EP0958302A2 - Purification of polyol fatty acid polyesters using a mixing vessel with controlled mixing - Google Patents

Abstract

Processes for treating a polyol fatty acid polyester comprise feeding an unrefined polyol fatty acid polyester containing impurities and soap, and a wash solution into a mixing vessel and dispersing the contents to form a mixture. The treated mixture is allowed to settle and separate into a first phase comprising treated polyol fatty acid polyester and a second phase comprising the wash solution, soap and impurities. A treated polyol fatty acid polyester is produced by the processes described herein. Impurities soluble in the wash solution, such as color bodies, and the like are among the impurities which can be removed by the processes of the present invention. Chelating agents can be included in the wash solution to aid in the removal of impurities such as trace metals. 00000

Description

PURIFICATION OF POLYOL FATTY ACID POLYESTERS USING A MIXING VESSEL WITH CONTROLLED MIXING

TECHNICAL FIELD

This invention relates to purification processes for polyol fatty acid polyester, which processes employ a wash solution in a mixing vessel with controlled mixing. Additionally, this invention relates to the purified polyol fatty acid polyester products resulting from the purification processes described herein.

BACKGROUND OF THE INVENTION

The food industry has recently focused considerable attention on the production of polyol fatty acid polyesters for use as low calorie fats in food products. As a result, there is a continuing need for processes which economically and efficiently produce a relatively high purity polyol fatty acid polyester.

To produce a polyol fatty acid polyester, a polyol can be reacted with a fatty acid lower alkyl ester in the presence of a basic catalyst. In general, polyols are readily soluble in an aqueous medium, e.g. water, while fatty acid lower alkyl esters are soluble in an organic medium. Thus, an emulsifier, solvent, phase transfer catalyst or a mixture thereof may be required to bring the polyol and the fatty acid lower alkyl ester into physical contact so that they can react chemically. The resulting polyol fatty acid polyester is soluble in an organic medium.

As can be appreciated, the product stream resulting from the reaction of a polyol to produce a polyol fatty acid polyester can therefore contain a variety of components in addition to the desired polyol fatty acid polyester. For example, residual reactants, e.g., unreacted fatty acid lower alkyl ester and/or unreacted polyol, emulsifier, solvent, phase transfer catalyst and/or basic catalyst can be present in the product stream. Additionally, there can be numerous by-products of the reaction itself. For example, numerous side reactions occur in addition to the transesterification of the polyol to form a polyol fatty acid polyester. Side reactions can include the breakdown of one chemical component into two or more by-products, and/or the initial reactants, catalysts, emulsifiers and solvents can chemically react with one another to form undesired by-products, for example, di- and tri-glycerides, beta-ketoesters, di-fatty ketones and unsaturated soaps. A common by-product of polyol polyester synthesis reactions is soap formed by saponification of fatty acid lower alkyl esters. Water, introduced either with the raw materials or through air leaks or resulting from dehydration reactions involving the polyol, can react with the strong base catalyst to form hydroxide ion, which in turn can react with lower alkyl ester to form soap. Additionally, the initial reactants and other reaction ingredients are often supplied with trace quantities of materials, e.g. trace metals, which are particularly undesirable in a final product which is intended for use as a food additive. Thus, the product stream resulting from the reaction of a polyol and a fatty acid lower alkyl ester can contain, in addition to the desired polyol fatty acid polyester, a variety of undesirable constituents which need to be substantially removed to yield the desired purified polyol fatty acid polyester.

Separation processes for purifying reaction product streams of polyol fatty acid polyesters are generally known to the art. U. S. Patent No. 4,861,413 to Pollard briefly discusses the use of a solid adsorbent for purification of a polyol fatty acid polyester reaction product. U.S. Patents Nos. 4,241,054, 4,517,360 and 4,518,771 to Volpenhein briefly discuss separation processes for the purification of a polyol fatty acid polyester reaction product. Volpenhein broadly discloses distillation, washing, conventional refining techniques or solvent extraction for purifying the polyol fatty acid polyester. However, the product stream resulting from the transesterification reaction of a polyol provides unique and challenging problems. For example, polyol fatty acid polyesters are often used as low calorie fats, whereby trace quantities of materials which are not suitable for consumption must be removed, whether or not they affect the product's use in nonfood applications. On the other hand, some of the breakdown products of the initial reaction ingredients, for example the caramelized by-product resulting from the breakdown of a polyol, can be suitable for consumption but impart undesirable color and/or increase the caloric content of the product stream, and are thus preferably removed from the reaction product. The complex and highly variable product stream resulting from the transesterification reaction of a polyol to form a polyol fatty acid polyester presents purification process design problems which are both challenging and unique.

A continuing need exists therefore for improved separation and purification processes to purify a polyol fatty acid polyester reaction product stream, particularly resulting from the transesterification of a polyol. More specifically, it is desirable to provide an economical and efficient separation process which can remove water soluble components, emulsifiers. trace metals and other undesirable impurities from polyol fatty acid polyester product.

SUMMARY OF THE INVENTION

Accordingly, it is an object of the present invention to provide improved purification processes for purifying polyol fatty acid polyesters. It is a related object of the present invention to provide improved purified polyol fatty acid polyesters, which can be used as food additives.

In one embodiment, the invention is directed to a process for purifying an unrefined polyol fatty acid polyester. The process steps include feeding an unrefined polyol fatty acid polyester into a mixing vessel wherein the unrefined polyol fatty acid comprises a polyol fatty acid polyester, soap and impurities. A wash solution is fed into the mixing vessel, and the unrefined polyol fatty acid polyester and the wash solution are dispersed to produce a mixture. At least a portion of the impurities and soap are transferred from the unrefined polyol fatty acid polyester to the wash solution. The mixture is allowed to settle and is then separated into two phases wherein a first phase comprises a purified polyol fatty acid polyester and the second phase comprises an impurity- and soap-containing wash solution. Another embodiment of the present invention is directed towards a purified polyol fatty acid polyester made according to the processes described herein.

In another embodiment, the invention is directed to a method of making a purified polyol fatty acid polyester wherein a polyol and a fatty acid lower alkyl ester (and optionally, a soap and/or other emulsifier or any mixture thereof) are reacted to produce a reaction product comprising a polyol fatty acid polyester, soap and impurities. The method comprises the steps of feeding the reaction product and a wash solution into a mixing vessel and dispersing the reaction product and the wash solution to produce a mixture. The mixture is created by controlled mixing of the wash solution and the unrefined polyol fatty acid polyester which provides superior contact between the two streams and thereby promotes the desired mass transfer of impurities from the unrefined polyol fatty acid polyester to the wash solution without the unwanted formation of stable emulsions. The process further comprises the step of separating, such as by settling, the mixture into two phases, wherein the first phase comprises the purified polyol fatty acid polyester and a second phase comprises the wash solution, followed by separating the first phase from the second phase.

Another embodiment of the present invention provides for the use of a mixing vessel in conjunction with dispersing the wash solution and the unrefined polyol fatty acid polyester under controlled conditions, to avoid the formation of stable emulsions.

DETAILED DESCRIPTION

The present invention will now be described in detail with reference to specific embodiments. In accordance with the present processes for producing a purified polyol fatty acid polyester, an unrefined polyol fatty acid polyester (often referred to as "crude" polyol fatty acid polyester) is fed into a mixing vessel. A wash solution is fed into the mixing vessel, and an unrefined polyol fatty acid polyester and the wash solution are dispersed to produce a mixture of the unrefined polyol fatty acid polyester and the wash solution. The mixture contains droplets having an average diameter preferably in the range of from about 5μ to about 3000μ, more preferably from about 5μ to about 70μ and most preferably, from about 5μ to about 20μ. When mixing is complete, the mixture settles into two phases due to the general immiscibility between the first phase containing the purified polyol fatty acid polyester and the second phase containing the wash solution, soap and impurities.

All droplet diameters reported herein were measured using a Lasentech scanning laser light detector. More specifically the Lasentech instrument is a focused beam reflectance measurement system which consists of a computer interface, a laser diode, detectors, a 10 meter fiber optic cable, and a measuring probe. The light from the laser diode travels down the fiber optic cable to the probe. The light is focused to a very small point in the probe through a sapphire window into the material of interest. When the light beam passes over a particle, or droplet in this case, light is scattered in the backward direction. This light is collected and is passed back to the field unit where it starts a clock. When the light has passed over the droplet, the backscattering stops and this stops the clock. By knowing the speed of the light beam and the length of the backscattering pulse, the diameter of the droplet can be determined. For a given set of conditions, the average droplet diameter is calculated by dividing the sum of all the diameters by the number of droplets measured.

As will be understood, the unrefined polyol fatty acid polyester can conventionally be produced by the reaction of a polyol with a fatty acid lower alkyl ester. However, the unrefined polyol fatty acid polyester can be provided from any available source or production method employed in the art. The purified polyol fatty acid polyester can be used as, among other things, a low calorie fat in foods and, in fact, the purified polyol fatty acid polyester of the present invention is particularly advantageous for use as a food additive owing to its improved purity.

As used herein, the teπn "wash solution" is intended to include solvents which, when mixed with an unrefined polyol fatty acid polyester under the process conditions described herein, tend to remove at least a portion of the impurities and soap from the unrefined polyol fatty acid polyester. Thus, a wash solution comprises solvents such as water, methanol, acetone and ethyl acetate. Water and more generally, aqueous based wash solutions are preferred for use in the processes described herein due to availability and cost, but it is understood that other solvents are appropriate for use with the processes and methods described herein if the solvents, when mixed with the unrefined polyol fatty acid polyester under the conditions described herein, remove at least a portion of the impurities from the unrefined polyol fatty acid polyester.

Optionally, the wash solution can contain one or more additives, for example, a chelating agent which chelates with metals present in the unrefined polyol fatty acid polyester. The chelating agent can attach, or "chelate", to a portion of the metals from the polyol fatty acid polyester and be carried with the chelated metals into the wash solution. It is important to note however that metals can be removed without the use of a chelant as demonstrated by Example 4 below. Tri-potassium citrate is a preferred chelating agent of the present invention, although other chelating agents are also appropriate and will be apparent to those skilled in the art. A preferred concentration for chelating agents in the present invention is less than about 5.0% by weight of the wash solution. The wash solution should preferably contain less than about 0.5% impurities by weight, prior to its contact with the unrefined polyol fatty acid polyester. An impurity in the water wash solution includes anything that does not aid in the removal of one or more impurities from the polyol fatty acid polyester. Thus, the wash solution can comprise a solvent which removes impurities from the unrefined polyol fatty acid polyester.

As used herein the term "polyol fatty acid polyester" is intended to include any polyol, as defined herein, which has two or more of its hydroxyl groups esterified with fatty acid groups. Preferably, the polyol has been esterified with four or more fatty acid groups. Suitable polyol fatty acid polyesters include sucrose polyesters having on average at least four, preferably at least about five, ester linkages per molecule sucrose; the fatty acid chains preferably have from about eight to about twenty-four carbon atoms. Other suitable polyol fatty acid polyesters are esterified linked alkoxylated glycerins, including those comprising polyether glycol linking segments, as described in U.S. Patent No. 5,374,446, incorporated herein by reference, and those comprising polycarboxylate linking segments, as described in U. S. Patent Nos. 5,427,815 and 5,516,544, incorporated herein by reference; more preferred are those described in U. S. Patent No. 5,516,544.

Additional suitable polyol fatty acid polyesters are esterified epoxide-extended polyols of the general formula P(OH)_A+£ (EPO)^ (FE)_B wherein P(OH) is a polyol, A is from 2 to about 8 primary hydroxyls, C is from about 0 to about 8 total secondary and tertiary hydroxyls, A + C is from about 3 to about 8, EPO is a C₃-Cg epoxide, N is a minimum epoxylation index average number, FE is a fatty acid acyl moiety and b is an average number is the range of greater than 2 and no greater than A + C, as described in U. S. Patent No. 4,861,613 and EP 0324010 Al, incorporated herein by reference. The minimum epoxylation index average number has a value generally equal to or greater than A and is a number sufficient so that greater than 95% of the primary hydroxyls of the polyol are converted to secondary or tertiary hydroxyls. Preferably the fatty acid acyl moiety has a C₇-C23 alkyl chain.

Preferred esterified epoxide-extended polyols include esterified propoxylated glycerols prepared by reacting a propoxylated glycerol having from 2 to 100 oxypropylene units per glycerol with C_{1 Q}-C24 fatty acids or with CJ_Q-C24 fatty acid esters, as described in U. S. Patent Nos. 4,983,329 and 5,175,323, respectively, both incorporated herein by reference. Also preferred are esterified propoxylated glycerols prepared by reacting an epoxide and a triglyceride with an aliphatic polyalcohol, as described in U. S. Patent No. 5,304,665, incorporated herein by reference, or with an alkali metal or alkaline earth salt of an aliphatic alcohol, as described in U. S. Patent No. 5,399,728, incorporated herein by reference. More preferred are acylated propylene oxide-extended glycerols having a propoxylation index of above about 2, preferably in the range of from about 2 to about 8, more preferably about 5 or above, wherein the acyl groups are Cg-C₂4, preferably C^-C_j , compounds, as described in U. S. Patent Nos. 5,603,978 and 5,641,534, both incorporated herein by reference. Particularly preferred are fatty acid-esterified propoxylated glycerols which exhibit a sharp metal before about 92 F (33°C) and have a dilatomeric solid fat index at 92 F (33°C) of less than about 30, as described in WO 97/2260, or which have a dilatomeric solid fat index of at least about 50 at 70 F (21°C) and at least about 10 at 98.6 F (37°C), as described in U. S. Patent Nos. 5,589,217 and 5,597,605, both incorporated herein by reference.

Other suitable esterified epoxide-extended polyols include esterified alkoxylated polysaccharides. Preferred esterified alkoxylated polysaccharides are esterified alkoxylated polysaccharides containing anhydromonosaccharide units, more preferred are esterified propoxylated polysaccharides containing anhydromonosaccharide units, as described in U. S. Patent No. 5,273,772, incorporated herein by reference.

As used herein, the term "unrefined" polyol fatty acid polyester refers to a composition containing predominantly polyol fatty acid polyester containing "impurities" and/or "soap", as defined below, prior to the processes described herein. The amount and type of impurities and soap will vary depending upon, among other things, the source of the polyol fatty acid polyester and the purification steps, if any, the polyol fatty acid polyester is subjected to before it is fed into the mixing vessel of the present invention.

As used herein, the term "polyol" is intended to include any aliphatic or aromatic compound containing at least two free hydroxyl groups. Suitable polyols can be selected from the following classes: saturated and unsaturated straight and branch chain linear aliphatics; saturated and unsaturated cyclic aliphatics, including heterocyclic aliphatics; or mononuclear or polynuclear aromatics, including heterocyclic aromatics. Carbohydrates and non-toxic glycols are preferred polyols.

Monosaccharides suitable for use herein include, for example, glucose, mannose, galactose, arabinose, xylose, ribose, apiose, rhamnose, psicose, fructose, sorbose, tagatose, ribulose, xylulose, and erythrulose. Oligosaccharides suitable for use herein include, for example, maltose, kojibiose, nigerose, cellobiose, lactose, melibiose, gentiobiose, turanose, rutinose, trehalose, sucrose and raffinose. Polysaccharides suitable for use herein include, for example, amylose, glycogen, cellulose, chitin, inulin, agarose, zylans, mannan and galactans. Although sugar alcohols are not carbohydrates in a strict sense, the naturally occurring sugar alcohols are so closely related to the carbohydrates that they are also preferred for use herein. Natural sugar alcohols which are suitable for use herein are sorbitol, mannitol, and galactitol.

Particularly preferred classes of materials suitable for use herein include the monosaccharides, the disaccharides and sugar alcohols. Preferred unesterified polyols include glucose, fructose, glycerol, polyglycerols, sucrose, zylotol, and sugar ethers. Preferred unesterified polyols also include alkoxylated polyols such as alkoxylated glycerol, alkoxylated polyglycerols, alkoxylated sorbitol, alkoxylated polysaccharides, and linked alkoxylated polyols such as linked alkoxylated glycerins. Polyols may be alkoxylated with C₃-Cg epoxides, such as propylene oxide, butylene oxide, isobutylene oxide, and pentene oxide, to produce epoxide-extended polyols having an epoxylation index minimum of at least about 2, preferably in the range of from about 2 to about 8, as described in U. S. Patent No. 4,816,613, incorporated herein by reference. Polyols may be also alkoxylated with an epoxide, preferably a C3-C10 1,2-alkylene oxide, in the presence of a ring- opening polymerization catalyst, as described in U. S. Patent Nos. 5,399,729 and 5,512,313, incorporated herein by reference. Suitable alkoxylated polyols are described in U. S. Patent Nos. 4,983,329; 5, 175,323; 5,288,884; 5,298,637; 5,362,894; 5,387,429; 5,446,843; 5,589,217; 5,597,605; 5,603,978 and 5,641,534, all incorporated herein by reference. Suitable alkoxylated polyols include alkoxylated sugar alcohols, alkoxylated monosaccharides, alkoxylated disaccharides, alkoxylated polysaccharides, alkoxylated C₂ - C_|0 aliphatic diols, and alkoxylated C₃ - C_j2 aliphatic triols. Preferred alkoxylated C₃ - C^ aliphatic triols are alkoxylated glycerols, more preferred are propoxylated glycerols, and particularly preferred are propoxylated glycerols having from about 3 to about 21 moles of propylene oxide per mole glycerol. Preferred alkoxylated polysaccharides are alkoxylated polysaccharides containing anhydromonosaccharide units, more preferred are propoxylated polysaccharides containing anhydromonosaccharide units, as described in U. S. Patent No. 5,273,772, incorporated herein by reference. Preferred linked alkoxylated glycerins include those comprising polyether glycol linking segments, as described in U. S. Patent No. 5,374,446, incorporated herein by reference, and those comprising polycarboxylate linking segments, as described in U. S. Patent Nos. 5,427,815 and 5,516,544, incorporated herein by reference; more preferred are those described in U. S. Patent No. 5,516,544. A particularly preferred polyol is propoxylated glycerin.

As used herein, the term "impurities" is intended to include a variety of constituents which are undesirable in the purified polyol fatty acid polyester product of the present invention. As will be understood, a particular component, e.g. a di- or tri-glyceride, can be an innocuous constituent of a polyol fatty acid polyester product for one application, but, on the other hand, can be undesirable, i.e. an impurity, in another application. For example, because both di- and tri-glyceride are caloric- containing fats, their presence in a polyol fatty acid polyester which is intended for use as a low calorie fat can be undesirable, whereby the glycerides would both be considered impurities. Likewise, if the polyol fatty acid polyester is intended for use as a food product, trace amounts of metals would be considered impurities if they are not appropriate for consumption by humans. Items such as breakdown products of an initial reactant which is used to form the polyol fatty acid polyester, for example the caramelized by-product of sucrose, can be both inert and suitable for consumption by an average consumer. However, by-products such as the caramelized by-product of a polyol can add undesirable color and/or adversely affect the viscosity of the polyol fatty acid polyester product. Thus, the breakdown product of the initial reactant can be considered an impurity even though it is generally inert and consumable. "Impurity", as used herein, is intended to include anything other than the desired polyol fatty acid polyester, the soap and the fatty acid lower alkyl esters as discussed in greater detail below.

Due to side reactions which occur simultaneously with the transesterification reaction, the polyol fatty acid polyester product can contain various by products which are also considered impurities. Di-fatty ketones and beta-ketoesters are two groups of reaction by-products which are also generally considered impurities and their removal is desirable and non-aqueous solvents are preferred to effect their removal. Fatty acids are often produced by the hydrolysis of a fatty acid lower alkyl ester. Additionally, unsaturated soaps can be formed by the reaction of methyl ester or fatty acid with a catalyst and aqueous wash solutions are preferred to effect their removal.

Among the many potential impurities in a reaction composition containing polyol fatty acid polyester are components from the reaction(s) used to form a polyol fatty acid polyester. As used herein, the term "reaction component" is intended to include any component suitable for use in the production of polyol fatty acid polyester. Suitable reaction components can include, but are not limited to, reactants such as polyol, lower alkyl fatty acid esters and/or glycerides, emulsifiers, catalysts and mixtures thereof.

Fatty acid lower alkyl ester is often reacted with a polyol to form a polyol fatty acid polyester. Additionally, a stoichiometric excess of fatty acid lower alkyl ester is typically provided to completely esterify the polyol. However, feeding excess quantities of fatty acid lower alkyl ester results in a reaction product containing an appreciable concentration of residual fatty acid lower alkyl ester. The residual fatty acid lower alkyl ester remaining in the reaction product is not normally soluble in water which is a preferred solvent of the present invention. Additionally, since the fatty acid lower alkyl ester is a feed stock in the reaction of a polyol to form a polyol fatty acid polyester, it is desirable to collect and recycle the residual fatty acid lower alkyl ester. Thus, fatty acid lower alkyl ester is generally not included within the meaning of the teπn "impurities" as defined herein. A more detailed description of the direct recycle of lower alkyl esters can be found in the U. S. Patent Application Serial No. 08/797,018, Attorney Docket Case 6506, entitled Lower Alkyl Ester Recycling In Polyol Fatty Acid Polyester Synthesis. The entire disclosure of U. S. Patent Application Serial No. 08/797,018 is incorporated herein by reference.

Fatty acid lower alkyl ester cannot normally be removed by contact with an aqueous based wash solution alone, although small amounts of both the fatty acid lower alkyl ester and the desired polyol fatty acid polyester can be unavoidably entrained in the wash solution. Fatty acid lower alkyl esters are preferably removed from the polyol fatty acid polyester by thermal evaporation. However, the lower alkyl ester evaporates at a lower temperature than does the polyol fatty acid polyester, and any impurities which have boiling points less than the boiling point of the polyol fatty acid polyester may be evaporated along with the lower alkyl ester. To produce a lower alkyl ester of sufficient purity for direct recycle into the polyol fatty acid polyester production process it is often desirable to remove as much of the soap and impurities as possible using the methods of the present invention prior to the evaporation step.

A preferred method for preliminary soap removal is to add a small amount of water to the crude to facilitate soap curd foπnation. Hydration is believed to increase the soap phase's specific gravity which aids in the separation process. The amount of water added depends on the level of soap in the unrefined polyol polyester. The ratio of water to soap on a weight basis is from about 3:1 to about 1:3, more preferably from about 2:1 to about 1:2.5 and most preferably from about 1.1 to about 1.2. The coagulated soap is then removed by common separation techniques such as settling, filtration or centrifugation. Additionally, it is desirable to minimize hydrolysis, which results in the formation of free fatty acid, during the treatment processes described herein. The free fatty acid formed by the hydrolysis of lower alkyl ester is difficult to separate from the lower alkyl ester due to the similarity in their vapor pressures. To avoid excessive hydrolysis it is generally preferred to maintain the mixture of wash solution and unrefined polyol fatty acid polyester at a pH of greater than about 5.5 and to avoid the use of acids. Moreover, residence time in the mixing vessel should be less than about 30 minutes, and preferably less than about 15 minutes. Thus, the methods of the present invention can be utilized to treat polyol fatty acid polyesters and to remove impurities from any excess lower alkyl ester making it more suitable for recycle.

When needed, a preferred emulsifier for use in the transesterification reaction of a polyol to form a polyol fatty acid polyester is alkali metal fatty acid soap. As used herein, the term "alkali metal fatty acid soap", or "soap" means the alkali metal salts of saturated and unsaturated fatty acids having from about eight to about twenty four carbon atoms. Accordingly, suitable alkali metal fatty acid soaps include, for example, the lithium, sodium, potassium, rubidium, and cesium salts of fatty acids such as capric, lauric, myristic, palmitic, linoleic, oleic, and stearic acids, as well as mixtures thereof. A mixture of fatty acid derived from soybean oil, sunflower oil, safflower oil, cottonseed oil, palm oil and corn oil is preferred for use herein. An especially preferred alkali metal fatty acid soap is, for example, the potassium soap made from palmitic acid and stearic acid. In addition to alkali metal soap, other emulsifiers such as sucrose fatty acid mono-, di- and tri-esters can be used. Solid mono- and di-glycerides can also be used, although they are less preferred.

While an emulsifier in general, and an alkali fatty acid soap specifically, are often desirable reaction components, they are generally undesirable in the polyol fatty acid polyester product. It is desirable to remove substantially all of the soap from the reaction product prior to the thermal evaporation of excess methyl ester to minimize color degradation during evaporation. Additionally, the presence of soap in substantial quantities, i.e. greater than about 4000 ppm can cause processing difficulties when the wash solution and the unrefined polyol fatty acid polyester are dispersed. Preferably the concentration of soap in the unrefined polyol fatty acid polyester be below about 4000 ppm, most preferably, below about 2500 ppm, to avoid the formation of stable emulsions when the unrefined polyol fatty acid polyester and the wash solution are dispersed.

A preferred method for preliminary soap removal is to add a small amount of water to the unrefined polyol fatty acid polyester to facilitate soap coagulation. Hydration is believed to increase the soap phase's specific gravity which aids in the separation process. The amount of water added depends on the level of soap in the unrefined polyol fatty acid polyester. The ratio of water to soap on a weight basis is from about 3:1 to about 1:3, more preferably from about 2: 1 to about 1:2.5 and most preferably from about 1:1 to about 1:2. The coagulated soap is then removed by common separation techniques such as settling, filtration or centrifugation.

Additionally, as will be discussed in greater detail below, the treated polyol fatty acid polyester, i.e., the polyol fatty acid polyester leaving the mixing vessel described herein, can be further treated by bleaching and/or filtration to further reduce the level of soap below detection limits, i.e., below about 50 ppm. The level of soap in a polyol fatty acid polyester can be measured by a neutralization titration using HC1, or other strong acid, to a predetermined endpoint.

A "base initiator", also known as a "basic catalyst", is generally used to allow the transesterification reaction of a polyol to form a polyol fatty acid polyester to occur at temperature below the degradation temperature of the polyol. Though basic catalyst is a preferred reaction component, it is generally considered an impurity in the polyol fatty acid polyester product stream. Discussions of the types of basic catalysts and their function in the transesterification of polyols can be found in U.S. Patent No. 3,963,699 to Rizzi et al., and U.S. Patent Nos. 4,517,360 and 4,518,772 to Volpenhein, which discussions are incorporated herein by reference. The basic catalyst is typically a strong base with an affinity for hydrogen and is often referred to as a base initiator because it serves to transform the polyol from a stable molecule to a reactive ion. Thus, the terms "basic catalyst" and "base initiator" are interchangeable as used herein. Specifically, the basic catalyst removes a hydrogen from the polyol molecule resulting in a polyol ion in a reactive state. For example, the basic catalyst converts sucrose to sucrate ion. Preferred basic catalysts are carbonate and methoxide ions, which can be complexed with an alkali or alkaline earth metal, for example, potassium or sodium.

As used herein, the term "phase transfer catalyst" is intended to include all chemical species which can interact with a polyol to form a chemical complex, wherein the complexed polyol can travel from one phase to a second phase, and wherein the uncomplexed polyol would not normally be soluble in the second phase. A phase transfer catalyst, as described herein, is to be distinguished from an emulsifier, e.g., a fatty acid soap, in that an emulsifier is believed to provide a single phase in which both chemical species are soluble, i.e. without the need for chemical complexing. As was the case with the other reaction components discussed above, a phase transfer catalyst and any breakdown product resulting therefrom, while often desirable in the transesterification of a polyol to form a polyol fatty acid polyester, is generally considered an impurity in a polyol fatty acid polyester product.

To reduce the levels of impurities in an unrefined polyol fatty acid polyester, the unrefined polyol fatty acid polyester is preferably treated in a mixing vessel with a wash solution resulting in a "treated polyol fatty acid polyester". Specifically, a wash solution is fed into the mixing vessel along with the unrefined polyol fatty acid polyester. The wash solution can be fed counter current or co- current to the unrefined polyol fatty acid polyester or the two solutions can be premixed prior to being fed into the mixing vessel. As used herein "mixing vessel" includes any conventional tank, column or other process equipment which allows the solutions to contact one another. Single stage columns, multistage columns, batch tanks, static mixers and bubble columns are examples of suitable mixing vessels and other appropriate mixing vessels are known to those skilled in the art.

Multistage columns with agitation are preferred mixing vessels for the processes described herein. Both co-current and counter-current are equally practical for multistage columns disclosed herein and they are equally efficient for a given droplet size and soap concentration. However, co- current operation is less efficient than counter-current with respect to the use of water, although co- current columns are generally easier to scale-up than counter-current columns. Once inside the column, the wash solution and the unrefined polyol fatty acid polyester are agitated creating a mixture which is sufficiently controlled to avoid the formation of stable emulsions.

The mixture of unrefined polyol fatty acid polyester and wash solution in the mixing vessel is preferably maintained at a temperature of from about 20°C to about 100°C, more preferably from about 40°C to about 95^CC, and most preferably from about 65°C to about 90°C. The mixing vessel can be operated at subatmospheric, atmospheric or superatmospheric pressures. One benefit to operating at superatmospheric pressure is that the temperature of the mixture can be increased slightly since the increase in pressure raises the boiling point of the constituents. Higher temperatures can be useful to maximize the solubility of the impurities in the wash solution thus, maximizing the purity of the polyol fatty acid polyester. Thus, the mixing vessel can be operated at higher temperatures without boiling the constituents. The benefits of operating the mixing vessels described herein at reduced or increased pressure must be weighed against the additional equipment and operational costs required with operating at other than atmospheric conditions. Thus, for purposes of efficiency and economics, it is preferred to operate the mixing vessels described herein at atmospheric pressure.

Often, it is desirable to pre ix the wash solution and the unrefined polyol fatty acid polyester prior to introducing them into the mixing vessel. The use of one inlet stream comprising a pre-mix of unrefined polyol fatty acid and the wash solution can provide manufacturing convenience and economic advantage over feeding the two streams separately to the mixing vessel.

Additionally, the unrefined polyol fatty acid polyester can be pre-treated to reduce the level of impurities and soap prior to being fed into the mixing vessel. For example, an unrefined polyol fatty acid polyester can be centrifuged to remove greater than about 90% by weight of the impurities and soap originally present therein prior to directing the polyol fatty acid polyester to the mixing vessel. As discussed above, it is preferred to remove most of the emulsifier, e.g. soap, if present, from the polyol fatty acid polyester in order to avoid the formation of stable emulsions in the wash solution/polyol fatty acid polyester mixture within the mixing vessel. The amount of impurities and soap actually removed in a centrifuge will depend on, at least, the concentration and type of impurities and soap in the unrefined polyol fatty acid polyester, the centrifuge used and the length of time the unrefined polyol fatty acid polyester is centrifuged.

The unrefined polyol fatty acid polyester may also be hydrated prior to centrifugation. The unrefined polyol fatty acid polyester is brought to a temperature of from about 50°C to about 95°C, preferably from about 65°C to 90°C, in a mixer. Water is added, and the water and unrefined polyol fatty acid polyester mixture is agitated while maintaining the temperature. Hydration is believed to increase the soap phase's specific gravity which aids in the separation process. The amount of water added depends on the level of soap in the unrefined polyol polyester. The ratio of water to soap on a weight basis is from about 3:1 to about 1:3, more preferably from about 2: 1 to about 1:2.5 and most preferably from about 1:1 to about 1:2. The coagulated soap is then removed by common separation techniques such as settling, filtration or centrifugation.

After the wash solution and the unrefined polyol fatty acid polyester are fed into the mixing vessel, they are dispersed to a level sufficient to produce a shear rate which results in the formation of a mixture and avoids the formation of stable emulsions. The mixture, as discussed above, contains droplets of one solution dispersed in the other solution. Preferably the droplets have an average diameter within the range of from about 5μ to about 3000μ. The mixture can contain droplets of wash solution dispersed in the unrefined polyol fatty acid polyester or visa versa, or the mixture can contain droplets of both solutions. The composition of the mixture will largely depend on the mass flow rates of each solution fed into the mixing vessel, as is discussed in greater detail below.

The dispersion will depend on, among other process parameters, the size and design of the mixing vessel, the mass flow rate of the solutions fed into the mixing vessel and the type and amount of agitation. "Agitation", as used herein includes any means for producing the mixture of wash solution and unrefined polyol fatty acid polyester. Agitation can be provided by a variety of commonly used processes and types of equipment. For example, impellers and rotating discs can be used to provide dynamic agitation, while forced gas (i.e., "bubbling"), static mixers and pulsation of the feed stream can provide acceptable non-dynamic agitation of the mixture in the mixing vessel. Agitation by impellers is preferred for use with the mixing vessels described herein, though it is understood that other methods of agitation are also suitable for use in the claimed methods.

As can be appreciated, when impellers are used for agitation their speed and design are important in promoting mixing and mass transfer of impurities from the unrefined polyol fatty acid polyester to the wash solution. By dispersing the mixture sufficiently to produce a shear rate which avoids the formation of stable emulsions, mass transfer of impurities and soap from the unrefined polyol fatty acid polyester to the wash solution can be optimized. As discussed above, other forms of agitation are appropriate for use with the present invention as long as the agitation is sufficient to produce a shear rate which avoids the formation of stable emulsions and simultaneously forms a dispersion containing the claimed droplet sizes.

The residence time of the mixture within the mixing vessel is also important in maximizing the extent of mass transfer of impurities from the unrefined polyol fatty acid polyester to the wash solution. Preferred residence times of the mixture in the mixing vessel are preferably within the range of from about 0.5 minutes to about 30 minutes, more preferably, from about 1 minute to about 15 minutes, most preferably, from about 1 minute to about 10 minutes and can be selected depending upon, for example, the concentration of impurities and soap in the unrefined polyol fatty acid polyester being fed into the mixing vessel and the desired level of impurities and soap in the treated product.

If the mixing vessel is a column, the number of stages in the column will necessarily affect the residence time as well as the amount of purification that occurs. Selection of the appropriate number of stages will depend on the height and diameter of the column, flow rates of each stream, and the method and amount of agitation, along with other process parameters. When the unrefined polyol polyester and the wash solution are fed co-currently, it is preferred that the column have from about 1 stage to about 7 stages. When the unrefined polyol polyester and the wash solution are fed counter current, it is preferred that the column have from about 5 stages to about 25 stages.

Another process parameter which can be varied to improve the mass transfer of impurities from the polyol fatty acid polyester to the wash solution is the amount of wash solution fed into the column. A preferred ratio of the mass feed rate of polyol fatty acid polyester to the mass feed rate of the wash solution is in the range of from about 3:1 to about 50: 1, and more preferably, from about 4:1 to 20: 1. More specifically, the ratio of the mass feed rate of polyol fatty acid polyester to the mass feed rate of the wash solution fed to a co-current multistage column is preferably in the range of from about 3: 1 to about 20:1, and the ratio of the mass feed rate of polyol fatty acid polyester to the mass feed rate of the wash solution fed to a counter current multistage column is preferably in the range of from about 4: 1 to about 40: 1.

As is discussed above, preferred mixing vessels for use with the present invention are multistage columns with agitation. Multistage columns suitable for use with the present invention include, but are not limited to, rotary disc contractors, Oldshue-Rushton extractors, Scheibel extraction towers, Kuhni towers, and the like. These columns are discussed by Perry, et al. Chemical Engineers Handbook, 6th Edition, 1984, pages 21-77 to 21-79, incorporated herein by reference. The columns in Perry et al. are schematically shown with counter current flow. A heavy liquid is fed from the top of a vertical column and removed from the bottom with a light liquid fed near the bottom and extracted near the top. As was discussed above, the two streams of the present invention can be fed counter current, i.e., the streams flow through the column in opposite directions, or co-current, i.e., both streams flow through the column in the same direction. When the two streams are fed at or near the same end of the column, they are normally removed at or near the opposite end of the column.

Baffles can be provided between stages within the column wherein the size and shape of the opening in the baffle is designed to provide the desired residence time within each stage and other process conditions. Likewise, within each stage, an impeller can be provided, and typically the impellers are connected to a single shaft which runs through the column. Thus, one shaft can drive all of the impellers, maintaining the agitation speed relatively constant within different stages. However, as can be appreciated, impellers with independent drive motors and/or gears can be provided at individual stages or between stages so that the respective impeller speeds vary from one stage to the next. Agitation speed within the column and within individual stages, the size and shape of the baffle openings separating stages and the number of stages are all design criteria which can be varied to achieve a desired purification.

Multistage columns can be provided with "calming" zones at one or both ends of the column wherein the treated mixture (that is, the resulting mixture following sufficient shear rate and residence time to achieve the desired degree of mass transfer of impurities from the polyol to the wash solution) is not agitated and can separate into two phases. If a calming zone is provided, the two phases can then be separated through the use of two extraction ports, i.e., a first port for extracting the first phase and a second port for extracting the second phase.

Having discussed the various solutions and process equipment suitable for use with the processes described herein, the next step is the post treatment processing of the mixture. As used herein "treated" is intended to mean the process of removing at least a portion of impurities and/or soap from the polyol fatty acid polyester. Hence, "treated polyol fatty acid polyester" means the polyol fatty acid polyester resulting when at least a portion of the impurities and soap have been removed by the processes described herein.

Preferably, the treated mixture is removed from the mixing vessel and allowed to settle and separate due to the forces of gravity into the two phases. Each of the two phases can then be separately removed as a treated polyol fatty acid polyester phase and an impurity- and soap- containing wash solution. Other methods of separation are equally appropriate and can be preferred in certain cases. For example, if time is a major consideration and capital and operational costs are not, the treated mixture can be transferred from the mixing vessel to a centrifuge where it can be separated into a light phase, which will normally comprise the treated polyol fatty acid polyester, and a heavy phase, which will normally comprise the impurity- and soap-containing wash solution. The treated polyol fatty acid polyesters of the present invention preferably have a Lovibond Red Scale value of below about 6, more preferably below about 4, and most preferably below about 2. The lower the Lovibond Red Scale value, the lower the level of color bodies in the polyol. The instrument used to measure color bodies was a Lovibond Automatic Tintometer with a red/yellow calibration standard (2.9 red/12.0 yellow).

The treated polyol fatty acid polyester can contain a small amount of the wash solution along with residual impurities and soap while the wash solution can contain a small amount of the polyol fatty acid polyester and other organic oils. It is preferred that the treated polyol fatty acid polyester contains less than about 1% by weight of the total of impurities and wash solution and less than about 100 ppm soap, and more preferably, less than about 50 ppm soap. It is preferred that the wash solution contain not greater than about 5 weight percent of organic oil. Since residual impurities, soap and wash solution can remain in the treated polyol fatty acid polyester after being treated in the mixing vessel, the treated polyol fatty acid polyester can be further refined in additional purification steps. For example, the treated polyol fatty acid polyester can be vacuum dried to remove wash solution and volatile impurities. Paniculate silica can also be contacted with the polyol fatty acid polyester to remove paniculate impurities and soap. Preferably, the treated polyol fatty acid polyester is vacuum dried prior to the removal of the excess fatty acid lower alkyl esters so that the concentration of wash solution, soap and impurities is less than 0.1% by weight. Additionally, as was discussed above, thermal evaporation to remove excess fatty acid lower alkyl esters, if any are present, can be employed and is often desirable.

The Detailed Description can be better understood when read in conjunction with the following examples wherein polyol fatty acid polyesters are made and water washed to form purified polyol fatty acid polyester product streams having the concentrations tabulated at the end of each example. In the examples, soap levels are measured using the titration methods discussed above and product color resulting from color bodies is measured using a commercially available Lovibond color analyzer or by measuring the absorbances at 440 and 550 nanometers using any commercially available UV- Visible spectrophotometer.

Example 1 This example compares a wash process using a multistage column with processes employing a packed column and a single stage agitated mixer-settler, respectively. Removal efficiencies of soap and water soluble color bodies are compared. While it is necessarily difficult to compare three different pieces of equipment under identical process conditions, in this example residence time for each piece of equipment is held constant at about 10-15 minutes to provide a meaningful comparison. Each piece of equipment is operated at a temperature in the range of from about 75 C to about 85 C. The wash solution is deionized water.

A. Packed Column

A packed column about 3 inches (7.5 cm) in diameter and about 21 inches (53 cm) in length packed with 3/8 inch (1 cm) glass Raschig rings, is used. Feed rates of the unrefined polyol polyester and wash solution are about 10 lb/hr (4.5 kg hr) each. The mean residence time of the polyol polyester and the wash solution is about 15 minutes. The polyol polyester and the wash solution are fed counter-current, with the wash solution entering the top of the column and the polyol polyester entering the bottom of the column. The contaminated wash solution exits at the bottom of the column and the purified polyol polyester exits at the top. The interface between the wash solution and the polyol fatty acid polyester phase is near the bottom of the packed column. The measured diameter of the water drops is about 3 mm.

B. Stirred Flask

A 1 liter round bottom flask, fitted with an agitator having a 2 inch (5 cm) long "half moon" impeller, is used for the mixer-settler. About 200 g of unrefined polyol polyester and about 37 g of wash solution are added to the flask and mixed in a batch mode for about 10 minutes at about 150 rpm. The wash solution becomes dispersed in the polyol polyester in water drops having an average diameter of about lOOOμ. The agitator is turned off. A wash solution phase is allowed to settle at the bottom of the flask below the polyol phase and is decanted from the polyol polyester phase.

C. Multistage Column

An Oldshue-Rushton column about 3 inches (7.5 cm) in diameter and about 16 inches (40 cm) in length, with seven stages is used as the multistage column. Each stage comprises two disc baffles with an inside diameter of about 1 5/8 inches (4 cm) and a vertical spacing of about 1 '/. inches (4 cm). A Rushton turbine impeller with a diameter of about 1 ' > inches (4 cm) is arranged in the middle of each stage. All impellers are mounted on a common shaft which rotates at a speed of 400 rpm. Flow rates of polyol polyester and wash solution are about 12.5 lb/hr (5.6 kg/hr) and about 3.2 lb/hr (1.4 kg/hr), respectively. The mean residence time of the polyol polyester and the wash solution in the column is about 14 minutes. The polyol polyester and wash solution are fed co- current into the top of the column. The product from the bottom of the column is allowed to settle by gravity into separate purified polyol fatty acid polyester and wash solution phases. The measured diameter of the drops is in the range of from about 5μ to about 70μ, with an average drop diameter of about 15μ.

Table I sets forth the washed product's soap content and color measurement for each mixing vessel and shows that the multistage column achieves the best results for removal of soap and color from the polyol polyester.

TABLE I

Polvol Polyester Analysis

Soap, ppm Color, AOCS Lovibond red

Starting material 638 4.2 Packed column 500 4.0 Mixing flask 179 2.4 Multistage column 161 1.8

Example 2

This example illustrates the effect of agitator rpm on color and soap removal in a multistage column. The same multistage column that is described in Example 1, C, is used for this example, including the same flow rates and flow patterns for the polyol polyester and the wash solution. The column is operated at a temperature in the range of from about 75°C to about 85°C. The starting unrefined material is a polyol polyester mixture comprising polyol polyester, fatty methyl ester, potassium stearate soap, sucrose, and water soluble sucrose by-products, and the wash solution source comprises deionized water. Agitator speeds range from 240 rpm to 600 rpm.

Table II sets forth the treated product's soap content and color measurement for each agitator speed and shows that the level of soap and color transferred from the polyol polyester phase to the wash solution is increased as agitator speed is increased.

TABLE II

Polvol Polyester Analysis

Color, AOCS Droplet Size

Soap, ppm Lovibond red Distribution

Starting material 638 4.2

240 rpm 218 1.8 15μ - 3000μ

400 rpm 161 1.8 Not Measured

550 rpm 110 1.5 Not Measured

600 rpm 98 1.3 5μ - 70μ

Example 3

This example illustrates the effect of residence time on color and soap removal in a multistage column. The same multistage column that is described in Example 1 is used for this example. The column is operated at a temperature in the range of from about 75°C to about 85°C. The agitator speed is set at 500 rpm and the unrefined starting material comprises a mixture of polyol polyester, fatty methyl ester, potassium stearate soap, sucrose, and water soluble sucrose byproducts. The wash solution source is 0.5% tripotassium citrate in deionized water. Flow rates of the polyol polyester and the wash solution are about 11.6 lb/hr (5.2 kg/hr) and about 4.1 lb/hr (1.8 kg/hr) respectively. The mean residence time for the polyol polyester and wash solution in the column ranges from 5 minutes to 10 minutes, as the number of mixing stages is varied from 3 to 7, respectively. The measured diameter of the drops is in the range of from about 5μ to about 70μ with an average drop diameter of about 15μ.

Table III sets forth the soap content and color measurement for each washed product and shows that the level of soap and color transferred from the polyol polyester phase to the wash solution phase increased as the residence time (and the number of mixing stages) were increased.

TABLE III Polvol Polyester Analysis Soap, ppm Color, AOCS Lovibond red

Starting material 638 4.2 5 min, 3 stages 156 2.3 10 min, 7 stages 94 1.8 Example 4

This example compares a production scale, multistage column to a single stage mixer- settler for removing trace levels of iron and calcium from polyol polyester. Each piece of equipment is operated at a temperature in the range of from about 75°C to about 85°C. The wash solution is deionized water.

A. Multistage Column

An Oldshue-Rushton column about 20 inches (51 cm) in diameter and about 98 inches (250 cm) in length, with seven stages is used as the multistage column. Each stage comprises two disc baffles with an inside diameter of about 10.25 inches (26 cm) and a vertical spacing of about 10 inches (25 cm). In the middle of each stage is a Rushton turbine impeller having a diameter of about 9.75 inches (25 cm). All impellers are mounted on a common shaft which rotates at a speed of 50-230 rpm. Flow rates of polyol polyester and wash solution are approximately 2650 lb hr (1200 kg/hr) and 477 lb/hr (210 kg/hr), respectively. The mean residence time of the polyol polyester and wash solution in the column is 2-15 minutes. The polyol polyester and wash solution are fed co- current into the top of the column. The measured size of the water drops is less than lOOOμ. The mixture from the bottom of the column is separated by a disc centrifuge into purified polyol fatty acid polyester and wash solution phases.

B. Mixer-Settler

An 850 gallon (3300 1) tank, fitted with an agitator with a 24 inches (61 cm) impeller is used as the mixer-settler. Approximately 2800 lbs. (1250 kg) of polyol polyester and 500 lbs (220 kg) of deionized water are added to the tank and mixed in a batch mode for about 10 minutes at about 20 rpm. The measured size of the water drops is about 3000μ. The agitator is turned off, and the wash solution phase settles to the bottom of the tank and is decanted from the crude polyol polyester.

Table IV sets forth the levels of calcium, iron and copper for each washed product and illustrates that a multistage column achieves the best results for removing trace levels of calcium and iron from the polyol polyester. The results for the mixer-settler are the average of 8 runs, while the results for the multistage column are the average of 4 runs. For both columns, the unrefined starting material comprises a mixture of polyol polyester, fatty methyl ester, potassium stearate soap, sucrose, and water soluble sucrose by-products and the wash solution comprises deionized water with no chelant. TABLE IV Polvol Polyester Analysis Calcium, ppm Iron, ppm Copper, ppm

Mixer-settler 2.51 0.49 0.08 Agitated column 0.27 0.13 0.07

Example 5

This example illustrates the effect of water washing on the removal of trace levels of iron, copper, calcium, and potassium from unrefined polyol fatty acid polyester. A single mixing vessel with a diameter of 20 inches (51.0 cm) and a Rushton turbine impeller with a diameter of 9.75 inches (25.0 cm) is used. The agitator speed is 230 rpm. Flow rates of polyol polyester and wash solution are approximately 2650 lb/hr (1200 kg/hr) and 477 lb/hr (210 kg/hr), respectively. The mean residence time of the polyol polyester and the wash solution in the mixing vessel is 2 minutes. The equipment is operated at a temperature in the range of from about 75°C to about 85°C. The wash solution is deionized water. The diameter of the drops is in the range of from about 5μ to about 70μ. The mixture from the bottom of the mixing vessel is separated by a disc centrifuge into a treated polyol fatty acid polyester phase and an impurity- and soap-containing wash solution phase.

Table V sets forth the treated polyol fatty acid polyester' s mineral content and shows that there is a significant reduction from levels in the unrefined polyol polyester.

TABLE V Polvol Polyester Analysis Iron, ppm Copper, ppm Calcium, ppm Potassium, ppm

Starting material 0.58 0.14 0.44 20.41 After water wash 0.17 0.06 0.35 0.77

Example 6

A. Preparation of Unrefined Esterified Propoxylated Glycerin Reaction Mix.

Glycerin, 992 parts, is heated with 80 parts of 85% potassium hydroxide solution at 110°C and 10 mm in a reactor with a dry ice trap for water removal until no further water is evolved. The reactor is pressurized with nitrogen and cooled to 92°C, and 3126 parts of propylene oxide is added on a pressure demand basis maintaining a reactor pressure of 55 psi. After the propylene oxide has been added the reaction is continued for an additional 5 hours. The reactor is then cooled and purged with nitrogen. A propoxylated glycerin with a molar ratio of propylene oxide to glycerin to 5: 1 is obtained. The propoxylated glycerin and cottonseed methyl esters are mixed in a molar ratio of methyl esters to propoxylated glycerin of 5:1. Sodium methylate, 0.13 mole sodium methylate/mole propoxylated glycerin, is added as additional basic catalyst. The propoxylated glycerin, cottonseed methyl esters and catalyst are heated at 150°C for 3 hours at 10 mm in a reaction flask equipped with a distilling head for methanol. Residual catalyst and soap levels in the esterified propoxylated glycerin (EPG) appear in Table VI.

B. Purification of Unrefined Esterified Propoxylated Glycerin Reaction Mix Using Mixing

Vessel With Controlled Mixing

Hydration And Preliminary Removal Of Catalyst And Soap

A 1 liter round bottom flask, fitted with a 2 inch (5 cm) long "half-moon" impeller is used for the mixer/settler. About 200 grams of the unrefined EPG of Example 6A is added to the flask and the temperature is raised to about 75°C. Water (2 grams) is then added and the mixture is agitated in a batch mode for about 10 minutes at about 150 rpm while maintaining the temperature at about 75°C. The agitator is turned off and phases are separated by centrifugation. Results for residual catalyst, soap and absorbances at 440 and 550 nanometers appear in Table VI.

Water Washing

The EPG is placed back in the 1 liter flask and the temperature is raised to about 75°C. Water (30 grams) is then added and the mixture is agitated in a batch mode for about 10 minutes at about 150 rpm while maintaining the temperature at 75°C. The agitator is turned off and the phases are separated by centrifugation. The polyol polyester phase is dried by heating the material to about 70°C for about 10 minutes under vacuum. Results for residual catalyst, soap and absorbances at 440 and 550 nanometers appear in Table VI.

C Reference Purification Method

About 200 grams of the crude from Example 6A is filtered through Whatman 40 filter paper using a Buchner Funnel. Results for residual catalyst, soap and absorbances at 440 and 550 nanometers appear in Table I. The resulting filtrate is added to a 1 liter flask described in Example 6B and is heated to 90°C. Magnesium silicate (1.2 grams of "Magnisol" of the FMC Corporation) is added and the mixture is agitated in a batch mode for about 2 hours at about 150 rpm while maintaining the temperature at about 90°C. The magnesium silicate is removed by centrifugation. Results for residual catalyst, soap and absorbances at 440 and 550 nanometers appear in Table VI. TABLE VI

Sample Catalyst (As Soap (As Absorbance at Absorbance

Sodium Potassium 440 nm^a at 550 nm^a

Methylate) Oleate)

Example 6A. Unrefined 0.14% 18,600 ppm N/A^b N/A^b

EPG.

Example 6B. Controlled mixing Purification

Method.

After hydration and soap None Detected 2,500 ppm 0.80 0.12 removal

After water wash None Detected 700 ppm 0.57 0.067

Example 6C. Reference

Purification Method

After filtration Trace 4,400 ppm 2.78 0.646

After centrifugation 1,200 ppm 1.02 0.16

^a Run neat in 1 cm cell.

" N/A = not available. Samples contained particulate.

Having shown and described the preferred embodiments of the present invention, further adaptation of the processes can be accomplished by appropriate modifications by one of ordinary skill in the art without departing from the scope of the present invention. A number of alternatives and modifications have been described herein and others will be apparent to those skilled in the art. For example, this reaction can be effectively run in a batch reaction process or a continuous reaction process. Additionally, although specific mixing vessels have been described, other mixing vessels can be used to produce the desired purified polyol fatty acid polyester. Likewise, while numerous polyols and fatty acid lower alkyl esters have been disclosed for the reaction mixture as preferred embodiments of the present invention, the constituents can be varied to produce other embodiments of the present invention as desired. Accordingly, the scope of the present invention should be considered in terms of the following claims and is understood not to be limited to the details of the compositions and methods shown and described in the specification.

Claims

WHAT IS CLAIMED IS:

1. A process for purifying an unrefined polyol fatty acid polyester, which process comprises the steps of: a) providing an unrefined polyol fatty acid polyester which comprises a polyol fatty acid polyester, impurities and soap, preferably the soap being present in an amount of less than about 4,000 ppm, most preferably less than about 2,500 ppm; b) feeding the unrefined polyol fatty acid polyester and a wash solution into a mixing vessel, preferably at a ratio of mass rate of feeding the unrefined polyol fatty acid polyester to mass rate of feeding the wash solution into the mixing vessel in the range of from about 50: 1 to about 3: 1; c) dispersing the wash solution and the unrefined polyol fatty acid polyester to produce a mixture containing droplets having an average diameter in the range of from about 5╬╝ to about 3,000╬╝, preferably in the range of from about 5╬╝ to about 70╬╝, and for a period of time sufficient for at least a portion of the impurities from the unrefined polyol fatty acid polyester to be transferred to the wash solution, preferably for a period of time less than about 30 minutes, more preferably less than about 15 minutes; and d) separating the mixture into a first phase comprising treated polyol fatty acid polyester and a second phase comprising impurity- and soap-containing wash solution; preferably wherein the polyol fatty acid polyester comprises an esterified linked alkoxylated glycerin, an esterified epoxide-extended polyol or mixtures thereof.

2. The process according to claim 1, further comprising the step of removing the mixture from the mixing vessel before separating it into two phases.

3. The process according to claim 1 or 2, wherein the step of dispersing produces a shear rate sufficient to form the mixture and to avoid the formation of stable emulsions.

4. The process according to any of claims 1 to 3, wherein the wash solution fed into the mixing vessel comprises deionized water, less than about 5.0% by weight of a chelating agent and less than about 0.5% by weight impurities.

5. The process according to any of claims 1 to 4, wherein the mixing vessel is a static mixer, a bubble column, an agitated tank, an agitated column or an agitated multistage column.

6. The process according to any of claims 1 to 5, wherein dispersing of the wash solution and the unrefined polyol fatty acid polyester to produce a mixture in the mixing vessel is conducted at a temperature of from about 20┬░C to about 100┬░C, and at atmospheric pressure.

7. The process according to any of claims 1 to 6, further comprising the step of vacuum drying the treated polyol fatty acid polyester to reduce the concentration of wash solution, soap and impurities in the resulting treated polyol fatty acid polyester to a concentration of less than about 0.1% by weight, and the step of filtering the treated polyol fatty acid polyester with particulate silica to further reduce the concentration of impurities and soap in the resulting treated polyol fatty acid polyester.

8. The process according to any of claims 1 to 7, further comprising the step of removing the soap from the unrefined polyol fatty acid polyester by adding water and separating out the soap phase before said unrefined polyol polyester is transfered to the mixing vessel.

9. The process according to any of claims 1 to 8 wherein the ratio of water to soap on a weight basis is from about 3:1 to about 1:3, preferably from about 2: 1 to about 1:2.5; most preferably from about 1:1 to about 1:2.

10. A treated polyol fatty acid polyester according any of claims 1 to 9, wherein the purified polyol fatty acid polyester comprises a polyol fatty acid polyester and less than about 1.0% by weight of the wash solution and impurities.

11. A process for preparing polyol fatty acid polyester, comprising the steps of: a) reacting a mixture comprising a polyol, preferably comprising a linked alkoxylated glycerin or an epoxide-extended polyol or a mixture thereof; fatty acid lower alkyl ester; and optionally an emulsifier or mixtures thereof, which includes, but is not limited to, a soap; to produce a reaction product comprising a polyol fatty acid polyester, impurities and soap, preferably the soap being present in the reaction product in a concentration of less than about 4,000 ppm, more preferably less than about 2,500 ppm; b) feeding the reaction product and a wash solution in a mass ratio of from about 50:1 to about 3:1, preferably from about 20: 1 to about 4:1, into a mixing vessel; c) dispersing the wash solution and the reaction product to produce a mixture containing droplets having an average diameter in the range of from about 5╬╝ to about 3,000╬╝, for a period of time sufficient for at least a portion of the impurities from the reaction product to be transferred to the wash solution; d) separating the mixture into a first phase comprising purified polyol fatty acid polyester and a second phase comprising impurity - and soap-containing wash solution; and e) separating the two phases.

12. A process according to Claim 11 comprising the additional step of preliminary soap removal before the reaction product is fed into a mixing vessel.

13. A process according to claims 11 or 12 wherein the ratio of the soap to the water on a weight basis is from about 3: 1 to about 1:3, preferably from about 2:1 to about 1:2.5; most preferably from about 1: 1 to about 1:2.

14. A purified polyol fatty acid polyester formed by the process of claims 1 or 11.