EP2326614A1

EP2326614A1 - Method for isolating di-trimethylol propane

Info

Publication number: EP2326614A1
Application number: EP09781689A
Authority: EP
Inventors: Gunter Rauchschwalbe; Ulrich Notheis; Michael Friederich; Hans-Dieter Gerriets; Carsten Hummelt; Christiane Oppenheimer-Stix; Paul Wagner
Original assignee: Lanxess Deutschland GmbH
Current assignee: Lanxess Deutschland GmbH
Priority date: 2008-08-16
Filing date: 2009-08-11
Publication date: 2011-06-01
Also published as: JP2011530567A; CN102143931B; US8642816B2; US20120010435A1; CN102143931A; JP5312591B2; WO2010020561A1; DE102008038021A1

Abstract

The present invention relates to a method for isolating ditrimethylol propane from secondary trimethylol propane production streams.

Description

- -

Process for the isolation of di-trimethylolpropane

The present invention relates to a process for the isolation of ditrimethylolpropane from side streams of trimethylolpropane preparation.

Ditrimethylolpropane (Di-TMP) is a starting material for the production of alkyd resins, high quality paints and coatings, plasticizers and lubricants.

It is known in principle that di-TMP is obtained as a by-product in the preparation of trimethylolpropane (TMP) and can be isolated during the workup of TMP from secondary streams.

Trimethylolpropane is industrially produced by the reaction of formaldehyde and n-butyraldehyde in an aqueous medium in the presence of bases. Intermediate stages are included

Monomethylol butyraldehyde and dimethylol butyraldehyde. The last step is the implementation of

Dimethylolbutyraldehyde to TMP, either by hydrogenation in the so-called

"Hydrogenation" takes place or by a Cannizzarro reaction of dimethylol butyraldehyde with

Formaldehyde and stoichiometric amounts of a base to TMP and the corresponding formic acid salt.

The hydrogenation process requires expensive technologies such as catalytic hydrogenation under pressure, while the C annizarro processes are easy to carry out with, for example, sodium hydroxide, sodium carbonate or calcium hydroxide as the base. It is particularly advantageous that when using calcium hydroxide as the base calcium formate is formed as by-product, which brings an additional value for the process.

In this context, methods are also known with which the proportion of di-TMP in TMP can be increased by controlling specific conditions. For example, it is described in JP 57011934 and JP 61021538 that this can be achieved by a formaldehyde content of less than 20% based on the total amount of water and formaldehyde. JP 0815740 describes the preparation of TMP and Di-TMP in a two-phase reaction system.

Furthermore, it is known from EP 0799 815 A to prepare di-TMP by reaction of 2-ethylacrolein with TMP and formaldehyde in the presence of a basic catalyst.

The workup of crude TMP reaction solution from Cannizarro process is described in many variations. It generally includes after neutralization in the - -

Reaction mixture remaining base steps for concentrating the crude aqueous solution, such as distilling off Leichsiedern and water, followed by steps for the separation of inorganic coupling products, in particular formates and steps for the purification of the reaction product TMP.

The separation of the inorganic formates is generally carried out after a concentration by filtration of the precipitated formates or by an extraction step in which TMP and organic by-products are separated from the aqueous formate solution. An extraction step for the separation of TMP and Di-TMP from the inorganic formates has the disadvantage that an additional stream of material adapted to the total amount of TMP product has to be circulated, evaporated and condensed, which is energetically unfavorable.

The target product TMP is generally distilled one or more times after the separation of formates for further purification. In these distillations, the di-TMP typically remains at the bottom of the TMP distillation. Due to its high boiling point, Di- TMP can only be recovered by distillation without undue decomposition.

DE 2058518 describes a method of separating di-TMP by steam distillation in vacuo from the remaining bottom. This method has the disadvantage that large amounts of water vapor are required and only a very impure product is obtained, which must be further purified by multiple crystallization from an organic solvent.

Di-TMP is enriched in the distillation bottoms of TMP distillation. Therefore, this sump typically serves as a convenient starting point for di-TMP recovery.

The present invention is therefore based on the object to obtain di-TMP in high purity from side streams of TMP production.

This object is achieved by a process for the isolation of di-TMP from distillation bottoms of a TMP distillation, which is characterized in that

a) the bottom of the distillation in a suitable solvent and taken under

Supply of mixing energy with water and optionally an acid is added in an amount, so that a multi-phase system, preferably a two-phase system - - forms at least one organic solvent phase and a viscous residue phase

b) the viscous residue phase is separated by phase separation from the organic solvent phase

c) the organic solvent phase obtained according to step b) is extracted with water

d) organic solvent which is in the aqueous phase obtained in step c) is removed, and

e) the di-TMP is isolated from the aqueous phase obtained according to step d).

Suitable distillation bottoms of a TMP distillation are, in particular, those obtained by distillation of TMP-containing crude products having a TMP content of less than 98% by weight.

preferably less than 95% by weight, the crude products containing TMP having been prepared by a process comprising at least the following steps:

i) reaction of formaldehyde and n-butyraldehyde in an aqueous medium in the presence of inorganic base

ii) At least partial removal of lighter than TMP boiling substances, in particular water and formaldehyde

iii) At least partial separation of inorganic formates.

The aforementioned TMP-containing crude products typically accumulate in TMP production processes.

Optionally, the crude products containing TMP are prepared by a process which, in addition to steps i), ii) and iii), also comprises the following step:

iv) neutralization of inorganic base after step i). - -

Step iii), the at least partial separation of inorganic formates can be carried out, for example, by extraction, filtration, sedimentation or centrifugation, preferably by filtration, sedimentation or centrifugation.

Preferred distillation bottoms of the aforementioned type are those in which the inorganic base in step i) is sodium or calcium hydroxide, preferably calcium hydroxide.

Typically, the distillation bottoms used in addition to di-TMP still contain amounts of trimethylolpropane and cyclic and linear formals of trimethylolpropane. The content of Di- TMP is typically between 5% and 60 wt .-% based on the mass of the distillation bottoms. The content of TMP is typically between 1% and 50% by weight, based on the mass of the distillation bottoms

Furthermore, the distillation bottoms may also contain inorganic salts. Typically, these salts are the formates.

The pH of the bottoms, measured as a 10% slurry in water, typically depends on the method used to obtain the TMP-containing crude products. Typical values can be between pH 6 and 10 at standard conditions.

According to step a), the distillation bottoms are taken up in a suitable solvent.

In a preferred embodiment, the distillation bottoms at a temperature of 50 to 100 ⁰ C, preferably between 70 to 95 ° C, preferably 75 ° C to 85 ° C was added to a suitable solvent.

Suitable solvents for extraction are solvents or mixtures of solvents which are not completely miscible with water and have a boiling point between the softening point of the distillation bottoms and the temperature of significant sump decomposition commencing. Preference is given to solvents having boiling points between 40 and 200 ^° C., more preferably between 70 and 160 ^° C., particularly preferably between 80 ^° C. and

150 ^° C. Examples of suitable solvents are aromatic and aliphatic hydrocarbons, esters, ethers, alcohols or ketones. Preference is given to ethers, esters or ketones. Especially preferred - are cyclohexanone, methyl isobutyl ketone, ethyl acetate and butyl acetate or mixtures of such solvents.

The appropriate amount of solvent depends on the viscosity and the softening point of the distillation bottoms and is easily adapted by a person skilled in the art by a preliminary test to a specific distillation bottoms. Preferred are amounts of solvent corresponding to the amounts of bottoms up to ten times. Preference is given to amounts of from 1 to 8 times the volume of the distillation bottoms, particularly preferably amounts of between twice and five times the amount based on the bottoms.

Furthermore, water and optionally but preferably an acid are added in an amount such that a multiphase system is formed from at least one organic solvent phase and one viscous residue phase.

The appropriate amounts of water and acid depend on the composition and the pH of the sump and are easily adapted by a person skilled in the art to a particular distillation bottoms. With gentle stirring, water is initially added in an amount of about 5 to 10% by weight, based on the distillation bottoms, and then in portions

Acid until any fine solid has dissolved and settles a second phase.

Preference is given to adding only enough water that no separate, aqueous phase is formed. The amount of water to be added is typically in the range of 1 to 100 wt .-% based on the mass of the distillation bottoms used, preferably between 5 and 30 wt .-%.

The amount of acid used, if appropriate, is typically in the range from 0.5 to 10% by weight, based on the distillation bottoms used, preferably in the range from 0.5 to 5% by weight. The amount of acid to be used is typically higher, the more alkaline the distillation bottoms used.

In principle, all acids are suitable, preferred are organic acids and those inorganic

Acids which do not form sparingly soluble salts with the cations optionally contained in the distillation bottoms. Sparingly soluble salts in the context of the invention are those which have a maximum solubility of less than 5 g / l in water at 20 ^° C. Particular preference is given to organic acids, very particular preference to formic acid and acetic acid. - -

The acid and the water can also be used together or as dilute aqueous solutions of the acids.

In a preferred embodiment, the supply of mixing energy, which can take place, for example, by mixing devices known per se, such as stirrers, is switched off and then for 5 minutes to 24 hours, preferably for 5 minutes to 8 hours, particularly preferably for 10

Minutes to 4 hours

In a likewise preferred embodiment, the polyphase system is additionally admixed with about 0.05 to 5% by weight, preferably 0.1 to 1.0% by weight, of activated carbon, based on the distillation bottoms.

In step b), the viscous residue phase by phase separation of the organic

Solvent phase in a conventional manner, e.g. separated by deposition.

In a further embodiment of the invention, the viscous residue phase is added again with 50 to 200% by weight of organic solvent, preferably heated, and left to settle again. As the lower phase is obtained in this way a much fluid oil than the original viscous residue phase. The resulting supernatant organic phase is preferably reused in the next batch for the same purpose.

According to step c), the organic solvent phase obtained in step b) is extracted with water. The extraction is preferably carried out after filtration of the organic solvent phase.

The amount of water used for the extraction is for example 2 to 100 wt .-%, preferably to

40 wt .-%, but at least it is so high that can form a separate aqueous phase.

The aqueous phase is separated off and the organic phase is optionally but preferably re-extracted at least once with water.

In a preferred variant, the organic phase after the water extraction back into the

Step a) used. - -

In step d), organic solvent which is present in the aqueous phase obtained in step c) or the optionally combined aqueous phases is removed.

The removal can be carried out in a manner known per se, for example, and preferably by distillation.

The distillation can for example be done at a pressure between 950 and 10 mbar. Preferably, it is distilled until the organic solvent from the sump is at least 90%, preferably at least 98%, removed from the aqueous phase.

According to step e), di-TMP is isolated from the aqueous phase, preferably by crystallization.

In a preferred embodiment, the distillation residue from step d) is diluted with water such that the Di-TMP content is between 10 and 25% by weight, preferably between 10 and 20% by weight.

Subsequently, the mixture is preferably heated until a clear solution is present and then slowly cooled with stirring at a cooling rate between 0.5 ⁰ C and 6 ° C per hour until incipient crystallization.

To complete the crystallization is held for 0.5 hours to 8 hours, preferably at temperatures below 10 ⁰ C. The precipitated crystals are, for example, by

Filtration, centrifugation or a similar method, optionally washed and dried.

In a preferred variant, the crystallization mixture is seeded at a suitable temperature, for example between 25 and 15 ° C. For example, seed crystals may be taken from a previous batch and triturated in water or obtained by flash cooling a small portion of the crystallization mixture.

In another preferred variant, a suspension of di-TMP in water at a temperature close to 0 ⁰ C is introduced and the warm crystallization solution in 0.25 to 24 hours, preferably in 0.5 to 12 hours added so that the proposed mixture remains at the originally set temperature. After dosing, the mixture is stirred for 0.5 hours to 8

Hours to complete the crystallization. In another preferred variant of the method, the moist, washed product is melted, residual solvent is removed by distillation and the melt is compounded, for example, on a flaking roll or a pastillizer.

In a preferred variant, the process according to the invention or individual steps thereof are carried out partly continuously or continuously.

Examples

General

Content determinations were carried out by GC with internal standard, calcium contents were determined titrimetrically with Titriplex solution.

Example 1 (for comparison): Extraction of the sump with water according to DE2358297

200 g of a distillation bottoms containing 6.5% by weight of trimethylolpropane, 34% by weight of di-TMP, 24.3% by weight of linear TMP formal and 2.5% by weight of calcium and a pH of 9 as a 10% aqueous suspension in water at 20 ⁰ C had been added at 40 ⁰ C under stirring with 400 g of water. A suspension of a dark sticky mass in water was obtained, which was not filterable. Even after addition of another 400 mL of water and heating to 80 ⁰ C, the tarry mass in the water remained undissolved.

Example 2 (for comparison): Extraction of the sump with organic solvents according to EP1491521

200 g of a distillation bottoms containing 6.5% by weight of trimethylolpropane, 34% by weight of di-TMP, 24.3% by weight of linear TMP formal and 2.5% by weight of calcium and a pH from 9 as

Had 10% aqueous suspension in water at 20 ⁰ C, were added at 80 ⁰ C with stirring with 800 g of ethyl acetate. A light suspension was obtained which did not form a clear solution even after several hours of heating. The light suspension was difficult to filter.

Example 3: Extraction of a distillation bottoms 200 according to the invention into a distillation bottoms comprising 6.5% by weight of trimethylolpropane, 34% by weight of di-TMP, 24.3% by weight of linear TMP formal and 2.5% by weight. % Calcium contained and a pH value of 9 than 10% aqueous suspension in water at 20 ⁰ C, were at 80 to 90 ⁰ C bath temperature below

Stirring with 800 g of butyl acetate. At 70 to 80 ⁰ C, 20 g of water were added and allowed to settle briefly. At 80 ^° C., 6 g of formic acid (99.5% by weight) and 1 g of active carbon were added, with gentle stirring. After stirring for a short time, the stirrer was switched off and the mixture was kept at 80 ^° C. for half an hour. This resulted in a dark, viscous phase. The supernatant organic solution was decanted and filtered through a fluted filter. - -

The viscous phase from the first extraction of the sump was again mixed with the same mass of butyl acetate and heated to 125 ° C. It was allowed to settle again and received as a lower phase, a fluid oil.

The still hot organic phase from the first extraction was mixed with 60 g of water and cooled to 25 ° C. The phases are separated and the organic phase extracted again with 20 g of water at 25 ° C.

The aqueous phases were combined and distilled at a top temperature of 95 ° C. 92 g of a two-phase mixture of butyl acetate and water were distilled off at a pressure of 100 mbar on a rotary evaporator. There remained 180 g of liquid residue, which was filled for crystallization with water to 480 g and 67.8 g of di-TMP (14.1 wt .-%).

Example 4 Crystallization by Crystallization 147 g of a solution prepared analogously to Example 3 and containing 13.9% by weight of di-TMP were inoculated at 22 ° C. with a suspension of di-TMP in water, in 24 hours Cooled to -2 ° C, stirred for three hours at -2 ° C and filtered. The filter cake was washed twice with 50 ml of ice water, sucked dry and the crystals dried in a vacuum oven to 60 ⁰ C. This gave 16.2 g of di-TMP with a purity of

98.3% corresponding to 78% of the use in the crystallization.

Example 5 Crystallization by Crystallization The procedure was as described in Example 4, but with the difference that the mixture was cooled in 8 hours. This gave 16.4 g of dried di-TMP with a purity of 98.9%, corresponding to 80% of the use in the crystallization.

Example 6: Extraction of the distillation bottoms with recycling of the butyl acetate phase The procedure was as described in Example 4, but with the difference that instead of fresh butyl acetate, the azeotropically dewatered butyl acetate phase from Example 3, which additionally contained 11.8 g of di-TMP has been. 480 g of an aqueous solution containing 78.3 g of di-TMP were obtained. Example 7: Semibatch crystallization with recycling of the wash water

200 mL of wash water from a previous crystallization, containing 9.9 g of di-TMP were brought to 10 ⁰ C and seeded with a suspension of di-TMP in water. Within three hours, the warm aqueous solution from Example 6 was added dropwise. The temperature in the template was kept at 10 ⁰ C while being dropped. The mixture was stirred for 2 hours at 5 ° C, filtered off, washed the filter cake twice with 100 ml of ice water, sucked dry and dried in a vacuum oven at 60 ⁰ C. This gave 54.0 g of di-TMP with a purity of 99.4 % corresponding to 77% of the content of the distillation residue used.

Claims

- Patent claims

1. A process for the isolation of di-TMP from distillation bottoms of a TMP distillation, characterized in that

a) the distillation bottom is taken up in a suitable solvent and mixed with the addition of mixing energy with water and optionally an acid in an amount so that a multiphase system, preferably a two-phase system of at least one organic solvent phase and a viscous residue phase is formed

e) the di-TMP is isolated from the aqueous phase obtained according to step d).

2. The method according to claim 1, characterized in that in step a) is additionally mixed with acid.

3. The method according to claim 1 or 2, characterized in that in step a) forms a two-phase system.

4. The method according to any one of claims 1 to 3, characterized in that as

Distillation bottoms of a TMP distillation are those obtained by distillation of TMP-containing crude products having a TMP content of less than 98 wt .-%, wherein the TMP-containing crude products were prepared by a process comprising at least the following steps: - - i) reaction of formaldehyde and n-butyraldehyde in aqueous medium in

Presence of inorganic base

ii) At least partial removal of lighter than TMP boiling substances

iii) At least partial separation of inorganic formates.

5. The method according to claim 4, characterized in that in step i) sodium or

Calcium hydroxide can be used as inorganic bases.

6. The method according to any one of claims 1 to 5, characterized in that the used

Distillation sumps have a content of di-TMP between 5% and 60 wt .-% based on the mass of the distillation bottoms.

7. The method according to any one of claims 1 to 6, characterized in that as

Solvents are used which are not completely miscible with water and have a boiling point between 40 and 200 ⁰ C.

8. The method according to any one of claims 1 to 7, characterized in that the polyphase system in step a) additionally 0.05 to 5 wt .-% of activated carbon based on the distillation bottoms added.

9. The method according to any one of claims 1 to 8, characterized in that in step e) di-TMP is isolated from the aqueous phase by crystallization.

10. The method according to any one of claims 1 to 9, characterized in that the method or individual steps a) to e) are carried out partially continuously or continuously.

11. Use of distillation bottoms of a TMP distillation to produce di-TMP with a purity of over 98%.