Process for the Separation of Ethyl Acetate From Ethanol and Water by Extractive Distillation

This invention relates to a process for separating ethyl acetate from ethanol and water using certain higher boiling liquids as the extractive agent in extractive distillation.

Extractive distillation is the method of separating close boiling compounds or azeotropes by carrying out the distillation in a multiplate rectification column in the presence of an added liquid or liquid mixture, said liquid(s) having a boiling point higher than the compounds being separated. The extractive agent is introduced near the top of the column and flows downward until it reaches the stillpot or reboiler. Its presence on each plate of the rectification column alters the relative volatility of the close boiling compounds in a direction to make the separation on each plate greater and thus require either fewer plates to effect the same separation or make possible a greater degree of separation with the same number of plates. When the compounds to be separated normally form an azeotrope, the proper agents will cause them to boil separately during extractive distillation and thus make possible a separation in a rectification column that cannot be done at all when no agent is present. The extractive agent should boil higher than any of the close boiling liquids being separated and not form minimum boiling azeotropes with them. Usually the extractive agent is introduced a few plates from the top of the column to insure that none of the extractive agent is carried over with the lowest boiling component. Thus usually requires that the extractive agent boil twenty Centigrade degrees or more higher than the lowest boiling component.

At the bottom of a continuous column, the less volatile components of the close boiling mixtures and the extractive agent are continuously removed from the column. The usual methods of separation of these two components are the use of another rectification column, cooling and phase separation, or solvent extraction.

The principal method of manufacturing ethyl acetate is to react acetic acid with ethanol in the presence of a catalyst such as hydrochloric acid or sulfuric acid. An excess of ethanol is used thus converting all of the acetic acid to ethyl acetate and water. However, when the mixture is subjected to rectification, a ternary azeotrope boiling at 70.2.degree. C. and comprising 82.6% ethyl acetate, 8.4% ethanol and 9% water comes off. Water is then added to this mixture which extracts the ethanol. However water is about 4% soluble in ethyl acetate and forms a minimum azeotrope with it. Thus both the ethanol and the ethyl acetate have to have the water removed as azeotropes by rectification. This reduces the yield per pass and requires additional recycling. Thus we see that conventional rectification is beset with problems of azeotrope formation and incomplete recovery due to recycling requirements. Extractive distillation is an attractive method of effecting the separation of ethyl acetate from ethanol and water if agents can be found that (1) will break the ethyl acetate-ethanol-water ternary azeotrope and (2) are easy to recover from the ethanol and water removed from the ethyl acetate.

Extractive distillation typically requires the addition of an equal amount to twice as much extractive agent as the ethyl acetate-ethanol-water on each plate in the rectification column. The extractive agent should be heated to about the same temperature as the plate into which it is introduced. Thus extractive distillation imposes an additional heat requirement on the column as well as somewhat larger plates. However this is usually less than the increase occasioned by the additional agents required in azeotropic distillation.

Another consideration in the selection of the extractive distillation agent is its recovery from the bottoms product. The usual method is by rectification in another column. In order to keep the cost of this operation to a minimum, an appreciable boiling point difference between the compound being separated and the extractive agent is desirable. We recommend twenty Centigrade degrees or more difference. It is also desirable that the extractive agent be miscible with water otherwise it will form a two phase azeotrope with the water in the recovery column and some other method of separation will have to be employed.

The object of this invention is to provide a process or method of extractive distillation that will enhance the relative volatility of ethyl acetate from ethanol and water in their separation in a rectification column. It is a further object of this invention to identify suitable extractive distillation agents which will eliminate the ethyl acetate-ethanol-water ternary azeotrope and make possible the production of pure ethyl acetate by rectification. It is a further object of this invention to identify organic compounds which, in addition to the above constraints, are stable, can be separated from ethanol and water by rectification with relatively few plates and can be recycled to the extractive distillation column and reused with little decomposition.

The objects of this invention are provided by a process for separating ethyl acetate from ethanol and water which entails the use of certain oxygenated, sulfur containing and/or nitrogenous organic compounds as the agent in extractive distillation.

We have discovered that certain oxygenated, sulfur containing and/or nitrogenous compounds, some individually but principally as mixtures, will effectively negate the ethyl acetate-ethanol-water ternary azeotrope and permit the separation of pure ethyl acetate by rectification when employed as the agent in extractive distillation. Table I lists the compounds, mixtures and approximate proportions that we found to be successful. Table II lists mixtures that we investigated and found to be relatively ineffective.

The compounds that are effective as extractive distillation agents when used alone are 1,3-butanediol, 1,4-butanediol, 1,5-pentanediol, hexylene glycol, diethylene glycol, triethylene glycol and tetraethylene glycol. The compounds which are effective when used in mixtures of two, three or four components are dimethylsulfoxide (DMSO), dimethylformamide (DMFA), glycerine, ethylene glycol, propylene glycol, 1,3-butanediol, 1,4-butanediol, 1,5-pentanediol, diethylene glycol triethylene glycol, tetraethylene glycol, hexylene glycol, 1,6-hexanediol, polyethylene glycol 300, diisobutylphthalate, diisooctylphthalate, diisodecylphthalate, N,N-dimethylacetamide, 3-chloro-1,2-propanediol, n-butanol, ethylacetoacetate, ethylene glycol phenyl ether, o-tert. butylphenol. The relative volatility of the agents shown in Table I varies from a high of 3.43 for the single compound 1,4-butanediol and 4.33 for glycerine-ethylene glycol to 2.28 for glycerine-1,5-pentanediol. Table II lists combinations of some compounds presented in Table I which failed to give relative volatilities as high as 2.28. This indicates the importance of employing these compounds in the proper ratio and combination.

The usefulness or utility of this invention can be demonstrated by referring to the data presented in Table I. All of the successful reagents show that ethyl acetate can be removed from its ternary azeotrope with ethanol and water by means of distillation in a rectification column and that the ease of separation as measured by the relative volatility is considerable. Without these extractive distillation agents, no change in the azeotrope composition will occur in the rectification column. The data also show that the most attractive agents will operate at a boilup rate high enough to make this a useful and attractive method of recovering high purity ethyl acetate from its ternary azeotrope with ethanol and water. The stability of the compounds used is such that complete recovery and recycle is obtainable by a simple distillation and the amount required for make-up is small.

The ethyl acetate-ethanol-water azeotrope is 82.6% ethyl acetate, 8.4% ethanol, 9% water. Fifty grams of the ethyl acetate-ethanol-water azeotrope and 50 grams of 1,4-butanediol were charged to an Othmer type glass vapor-liquid equilibrium still and refluxed for eleven hours. Analysis indicated a vapor composition of 93.2% ethyl acetate, 6.8% ethanol, a liquid composition of 81.6% ethyl acetate, 18.4% ethanol. This indicates a relative volatility of 3.10. Ten grams of 1,4-butanediol were added and refluxing continued for another twelve hours. Analysis indicated a vapor composition of 94.9% ethyl acetate, 5.1% ethanol, a liquid composition of 83.2% ethyl acetate, 16.8% ethanol which is a relative volatility of 3.73.

Fifty grams of the ethyl acetate-ethanol-water azeotrope, 25 grams of glycerine and 25 grams of 1,4-butanediol were charged to the vapor-liquid equilibrium still and refluxed for twelve hours. Analysis indicated a vapor composition of 93.8% ethyl acetate 6.2% ethanol and a liquid composition of 80.1% ethyl acetate, 19.9% ethanol which is a relative volatility of 3.75. Five grams of glycerine and five grams of 1,4-butanediol were added and refluxing continued for another twelve hours. Analysis indicated a vapor composition of 95.6% ethyl acetate, 4.4% ethanol and a liquid composition of 81.8% ethyl acetate, 18.2% ethanol which is a relative volatility of 4.13.

Fifty grams of the ethyl acetate-ethanol-water azeotrope, 17 grams of glycerine, 17 grams of ethylene glycol and 17 grams of 1,5-pentanediol were charged to the vapor-liquid equilibrium still and refluxed for 13 hours. Analysis indicated a vapor composition of 92.3% ethyl acetate, 7.7% ethanol and a liquid composition of 80.9% ethyl acetate, 19.1% ethanol which is a relative volatility of 3.29. Three grams each of glycerine, ethylene glycol and 1,5-pentanediol were added and refluxing continued for another ten hours. Analysis indicated a vapor composition of 92.3% ethyl acetate, 7.7% ethanol, a liquid composition of 79.6% ethyl acetate, 20.4% ethanol which is a relative volatility of 3.08.

All the systems reported in Tables I and II were determined in the manner of Example 1, 2 and 3. The relative volatilities shown in Tables I and II are the average of the two different concentrations of extractive distillation agents. These examples show how an initial evaluation of potential extractive distillation agents can be accomplished for single, binary and ternary agents. The final step in this invention is to determine the efficacy of these agents in a rectification column. When a mixture of ethyl acetate, ethanol and water is charged to a rectification column, we encounter a system involving three compounds and four azeotropes. Their boiling points and compositions are shown in Table III.

In conventional rectification, the lowest boiling component in Table III will boil off first, namely the ethyl acetate-ethanol-water azeotrope at 70.2.degree. C. However when the proper extractive distillation agent is employed, the ternary azeotrope and all three binary azeotropes are suppressed and pure ethyl acetate comes off as overhead. The following examples will elaborate.

A column consisting of six 11/2 inch diameter glass perforated plates equipped with a vacuum jacket was employed. The column was fitted with a Corad constant reflux ratio distilling head. Between the Corad head and the top of the column, a feed line from a constant flow bellows pump was introduced. The stillpot was equiped with a sampling tube. The column was calibrated with a test mixture of ethylbenzene and p-xylene, which possesses a relative volatility of 1.06. At total reflux, the column calibrated 4.5 theoretical plates. A run was then made with a 700 gram charge to the stillpot comprising 35.4% ethyl acetate, 60.7% ethanol and 3.9% water. The extractive agent was fed to the bellows pump from a steam jacketed calibrated reservoir which maintained it at about 95.degree. C. The pump was started and a rate of introduction of the extractive agent at the top of the column maintained at about twice the boilup rate as determined in the Corad head. The extractive agent in this example was 1,4-butanediol. The column was operated at total reflux for about 1.5 hours with sampling after one hour and again after 1.5 hours. The following data was obtained.

The extractive distillation agent, 1,4-butanediol, was reclaimed by distilling from a conventional distilling flask and re-run in the same manner as above. The following data was obtained this time.

It will be noted that equilibrium was attained after about an hour with the relative volatility becoming almost constant. Without the extractive agent the overhead would have approached 82.6% ethyl acetate, the ternary azeotrope composition. With the extractive agent, the ternary appears to be completely absent and the ethyl acetate concentration in the overhead approached 100%. When the extractive distillation agent, 1,4-butanediol, is reclaimed and re-used as shown in the second part of this example, it performs just as well. This is to demonstrate that the 1,4-butanediol can be constantly recycled.

A run was made in the same manner as Example 4 in which the charge to the stillpot comprised 20.6% ethyl acetate, 77.1% ethanol and 2.3% water. The extractive agent was 50% glycerine, 50% diethylene glycol. After two hours of operation, the following data was obtained.

The extractive distillation agent was reclaimed by distilling from a conventional distilling flask and re-run in the same manner as above. The following data was obtained from the re-run.

Again, equilibrium was attained after about an hour and remained constant after that. Almost pure ethyl acetate is obtained with only 4.5 theoretical plates indicating that the mixture glycerine-diethylene glycol is an attractive extractive distillation agent for this separation.

A run was made in the same manner as Example 4 in which the charge to the stillpot comprised 21.5% ethyl acetate, 76.1% ethanol and 2.4% water. The extractive agent was 33.3% glycerine, 33.3% ethylene glycol, 33.3% 1,4-butanediol. After 1.5 hours of operation, the following data was obtained.

The extractive distillation agent was reclaimed by distilling from a conventional distilling flask and re-run in the same manner as above. The following data was obtained from the re-run.

Equilbrium was attained in about an hour and the relative volatility remained constant in the range 3.7-3.8. The ternary mixture glycerine, ethylene glycol, 1,4-butanediol is an attractive extractive distillation agent for this separation and it can easily be reclaimed and re-used.

A run was made in the same manner as Example 4 in which the charge to the stillpot comprised 20.6% ethyl acetate, 77.1% ethanol and 2.3% water. The extractive agent was 25% glycerine, 25% hexylene glycol, 25% tetraethylene glycol, 25% 1,5-pentanediol. After two hours of operation the following data was obtained.

The extractive distillation agent was reclaimed by distilling from a conventional distilling flask and re-run in the same manner as above. The following data was obtained from the re-run.

Equilibrium was attained in about an hour and the relative volatility for this quaterary extractive distillation agent, glycerine, hexylene glycol, tetraethylene glycol, 1,5-pentanediol remained constant in the range 2.93 to 3.05.

In the manner described in Examples 4,5,6 and 7, data was gathered on several extractive distillation agents and the results summarized in Table IV. In each case, the operation was carried for 1.5 or two hours at total reflux and sampling done at 1, 1.5 and 2 hours. The extractive agent was separated from the ethylacetate-ethanol-water mixture in a distilling flask and the run repeated with the recovered agent, this to demomstrate the ability of these agents to be recovered and recycled without loss of efficiency.

We have shown by the use of the proper compound or combination of compounds as agents, ethyl acetate can be effectively removed and recovered from its mixture or ternary azeotrope with ethanol and water.