KR20110084567A - A method for conversion of aldehyde prepared from olefin as alcohol and an apparatus used for this method - Google Patents

Abstract

PURPOSE: A method for converting olefin-derived aldehydes into alcohols is provided to rapidly change olefin-derived aldehydes to desired alcohols, to avoid a separate hydrogenation reactor, and to reduce a reaction process. CONSTITUTION: A method for converting olefin-derived aldehydes into alcohols comprises: performing the hydroformylation by supplying a hydroformylation catalyst and synthetic gas including olefin, carbon monoxide and hydrogen to a venturi-loop reactor or a stirred reactor including a sparger; and performing the hydrogenation of the aldehyde prepared by the hydroformylation by supplying a hydrogenation catalyst and hydrogen gas on the outside circulation loop of the reactor.

Description

A method for conversion of aldehyde prepared from olefin as alcohol and an apparatus used for this method}

The present invention relates to a method for converting olefin-derived aldehydes to alcohols and a reaction apparatus used therein. More particularly, the present invention provides a method for controlling hydroformylation and hydrogenation by appropriately adjusting the supply sequence of syngas and hydrogen gas. Not only can alcohol be rapidly converted from aldehydes prepared from olefins, but it also relates to a process for shortening the reaction process and a reaction apparatus used therein.

A method of hydroformylating olefins with carbon monoxide and hydrogen in the presence of transition metal catalysts such as cobalt and rhodium compounds to produce aldehydes having one more carbon is known as oxo synthesis.

In general, large amounts of straight chain aldehydes are preferred for hydroformylation of olefins that produce aldehydes. Linear terminal olefins (α-olefins) can be hydroformylated very easily using phosphine modified rhodium or cobalt catalysts, but unmodified cobalt and rhodium catalysts for low reactive olefins, internal olefins and internal side chain olefins It is used first.

Through numerous literatures, such as German Patent No. 2,139,630, the olefins loaded on the cobalt catalyst in the hydroformylation step are hydroformylated by synthesis gas at a temperature of 70 to 170 ° C. and a pressure of 100 to 400 bar in a high pressure reactor to obtain a corresponding It is known that aldehydes can be obtained. Some of the aldehydes formed may be hydrogenated with alcohols under hydroformylation conditions, especially at high temperatures.

The reaction products containing useful by-products, i.e., non-hydroformylated residual olefins, and catalysts, in addition to aldehydes and alcohols, are separated from the gas phase and then added to the corresponding alcohols in further process steps such as hydrogenation and distillation. Is switched.

In this prehydrogenation step, ie hydroformylation step, a synthesis gas of a mixture of carbon monoxide and hydrogen is used. Since hydrogen gas is also included in the synthesis gas, it would be particularly appealing to be able to complete catalysts, reaction conditions and the like that can hydrogenate the products of the preceding hydroformylation step together in the presence of the synthesis gas.

In order to solve the above problems, the present inventors continue to study, and as a result, by appropriately adjusting the supply sequence of syngas and hydrogen gas, hydroformylation reaction and hydrogenation reaction are performed to quickly convert the desired alcohol from olefin-derived aldehydes. It has been found that not only is it possible but also that the reaction process can be shortened and the present invention has been completed.

That is, an object of the present invention is to provide a method for rapidly converting aldehydes prepared from olefins to alcohols.

Another object of the present invention is to provide a reaction apparatus capable of shortening the reaction process while achieving the above method.

As means for solving the above problems, in the present invention

A hydroformylation reaction is performed by supplying a syngas containing olefin, carbon monoxide and hydrogen, and a hydroformylation catalyst into a venturi-loop reactor or a stirred reactor equipped with a sparger.

Provides a method for converting olefin-derived aldehyde to alcohol, characterized in that the hydrogenation reaction for the aldehyde produced by the hydroformylation reaction by supplying a hydrogenation catalyst and hydrogen gas on the outer circulation loop of the reactor. .

In the present invention,

Hydroformylation reactors for preparing aldehydes from olefins; A hydrogenation catalyst filling cartridge provided on an outer circulation loop of the hydroformylation reactor; And a heat exchanger;

The hydroformylation reactor is a stirred reactor equipped with a venturi-loop reactor or a sparger, and a hydrogen supply pipe is provided in a circulation loop between the lower portion of the hydroformylation reactor and the hydrogenation cartridge, and the hydrogenation cartridge and heat Provided is a reaction apparatus for converting olefin-derived aldehydes to alcohols, wherein an alcohol separation pipe is provided in the circulation loop between the exchangers.

EMBODIMENT OF THE INVENTION Hereinafter, this invention is demonstrated in detail.

In the present invention, olefins are hydroformylated to produce normal- and iso-butylaldehyde, and these are added for the production of solvents and plasticizers through heterogeneous hydrogenation catalysts charged in the reactor or in an external circulation loop by addition of hydrogen gas. It is a technical feature to quickly carry out the hydrogenation reaction to the corresponding alcohol which can be used.

The reactor is a venturi-loop reactor or sparger in view of the necessity of spraying a small gas phase droplet in the liquid phase of the gas phase reactant to have a wide contact surface in order to facilitate the contact and reaction between the gaseous reactant and the liquid or solid phase catalyst. Using a stirred reactor equipped with It is preferable. In addition, for the purpose of facilitating mixing and mass transfer, a type of reactor partitioned into a liquid-phase two stage may be applied, or one or more holes may be formed on the nozzle.

The hydroformylation catalyst composition used in the present invention is composed of a metal-carbonyl complex catalyst and a ligand as a catalyst solution for homogeneous hydroformylation reaction, and the concentration of the metal-carbonyl complex catalyst is 10 to 2000 ppm. The concentration of the ligand is preferably 1 to 30 wt%.

As the homogeneous hydroformylation catalyst, a homogeneous catalyst mainly composed of Group VIII transition metals such as rhodium (Rh), cobalt (Co), and iridium (Ir) may be used. As a ligand, hydride (H ⁻ ), Carbonyl (CO), triphenylphosphine (TPP) and the like can be used, but not limited thereto, and those known in the art can be used. Although rhodium catalysts are expensive, they provide more stable reaction conditions for hydroformylation processes than cobalt or iridium catalysts, and most commercial processes employ them because of their superior catalytic activity and high selectivity.

In addition, the hydrogenation catalyst composition used in the present invention includes copper on a support as a catalyst for a heterogeneous hydrogenation reaction. The catalyst may be a higher catalyst wherein copper is part of the alloy and / or the catalyst comprises an additional promoter metal. Suitable alloys include Group 8 to 11 metals. Suitable promoter metals include Group 1-7 metals. However, it has been found that conventional catalysts based on copper as the only active ingredient are very acceptable.

Suitable catalyst supports include inert carriers based on metal or glass sponges, inorganic carbides, or oxides, or carbon. For example, the support may be based on oxides of Groups 2-6 and 12-14 metals and mixtures thereof, such as ZnO, titania, alumina, zirconia, silica and / or zeolites. Preferred supports are resistant to acidic media. Suitable results can be achieved with ZnO phase, silica phase, and Cr ₂ O ₃ phase copper.

For example, any catalyst used in the current hydrogenation process, such as a catalyst supporting Al ₂ O ₃ as a support using copper as a main component and Zn as a promoter, can be used without limitation.

The support described above may be used as a powder or molded into shaped articles such as pellets, granules, or extrudates, for example. Alternatively, the support may be in the form of a honeycomb, foam, sponge or similarly large monolith.

In addition, the amount of copper used may also vary widely, for example on the support in an amount of 0.1 to 80% by weight, preferably 10 to 50% by weight, more preferably 25 to 35% by weight. May exist.

The synthesis of copper catalysts is common and typically involves coprecipitation of copper and the support precursor. Optionally, also the carrier is doped with a copper solution, the loaded carrier is calcined and then it is H ₂ at high temperature. It can be prepared by reducing under. The copper catalyst thus supported can be used in semi-continuous processes of continuous processes, batch processes.

Specifically, the catalyst is prepared by co-precipitating a metal precursor, followed by drying, calcining, and molding to prepare a metal catalyst in an oxidized form. The catalyst thus prepared is charged into a cartridge, and after being mounted in a loop reactor, the catalyst is reduced to high temperature with hydrogen and converted into an active catalyst before the reactant is introduced.

Finally, the heterogeneous hydrogenation catalyst can be used in a suitable content in the range of 0.1 to 50% by weight, preferably 1.0 to 10% by weight of the catalyst calculated as the weight of the olefin. The hydrogenation catalyst is installed in a cartridge filled form on the circulation loop of the venturi-loop to convert aldehydes produced in the reactor to alcohol.

Preferred types of olefins for use in the present invention are ethylene, propylene, butene, 1-hexene, 1-octene, 1-nonene, 1-decene, 1-undecene, 1-tridecene, 1-tetradecene, 1-penta Decene, 1-hexadecene, 1-heptadecene, 1-octadecene, 1-nonadecene, 1-eicosene, 2-butene, 2-methylpropene, 2-pentene, 2-hexene, 2-heptene, 2 -Ethylhexene, 2-octene, styrene, 3-phenyl-1-propene, 1,4-hexadiene, 1,7-octadiene, 3-cyclohexyl-1-butene, allyl acetate, allylbutyrate, methylmetha Acrylate, vinyl methyl ether, vinyl ethyl ether, allyl ethyl ether, n-propyl-7-octenoate, 3-butenenitrile, 5-hexenamide, 4-methylstyrene, 4-isopropylstyrene, and the like. In particular, the carbon number and the linear type are preferable for the present invention.

As the injected synthesis gas, the mixing ratio of CO to H ₂ is preferably 5:95 to 70:30, and more preferably 50:50. Meanwhile, hydrogen required for the hydrogenation reaction is separately supplied into the circulation loop by an amount necessary for hydrogenation separately before the hydrogenation catalyst cartridge installed in the loop.

The olefin and syngas are each fed to the inside of the reactor in a molar ratio of olefin: CO: H ₂ in the range of 1: 1.2: 1.2 to 1: 0.8: 0.8, preferably 1: 1: 1 under pressure of 5 to 200 bar, respectively. do. In addition, the amount of additional hydrogen is preferably supplied in a molar ratio of the supplied olefin and olefin: H ₂ 1: 0.8 to 1: 1.2, preferably 1: 1.

The solvent used in the catalyst mixed solution is not limited thereto, for example, aldehydes such as propane aldehyde, butyl aldehyde, pentyl aldehyde, or valer aldehyde; Ketones such as acetone, methyl ethyl ketone, methyl isobutyl ketone, acetophenone, or cyclohexanone; Alcohols such as ethanol, pentanol, octanol and tensanol; Aromatics such as benzene, toluene and xylene; Ethers such as tetrahydrofuran, dimethoxyethane and dioxane; And paraffin hydrocarbons such as heptane. Preferably, the aldehyde produced through the hydroformylation reaction from the olefin used as the raw material is used as the raw material. For example, propylene aldehyde is used when propylene is a raw material, and pentyl aldehyde is used when butylene is a raw material.

In addition, the concentration of the catalyst mixture solution is preferably 10 to 2000 ppm for the metal carbonyl complex catalyst and 1 to 30 wt% for the ligand.

Normally, iso-butylaldehyde is produced first because only the hydroformylation catalyst is contained in the loop reactor. The production ratio of the generated normal-, iso-butylaldehyde can be adjusted within the range of 1: 1 to 30: 1 depending on the type of ligand. Triphenylphosphine (TPP) in the commonly used phosphine ligand is particularly suitable for use in the present invention because aldehyde can be produced in a ratio of about 10: 1. On the other hand, after passing through the hydrogenation catalyst cartridge of the outer circulation loop, the normal-, iso-butylaldehyde is hydrogenated to produce normal-, iso-butanol, and this ratio maintains the ratio of the aldehyde generated in the reactor.

The hydroformylation reaction is carried out at a temperature of 50 to 200 ℃, preferably 50 to 150 ℃, pressure is 5 to 100 bar, preferably 5 to 50 bar. In particular, the rotational flow rate of the venturi-loop is preferably one rotation of the solution in the reactor.

On the other hand, the reaction mixture in the reactor of the present invention contains aldehydes, unconverted olefins and catalyst compositions and the like. The catalyst composition in the reactor includes a rhodium catalyst and a ligand capable of carrying out the hydroformylation reaction, and includes a copper catalyst, a nickel catalyst or a copper-zinc catalyst for hydrogenation reaction in the reactor or on an external circulation loop.

Furthermore, the reaction mixture is fed to a distillation column to recover normal- and iso-butylaldehyde, normal-butanol and iso-butanol.

In the present invention, a reaction apparatus capable of rapidly converting an olefin-derived aldehyde into an alcohol is provided.

First, it is possible to use a stirred reactor equipped with a venturi-loop or a sparger as a reactor for the hydroformylation reaction, and using a venturi-loop reactor as described in the following examples will facilitate gas-liquid contact. It is more preferable in view of reaction efficiency.

The venturi-nozzle reactor has a nozzle coupled to the venturi as an injection means is provided at the upper end of the reactor, and the nozzle is formed integrally at the lower end of the reactor inlet, but has an enlarged shape consisting of an expansion part that is widened toward the reactor outlet side. In addition, it is preferable that one or more holes are formed in the upper part of the expansion pipe to induce mixing and delivery promotion.

The diameter of the nozzle is 0.1 to 500 mm, the diameter of the inlet is preferably 1 to 10 times the diameter of the nozzle. In addition, the inlet is preferably a venturi tube is coupled to the ejector. The venturi tube includes a diffusion portion consisting of an inlet formed in the form of a straight tube and a tube extending downward, wherein the inlet is coupled to the ejector and the diameter of the inlet is the same as the diameter of the inlet of the diffuser. Smaller than the diameter of the outlet. At the same time, it is preferable that the outlet direction of the diffusion portion is toward the bottom of the reactor. The diameter of the inlet is preferably 0.2 to 100 mm, and the length of the diffusion inlet is preferably 1/50 to 1/2 of the total length of the reactor. The diameter of the diffuser inlet is equal to the diameter of the inlet and the diameter of the diffuser outlet is preferably 0.1 to 10 times the diameter of the diffuser inlet. In addition, it is preferable that the length of the diffusion portion is 0.1 to 10 times the length of the inlet portion, and the length of the entire venturi tube combined with the inlet portion and the diffusion portion is preferably 0.01 times to 0.95 times the length of the main body, and is 0.05 times to 0.75 times the length of the main body. More preferred.

A dispersion plate is provided between the injection means and the reactor outlet to switch the flow of olefin and syngas, the dispersion plate is 0.5 to 0.9 times the diameter of the reactor, 1/3 to 2 / of the venturi and reactor outlet. It is preferably located between three and is flat, convex or concave with respect to the reactor outlet. In the outer circulation loop of the venturi loop reactor, a cartridge loaded with a hydrogenation catalyst is installed, and a separate line for supplying hydrogen or a mixed gas of hydrogen and CO is installed in front of the cartridge of the hydrogenation catalyst.

Hereinafter, in order to clearly understand and easily carry out the present invention, it will be described by the accompanying schematic drawings. In FIG. 1, various standard items actually used in a factory, such as a valve, a temperature measuring device, and a pressure regulating device, which can be easily recognized by those skilled in the art, are omitted.

1 schematically shows the hydroformylation process of an olefin according to one embodiment of the invention. The olefin (e.g., propylene) and the synthesis gas (carbon monoxide + hydrogen) are respectively composed of a homogeneous hydroformylation catalyst solution and a heterogeneous hydrogenation catalyst through the olefin supply pipe (10) and the synthesis gas supply pipe (11). The composition is fed to a nozzle 20 at the top of the reactor 100 in which it is charged.

In order to increase the efficiency of the gas-liquid reaction, a nozzle 20 and a venturi 30 coupled to the nozzle are installed inside the reactor 100, and the supplied olefin and syngas are vented through the nozzle 20. The jet 30 is continuously sprayed and supplied. As such, the oxo reactor 100 may be a reactor equipped with a nozzle or a nozzle and a venturi for the purpose of increasing the efficiency of the gas-liquid reaction therein, and preferably, may be a venturi-loop reactor. have.

The hydrogenation catalyst is also mounted on an outer circulation loop filled in the hydrogenation catalyst cartridge 200, and additional hydrogen gas for hydrogenation is supplied through a hydrogen gas supply pipe 60 connected to the front end of the hydrogenation catalyst cartridge. The hydrogen gas supplied is subjected to a hydrogenation reaction in the presence of a catalyst to convert aldehydes to the corresponding alcohols without a separate hydrogenation reactor. The alcohol of interest is recovered from the reaction mixture and the remaining reaction mixture may be recycled to the reactor 100.

In some cases, a portion of the recycled reaction mixture may be withdrawn to regenerate the catalyst, or fresh catalyst solution or reactivated catalyst solution may be added to the recycle stream of the reaction mixture. The heat exchanger 50 may be provided between the circulation pipes 14 and 16, but the position is not limited to a specific position on the circulation cycle. The heat exchanger 50 serves to maintain the reaction mixture recycled to the reactor 100 at a temperature suitable for the reaction conditions.

According to the present invention, by appropriately adjusting the supply sequence of the synthesis gas and hydrogen gas to perform the hydroformylation reaction and hydrogenation reaction, it is possible to quickly convert the desired alcohol from the olefin-derived aldehyde, and also does not require a hydrogenation reactor separately The process can be shortened.

1 is a schematic device diagram showing a series of processes for rapidly converting an aldehyde prepared from an olefin into an alcohol according to an embodiment of the present invention.

Hereinafter, the present invention will be described in more detail with reference to Examples and Comparative Examples, which are intended to help a specific understanding of the present invention, and the scope of the present invention is not limited to the Examples.

< Example  One: Venturi When using a loop reactor

A venturi-loop reactor 100 having a capacity of 3 liters was manufactured and installed as shown in FIG. 1. The reactor 100 was allowed to flow the heat medium oil in the jacket instead of the external heat exchanger 70 to maintain a constant temperature inside the reactor.

The diameter of the nozzle 20 mounted in the venturi-loop reactor 100 was 1.7 mm, the diameter of the inlet was 8.0 mm, the length was 50 mm and the diameter of the diffuser was 25 mm and the length was 200 mm.

In 800 g of purified n-butylaldehyde, 48 g of triphenylphosphine (TPP) and 0.8 g of rhodium triphenylphosphine acetylacetonate carbonyl (ROPAC) were dissolved to dissolve n-butylaldehyde catalyst solution (for homogeneous hydroformylation reaction). Catalyst).

Further, the copper zinc metal catalyst was supported on silica, and 100 g was charged into the cartridge 200 on the reactor circulation loop together as a catalyst for heterogeneous hydrogenation reaction. That is, the prepared catalyst solution is added to the reactor 100 and the heterogeneous catalyst is added to the cartridge, respectively, and then the external circulation pump 40 is operated to slowly circulate the catalyst solution at a rate of 1.5 liters per minute while the reactor 100 The entire system was purged three times with purified nitrogen gas through the top nozzle 20.

The external circulation pump 40 was continuously maintained at a rate of 2.0 liters per minute, while the heat medium oil was poured into a jacket outside the venturi-loop reactor 100 to maintain the temperature inside the reactor 100 at 90 ° C. When the temperature stabilized at 90 ° C., propylene was fed at a flow rate of 12 g / min until the internal pressure of the reactor 100 was 16.2 bar.

5 minutes after the feed, confirm that the internal temperature of the venturi-loop reactor 100 was maintained at 90 ° C., and then set the synthesis gas (mixed gas having a molar ratio of carbon monoxide and hydrogen of 50:50) at a supply pressure of 18.8 bar. The reaction was started at the same time as feeding to the nozzle neck 20 of the nozzle. At the same time, hydrogen was supplied to the hydrogen pipe 60 by the hydrogen content supplied to the reactor.

The flow rate of the syngas supplied to the reactor 100 was measured over time while maintaining the internal temperature of the venturi-loop reactor 100 at 90 ° C. through an automatic temperature control device (not shown) connected to the reactor 100. . After completion of the reaction for 2 hours, the operation of the external circulation pump 40 was immediately stopped, the temperature of the reactor 100 was lowered to room temperature, the pressure was released, and the mixture of the entire catalyst solution and the product was recovered to the separation pipe 17 to weigh. As a result of measurement, the total solution weight was 1,302 g, the butyl aldehyde produced by the reaction was 103 g, and the butanol was 351 g.

< Example  2 : Stirring  When using a reactor>

Instead of the venturi-loop reactor of Example 1, a stirred reactor equipped with a sparger with the same capacity was used and a heterogeneous catalyst cartridge was charged into the reactor. At this time, additional hydrogen for hydrogenation was introduced into the reactor along with syngas (50:50).

The total weight of the mixture of the catalyst solution and the product obtained after the reaction for 2 hours was 1,200 g, the weight of butylaldehyde produced after the reaction was 180 g, but the weight of butanol 172 g.

< Comparative example : If no additional hydrogen gas is supplied>

The same process as in Example 1 was repeated except that no additional hydrogen gas was supplied.

The total weight of the mixture of catalyst solution and product obtained after 2 hours of reaction was 1,300 g, the weight of butylaldehyde produced by the reaction was 452 g, and no butanol was produced.

 The configuration and measurement results of Example 1-2 and Comparative Example are summarized as Table 1 below.

division Example 1 Example 2 Comparative example Reactor type Venturi-Loop Stirred reactor with sparger Venturi-Loop Hall presence 3 (from the top of the nozzle
70 mm position) - - Of catalyst solution and product
Mixture total weight (g) 1,302 1,200 1,300 Butylaldehyde
Production amount (g) 103 180 452 Butanol production amount (g) 351 172 -

As shown in Table 1, it was confirmed that in the case of Example 1 using the venturi-loop reactor to supply additional hydrogen, butyl aldehyde is converted to alcohol, it is carried out using a stirred sparging reactor equipped with additional hydrogen In case of Example 2, the content of the product was reduced compared to Example 1, and the conversion to butanol was less.

On the other hand, there was no conversion to butanol in the comparative example where no additional hydrogen was supplied, and only aldehyde was produced. Therefore, conversion of aldehyde to alcohol was confirmed when hydrogen was added, and it was confirmed that the improvement effect was particularly excellent when using a venturi-loop reactor rather than a sparger-mounted stirred reactor.

10: olefin feed piping
11: syngas supply piping
12: hydrogen gas supply piping
13, 14, 15, 16: Circulation piping
17: Alcohol separation piping
20: nozzle
30: Venturi
40: external circulation pump
50: heat exchanger
60: hydrogen supply piping
100: oxo reactor
200: hydrogen filling cartridge

Claims (11)

A hydroformylation reaction is performed by supplying a syngas containing olefin, carbon monoxide and hydrogen, and a hydroformylation catalyst into a venturi-loop reactor or a stirred reactor equipped with a sparger.
A method for converting an olefin-derived aldehyde to an alcohol, wherein the hydrogenation reaction is performed on an aldehyde produced by a hydroformylation reaction by supplying a hydrogenation catalyst and a hydrogen gas on an outer circulation loop of the reactor.
The method of claim 1,
The catalyst composition for hydroformylation reaction includes a metal-carbonyl complex catalyst and a ligand, the concentration of the metal-carbonyl complex catalyst is 10 to 2000 ppm, the concentration of the ligand is 1 to 30 wt% A method for converting an olefin-derived aldehyde into an alcohol.
The method of claim 1,
The catalyst for the hydrogenation reaction is an olefin-derived aldehyde-to-alcohol conversion method comprising a copper catalyst, a nickel catalyst or a copper-zinc catalyst on the inner or outer circulation loop.
The method of claim 1,
The molar ratio of the olefin and the synthesis gas is 95: 5 to 5:95, and the mixing ratio of the synthesis gas CO to H ₂ is 5:95 to 70:30.
The method of claim 4, wherein
The olefin and syngas are respectively converted to olefin-derived alcohol to alcohol, characterized in that the feed through the nozzle at a spray linear velocity of 5 to 40 m / s under a pressure of 5 to 200 bar.
The method of claim 1,
Supplying the reaction mixture after the reaction to a distillation column and recovering the normal- and iso-butanol; Method of converting olefin-derived aldehyde to alcohol, further comprising.
Hydroformylation reactors for preparing aldehydes from olefins; A hydrogenation catalyst filling cartridge provided on an outer circulation loop of the hydroformylation reactor; And a heat exchanger;
The hydroformylation reactor is a stirred reactor equipped with a venturi-loop reactor or a sparger, and a hydrogen supply pipe is provided in a circulation loop between the lower portion of the hydroformylation reactor and the hydrogenation cartridge, and the hydrogenation cartridge and heat A reactor for converting olefin-derived aldehydes to alcohols, wherein an alcohol separation pipe is provided in the circulation loop between the exchangers.
The method of claim 7, wherein
The venturi-nozzle reactor is provided with a nozzle as an injection means, and the nozzle is formed integrally at the bottom of the reactor inlet, and has an enlarged shape consisting of an enlarged portion extending toward the reactor outlet side, and at least one hole in the upper portion of the expansion pipe. A reaction apparatus for converting an olefin-derived aldehyde to an alcohol, wherein a hole is formed to induce mixing and delivery promotion.
The method of claim 8,
The diameter of the nozzle is 0.1 to 500 mm, the inlet diameter of the inlet and the diffusion is 1 to 10 times the diameter of the nozzle, respectively, and the reactor outlet diameter of the diffusion is 0.1 to 10 of the inlet diameter of the diffusion. Reactor for converting olefin-derived aldehyde to alcohol, characterized in that the double.
The method of claim 9,
The total length of the diffusion portion is 0.1 to 10 times the length of the inlet portion, the reaction apparatus for converting aldehyde-derived aldehyde to alcohol.
The method of claim 9,
The length of the venturi is 0.01 ~ 0.95 times the length of the reactor body, the reaction apparatus for conversion from olefin-derived aldehyde to alcohol.

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