.7 g / L acetate as a result of analysis of the fermentation broth obtained by fermentation for 72 hours following the injection of the second solution of glucose solution.

[Example 2]

Into a three-necked flask equipped with a stirrer, 950 ml of the fermentation broth pretreated in Example 1 and 500 ml of dichloromethane as extractant were added and the strength of the agitation was adjusted to maintain phase separation between the aqueous solution and the organic solvent for 1 hour. Was stirred. 250 mL of the organic solvent layer was transferred to the flask for solvent distillation through the bottom outlet of the flask, where the organic solvent condensed after atmospheric distillation was again mixed with the fermentation broth and reused for extraction of the organic acid. Thereafter, the extraction and distillation were performed continuously for 6 hours while maintaining a constant level of the extraction flask. Analysis of the final aqueous solution layer showed that extraction efficiency of butanoic and acetic acid was 94.8% and 5.3%, respectively. 41.6 g of butanoic acid was recovered by distillation from the lower organic solvent layer containing organic acid, and GC analysis showed 99.8% purity, which contained 0.2% acetic acid as impurities (see FIGS. 4 and 5). ).

Example 3

The acidification process of butanate by the addition of inorganic or organic acid of Example 1 can be carried out in the same way by passing an acidic gas containing carbon dioxide. Particularly, when the aqueous solution of fermentation product and the organic solvent to be extracted are passed through the acidic gas, acidification and Carbonic acid extraction can also be performed simultaneously.

950 ml of the fermentation broth obtained by the fermentation process of Example 1 and 500 ml of dichloromethane as extractant were placed in a 3 L extraction autoclave equipped with a stirrer and pressurized at 150 ° C. or higher using carbon dioxide at room temperature. After stirring for 1 hour, the phases were separated to lower the pressure to normal pressure. Then, butanoic acid contained in the organic solvent was recovered by distillation under reduced pressure in the same manner as in Example 2, and the phase-separated fermentation broth layer was added to the extraction tank again in order to increase extraction efficiency, and the above process was repeated three more times to extract 85.2%. Efficiency was obtained and butanoic acid of purity 99.1% was obtained by atmospheric distillation.

In another method, the fermentation broth and the organic solvent were continuously passed through a pump through a countercurrent method through two extraction tanks pressurized by carbon dioxide, followed by distillation under reduced pressure after phase separation, in which case 93.5% of Extraction efficiency was obtained, and butanoic acid having a purity of 99.3% was obtained by atmospheric distillation. The carbon dioxide absorbed in the fermentation broth and organic extraction phase reacted with the salt of organic acid to produce a reusable bicarbonate of ammonium or sodium, precipitated in aqueous solution during the extraction process, separated by filtration, and then thermally decomposed by thermal decomposition at a temperature of 100 ° C. or higher. After removal, it could be reused for pH control of the fermentor again (see FIG. 6).

Example 4

Reaction extraction was attempted to separate butanoic acid from the fermentation broth. Trioctylamine (98%, manufactured by Aldrich) was used as an extractant, and dichloromethane was used as a diluent. 1 L fermentation broth and 1 L of dichloromethane solution containing 0.5 M trioctylamine were added to a 2 L flask equipped with a stirrer and stirred at room temperature for 1 hour until sufficient phase separation was achieved. I was stationed. After the extraction was completed, the aqueous phase contained 2.2 g / L butanoic acid and 11.7 g / L acetic acid, and extraction efficiency (E%) was 96.0% and 40.0% for butanoic acid and acetic acid, respectively. The organic solvent extraction layer containing the organic acid was transferred to a 1 L flask with a condenser to recover butanoic acid through distillation. Meanwhile, the extraction efficiency was calculated by measuring the concentration of the organic acid in the phase separated aqueous solution layer using HPLC. 18 g of butanoic acid was recovered by distillation from the lower organic solvent layer containing the organic acid, and the GC analysis showed a purity of 95.4%. It contained 3.2% acetic acid and 0.9% trioctylamine as impurities.

Example 5

This embodiment relates to the preparation of Ru-Sn-ZnO catalyst and the hydrogenation of butanoic acid using the same. 300 ml of 1.15 g of ruthenium chloride (RuCl ₃ , Ru 43.6 wt%), 1.901 g of tin (II) chloride (SnCl ₂ · 2H ₂ O) and 31.07 g of zinc nitrate (Zn (NO ₃ ) ₂ · 6H ₂ O) The solution (1) and sodium hydroxide solution (2) dissolved in deionized water were added dropwise simultaneously at room temperature and vigorously stirred to prepare a catalyst slurry solution by coprecipitation. Finally, the pH of the slurry solution was adjusted to 7.2, and the slurry solution was slowly heated to hydrothermally mature at 80 ° C for 5 hours. Thereafter, the temperature of the solution is reduced to room temperature, and the solution is sufficiently washed with deionized water and then filtered. The filtered cake was dried at 120 ° C. for 10 hours, and then the dried cake was made into a powder, molded into a tableting method, and then crushed and fractionated into a 20-40 mesh size. The fractionated catalyst was calcined at 450 ° C. for 6 hours in an air atmosphere.

2.0 g of a calcined oxide catalyst was charged in a tubular reactor, and slowly heated up while flowing a 5% H ₂ / N ₂ mixed gas, and activated at 280 ° C. for 12 hours.

N-butanoic acid obtained by fermentation and separation and purification in Examples 1 and 2 after catalytically reducing the catalyst was reacted with a reaction temperature of 250 ° C., a reaction pressure of 25 atm, WHSV = 1.0 hr ⁻¹ , H ₂ / n-butanoic acid (mol / mol) = 35 was reacted continuously. The product was collected and analyzed by GC (gas chromatography). As a result of the reaction, the conversion rate of n-butanoic acid was 99.9% and the selectivity of n-butanol was 98.3% after 100 hours.

Example 6

In the hydrogenation of the catalyst prepared in Example 5 as in the method described in Example 5, the activity of the catalyst was investigated while varying the reaction pressure. Except for the reaction pressure, the other conditions were the same as in Example 5. Experimental results are shown in the following [Table 1], the catalyst of the present invention showed a high activity even under low pressure of less than 5 atm.

Reaction pressure (atmospheric pressure) n-butanoic acid conversion (%) n-butanol selectivity (%) 20
10
7
2 99.9
99.9
99.9
99.6 98.6
98.3
98.4
98.5

Reaction conditions: WHSV = 1.0 hr ^-1 , H ₂ / n-butanoic acid (mol / mol) = 35

Example 7

In the reaction of the catalyst of Example 5 in the same manner as described in Example 5, the reaction was carried out under the same conditions except that n-butanoic acid having a water content of 10 wt% was reacted under the condition of WHSV = 1.1 hr ^-1 . . The reaction result was 99.9% n-butanoic acid conversion, 98.2% selectivity of n-butanol.

Example 8

In the reaction of the catalyst of Example 5 in the same manner as described in Example 5, the reaction was carried out continuously at a reaction pressure of 250 ° C. and 7 atmospheres for 1000 hours. After 1000 hours, the conversion rate of n-butanoic acid was 99.9% and the selectivity of n-butanol was 98.6%.

Example 9

A catalyst having a composition of Ru _4.75 Sn _8.07 Zn ₉₃ Si ₇ Ox was prepared in the same manner as in Example 5. SiO ₂ used was diluted with colloidal silica (Ludox SM-30, manufactured by Grace Davison) having an average particle size of 7 nm in deionized water having a pH of 9.5 (solution C). After the slurry was prepared, workup was carried out in the same methods and conditions as in Example 9 and hydrogenation of n-butanoic acid was carried out under the same reaction conditions as in Example 5.

The reaction result after 100 hours was 98.5% of n-butanoic acid conversion, 95.2% of the selectivity of n-butanol, and 3.5% of n-butanoic acid butyl ester which is an intermediate.

Example 10

A catalyst having a composition of Ru _4.75 Sn _8.07 Zn ₉₃ Ti ₇ Ox was prepared in the same manner as in Example 5 and Example 9. The Ti component was used by dissolving titanium isopropoxide (Ti (OiP) ₄ ) in an isopropanol solution (solution C). After the slurry was prepared, it was worked up as in Example 9 and hydrogenated n-butanoic acid under the reaction conditions of Example 5.

The reaction result after 100 hours was 97.7% n-butanoic acid conversion, 94.8% selectivity of n-butanol, and 3.9% selectivity of intermediate n-butanoic acid butyl ester.

Example 11

A catalyst having a composition of Ru _4.7 Cu _0.5 Sn _8.0 Zn ₁₀₀ Ox was prepared in the same manner as in Example 5. Cu dissolved copper nitrate (Cu (NO ₃ ) ₂ .3H ₂ O) together with Ru and Sn compounds (solution (1)) to prepare a catalyst. Post-treatment was carried out in the same methods and conditions as in Example 5 and hydrogenation of n-butanoic acid was carried out under the same reaction conditions.

After 100 hours, the conversion was 99.9% for n-butanoic acid and 98.9% for n-butanol.

Example 12

In preparing a catalyst having a composition of Ru _4.7 Co _0.5 Sn _8.0 Zn ₁₀₀ Ox in the same manner as in Example 5, the zinc oxide (ZnO) powder was first dispersed in water, and then Ru, Co, Sn components were dissolved in deionized water. A solution dissolved together with a sodium hydroxide solution was prepared by simultaneously dropping at room temperature. At this time, Co (NO ₃ ) ₂ · 6H ₂ O was used. Thereafter, the resultant was treated in the same manner as in Example 5, and the catalytic performance was examined under the same conditions.

After 100 hours, the conversion rate of n-butanoic acid was 99.9%, the selectivity of n-butanol was 95.2%, and the n-butanoic acid butyl ester was 3.7%.

Example 13

In preparing a catalyst having a composition of Ru _4.7 Pt _0.3 Re _0.3 Sn _8.0 Zn ₁₀₀ Ox, a slurry of the mixed oxygen-containing compound of Sn and Zn components was first prepared by coprecipitation in the catalyst preparation process of Example 10, and the slurry was stirred. The catalyst was prepared by dropping a solution in which Ru and Pt components were dissolved together in deionized water simultaneously with sodium hydroxide solution to adjust pH. At this time, Pt component was used H ₂ PtCl ₆ · 6H ₂ O. Thereafter, hydrothermal aging and washing and drying were performed in the same manner as in Example 4. The dried catalyst cake was powdered and loaded with a solution of Re ₂ O ₇ dissolved in deionized water. Thereafter, drying, firing, molding, crushing and fractionation, and firing were carried out under the same conditions as in Example 5, and the catalyst performance was investigated under the same conditions. After 100 hours, the conversion rate of n-butanoic acid was 99.9% or more and the selectivity of n-butanol was 98.4%.

Example 14

This embodiment relates to the preparation of a copper-silica-based nanocomposite catalyst and the hydrogenation of butanoic acid using the same. First, a solution (1) in which 50 g of copper nitrate [Cu (NO ₃ ) ₂ .3H ₂ O] was dissolved in 200 mL of deionized water was prepared to prepare a copper-silica nanocomposite catalyst. A solution of (2) prepared by adding sodium hydroxide aqueous solution to 100 ml of deionized water, adjusting the pH to 9.2, and adding 13.75 g of colloidal silica Ludox SM-30 thereto, and dissolving 16.6 g of sodium hydroxide in 200 ml of deionized water ( 3) was prepared. In the reactor to which the stirrer is attached, solutions A, B, and C are simultaneously added dropwise to carry out the precipitation process at 20 ° C. or lower. Thereafter, the obtained slurry solution was hydrothermally aged for 6 hours while being heated to 85 ° C. The resulting slurry was sufficiently washed with deionized water, filtered and the cake obtained was dried at 120 ° C. for 12 hours and then powdered.

The powder obtained was crushed to a size of 20 to 40 mesh after pressure molding, and then calcined at 600 ° C. for 6 hours to obtain an oxide catalyst. The copper oxide particle size of the catalyst was 4 nm, as measured by the XRD line broading method. 1.0 g of the catalyst was charged in a tubular reactor (ID = 7 mm) and heated to 280 ° C. while flowing N ₂ gas containing 5% H ₂ to activate the catalyst. The reaction was then carried out while adjusting the reactor temperature and pressure to 265 ° C., 370 psi and feeding the n-butanoic acid obtained by the fermentation and separation purification in Example 2 at a rate of 0.9 cc / hr under a hydrogen gas flow of 130 ml / min. Was performed. 24 hours after the start of the reaction, the conversion rate of n-butanoic acid was 99.9%, the selectivity of n-butanol was 94.3%, and the selectivity of n-butanoic acid butyl ester was 3.2%.

Example 15

This example relates to the preparation of a Cu-ZnO nanocomposite catalyst and to the hydrogenation of butanoic acid using the same. 50 ml of copper nitrate [Cu (NO ₃ ) ₂ · 3H ₂ O] and 15.05 g of zinc nitrate [Zn (NO ₃ ) ₂ · 6H ₂ O] in 200 ml of deionized water (1) and 200 ml of deionized water A solution (2) in which 20.6 g of sodium hydroxide was dissolved in was prepared. The coprecipitation process was performed by dropwise adding solutions (1) and (2) to the reactor to which the stirrer was attached. The subsequent procedure was the same as in Example 14, and the catalyst was calcined at 450 ° C. for 6 hours to obtain an oxide catalyst. The particle size of the copper oxide was 12 nm as measured by the XRD line broadening method.

1.0 g of the catalyst was charged into a tubular reactor and activated in the same manner as in Example 14. Then, the reaction was carried out under the same reaction conditions. 24 hours after the initiation of the reaction, the selectivity of n-butanol was 81.5% and that of n-butanol was 18.2%.

Example 16

This embodiment relates to the preparation of a Cu-SiO ₂ -TiO ₂ nanocomposite catalyst and to the hydrogenation of butanoic acid using the same. The catalyst was prepared in the same manner as in Example 15. However, TiO ₂ was used as a precursor of titanium (IV) isopropoxide [Titanium (IV) isopropoxide], which was dissolved in isopropanol. The copper oxide particle size of the catalyst calcined at 600 ° C. was 15 nm. 1.0 g of the catalyst was charged to a tubular reactor and activated in the same manner as in Example 13, and the reaction was carried out under the same conditions. 24 hours after the start of the reaction, the conversion of n-butanoic acid was 99.9%, the selectivity of n-butanol was 94.5%, and the selectivity of butyl n-butanoate was 1.3%.

Example 17

This embodiment relates to the preparation of CuO-CoO-ZnO-CaO-MgO-TeO ₂ -SiO ₂ nanocomposite catalyst and hydrogenation of butanoic acid using the same. Deionized water 200 ㎖ the copper nitrate _{[Cu (NO 3) 2 ·} 3H 2 O] 50 g, cobalt nitrate _{[Co (NO 3) 2 ·} 3H 2 O] 2.3 g, zinc nitrate _{[Zn (NO 3) 2 ·} 3H ₂ O] 0.15 g was dissolved to prepare a solution (1). Aqueous solution of sodium hydroxide was added to 100 ml of deionized water to adjust the pH to 9.2, and a solution (2) containing 11 g of colloidal silica Ludox SM-30 was prepared. A solution of 17.3 g of sodium hydroxide dissolved in 200 ml of deionized water (3 ) Was prepared. The solution (1), (2) and (3) were added dropwise to the reactor to which the stirrer was attached at the same time, and the coprecipitation process was performed at 20 degrees C or less. At this time, the dropping rate of the solution (3) was adjusted to adjust the pH, and after completion of coprecipitation, the final pH of the slurry solution was adjusted to 9.30. Thereafter, after hydrothermal aging at 85 ° C. for 6 hours, the obtained slurry was sufficiently washed with deionized water, filtered and the precipitate was recovered. To the cake obtained was removed 0.13 g calcium acetate [Ca (OAc) ₂ H ₂ O], 0.22 g magnesium acetate [Mg (OAc) ₂ 4H ₂ O] and telluric acid [Te (OH) ₆ ] 0.006 g. A solution dissolved in deionized water was added, mixed, dried at 120 ° C. for 12 hours, and then powdered. The powder was crushed to a size of 20-40 mesh after pressure molding, and fractionated and calcined at 600 ° C. for 5 hours to obtain an oxide catalyst. The copper oxide particle size of the catalyst was 5.6 nm as measured by the X-ray diffraction line broadening method.

1.0 g of the catalyst was charged to a tubular reactor, activated in the same manner as in Example 14, and then reacted under the same reaction conditions. 24 hours after the initiation of the reaction, the conversion of n-butanoic acid was 100%, the selectivity of n-butanol was 96.2%, and the selectivity of n-butanoic acid butyl ester was 1.4%.

Example 18

Except for using n-butanoic acid: butanoic anhydride = 50: 50 (weight ratio) instead of n-butanoic acid as the reactant in Example 14, the same. 24 hours after the start of the reaction, the conversion of n-butanoic acid was 100%, the selectivity of n-butanol was 96.0%, and the selectivity of n-butanoic acid butyl ester was 1.2%.

Comparative Example 1

A catalyst having a composition of Ru ₄ Sn _7.5 (Al ₂ O ₃ ) ₁₀₀ was prepared in the same manner as in Example 5. After the slurry was prepared, workup was carried out in the same methods and conditions as in Example 9 and hydrogenation of n-butanoic acid was carried out under the same reaction conditions as in Example 5.

The reaction result after 240 hours was 90.5% of n-butanoic acid conversion, 85.7% of n-butanol selectivity, and 12.3% of n-butanoic acid butyl ester.

Example 19

Reaction extraction was attempted to separate butanoic acid from the pretreated fermentation broth. Tributyl phosphate (98%, manufactured by Aldrich) was used as the extractant. Into a 2 L flask equipped with a vacuum pump and a stirrer, 200 mL of the purified fermentation broth and 1 L of tributyl phosphate were added, and the vacuum pump was turned on to maintain a vacuum degree of about 200 mmHg. Thereafter, the flask containing the reactant was heated to adjust the final temperature of the reaction solution to maintain 110 ° C. The acetic acid, water and ammonia mixed gas obtained in the gas phase in the reaction process were further condensed at room temperature to separate the ammonia gas from the acetic acid aqueous solution. After the reaction for about 1 hour, the vacuum pump was turned off and the tributylphosphate extract containing butanoic acid was transferred to a 1 L flask equipped with a condenser to recover butanoic acid by distillation at 170 ° C. The concentration of the recovered butanoic acid was analyzed by GC, and the purity was found to be 99.5% (see FIG. 7).

Example 20

In order to separate hydrogen and carbon dioxide generated as by-products during the fermentation of glucose, a mixed gas (hydrogen / carbon dioxide = 1) was introduced in a pressure circulation operation using a zeolite-filled adsorption tower. At this time, the adsorption temperature was 30 ° C., the adsorption pressure was 15 atm, and desorption was performed at atmospheric pressure and 120 ° C. Through this process, hydrogen and carbon dioxide with a purity of 99.9% or more were obtained, and the total recovery was 83%.

Claims

A ruthenium-based catalyst of the general formula (1), which is used to directly reduce the C1-10 monocarboxylic acid or a derivative thereof by hydrogen.
[Formula 1]
Ru (a) Sn (b) Zn (d) Ox
Where
(a), (b) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) represents 1-20 and (b) represents 1-40;
x is the number of atoms of oxygen, which is determined by the valence and composition ratio of other components.

The method of claim 1, wherein the ruthenium-based catalyst is represented by the following formula (2) further comprising at least one component A selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir and Pt A ruthenium-based catalyst characterized by:
(2)
Ru (a) Sn (b) A (c) Zn (d) Ox
Where
-(a), (b), (c) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) is 1-20, (b) is 1- 40, (c) represents over 0 to 20;
x is the number of atoms of oxygen, which is determined by the valence and composition ratio of other components.

The ruthenium catalyst according to claim 2, wherein the ruthenium catalyst is represented by the following Chemical Formula 3 further comprising at least one component B selected from the group consisting of Si, Ti, and Al:
(3)
Ru (a) Sn (b) A (c) Zn (d) B (e) Ox
Where
A represents at least one component selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir and Pt;
B represents at least one component selected from the group consisting of Si, Ti and Al;
-(a), (b), (c), (d) and (e) are the component ratios based on the number of atoms of each component, based on the case where (d) + (e) is 100,
(a) is 1-20;
(b) is 1 to 40;
(c) is greater than 0 and 20;
(d) d is at least 50;
(e) represents greater than 0 and less than or equal to 50;
x is the number of atoms of oxygen, determined by the valence and composition ratios of the other components.

Process for producing high purity n-butanol comprising the following steps (1) to (4):
(1) fermenting the biomass using the microorganisms;
(2) separating n-butanoic acid from the fermentation broth obtained in (1);
(3) directly gas-reducing the n-butanoic acid separated in (2) by hydrogen over a ruthenium-based catalyst of Formula 1 below; And
(4) Butanol purification step by distillation of butanol obtained in (3).
[Formula 1]
Ru (a) Sn (b) Zn (d) Ox
Where
(a), (b) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) represents 1-20 and (b) represents 1-40;
x is the number of atoms of oxygen, which is determined by the valence and composition ratio of other components.

The method according to claim 4, wherein the ruthenium-based catalyst is represented by the following Chemical Formula 2 further comprising at least one component A selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir and Pt. Characterized in that the process for producing n-butanol:
(2)
Ru (a) Sn (b) A (c) Zn (d) Ox
Where
-(a), (b), (c) and (d) are component ratios based on the number of atoms of each component, and when (d) is 100, (a) is 1-20, (b) is 1- 40, (c) represents over 0 to 20;
x is the number of atoms of oxygen, which is determined by the valence and composition ratio of other components.

The method of claim 5, wherein the ruthenium-based catalyst is represented by the following Chemical Formula 3 further comprising at least one component B selected from the group consisting of Si, Ti, and Al:
(3)
Ru (a) Sn (b) A (c) Zn (d) B (e) Ox
Where
A represents at least one component selected from the group consisting of Co, Ni, Cu, Ag, Rh, Pd, Re, Ir and Pt;
B represents at least one component selected from the group consisting of Si, Ti and Al;
-(a), (b), (c), (d) and (e) are the component ratios based on the number of atoms of each component, based on the case where (d) + (e) is 100,
(a) is 1-20;
(b) is 1 to 40;
(c) is greater than 0 and 20;
(d) d is at least 50;
(e) represents greater than 0 and less than or equal to 50;
x is the number of atoms of oxygen, determined by the valence and composition ratios of the other components.

The method according to any one of claims 4 to 6, wherein the oxide catalyst of any one of formulas (1) to (3) uses a mixed gas containing hydrogen before carrying out the hydrogenation of n-butanoic acid. It is activated in, characterized in that for producing n-butanol.

The process for producing n-butanol according to any one of claims 4 to 6, wherein the n-butanoic acid is gas phase reduced at a reaction temperature of 150 to 400 ° C and a reaction pressure of 1 to 50 atmospheres.

Process for producing high purity n-butanol comprising the following steps (1) to (4):
(1) fermenting the biomass using the microorganisms;
(2) separating n-butanoic acid from the fermentation broth obtained in (1);
(3) directly gas-reducing the n-butanoic acid separated in (2) by hydrogen over a copper-based catalyst; And
(4) Butanol purification step by distillation of butanol obtained in (3)
{The copper-based catalyst is obtained by reducing a composite oxide of a copper oxide component and at least one diluent selected from the group consisting of silica, alumina, titania, and zinc oxide, and the content of the copper oxide component in the catalyst is 40-. 95 wt% and the size of the particles of copper oxide is 50 nm or less.

The process for producing n-butanol according to claim 9, wherein the n-butanoic acid is gas phase reduced at a reaction temperature of 220 to 300 ° C and a reaction pressure of 5 to 70 atm.

The method for producing n-butanol according to claim 4 or 9, wherein the microorganism of step (1) is Clostridium series.

10. The process for producing n-butanol according to claim 4 or 9, wherein the molar ratio of hydrogen to n-butanoic acid in step (3) is 10 to 200: 1.

The method for producing n-butanol according to claim 4 or 9, wherein the feeding rate (LHSV) of n-butanoic acid in step (3) is 0.05 to 5 hr ⁻¹ .

10. The inorganic or organic acid containing sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, acetic acid, carbon dioxide gas, hydrochloric acid gas, nitrogen oxide, sulfuric acid according to claim 4 or 9 for acidification of the fermentation broth obtained in step (1). Method for producing n-butanol, characterized in that using a combination of one or more of the acidic gas containing a cargo.

15. The method of claim 14, wherein in the acidification of the fermentation broth obtained in step (1), carbon dioxide is pressurized to a mixed solution of the fermentation broth and an organic solvent used as an extractant at a temperature in the range of 5 to 50 ° C. and a pressure of 50 psig or more. A process for producing n-butanol, wherein acidification and extractive distillation are carried out simultaneously by distilling butanoic acid extracted into an organic solvent.

The organic solvent according to claim 4 or 9, wherein the organic solvent is separated and purified by extractive distillation of the fermentation broth obtained in the step (1), and an aromatic solvent containing benzene, toluene, and xylene, a part of which is chlorine or fluorine. Substituted aromatic solvent, dichloromethane, chloroform, organic solvent containing halogen element including dichloroethane, ketone solvent including methyl ethyl ketone, methyl isobutyl ketone, butanol, pentanol, hexanol, heptanol, octanol A method for producing n-butanol, characterized in that one or more combinations of aliphatic alcohol solvents are used.

10. The method of claim 4 or 9, wherein the mixture of ammonium butyrate and ammonium acetate contained in the fermentation broth obtained in step (1) is mixed with the organic solvent extractant in step (2), and then pyrolyzed, and the organic solvent Method for producing n-butanol, characterized in that by distilling butane and acetic acid contained in the extractant.

18. The method for producing n-butanol according to claim 17, wherein any one of a trialkylamine or a trialkyl phosphate organic solvent containing a C1-20 alkyl group is used as the organic solvent extractant.

18. The process for producing n-butanol according to claim 17, wherein the pyrolysis is carried out at a temperature of 110 to 150 DEG C and a pressure of 1 atm or less.

10. The method according to claim 4 or 9, wherein the mixed gas of carbon dioxide and hydrogen generated in step (1) is separated, so that carbon dioxide is used for acidification of ammonium butyrate and hydrogen is used for hydrogenation of step (3). A method for producing n-butanol.