WO2016182190A1 - Method for continuously preparing neopentyl glycol - Google Patents

Abstract

The present invention relates to a method for continuously preparing neopentyl glycol. A method for continuously preparing neopentyl glycol, according to the present invention, enables simplifying of following procedures and increased yield of neopentyl glycol by means of extracting hydroxypivaldehyde at an increased efficiency.

Description

 [Specification ]

 [Name of invention]

 Continuous production method of neopentyl glycol

Technical Field

 Cross Citation with Related Applications

 This application claims the benefit of priority based on Korean Patent Application No. 10-2015-0066894 dated May 13, 2015, and all content disclosed in the literature of that Korean patent application is incorporated as part of this specification. The present invention relates to a process for the continuous production of neopentyl glycol in high yield and simplified processes.

Background Art

 Neopentyl glycol, synonyms:

2,2-dimethyl-1,3-propanediol, or NPG), is an organic compound used for the synthesis of polyesters, paints, lubricants and plasticizers.

 NPG isobutyl aldehyde (synonyms:

2-methylpropanal) and hydroxyfibaldehyde produced by the aldol condensation reaction of aqueous formaldehyde solution. (hydroxypivalaldehyde, synonyms:

Obtained by hydrogenation of 3-hydroxy-2,2-dimethylpropanal (hereinafter HPA)

Isobutyraldehyde Formaldehyde Hydroxypivalaldehyde

Hydroxypivalaldehyde Neopentyl glycol By the way, the product of aldol condensation reaction to obtain HPA, in addition to HPA Unreacted raw compounds, catalysts, and by-products such as 2,2,4-trimethyl-1,3-pentanediol neopentyl glycol hydroxy pivalate and neopentyl glycol isobutylate are included. In particular, it is important to minimize the production of by-products in the reaction to obtain the HPA, because the complex separation process and equipment is required to separate the by-products.

 In particular, formaldehyde in the raw material for the production of HPA is azeotropic with water contained in the product of the aldol condensation process is difficult to recover, and may act as a catalyst poison to the hydrogenation reaction of HPA. For this reason, the residual of formaldehyde should be minimized in the product of the aldol condensation process.

 In this regard, it is possible to improve the yield of HPA by adjusting the molar ratio of the reaction product or the composition of the catalyst in the aldol condensation reaction, or by applying a plurality of continuous stirred-tank reactors (CSTRs), and formingaldehyde. Attempts have been made to minimize the amount of residues and by-products produced. In addition, various purification processes have been proposed to obtain high purity NPG from the product of the aldol condensation process.

 However, the methods proposed so far are not only low in yield of HPA, but also require complicated processes to obtain NPG due to inefficient purification, and have limitations that are accompanied by excessive facility cost and operation cost. Prior Art Documents

 [Patent literature]

(Patent Document 1) US Registered Patent No. 3939216 (19 ⁷ 6.02.17)

 (Patent Document 2) Korean Registered Patent No. 0231644 (1999.08.31)

 [Problem to solve]

 The present invention aims to provide a process for the continuous production of NPG with high yields and simplified processes.

[Measures of problem] According to the invention,

 Aldol condensation process to obtain a product containing HPA through the aldol condensation reaction of aqueous formaldehyde and isobutylaldehyde in the presence of a catalyst,

 An extraction step of bringing the product of the aldol condensation step into contact with an extraction solvent to obtain an extract containing HPA;

 A low boiling point material separation process of distilling the extract to obtain a distillate from which a low boiling point material having a lower boiling point than HPA is removed;

 A hydrogenation process in which the distillate from which the low boiling point material has been removed is hydrogenated in the presence of a catalyst to obtain a product containing NPG; and

 A purification step of distilling the product of the hydrogenation step to obtain NPG;

 The extraction process is carried out in an extraction column having a plurality of stages partitioned by perforated trays. Hereinafter, a method of continuously manufacturing NPG according to an embodiment of the present invention will be described.

 Prior to that, unless otherwise stated throughout the specification, the terminology is merely for reference to particular embodiments and is not intended to limit the invention. As used herein, the singular forms “a,” “an” and “the” include plural forms as well, unless the phrases clearly indicate the opposite. In addition, the meaning of "included" as used in the specification specifies a specific characteristic, region, integer, step, operation, element or component, excluding the addition of other specific characteristics, region, integer, step, operation, element, or component. It is not meant to be.

In addition, the feed of the extraction process is a liquid mixture containing the solute to be extracted, and the solute of the solute that is soluble to the extraction solvent and the other components that do not have the solubility It is a compound. When an extraction solvent is added to the feed, the solute is dissolved from the feed into the extraction solvent by mass transfer. Extraction solvents in which a significant amount of solute is dissolved form an extract solution, and feeds that lose a significant amount of solute To form a trafficin solution. On the other hand, the inventors' continuous studies have shown that when the product of the aldol condensation process is brought into contact with the extraction solvent to improve the efficiency of the extraction process of obtaining the extract containing HPA, the subsequent process can be markedly simplified.

 Specifically, when the extraction process is carried out in an extraction column having a plurality of stages partitioned by the porous plates, HPA extraction efficiency of 99% or more can be ensured and the water content can be significantly lowered. Accordingly, the low boiling point material included in the product of the aldol condensation process may be separated by only one step after the extraction process, and may be recycled without additional purification facilities for the separated low boiling point material.

 In addition, as a result of the continuous study by the present inventors, the aldol condensation process for obtaining HPA was sequentially performed in three or more series of continuous stirring reactors connected in series, and isobutylaldehyde in the raw material compound at different ratios in each reactor. Simultaneously with the quarter addition, it was confirmed that HPA can be obtained with a significantly improved yield when the reaction mixture of the aldol condensation reaction product is allowed to react under different residence times in each reaction vessel.

 In addition, it was confirmed that the aldol condensation process can not only significantly reduce the amount of unreacted formaldehyde, but also effectively suppress the formation of by-products such as neopentyl glycol hydroxy pivalate. In particular, in the aldol condensation process by sequentially reducing the ratio of isobutyl aldehyde branched into each reaction stage, and sequentially increasing the residence time of the reaction product in each reaction stage, a more improved effect can be expressed. According to one embodiment of this invention,

 Aldol condensation step of obtaining a product containing HPA through the aldol condensation reaction of aqueous formaldehyde and isobutylaldehyde in the presence of a catalyst,

An extraction step of contacting the product of the aldol condensation step with an extraction solvent to obtain an extract containing HPA; A low boiling point material separation process of distilling the extract to obtain a distillate from which a low boiling point material having a lower boiling point than HPA is removed;

 A hydrogenation process in which the distillate from which the low boiling point material has been removed is hydrogenated in the presence of a catalyst to obtain a product containing NPG, and

 A purification step of distilling the product of the hydrogenation step to obtain NPG;

 The extraction process is provided for a continuous production method of NPG, which is carried out in an extraction column having a plurality of stages partitioned by porous plates.

 In the accompanying drawings, FIG. 1 schematically illustrates a method of continuously manufacturing NPG according to one embodiment of the present invention, and FIG. 2 schematically illustrates an aldol condensation process in the method of continuously manufacturing NPG.

 Referring to Figure 1, the continuous production method of the NPG Aldol condensation reaction system 100, extraction column 200, low boiling point material separation column 300, hydrogenation reaction system 400, distillation column 500, and high boiling It may be carried out in a flow including a point material removal tower 600.

 Hereinafter, with reference to FIGS. 1 and 2, each process that may be included in the method for continuously manufacturing the NPG will be described.

(1) aldol condensation process

 The aldol condensation step is a step of obtaining a product containing HPA through an aldol condensation reaction of an aqueous formaldehyde solution and isobutylaldehyde in the presence of a catalyst.

 The aldol condensation process may be carried out in three or more, preferably three to five groups, more preferably three or four groups of continuous stirring reaction in series. The increase in the efficiency of the aldol condensation reaction may be expected by increasing the number of continuous stirring reactions, but it is preferable to determine the number of reaction reactions in consideration of process efficiency and equipment complexity.

 FIG. 2 schematically illustrates one embodiment of an aldol condensation reaction system 100 comprising three continuous stirred reaction reactors.

Referring to Figure 2, the aldol condensation process is three continuous stirring It may be carried out in the aldol condensation reaction system 100 including the counterunggi (R1, R2 and R3). In the aldol condensation reaction system 100, the catalyst (F0-TEA) and the raw material compounds (FO-iBAL and F0-FA) applied to the aldol condensation reaction are introduced into the first reactor (R1) to start reaction. The reaction product is sequentially delivered to the other reaction vessels R2 and R3 through the connecting pipes F1 and F2 and the reaction proceeds.

 In particular, in the aldol condensation process, isobutylaldehyde (FO-iBAL) in the raw material compound is branched (S1, S2 and S3) into each reactor (R1, R2 and R3) at different ratios, The reaction is carried out under different residence times in each reaction.

 Preferably, in the aldol condensation process, the ratio of isobutyl aldehyde branched into each reactor may be sequentially decreased, and the residence time of the reaction product in each reactor may be sequentially increased. Here, the deceleration width of the isobutyl aldehyde content and the increase width of the reaction time residence time is not particularly limited.

Specifically, in the case of the aldol condensation reaction system 100 including three continuous stirring reaction groups R1, R2 and R3, 89 to 94 weight ⁰ based on the total content of isobutylaldehyde added to the reaction system. /. Isobutylaldehyde is charged to the first reaction vessel (R1), 5 to 10 weight ⁰ /。 isobutylaldehyde is charged to the second reactor (R2), 1 to 3 weight ⁰ /。 isobutyl Aldehyde may be added to the third reaction stage (R3). That is, in consideration of the activity of the catalyst and the overall efficiency of the aldol condensation reaction, it is preferable to add at least 89% by weight of isobutylaldehyde to the first reaction stage (R1), and to the third reaction stage (R3). 3 parts by weight ⁰ /. it is preferable that less than isobutyl aldehyde is put in.

In particular, with the branched dosing of the isobutylaldehyde, the residence time of the reaction product in the three consecutive stirred agitators is, on the premise of increasing sequentially, from 10 to 13 minutes in the first reaction period (R1), the second 13 to 17 minutes in the reactor (R2), and 17 to 19 minutes in the third reaction stage (R3). Here, the residence time of the counterungmul in each counterunggi is the space velocity of the counterungung, In particular, the aldol condensation reaction can be controlled within the above-described range through measurement of the liquid hourly space velocity (LHSV = Reactant Liquid Flow Rate I Reactor Volume).

 In the aldol condensation process, the Reynolds number, the linear velocity at the tip of the impeller, and the linear velocity at the wall surface of the semi-ungwoon for effective agitation of the reactants in each reactor. And other factors should be considered. Preferably, in the aldol condensation semi-agitator system, the Reynolds number of each semi-unggi is 50000 or more, and the difference between the linear velocity at the tip of the impeller and the wall of the reactor may be adjusted to 2 to 5 m / sec.

 And the aldol condensation reaction of formaldehyde aqueous solution and isobutyl aldehyde is exothermic reaction. Therefore, it is preferable to remove the semiungung heat while circulating the semiungung of each halfunggi to the outside of the semiungunggi. Particularly, in circulating the reaction product to the outside, by using the injector equipped with a venturi nozzle, the reaction product may be strongly sprayed into the reaction device to ensure more improved reaction efficiency. In other words, the aldol condensation process is connected in series via a semi-acre water circulation unit including a circulation pip, a heat exchanger and a reactant injector, respectively.

It may be carried out in three or more continuous stirred reactors.

On the other hand, in the aldol condensation step, isobutyl aldehyde as is advantageous in that the amount of isomer used to 0.5 _^0/0 of less than suppressing the formation of by-products.

 In addition, isobutyl aldehyde may be used in a molar ratio of 1.1 to 1.5, preferably in a molar ratio of 1.1 to 1.2 with respect to 1 mol of formaldehyde. That is, in order to induce complete reaction of the formaldehyde used in the aldol condensation reaction, isobutylaldehyde may be used in excess of formaldehyde, preferably in a molar ratio of 1: 1 or more. However, when isobutyl aldehyde is used too much, the production of by-products due to Tishchenko banung may be increased. Therefore, isobutyl aldehyde is preferably used in a molar ratio of less than 1: 1.5 relative to formaldehyde.

In the above-mentioned aldol condensation step, formaldehyde is used as an aqueous solution of formaldehyde having a concentration of formaldehyde having a concentration of 35 to 45 and increasing ⁰ /. It is advantageous for the improvement of reaction efficiency and the reduction of waste water generation. In general, methanol is added to the aqueous formaldehyde solution to prevent the polymerization of formaldehyde, the content of which is relative to the aqueous formaldehyde solution.

It is preferable that it is 0.1-5 weight ⁰ /.

 In the aldol condensation process, the catalyst is L H, NaOH, KOH,

Hydroxides such as Ca (OH) ₂ ; Alkali metal carbonates such as NaCO ₃ , LiCO ₃ , KCO ₃ , Ca (CO ₃ ) ₂ , NH ₄ CO ₃ ; Tertiary amine compounds such as trimethylamine, triethylamine, tripropylamine can be used. Tertiary amine compounds, particularly triethylamine, in the catalyst may be more preferably used in view of improving the efficiency of the aldol condensation reaction.

 In addition, the catalyst may be used in a molar ratio of 0.01 to 0.5, preferably 0.15 to 0.25, and more preferably 0.18 to 0.22 with respect to 1 mol of formaldehyde. That is, in order to express the catalytic effect, the catalyst may be used in a molar ratio of 1: 0.01 or more relative to formaldehyde. However, if the catalyst is used too much, recovery of the catalyst may be required and generation of by-products may be caused. Therefore, the catalyst is preferably used in a molar ratio of 1: 0.5 or less relative to formaldehyde.

On the other hand, in the aldol condensation process, the reaction temperature may be maintained at 70 to 100 ^° C, preferably 70 to 85 ^° C. In order to ensure the yield of the reaction, the reaction temperature is preferably 70 ^° C or more. However, when the reaction temperature is too high, the production of by-products may be accelerated, and the reaction temperature is preferably 100 ^° C. or less. The aldol condensation reaction may be performed under pressure to ensure yield.

The aldol condensation process performed under the above-described conditions enables the maximization of the mixing efficiency of the raw material compound, thereby improving the efficiency of the aldol condensation reaction, and minimizing the remaining of the non-banung formaldehyde and the generation of by-products. Specifically, the aldol condensation process may ensure a high HPA yield of 99% or more and a low residual formaldehyde concentration of 2000 ppm or less. (2) Extraction process

 The extraction step is a step of obtaining the extract containing HPA by bringing the product of the aldol condensation step into contact with the extraction solvent.

 In particular, in the present invention, the extraction process is performed in an extraction column having a plurality of stages partitioned by the porous plates. Accordingly, the extraction process can ensure a significantly improved HPA extraction efficiency, it is possible to simplify the subsequent low boiling point material separation process.

 In the extraction process, the extraction column 200 of the excellent stirring system having a stage partitioned by the perforated plates having the vertically repeating movement as the extraction column according to the liquid-liquid contacting method can be preferably applied. Specifically, the extraction column 200 includes a Kuhni column, a Karr type reciprocating plate column, a rotary-disk contactor, a Scheibel column, and a spray extraction column. ), Packed extraction columns, pulse packed columns, and the like may be used.

 In addition, the extraction process may be performed in an extraction column having 20 or more stages, preferably 20 to 30 stages, stages partitioned by the porous plates so that the divided extraction efficiency can be expressed under the extraction column. . At this time, the height of one stage in the extraction column may be advantageous to improve the extraction efficiency of 300 to 500 mm. However, the number of stages and the height of the stage of the extraction column may be an example limited to the pilot column, and may be extended to an appropriate range in the commercialization process.

 In the extraction process, the product of the aldol condensation process supplied to the extraction column 200 is brought into contact with the extraction solvent, and extracts containing a significant amount of HPA and a weight loss of a significant amount of HPA are lost. ution). At this time, the relatively light phase of the extract is obtained through the upper outlet of the extraction column 200, the relatively heavy phase of the extract is obtained through the lower outlet of the extraction column (200).

In the extraction process, as the extraction solvent having solubility in HPA, preferably octanol may be used. The extraction solvent may be used in a weight ratio of 1: 0.3 to 1: 0.7, preferably 1: 0.4 to 1: 0.6, based on the product of the aldol condensation process supplied to the extraction column 200. In other words, in order to ensure a good extraction efficiency, the extraction solvent is preferably used in a weight ratio of 1: 0.3 or more with respect to the product. In addition, even when the weight ratio of the extraction solvent exceeds 1: 0.7, the extraction efficiency may be improved, but the loss amount of HPA may be increased in the subsequent low boiling point material separation process, and the reflux flow of the azeotropic solvent to prevent this is excessive. It can be high, which is undesirable.

And, since the HPA can be cured when the temperature is excessively low, the temperature of the extraction process is preferably maintained at 40 ^° C or more. However, if the temperature is too high, the phase separation of the extract may not be made, it is preferable that the temperature of the extraction process is maintained at 90 ^° C or less.

According to an embodiment of the present invention, an extraction efficiency of 99% or more may be secured through the extraction process as described above. That is, the extract obtained through the extraction process may contain more than 99% by weight of the HPA contained in the product of the aldol condensation process. In addition, since most of the water contained in the product of the aldol condensation process is discharged to the weight balance, the extract contains less than 3 weight ⁰ /.

As such it, the loss of HPA in the extraction step may be minimized as a 99 weight _^0/0 over the HPA obtained in the aldol condensation step extraction through the extraction process. In addition, the extraction process may lower the equipment burden and energy consumption of the subsequent low-boiling point material separation process.

(3) low boiling point material separation process

 The low boiling point material separation step is a step of distilling the extract to obtain a distillate from which a low boiling point material having a lower boiling point than HPA is removed.

In addition to HPA, the extract contains low-boiling substances such as isobutyl aldehyde, aldol condensation reaction catalyst, water contained in aqueous formaldehyde and methane. This low boiling point material may be separated from the extract by distillation. In particular, in the present invention, as the extraction efficiency of 99% or more HPA is secured in the extraction process, the low boiling point material can be separated by only one distillation after the extraction process. In addition, isobutylaldehyde and the catalyst in the separated low boiling point material may be recycled to the aldol condensation process.

 In the low boiling point material separation process, the extract liquid supplied to the low boiling point material separation column 300 is contacted with an azeotropic solvent and heated to an appropriate temperature to be distilled by evaporation and expansion.

 In this case, in order to efficiently separate the HPA contained in the extract from the low boiling point material, the low boiling point material separation process is preferably carried out by azeotropic distillation. As the solvent applied to the azeotropic distillation method, a common one having a lower boiling point and azeotropic boiling point than HPA may be applied. (4) hydrogenation process

 The hydrogenation step is a step of hydrogenating the distillate from which the low boiling point material is removed in the presence of a catalyst to obtain a product containing NPG.

As the catalyst for the hydrogenation reaction, a conventional nickel catalyst may be used. The catalyst may be used in an amount of 2 to 10 weight ⁰ / .about HPA contained in the distillate.

 The hydrogenation reaction is a gas-liquid reaction. Therefore, in order to increase the contact efficiency of the reactants, the hydrogenation reaction system may include a hydrogenation reaction system 400 having a venturi nozzle for spraying the HPA-containing distillate into the reaction system.

In addition, the hydrogenation reaction is preferably performed under a hydrogen pressure of 100 to 1500 psig and a temperature of 100 to 200 ^° C. in terms of securing a yield.

(5) purification process

In the purification step, the product of the hydrogenation step is distilled to obtain NPG. It is a process of obtaining.

 In the product of the hydrogenation process, in addition to crude NPG, Mibanung HPA,

HPA dimer high boiling point material may be included. Accordingly, the product of the hydrogenation process may be distilled in the distillation column 500 to obtain high purity NPG.

 Then, if necessary, a process of separating the high boiling point material by supplying the material separated from the NPG through the distillation to the high boiling point material removal tower 600 may be performed. 【Effects of the Invention】

 The continuous manufacturing method of NPG according to the present invention enables extraction of HPA with improved efficiency, which simplifies subsequent processing and improves NPG yield.

[Brief Description of Drawings]

 1 schematically shows a method of continuously manufacturing NPG according to an embodiment of the present invention.

 Figure 2 schematically shows an aldol condensation process in the continuous production method of NPG according to an embodiment of the present invention. [Explanation of code]

 R: raw material compound

 100: aldol condensation reaction system

 200: extraction column

 300: low boiling point material separation column

 400: hydrogenation reaction system

 500: distillation column

 600: high boiling point material removal tower

 E: extraction solvent

 H: hydrogen

NPG: neopentyl glycol HB: high boiling point material

 FO-iBAL: Isobutylaldehyde Supply Line

 F0-FA: formaldehyde aqueous solution supply line

 F0-TEA: catalyst supply line

 SO: distributor

 S1, S2, S3: Isobutylaldehyde Branch Input Line

 R1, R2, R3: Continuous Stirring Reactor

[Specific contents to carry out invention]

 Hereinafter, preferred embodiments of the present invention are provided to aid in understanding the present invention. However, the following examples are only for illustrating the present invention, and the present invention is not limited thereto. Example

 Degree. The device of the same structure as 1 was prepared. Among them, an aldol condensation reaction system 100 including three continuous stirring reactors R1, R2 and R3 connected in series is used for the aldol condensation process. In addition, as the extraction column 200 of the extraction process, a Kuhni column (400 mm in height) having a total of 24 stages stages partitioned by the perforated plates having vertical and repeating motions was used.

As starting compound for the aldol condensation process, was prepared isobutyl aldehyde and formaldehyde solution (concentration 42 weight aldehydes _^0/0, methanol, 1 part by weight ⁰ /. Content). Triethylamine (TEA) was prepared as a catalyst.

Formaldehyde: isobutylaldehyde: triethylamine was used in a molar ratio of 1: 1.1: 0.2. Formaldehyde aqueous solution and catalyst were added to the first reactor. And, based on the total content of isobutyl aldehyde, 91% by weight of isobutylaldehyde is in the first half foot group (R1), 7.5 weight ⁰ /. Isobutylaldehyde in the second half foot group (R2), 1. 5 weights ⁰ /. Of isobutylaldehyde were each branched to the third half-aerator (R3). At the same time, the residence time of the semi-treatment in each reaction period was adjusted as shown in Table 1 below. Table 1

그리고, 상기 알돌 축합 공정은 72 내지 78 ^°C의 온도와 3 atm의 압력 하에서 연속적으로 수행되었고， 이를 통해 HPA가 함유된 생성물이 얻어졌다 (전환율 89.8%, 생성물 내 잔류 포름알데하이드 농도 2000 ppm, HPA 수율 99.20%).

In addition, the aldol condensation process was carried out continuously at a temperature of 72 to 78 ^° C and a pressure of 3 atm, through which a product containing HPA was obtained (conversion rate 89.8%, residual formaldehyde concentration in the product 2000 ppm, HPA Yield 99.20%).

On the other hand, the product of the aldol condensation process was introduced into the extraction column (200). At this time, the extraction column 200 has been introduced into the octanol in 50 parts by weight _^0/0 compared to the product by solvent extraction. Extraction of HPA was performed by vigorous stirring in the extraction column, and the composition of the organic layer in the extract obtained therefrom is shown in Table 2 below.

 Subsequently, the extract was distilled in the low boiling point material separation column 300 to separate isobutyl aldehyde, triethylamine, water, methanol, and the like, which were low boiling point materials. The separated low boiling point material was discharged to the top of the low boiling point material separation column 300 and recycled to the aldol condensation reaction system 100. The composition of the low boiling point material is shown in Table 2 below.

 The distillate from which the low boiling point material was removed was continuously introduced into the hydrogenation reaction system 400, and the hydrogenation process was performed in the presence of a nickel catalyst. The product of the hydrogenation process was continuously introduced into the distillation column 500 to purify, finally obtaining NPG.

Table 2

 Organic layer low boiling point product (wt%) (wt%) (wt%) in extract of aldol condensation process

HPA 57.3 45.4 4

 Z 23.8 2.7 5 Octanol 0.4 37.4 2 Isobutylaldehyde 4.1 3.2 21

Formaldehyde 0.3 0.2 2 Methanol 2.0 1.5 7

TEA 1 1 .4 9.0 59 0.8 0.6 0 neopentyl glycol isobutyl acrylate With reference to Table 2, the extract obtained through the extraction process, containing about 99.7 wt. _^0/0 of HPA containing the product of the aldol condensation step Was confirmed. And, the extract contained less than 3 weight ⁰ /. As such, the extraction process showed more than 99% and excellent HPA extraction efficiency.

Claims

[Claim]  [Claim 1]  Aldol condensation step of obtaining a product containing hydroxyfibaldehyde through the aldol condensation reaction of aqueous formaldehyde and isobutylaldehyde in the presence of a catalyst,  An extraction step of contacting the product of the aldol condensation step with an extraction solvent to obtain an extract containing hydroxyfibaldehyde;  A low boiling point material separation process of distilling the extract to obtain a distillate from which a low boiling point material having a lower boiling point than hydroxyfibaldehyde is removed;  A hydrogenation process in which the distillate from which the low boiling point material has been removed is hydrogenated in the presence of a catalyst to obtain a product containing neopentyl glycol, and  A purification step of distilling the product of the hydrogenation step to obtain neopentyl glycol;  Wherein said extraction process is carried out in an extraction column having a plurality of stages partitioned by porous plates. [Claim 2]  The method of claim 1,  Wherein said extraction process is carried out in an extraction column having 20 to 30 stages of stages. [Claim 3]  The method of claim 1,  The extraction process is a continuous production method of neopentyl glycol is carried out in the extraction column having a height of 300 to 500 mm in one stage. [Claim 4]  According to claim 1, The extraction solvent is octanol, continuous preparation of neopentyl glycol, used in a weight ratio of 1: 0.3 to 1: 0.7 relative to the product of the aldol condensation process Way. [Claim 5]  The method of claim 1, The extract obtained through the extraction step is a continuous production method of neopentyl glycol containing more than 99% by weight ⁰ / ^° of hydroxyfibaldehyde contained in the product of the aldol condensation reaction step. [Claim 6]  The method of claim 1, The extract is obtained through extraction step method for producing neopentyl glycol containing less than 3 wt. _^0/0 water. [Claim 7]  The method of claim 1,  The aldol condensation process is carried out in three or more continuous stirred reaction reactor in series,  The isobutyl aldehyde is branched into each reaction at different ratios,  The reaction product of the aldol condensation reaction is reacted under different residence times in each reaction vessel, and a method for continuously preparing neopentyl glycol. [Claim 8]  The method of claim 7, wherein  In the aldol condensation process, the ratio of isobutyl aldehyde branched into each reaction reactor is sequentially reduced, The residence time of the reaction product in each reaction system increases sequentially, neopentyl glycol. [Claim 9] The method of claim 7,  The aldol condensation process is carried out in a series of three continuous stirring reaction vessel in series, neopentyl glycol method of continuous production. [Claim 10]  The method of claim 9, Based on the total content of isobutyl aldehyde added to the three continuous stirring reactors, 89 to 94 weight ⁰ /. Isobutyl aldehyde is charged to the first reactor, 5 to 10 weight ⁰ /. Isobutyl Aldehyde is introduced into the second reaction vessel, 1 to 3 weight ⁰ /. Isobutylaldehyde is introduced into the third reactor, a continuous process of neopentyl glycol. [Claim 1 11]  The method of claim 9,  The residence time of the reactants in the three continuous stirred reactors is 10-13 minutes in the first reactor, 13-17 minutes in the second reactor, and 17-19 minutes in the third reactor. Manufacturing method.