Background of the Invention Nonionic and anionic surfactants are important constituents in many applications. Both aromatic and aliphatic sulphates and sulphonates are an important group of anionic surface-active agents used extensively in a number of industrial applications. These include operations in drilling for and recovery of crude oil; emulsifiers for pesticides used in crop protection; in shampoos and creams for personal care; bar soaps; laundry detergents; dishwashing liquids, hard surface cleaners; emulsifiers for emulsion polymerisation systems; lubricants; wetting agents; and dispersants in a variety of specialised industrial applications.

The surfactants used in cleaning applications are designed to remove a wide variety of soils on fabrics and hard surfaces. Surfactants in this application have a balance of particulate soil removal and grease and oily soil removal characteristics. Especially in detergent compositions for cleaning fabrics, the surfactants used should have the ability to remove a broad spectrum of soil types.

In many cases, however, a surfactant which exhibits high detergency power will be poorly soluble in cold water. For example, surfactants present in laundry powder detergents should dissolve completely in a

relatively short time interval under whatever wash temperature and agitation conditions are employed in the wash cycle chosen by the consumer. Undissolved detergent not only fails to provide cleaning benefits, but also may become entrapped in the laundry articles and remain behind as a residue either in the machine or on the garments themselves. The problem of dispersion and solubilisation in the wash cycle are made worse under conditions of cold water washing especially at or below about 10°C (50°F). Lower wash temperatures are becoming ever increasing factors in today's wash loads as both energy conservation and increased use of highly coloured, delicate fabrics lead to wash conditions that make powders difficult to dissolve.

In contrast to nonionic surfactants, which exhibit inverse solubility behaviour and which, by virtue of hydrogen bridge bonds, show better solubility in cold water than in warm water, anionic surfactants show conventional behaviour, i. e. their solubility increases more or less linearly with the temperature until the solubilised product is reached. The surfactant employed, whether anionic or nonionic, should be designed to remain homogeneous in the wash media at cold water washing temperatures to optimise the cleaning performance of the surfactant. Accordingly, surfactants with the ability to remove sebum types of soil and which have low Krafft point temperatures are desirable.

Surfactants which have good washing and cleaning performance have low Krafft temperatures. The Krafft temperature refers to the temperature at which the solubility of an anionic surfactant undergoes a sharp, discontinuous increase with increasing temperature. The solubility of an anionic surfactant will increase slowly

with an increase in temperature up to the temperature point at which the solubility exhibits an extremely sharp rise. The temperature corresponding to the sharp rise in solubility is the Krafft temperature of anionic surfactant. At a temperature approximately 4°C above the Krafft temperature, a solution of almost any composition becomes a homogeneous phase. Further, the Krafft temperature is a useful indicator of detergency performance because at and above the Krafft temperature, surfactants begin to form micelles instead of precipitates, and below the Krafft temperature point, surfactants are insoluble and form precipitates. At the Krafft point temperature, the solubility of a surfactant becomes equal to its critical micelle concentration, or CMC. The appearance and development of micelles are important since certain surfactant properties such as foam production depend on the formation of these aggregates in solution.

Each type of surfactant will have its own characteristic Krafft temperature point. In general, the Krafft temperature of a surfactant will vary with the structure and chain length of the hydrophobic hydrocarbyl group and hydrophilic portion of the molecule. Krafft temperature for ionic surfactants is, in general, known in the art. See, for example, Myers, Drew, Surfactant Science and Technology, pp. 82-85, VCH Publishers, Inc.

(New York, N. Y., USA), 1988 (ISBN 0-89573-399-0), and K.

Shinoda in the text"Principles of Solution and Solubility", translation in collaboration with Paul Becher, published by Marcel Dekker, Inc. 1978 at pages 160-161.

A surfactant which exhibits a high Krafft point is generally insufficient in detergency and foaming power.

Since the Krafft point is a factor having an influence on the surface activating capacities of a surfactant, at temperatures lower than the Krafft point, surface- activating capacities such as detergency, foaming power and emulsifying power begin to deteriorate, and the surfactant may precipitate on the fabric. Thus, the surfactant should desirably possess a low Krafft point, especially in light of current performance requirements in cold water washing temperatures.

However, even surfactants with good detergency and high cold water solubility limits, as shown by their low Krafft point temperatures, may nevertheless leave behind precipitates on the surface to be cleaned if the surfactant is not tolerant to the concentration of electrolytes (typically magnesium and calcium) present in the aqueous washing medium. The electrolyte of most concern in wash water is calcium due to its high concentration in many aqueous media and its ability to exchange with the soluble sodium cation on sulphated surfactants to form an insoluble calcium salt of the sulphated surfactant, which precipitates out on to the substrate to be cleaned as a particle or film. The hardness of the water, or concentration of calcium and other electrolytes in water, will vary widely depending on the purification method and efficiency of water treatment plants which dispense water to the consumer of the detergent or cleaning composition. Accordingly, there remains a need to provide a surfactant which is tolerant to high concentrations of calcium so as to provide a cleanser which performs as expected in a wide variety of aqueous media.

Due to constraints on water consumption, especially in locations where the supply of drinking water to a

population is limited, inadequate, or expensive, there is a desire to employ unprocessed or lightly processed water having a high concentration of saline as a wash media.

In particular, there exists a need in some locations to use sea water or brackish water which is unprocessed or lightly processed as the aqueous media for many applications outside of drinking water, such as dishwashing and laundry water. The need to provide for a surfactant which is tolerant to high concentrations of electrolytes, such as calcium, is readily apparent if one must wash or clean a substrate in sea water or brackish water. Thus, there also exists a desire to find a surfactant composition, which is so highly tolerant to calcium that it is suitable for use in seawater or brackish as a cleansing agent.

It would also be desirable to manufacture a surfactant which can be easily and economically stored and transported. Polyoxyethylene nonionic linear alcohol surfactants, especially those containing from 3 or more ethylene oxide units, are solid or waxy products at ambient conditions (25°C and 1 atm). Since these waxy or solid products cannot be pumped at ambient conditions, they must first be melted into the liquid phase and kept as a liquid during offloading and feeding into a reaction vessel or a blend tank. Further, the waxy and solid polyoxyethylene linear alcohols must be shipped and/or transported in drums, which take up more warehouse space than liquid storage tanks. It would be desirable to produce a polyoxyalkylene surfactant which is flowable and pumpable at ambient conditions, and yet more desirable to produce such an surfactant which is flowable and pumpable in cold climates where temperatures drop to 0°C.

Summary of the Invention In accordance with the present invention there is provided a branched primary alcohol composition comprising a branched ether primary alcohol represented by the formula wherein Ri represents hydrogen or a hydrocarbyl radical having from 1 to 3 carbon atoms, R2 represents a hydrocarbyl radical having from 1 to 7 carbon atoms, x is a number ranging from 0 to 16, wherein the total number of carbon atoms in the alcohol ranges from 9 to 24.

There are also provided derivatives of the branched primary alcohol compositions such as alkoxylates, sulphates, and alkoxysulphates of such alcohol compositions. The derivatives are useful as detergent compositions having cold water solubility and high tolerance to calcium.

In accordance with the present invention there is also provided a process to produce a branched alcohol composition comprising: contacting an olefin having an average carbon number in the range of 3 to 18, preferably 6 to 18, with 1,3- propane diol in the presence of a catalyst, preferably an acid catalyst, effective to react the olefin with the diol under conditions effective to produce the branched alcohol composition, the diol and olefin preferably being contacted at a temperature within the range of from 50°C to 250°C.

Description of the Preferred Embodiments It has now been found that a surfactant and a composition exhibiting high calcium tolerance can be provided using the composition of the present invention containing derivatives of certain branched primary alcohol. It has been further found that the product has better cold water solubility than a linear alkyl sulphate having a comparable carbon number as measured by its Krafft point.

There is now provided a certain branched primary alcohol sulphate composition and a certain branched primary alcohol alkoxysulphate composition having a calcium tolerance of 5000 ppm CaCl2 or more, and as much as 50, 000 or more, preferably, 20,000 CaCl2 or more, more preferably 50,000 ppm or more, most preferably surfactant and a composition which possesses high calcium tolerance.

There is also provided a branched ether primary alcohol having a remote alpha branch ether trimethylene group, derivatives thereof such as alkoxylates (e. g., ethoxylates and/or propoxylates), the sulphates of each, and biodegradable branched ether surfactant compositions.

The remote alpha branch ether trimethylene moiety is structurally represented as: wherein R2 represents a hydrocarbyl radical having from 1 to 7 carbon atoms, preferably 1 carbon atom.

The term"hydrocarbyl"as used herein means that the radical concerned is primarily composed of hydrogen and carbon atoms but does not exclude the presence of other atoms or groups in a proportion insufficient to

detract from the substantially hydrocarbon characteristics of the radical concerned. Such radicals include: (i) Hydrocarbon groups, for example, aliphatic (e. g. alkyl or alkenyl), alicyclic (e. g. cycloalkyl or cycloalkenyl) and aromatic groups, aromatic groups having aliphatic or alicyclic substituents, and aliphatic and alicyclic groups having aromatic substituents. Examples of hydrocarbon groups include methyl, ethyl, ethenyl, propyl, propenyl, butenyl, cyclohexyl, t-butylphenyl, 2-benzethyl and phenyl groups; (ii) Substituted hydrocarbon groups, that is, groups having one or more non-hydrocarbon substituents which do not detract from the substantially hydrocarbon characteristics of the group. Examples of suitable non- hydrocarbon substituents include hydroxy, nitrile, nitro, oxo, chloro groups, and groups having ether or thioether linkages; and (iii) Hetero groups, that is, groups containing an atom other than carbon in a chain or ring otherwise composed of carbon atoms, the said atom not detracting from the substantially hydrocarbon characteristics of the group and inert to reactions.

Nitrogen, oxygen and sulphur may be mentioned as suitable hetero atoms. The hydrocarbyl radicals preferably contain only one non-hydrocarbon substituent or one non-carbon hetero atom if such substituents or atoms are present.

Anionic surfactants in detergent formulations are generally known to be subject to precipitation from wash water solutions containing hard water ions, e. g., magnesium and particularly calcium. Without intending to

be bound by the theory, it is believed that the tolerance of the surfactant molecules of the present invention, the compositions containing these molecules, and the formulations thereof, to calcium ions in wash solutions is attributable to the unique structure of the branched primary alcohol having a remote alpha branch ether trimethylene group.

The certain branched primary alcohol composition of the present invention is represented by the formula: wherein R1 represents hydrogen or a hydrocarbyl radical having from 1 to 3 carbon atoms, preferably hydrogen, R2 represents a hydrocarbyl radical having from 1 to 7 carbon atoms, preferably 1 carbon atom, x is a number ranging from 0 to 16, preferably from 3 to 13, wherein the total number of carbon atoms in the alcohol ranges from 9 to 24, preferably from 9 to 20.

The branched ether surfactant of the present invention is made by reacting an olefin with 1,3-propane diol in the presence of a suitable catalyst under primary alcohol forming conditions.

An olefin means any compound containing at least one carbon-carbon double bond. The desired average chain length of the olefin ranges from 3-18 aliphatic carbon atoms, preferably from 6-18, and more preferably from 12- 16 aliphatic carbon since molecules within this range are used in many washing applications. The most suitable chain length, however, will depend upon the particular end use, such as dish washing, liquid hand soap, bar

soap, laundry detergent, hard surface cleaners, or oil field applications.

The olefins may be linear or branched, may contain multiple double bonds anywhere along the chain, and may also contain acetylenic unsaturation. Further, the olefins may be substituted or unsubstituted, or may contain heteroatoms. The olefin may also be a bridged alpha olefin, such as Ci-Ca alkyl substituted norbornenes. Examples of norbornenes include 5-methyl- 2-norbornene, 5-ethyl-2-norbornene, and 5- (2'- ethylhexyl)-2-norbornene.

The olefin may contain an aryl, alkaryl, or cycloaliphatic group along with an aliphatic moiety within the same olefin compound, or the olefin may consist solely of an aliphatic compound. Examples of aryl groups include phenyl and naphthyl. Examples of cycloaliphatic moieties include the cyclo propyls, butyls, hexyls, octyls and decyls. Examples of alkaryls include tolyl, xylyl, ethylphenyl, diethylphenyl, and ethylnaphthyl. Preferably, the olefin composition comprises at least 90 wt. %, more preferably at least 95%, most preferably at least 98 wt. % aliphatic compounds.

The olefin may contain branched or linear olefins, or both. Examples of branching include alkyl, aryl, or alicyclic branches, preferably alkyl branches, and especially those alkyl groups having from 1 to 4 carbon atoms. The location of a branch on the olefin is not limited. Branches or functional groups may be located on the double bond carbon atoms, on carbon atoms adjacent to the double bond carbon atoms, or anywhere else along the carbon backbone.

The number of unsaturated bond sites along the chain is also not limited. The olefin may be a mono-, di-or

tri-unsaturated olefin, optionally conjugated. The olefin may also contain acetylenic unsaturation.

Preferably, the olefin composition comprises at least 90 wt. %, more preferably at least 95 wt. %, most preferably at least 98 wt. % mono-unsaturated olefin.

The olefin composition may comprise alpha olefins or internal olefins. An alpha olefin is an olefin whose double bond is located on both of a and carbon atoms.

An a carbon atom is any terminal carbon atom, regardless of how long the chain is relative to other chain lengths in a molecule. Specific non-limiting examples of alpha olefins suitable for use in the present invention include 1-propylene, 1-butene, 1-pentene, 1-isopentene, 1-hexene, 2-methyl-1-hexene, 1-octene, 1-nonene, 1-decene, 1- undecene, 1-dodecene.

An internal olefin (s) is an olefin whose double bond is located anywhere along the carbon chain except at any terminal carbon atom. The olefin composition feedstock is generally produced by commercial processes such as the oligomerisation of ethylene, optionally followed by isomerisation and disproportionation, such as those manufactured by Shell Chemical Company under the trademark NEODENE, or those manufactured by Chevron Chemical Company and BP-Amoco. Specific procedures for preparing suitable linear olefins from ethylene are described in US-A-3676523, US-A-3686351, US-A-3737475, US-A-3825615 and US-A-4020121. While most of such olefin products are comprised largely of alpha-olefins, higher linear internal olefins are also commercially produced, for example, by the chlorination dehydrochlorination of paraffins, by paraffin dehydrogenation, and by isomerization of alpha-olefins. Linear internal olefin

products in the C6 to C18 range are marketed by Shell Chemical Company and by Chevron Company.

Alternatively, the olefin composition may be produced by the Fisher-Tropsch process, which typically contains a high proportion of paraffins. A Fischer- Tropsch process catalytically hydrogenates CO to produce compositions containing aliphatic molecular chains.

Other processes for making feedstocks which may contain mixtures of olefins and paraffins include the dehydrogenation of paraffin, such as those made by the PacolTM processes of UOP, and the cracking of paraffin waxes.

The olefin feedstock composition may be a processed stream that has been fractionated and/or purified by a conventional distillation, extraction, or other separation operation to obtain a desired carbon number cut. Such operation produce compositions containing a mixture of carbon numbers or a single carbon cut composition. In these feedstocks, a mixture of olefins having different carbon numbers within the stated range and outside of the stated range may be present. However, the average carbon number of the mixture of all olefins is within the stated range. The feedstock stream preferably contains an average aliphatic carbon number ranging from C6-Cl6, and more preferably ranging from Cl2- C16, and wherein the predominant olefin species is within these ranges, inclusive. In addition to mixtures of olefins within this range, one may also employ what are known as single carbon cuts of olefins as feedstocks, wherein the single cut is within this range. For example, the feedstock employed may be a single C6, CS, C9, Coo, Cll, Cl2, C14, or C16 carbon cut.

The most preferred olefin composition feedstocks are those obtained from ethylene oligomerisation and Fischer- Tropsch (FT) synthesis. In one embodiment, the feedstock used comprises an alpha olefin composition having at least 70 wt. %, or more, more preferably at least 80 wt. %, or more, most preferably at least 90 wt. %, or more, of linear alpha mono-olefins within the desired carbon number range, (e. g. C6, C9-11, C11-15, C14-15, C15-18), the remainder of the product being olefin of other carbon number or carbon structure, diolefins, paraffins, aromatics, and other impurities resulting from the synthesis process.

The catalyst used in the synthesis of the branched ether primary alcohol is preferably an acid catalyst.

The acid catalyst is any conventional acidic catalyst effective to catalyse the reaction of the olefin with the diol to produce the branched alcohol surfactant of the present invention. Conventional acidic catalysts include, broadly, the Bronsted acids, Lewis acids or Friedel-Crafts catalysts, zeolites, and ionic exchange resins. The catalyst may be homogeneous or heterogeneous in the reaction mixture of olefin, diol, and reaction product. The reactants may contact a heterogeneous catalyst in suspension or on a fixed bed.

Suitable Lewis Acids typically include the halides and alkyl compounds of the elements in Groups IV B to XVIII B and III A to VI A of the Periodic Table of the Elements. Examples of Lewis acids and Friedel-Crafts catalysts are the fluorides, chlorides, and bromides of boron, antimony, tungsten, iron, nickel, zinc, tin, aluminium, gallium, indium, zirconium, vanadium, bismuth, titanium and molybdenum. The use of complexes of such halides with, for example, alcohols, ethers,

carboxylic acids, and amines are also suitable. More specific examples include BF3, BC13, aluminium bromide, FeCl3, SnCl4, SbCls, AsFs, AsF3, TiCl4, trimethyl aluminium, triethyl aluminium, and AlR [n] X [3-n] wherein n is an integer from 0 to 3, R is C1-C12 alkyl or aryl, and X is a halide, for example, Al (C2H5) 3, Al (C2H5) 2Cl, Al (C2Hs) C12, and AlCl3, titanium tetrachloride, zirconium tetrachloride, tin tetrachloride, vanadium tetrachloride and antimony pentafluoride.

Specific examples of Bronsted acids include, but are not limited to, phosphoric acid, sulphuric acid, sulphur trioxide, sulphonic acid, boric acid, hydrofluoric acid, fluorosulphonic acid, trifluoromethanesulphonic acid, and dihydroxyfluoroboric acid, perchloric acid and the perchlorates of magnesium, calcium, manganese, nickel and zinc; metal oxalates, sulphates, phosphates, carboxylates and acetates; alkali metal fluoroborates, zinc titanate; and metal salts of benzene sulphonic acid.

Suitable organic sulphonic acids include the alkane- and cycloalkane sulphonic acids, as well as arenesulphonic acids and heterocyclic sulphonic acids.

Specific examples of the alkane sulphonic acids include methanesulphonic acid, ethanesulphonic acid, propanesulphonic acid, butanesulphonic acid, pentanesulphonic acid, hexanesulphonic acid, dodecanesulphonic acid, hexadecanesulphonic acid, trifluoromethane sulphonic acid, sulphosuccinic acid, and cyclohexylsulphonic acid. Specific examples of arenesulphonic acids include benzenesulphonic acid, toluenesulphonic acid, styrene- (i. e. vinyl benzene) sulphonic acid, 5-sulphosalicylic acid, phenolsulphonic acid, and 1,6-naphthalene disulphonic acid. Specific examples of heterocyclic sulphonic acids include

sulphanilic acid. Alkyl and aryl groups of the sulphonic acid molecule are suitably substituted with relatively inert organic and/or inorganic substituents. Examples of substituted organic sulphonic acids include 4-hydroxybenzene sulphonic acid, trifluoromethane sulphonic acid, isethionic acid, and taurine.

A class of sulphur based acids commonly used in homogeneous acidic catalyzed reactions include sulphuric acid, sulphur trioxide, Cl to C30 alkyl sulphuric acids, sulphanilic acid, toluenesulphonic acid, styrenesulphonic acid, methanesulphonic acid, and 5-sulphosalicylic acid.

Also included as an acid catalyst are any of the alkoxylation catalysts, magnesium in combination with halides of aluminium, boron, zinc, titanium, silicon, or molybdenum; BF3 or SiF4 in combination with an alkyl or alkoxide compound of aluminium, gallium, indium, thallium, titanium, zirconium and hafnium; and a mixture of HF and one or more metal alkoxides.

Instead of an acidic homogeneous catalyst, one may also employ a solid acidic heterogeneous catalyst.

Solid acidic catalysts include acidic polymeric resins, supported acids, and acidic inorganic oxides. The solid acidic catalysts have the advantage of avoiding the difficult separation steps for removing the catalyst from unreacted diol in the product mixture, and further avoid the need to deactivate the catalyst in the event that the catalyst is not removed from the product mixture. In one embodiment of the present invention, the diol is pretreated to reduce the quantity of carbonyl compounds present as impurities in the diol composition prior to reaction with the olefin in the presence of a solid acidic heterogeneous catalyst, thereby extending the life of the solid acidic catalyst.

Typical carbonyl impurities present in a diol include aldehydes or acetals. One example of a suitable pre- treatment is to hydrotreate the diol. Suitable hydrotreating methods include treatment with sodium borohydride or catalytic hydrogenation such as nickel on alumina or silica catalyst. In a more preferred embodiment, the amount of carbonyl impurities present in the diol is reduced to less than 100 ppm, more preferably to less than 50 ppm, most preferably to less than 10 ppm.

An example of a solid acidic polymeric resin is a solid acidic ion exchanger having acid active sites and a strong acid activity of each acid site. Common acidic ion exchange resins are sulphated resins, wherein the resins are copolymers of styrene and divinylbenzene, phenol based resins, poly (tetrafluoroethylene) polymers or siloxane polymers. Specific examples of such resins include the line of AMBERLYSTO catalysts, including AMBERLYSTO 15,36 or 38, NAFIONO or DELOXANO catalysts.

Other supported solid acidic catalysts include the Lewis acids (examples include BF3, BC13, AlC13, AlBr3, FeCl2, FeCl3, ZnCl2, SbFs, SbCls and combinations of A1C13 and HC1) which are supported on solids such as silica, alumina, silica-aluminas, zirconium oxide or clays.

When supported liquid acids are employed, the supported catalysts are typically prepared by combining the desired liquid acid with the desired support and drying.

Supported catalysts which are prepared by combining a phosphoric acid or sulphur based acid with a support are low in cost.

Acidic inorganic oxides which are useful as catalysts include, but are not limited to, aluminas, silica-aluminas, aluminophosphates, natural and

synthetic pillared clays, and natural and synthetic zeolites such as faujasites, mordenites, L, omega, X, Y, beta, ZSM, and MCM zeolites.

Representative examples of naturally occurring zeolites include faujasit, mordenite, zeolites of the chabazite-type such as erionite, offretite, gmelinite and ferrierite. Clay catalysts, another class of crystalline silicates, are hydrated aluminium silicates.

Typical examples of suitable clays, which are acid- treated to increase their activity, are made from halloysites, kaolinites and bentonites composed of montmorillonite. These catalysts can be synthesized by known methods and are commercially available.

Suitable synthetic zeolites include ZSM-4 as described in US-A-4021447, ZSM-5 as described in US-A-3702886, ZSM-11 as described in US-A-3709979, ZSM-12 as described in US-A-3832449 and US-A-4482531, ZSM-18 as described in US-A-3950496, ZSM-20 as described in US-A-3972983, ZSM-21 as described in US-A-4046859, ZSM-25 as described in US-A-4247416, ZSM-34 as described in US-A-4086186, ZSM-38 as described in US-A-4046859, ZSM-39 as described in US-A-4287166, ZSM-43 as described in US-A-4247728, ZSM-45 as described in US-A-4495303, ZSM-48 as described in US-A-4397827, ZSM-50 as described in US-A-4640829, ZSM-51 as described in US-A-4568654, ZSM-58 as described in US-A-4698217, MCM-2 as described in US-A-4647442, MCM-14 as described in US-A-4619818, MCM-22 as described in US-A-4954325, MCM-36, MCM-49 as described in US-A-5236575, MCM-56, SSZ-25, SSZ-31, SSZ-33, SSZ-35, SSZ-36, SSZ-37, SSZ-41, SSZ-42, beta as described in US-A-3308069 and US-E-28341, X as described in US-A-3058805, Y as described in US-A-3130007, and mordenite as described in US-A-3996337. If desired, the

zeolites can be incorporated into an inorganic oxide matrix material such as a silica-alumina.

Representative examples of useful silica alumina phosphate catalysts include SAPO-5, SAPO-11 and SAP041 as described in US-A-4440871.

Intermediate pore size (up to 7.5 x 10-7 mm (7.5 Angstroms) in the largest dimension at the pore opening) and larger pore zeolites are preferred. Large pore size zeolites are most preferred because they can accommodate the larger olefin molecules, thereby providing a higher active surface area for reaction between the diols and olefins.

Examples of intermediate pore size zeolites include ZSM-5, ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35, ZSM-38, ZSM-48, ZSM-57 and ZSM-58.

Larger pore size zeolites include MCM-22, zeolite Beta, zeolite Y and ZSM-20. Examples of a preferred modified Y type zeolite include those disclosed in US-A-5059567.

Such zeolite catalyst should be at least partly in the acidic (H) form to confer the acidity for the reaction but may contain other cations such as ammonium (NH4+).

The form and the particle size of the catalyst are not critical to the present invention and may vary depending, for example, on the type of reaction system employed. Non-limiting examples of the shapes of the catalyst in the present invention include balls, pebbles, spheres, extrudates, channelled monoliths, honeycombed monoliths, microspheres, pellets, or structural shapes, such as lobes, trilobes, quadralobes, pills, cakes, honeycombs, powders and granules, formed

using conventional methods, such as extrusion or spray drying.

The diol and olefin react through the hydroxyl- double bond sites in the presence of an acidic catalyst to produce a branched primary alcohol ether surfactant of the present invention containing within the molecule the remote alpha branch ether trimethylene moiety. For illustrative purposes, when the olefin is an alpha- olefin, the reaction proceeds according to the following equation: Ri and R2 represents the hydrocarbyl group as described above, and R2'is R2 less hydrogen where the linkage with the CH group is by double bond and x is the same as described above. When the olefin is reacted with the diol, the hydroxyl hydrogen becomes bonded to the R2'to become R2.

The products produced from the reaction of the olefin and diol compositions include the isomers of the olefin-diol adduct, olefin dimers, diolefin ether adducts, and diol dimers. Isomers of the olefin-diol adduct are made by reaction of the diol at the electropositive stable double bond carbon. In the

presence of an acidic catalyst, double bond isomerisation may occur, resulting in an product mixture which contains branches of different carbon number length depending upon the position of the double bond at the time the diol reacts with the olefin. To illustrate, the reaction of 1,3-propanediol with 1-dodecene in the presence of an acidic catalyst may produce the following isomers: I1 is made by the nucleophilic attack of the oxygen atom with an olefin when the double bond is in the alpha 1,2 carbon atom position. In this case, no double bond isomerisation occurs, resulting in the desired product.

Is is made when the olefinic double bond is isomerised to the 2,3 carbon atoms, and 13 is made when the olefinic double bond is isomerised to the 3,4 carbon atoms.

Double bond isomerisation can be minimized by selection of an acidic catalyst which does not tend to double bond isomerise the olefin. Double bond isomerisation may also be minimized by reducing the residence time of the diol-

olefin reaction, and by carrying out the diol-olefin reaction at temperatures higher than typical temperatures favoured for double bond isomerisation. In general, double bond isomerisation is favoured at temperatures ranging from 50°C to 150°C.

Another by-product, the diolefin ether adduct, is made when two olefin molecules react with diol across the diol hydroxyl groups. To illustrate, such a by-product is represented by the formula: wherein Rl, R2, and x are as described above. Formation of this by-product is minimized by using a molar excess of propanediol to olefins. While suitable molar ratios of diol to olefin range from 0.1: 1 to 100: 1, it is preferred to use a diol to olefin ratio of at least 1: 1, more preferably from greater than 1: 1, and most preferably at least 1.5: 1. An alternative which simulates a molar excess of diol to olefin to obtain the same effect, the olefin may be slowly added over a period of time to the whole amount of diol to be reacted over a period to the diol to the olefin/catalyst mixture, having the effect of a large molar excess of diol.

Other by-products which may be formed in the reaction of an olefin with a diol include the dimers of the olefins contained in the olefin composition, the dimers of the diols used in the diol composition.

The olefin-diol adducts of the present invention are obtained in high purity. Based on the weight percentage of reaction products, the reaction of the

olefin with diol in the presence of an acid catalyst, the selectivity of the olefin-diol product is 80 wt. % or more of the total reacted product mixture, more preferably 85 wt. % or more, most preferably 90 wt. % or more.

The process for making the branched ether surfactant compositions of the present invention is flexible in that suitable product can be made under a wide range of operating conditions. The reaction temperature and pressure is not limited, so long as the reaction proceeds forward within the desired time and the product and reactants do not decompose. The reaction is carried out under conditions effective to react the olefin and diol to produce the branched primary alcohol composition of the present invention.

Suitable reaction temperatures range from 50°C to 250°C, more preferably from 100°C to 200°C. The system pressure may be sub-atmospheric, atmospheric, or super- atmospheric, depending upon the equipment design and process flow chosen. The residence time in batch operations ranges from 5 minutes to 3 hours.

In a homogeneous batch process, olefin, diol, and catalyst are added to a reaction vessel and heated. The order of addition is not limited. However, yield of the is increased by adding the diol to the olefin.

Accordingly, in a preferred embodiment, olefin and catalyst are heated in a reaction vessel, and the diol is added to the heated olefin and catalyst in the reaction vessel.

SULPHATION Anionic surfactants useful in preparing detergents having calcium tolerance and have solubility in cold water include alkyl ether sulphates of the branched

primary alcohol of the present invention. These materials have the respective formulae XOS03M, wherein X is represented by the formula and M is hydrogen or a cation such as ammonium, alkanolammonium (e. g. triethanolammonium), a monovalent metal cation (e. g. sodium and potassium), or a polyvalent metal cation (e. g. magnesium and calcium). Preferably, M should be chosen such that the anionic surfactant component is water soluble. R1represents hydrogen or a hydrocarbyl radical having from 1 to 3 carbon atoms, Rz represents a hydrocarbyl radical having from 1 to 7 carbon atoms, x is a number ranging from 0 to 16, wherein the total number of carbon atoms in the alkyl ether sulphate ranges from 9 to 24.

In accordance with the present invention there is also provided a process to produce a branched alkyl ether sulphate composition comprising: a) contacting an olefin having an average carbon number in the range of 3 to 18 with 1,3-propane diol in the presence of a catalyst effective to react the olefin with the diol thereby producing a branched alcohol composition; and b) contacting the branched alcohol composition with a sulphating agent under conditions effective to produce a branched alkyl ether sulphate composition.

The branched primary alcohol composition may be directly sulphated, or first alkoxylated followed by sulphation as described above. Alkoxylation of the branched primary alcohol is described below. The general class of alcohol alkoxysulphates can be characterised by the chemical formula: wherein Rlrepresents hydrogen or a hydrocarbyl radical having from 1 to 3 carbon atoms, R2 represents a hydrocarbyl radical having from 1 to 7 carbon atoms, x is a number ranging from 0 to 16, preferably from 3 to 13, A is an alkylene radical, preferably having carbon number in the range of 2 to 4, more preferably 2 or 3, most preferably 2, y is a number ranging from 1 to 9, wherein the total number of carbon atoms in the alcohol ranges from 9 to 24, and M is hydrogen or a cation described above. AO represent an oxyalkylene group.

The sulphating agents suitable for use in sulphating the branched primary alcohol or its alkoxylated derivative include those compounds capable of forming the carbon to oxygen to sulphur bonds necessary for the formation of an alkyl ether sulphate or alcohol alkyoxylsulphate. The particular sulphating agents used are typically a function of the compounds to be sulphated. These sulphating agents can be any sulphating agent known in the art for the sulphation of alcohols and include sulphur trioxide, chlorosulphonic acid or oleum.

Sulphation processes are described, for instance, in US-A-3462525, US-A-3428654, US-A-3420875, US-A-3506580, US-A-3579537 and US-A-3524864. Suitable sulphation

procedures include sulphur trioxide (S03) sulphation, chlorosulphonic acid (ClSO3H) sulphation and sulphamic acid (NH2SO3H) sulphation. When concentrated sulphuric acid is used to sulphate alcohols, the concentrated sulphuric acid is typically from 75 percent by weight to 100 percent by weight, preferably from 85 percent by weight to 98 percent by weight, in water. Suitable amounts of sulphuric acid are generally in the range of from 0.3 mole to 1.3 moles of sulphuric acid per mole alcohol, preferably from 0.4 mole to 1.0 mole of sulphuric acid per mole of alcohol.

A typical sulphur trioxide sulphation procedure includes contacting the branched primary alcohol or its alkoxylate and gaseous sulphur trioxide at about atmospheric pressure in the reaction zone of a falling film sulphator cooled by water at a temperature in the range of from 25°C to 70° C to yield the sulphuric acid ester of alcohol or its alkoxylate. The sulphuric acid ester of the alcohol or its alkoxylate then exits the falling film column and is neutralised with an alkali metal solution, e. g. sodium or potassium hydroxide, to form the alcohol sulphate salt or the alcohol alkoxysulphate salt.

The sulphation reaction is suitably carried out at temperatures in the range of from-20°C to 50°C, preferably from 5°C to 40°C, and at pressures in the range of from 1 atmosphere to 5 atmospheres, preferably from 1 atmosphere to 2 atmospheres, and more preferably, about 1 atmosphere. Suitable residence times for the sulphation reaction range from a second to an hour, preferably from 2 minutes to 30 minutes.

The neutralisation reaction is accomplished using one or more bases such as ammonium or alkali metal or alkaline earth metal hydroxides or carbonates or bicarbonates dispersed in a non-surfactant carrier.

Suitable bases include sodium hydroxide, sodium carbonate, potassium hydroxide and calcium hydroxide, with ammonium hydroxide, sodium hydroxide or potassium hydroxide being the preferred base. The amount of base added is in an amount sufficient and in a time sufficient to neutralise the acidity of the alkyl ether sulphonic acid.

The neutralisation procedure can be carried out over a wide range of temperatures and pressures. Typically, the neutralisation procedure is carried out at a temperature in the range of from 0°C to 35° C, and typically at atmospheric pressure.

ALKOXYLATES Alkoxylates of the branched primary alcohol of the present invention can be prepared by the sequential addition of alkylene oxide to the branched primary alcohol in the presence of a catalyst. Any known conventional alkoxylation method can be used.

The present invention is preferably applied to processes utilizing an alkylene oxide (epoxide) reactant which comprises one or more vicinal alkylene oxides, particularly the lower alkylene oxides and more particularly those in the C2 to C4 range. In general, the alkylene oxides are represented by the formula

wherein each of the R1, R2, R3 and R moieties is individually selected from the group consisting of hydrogen and alkyl moieties. Reactants which comprise ethylene oxide, propylene oxide, or mixtures of ethylene oxide and propylene oxide are more preferred, particularly those which consist essentially of ethylene oxide and propylene oxide. Alkylene oxide reactants consisting essentially of ethylene oxide are considered most preferred from the standpoint of commercial opportunities for the practice of alkoxylation processes, and also from the standpoint of the preparation of products having narrow-range ethylene oxide adduct distributions.

An illustration of the branched alkanol alkoxylate product of the present invention by adding y numbers of alkylene oxide molecules to the branched primary alcohol of the present invention is presented by the formula: wherein Ri represents hydrogen or a hydrocarbyl radical having from 1 to 3 carbon atoms, R2 represents a hydrocarbyl radical having from 1 to 7 carbon atoms, x is a number ranging from 0 to 16, preferably from 3 to 13, A is an alkylene radical, preferably having carbon number in the range of 2 to 4, more preferably 2 or 3, most preferably 2, y is a number ranging from 1 to 9, wherein the total number of carbon atoms in the alcohol ranges from 9 to 24. AO represent an oxyalkylene group.

In terms of processing procedures, the alkoxylation reaction in the present invention may be conducted in a generally conventional manner. For example, the catalyst in the liquid active hydrogen containing reactant is contacted, preferably under agitation, with alkylene oxide reactant, which is typically introduced in gaseous form, at least for the lower alkylene oxides.

In preferred embodiments, the alkylene oxide reactant is ethylene oxide or propylene oxide or a mixture of ethylene oxide and propylene oxide. The reaction is carried out in the presence of a catalytically effective amount of an alkoxylation catalyst. In a particularly preferred embodiment, ethylene oxide is contacted and reacted with the branched primary alcohol of the present invention in the presence of a catalytically effective amount of a catalyst for alkoxylation.

Any conventional alkoxylation catalyst can be used.

One example of a typical catalyst is solid or aqueous solution of KOH. Examples of these catalysts can be found in US-A-1970578 and in DE-C-605973.

Another example of a suitable alkoxylation catalyst is described in US-A-5057627. Alkoxylation can be catalysed by phosphate salts of the rare earth elements.

These catalysts were typically prepared by adding an aqueous solution of a rare earth compound such as lanthanum chloride to an aqueous sodium orthophosphate or H3PO4 solution.

While these procedures describe a batch mode of operation, the present invention is equally applicable to a continuous process.

Overall, the two reactants are utilised in quantities which are predetermined to yield an alkoxylate

product of the desired mean or average adduct number.

The average adduct number of the product is not critical to this process. Such products commonly have an average adduct number in the range from less than one to 30, or greater.

In general terms, suitable and preferred process temperatures and pressures for purposes of the present invention are the same as in conventional alkoxylation reactions between the same reactants, employing conventional catalysts. A temperature of at least 90°C, particularly at least 120°C, and most particularly at least 130°C, is typically preferred from the standpoint of the rate of reaction, while a temperature less than 250°C, particularly less than 210°C, and most particularly less than 190°C, is typically desirable to minimise degradation of the product. As is known in the art, the process temperature can be optimised for given reactants, taking such factors into account.

Superatmospheric pressures, e. g. pressures between 69 and 1034 kPa g (10 and 150 psig), are preferred, with pressure being sufficient to maintain the active hydrogen containing reactant substantially in the liquid state.

When the alkylene oxide reactant is a vapour, alkoxylation is then suitably conducted by introducing alkylene oxide into a pressure reactor containing the alcohol reactant and the catalyst. For considerations of process safety, the partial pressure of a lower alkylene oxide reactant is preferably limited, for instance, to less than 414 kPa a (60 psia), and/or the reactant is preferably diluted with an inert gas such as nitrogen, for instance, to a vapour phase concentration of about 50 percent or less. The reaction can, however, be safely accomplished at greater alkylene oxide concentration,

greater total pressure and greater partial pressure of alkylene oxide if suitable precautions, known to the art, are taken to manage the risks of explosion. A total pressure of between 276 and 758 kPa g (40 and 110 psig), with an alkylene oxide partial pressure between 103 and 414 kPa g (15 and 60 psig), is particularly preferred, while a total pressure of between 345 and 621 kPa g (50 and 90 psig), with an alkylene oxide partial pressure between 138 and 345 kPa g (20 and 50 psig), is considered more preferred.

The time required to complete a process according to the present invention is dependent both upon the degree of alkoxylation that is desired (i. e. upon the average alkylene oxide adduct number of the product) as well as upon the rate of the alkoxylation reaction (which is, in turn dependent upon temperature, catalyst quantity and nature of the reactants). A typical reaction time for preferred embodiments, particularly for when the alkylene oxide is gaseous is less than 24 hours.

After the alkoxylation reaction has been completed, the product is preferably cooled. If desired, catalyst can be removed from the final product, although catalyst removal is not necessary to the process of the present invention. Catalyst residues may be removed, for example, by filtration, precipitation or extraction. A number of specific chemical and physical treatment methods have been found to facilitate removal of catalyst residues from a liquid product. Such treatments include contact of the alkoxylation product with strong acids such as phosphoric and/or oxalic acids or with solid organic acids such as NAFION H+ or AMBERLITE IR 120H; contact with alkali metal carbonates and bicarbonates ; contact with zeolites such as type Y zeolite or

mordenite; or contact with certain clays. Typically, such treatments are followed by filtration or precipitation of the solids from the product. In many cases filtration, precipitation or centrifugation is most efficient at elevated temperature.

The tolerance of the sulphated branched primary alcohols to calcium ions was determined by titration of test solutions of each of the compounds with calcium chloride. Specifically, the tolerance of the anionic surfactants to calcium ions was determined by taking lOcc of a 0.06% by weight anionic surfactant solution in distilled water adjusted to a pH of 5 using sodium hydroxide, added to a capped bottle, and placed into a oven maintained at 40°C. Addition of 10 micro litre aliquots of 10% solutions of calcium chloride in distilled water added to provoke a precipitate formation from the reaction of the surfactant and the salt. After a sufficient amount of time had elapsed for equilibration and phase separation, the clear, top, portion was measured for activity by/via the two phase titration method disclosed in Reid, V. W., G. F. Longman and E.

Heinerth,"Determination of Anionic-Active Detergents by Two-phase Titration,"Tenside 4,1967,292-304. The reported calcium chloride tolerance is the ppm amount of calcium chloride which was added to precipitate 50 weight% of the anionic surfactant.

The sulphated branched primary alcohol compositions of the present invention have several orders of magnitude higher calcium tolerance over linear alkylbenzene sulphonates and branched alkyl sulphates having the same carbon number. In one embodiment, there is provided a sulphated branched primary alcohol composition and derivatives thereof having a calcium tolerance of 5000

ppm CaCl2 or more. Preferably, the sulphated branched primary alcohol composition and derivatives thereof have a calcium tolerance of 20,000 CaClz or more, more preferably 50,000 ppm or more, most preferably 75,000 or more, and even 100,000 ppm or more. By comparison, linear alkylbenzene sulphonates have calcium tolerance values under 250, linear alkylsulphates have calcium tolerance values under 100, and branched alkyl sulphates have calcium tolerance values under 500.

Such high calcium tolerance renders the surfactant compositions made by the branched primary alcohol compositions of the present invention suitable for use in aqueous media having large levels of electrolytes. In one embodiment, there is provided a surfactant composition which is tolerant to aqueous media containing at least 100,000 ppm calcium chloride In another embodiment, there is provided a surfactant composition which is tolerant to sea water having a salinity of at least 25,000 ppm, preferably at least 30,000, more preferably about 34,000 ppm or more of total dissolved solids, and a cumulative amount of calcium and magnesium of at least 1000 ppm, more preferably at least 1500ppm, most preferably at least 1700 ppm.

A useful test to determine whether a surfactant solution is tolerant to sea water is as follows: a 0.06% active surfactant solution in sea water is prepared and visually inspected for turbidity. The composition shown below was visually observing whether any surfactant precipitates (fail) or whether no precipitation occurs (pass).

The sea water used for a test to determine whether a particular surfactant composition is tolerant to sea

water has a composition of about 34 ppt salinity, with an ion concentration as follows: <BR> <BR> ION Conc. (mg/1) ION Conc. (mg/1) Chloride 19251 Sodium 10757 Sulphate 2659 Magnesium 1317 Potassium 402 Calcium 398 Carbonate/Bicarbonate 192 Strontium 8.6 Boron 5.6 Bromide 2.3 Iodide 0.22 Lithium 0.18 Trace amounts of between 0.01 and 0.05 mg/1 of each of copper, iron, nickel, zinc, maganese, molybdenum, cobalt, vanadium, aluminium, barium and fluorine are present.

Other trace amounts of elements are be present in the following quantities: Lead at < 0.005 mg/1 Arsenic at < 0.0002 mg/1 Chromium at < 0.0006 mg/1 Trace amounts of Tin, Antimony, Rubidium and Selenium.

No amounts of Mercury, Nitrate and Phosphate.

In an independent embodiment of the present invention, the branched ether surfactant compositions of the present invention exhibit low Krafft temperature points. The Krafft temperature of anionic surfactants are measured by diluting the anionic surfactant to a homogeneous aqueous 1 weight % surfactant solution in water, freezing 25 cc aliquots of the solution in a freezer overnight at approximately-4 deg C to force the surfactant out of solution, and then warming the solution in a temperature-controlled water bath in one degree

intervals at a rate of one degree/hour. The reported Krafft temperature is the lowest temperature where the solution is fully transparent as determined by visual inspection.

In this embodiment, the sulphates of the branched ether primary alcohols, their derivatives, and their branched ether surfactant compositions exhibit Krafft temperatures of 10°C or less, more preferably 0°C or less. The branched ether surfactant compositions containing the sulphates of the branched ether primary alcohols and/or their derivatives are highly soluble in the aqueous wash media, thereby contributing to improved detergency performance and reducing the tendency toward precipitation, especially at colder wash temperatures of 10°C (50°F) or less.

In yet another independent embodiment of the present invention, the branched ether surfactant compositions of the present invention exhibit cold water detergency values of at least 22% measured at 10°C (50°F). In a preferred embodiment, the branched ether surfactant composition has a cold water detergency value of at least 28% measured at 10°C (50°F). In yet a more preferred embodiment, the sulphates of the branched ether primary alcohols, their derivatives, and their branched ether surfactant compositions simultaneously exhibit cold water detergency values of at least 22% at 10°C (50°F), Krafft temperatures of 10°C or less, more preferably 0°C or less, and have a calcium tolerance of 5000 ppm CaCl2 or more.

The detergency evaluations can be conducted from a standard high density laundry powder (HDLP) Detergency/Soil Redeposition Performance test. The

evaluations can be conducted using Shell Chemical Company's radiotracer techniques at 10°C (50°F) and 32°C (90°F) temperatures at a water hardness of 150 ppm as CaCO3 (CaCl2/MgCl2 = 3/2 on a molar basis). The sulphated branched ether surfactant compositions of the present invention can be. tested, on a 1/4 cup basis, against multisebum, cetanesqualane and clay soiled permanent press 65/35 polyester/cotton (PPPE/C) fabric. The HDLPs are tested at 0.74 g/1 concentration, containing 27 wt % of the sulphated branched ether surfactant composition, 46 wt % of builder (zeolite-4A), and 27 wt % of sodium carbonate.

The composition of the radiolabelled Multisebum Soil is as follows: Component Label % wt.

Cetane 3H 12.5 Squalane 3H 12. 5 Trisearin 3H 10 Arachis (Peanut) Oil 3H 20 Cholesterol 14C 7 Octadecanol 14C 8.0 Oleic Acid 14C 15.0 Stearic Acid 14C 15.0 A Terg-O-Tometer is used to wash the swatches at 15 minute intervals. The wash conditions are set to measure both cold water detergency at 10°C (50°F) and warm water detergency at 32°C (90°F). The agitation speed is 100 rpm. Once the 4"x 4"radiotracer soiled swatches are washed by the Terg-O-Tometer, they are hand rinsed. The wash and rinse waters are combined for counting to measure sebum soil removal. The swatches are counted to measure clay removal.

For details concerning the detergency methods and radiotracer techniques, reference may be had to B. E.

Gordon, H. Roddewig and W. T. Shebs, HAOCS, 44: 289 (1967), W. T. Shebs and B. E. Gordon, JAOCS, 45: 377 (1968), and W. T. Shebs, Radioisotope Techniques in Detergency, Chapter 3, Marcel Dekker, New York (1987).

The sulphates of the branched ether surfactant compositions of the present invention are also biodegradable. The biodegradation testing methods for measuring the biodegradability of the sulphates can be conducted in accordance with the test methods established in 40 CFR §796. 3200, also known as the OECD 301D test method. By a biodegradable composition or surfactant is meant that that the compound or composition gives a measured biochemical oxygen demand (BOD) of 60% or more within 28 days, and this level must be reached within 10 days of biodegradation exceeding 10 percent.

The Krafft point can be measured by preparing 650 ml of a 0.1% dispersion of glycasuccinimide in water by weight. If the surfactant was soluble at room temperature, the solution was slowly cooled to 0° C. If the surfactant did not precipitate out of solution, its Krafft point was considered to be < 0° C (less than zero). If the surfactant precipitated out of solution, the temperature at which precipitation occurs was taken as the Krafft point.

If the surfactant was insoluble at room temperature, the dispersion was slowly heated until the solution became homogeneous. It was then slowly cooled until precipitation occurred. The temperature at which the surfactant precipitates out of solution upon cooling was taken as the Krafft point.

DETERGENT COMPOSITIONS The sulphated branched primary alcohol or alcohol alkoxysulphate compositions of the present invention find particular use in detergents, specifically laundry detergents. The alkoxylated branched primary alcohol composition of the present invention also find particular use in detergents, specifically dishwashing detergents.

Particularly, these alkoxylated branched primary alcohol compositions of the present invention have low odour compared with conventional detergent range alkoxylated alcohol compositions currently available commercially. A biodegradable detergent composition can be prepared using the branched ether derivative compositions of the present invention.

The detergent compositions are generally comprised of a number of components, besides the sulphated primary alcohol, alcohol alkoxylsulphate, or alkoxylated branched primary alcohol composition of the present invention.

The detergent composition may include: other surfactants of the ionic, nonionic, amphoteric or cationic type; builders (phosphates, zeolites), and optionally cobuilders (polycarboxylates); bleaching agents and their activators; foam controlling agents; enzymes; anti- greying agents; optical brighteners; and stabilisers.

Such additional detergent components useful for the present invention are described in detail in US-A-6087311; US-A-6083893; US-A-6159920; US-A-6153574; WO-A-9405761; and GB-A-1429143.

The following Examples are provided to further illustrate certain specific aspects of the present invention but are not intended to limit its broader scope.

Example 1: A reaction of 1-dodecene with 1,3-propanediol using a homogeneous acid catalyst, p-toluene sulphonic acid, to manufacture the surfactant of the present invention is provided.

To a 500 ml round bottom flask equipped with an overhead stirrer, condenser and N2 inlet system was added 100 grams (0.6 moles) of 1-dodecene (acquired from Aldrich Chemical Company) and 137 grams (1.8 moles) of 1,3-propanediol (obtained from Shell Chemical Company) and 4.56 grams (0.024 moles) of toluene sulphonic acid monohydrate. The mixture was heated to 150°C for four hours at which time the reaction mixture was cooled to room temperature.

The reaction mixture consisted of two phases at room temperature. The two phases were separated by a separatory funnel. Each phase was analysed by gas chromatography. 130g of liquid were recovered in the top phase, and 107g of liquid were recovered in the bottom phase. Analysis of the top phase indicated the formation of 24% wt of 3-dodecyloxy-1-propanol product, 72% wt unreacted dodecenes, 2% wt dodecene dimers and 2% wt 1,3- propanediol, didocecyl ether, based on the weight of the top phase liquid. There was less than 1% wt 1,3-

propanediol or 1,3-propane diol oligomers in the top phase, indicating good phase separation. Analysis of the bottom phase indicated 94% wt unreacted 1,3-propanediol with about 6wt% linear dimer of the propanediol, based on the weight of the bottom phase liquid. There was less than 1% wt dodecene or other dodecyl based adducts in the bottom phase, further confirming good phase separation between the product and unreacted olefin in the upper phase and the propanediol and dimers thereof in the lower phase.

Removal of the unreacted dodecenes in the upper phase by distillation afforded 29.5 grams of a mixture of isomers of 3-dodecyleneoxy-1-propanol. Selectivity to the 3-dodecyloxy-1-propanol product was 97%.

Example 2: The reaction in example 1 was repeated using a lower quantity of 1,3-propanediol, and by adding the 1,3- propanediol to the 1-dodecene slowly during the reaction.

To a 500 ml round bottom flask equipped with an overhead stirrer, condenser and N2 inlet system was added 168 grams (1.0 mole) of 1-dodecene (acquired from Aldrich Chemical Company) and 2.25 grams (0. 01 moles) of toluene sulphonic acid monohydrate. The mixture was heated to 150 C at which time 23 grams (0.3 moles) of 1,3- propanediol (obtained from Shell Chemical Company) was added slowly at the rate of 10 grams per hour. The reaction was stirred for an additional hour after the 1,3-propanediol had been added. The reaction mixture was cooled to room temperature.

The reaction mixture consisted of two discrete phases at room temperature. Dodecene was removed from the upper phase via distillation affording 15 grams of a

clear oil. Analysis of this product mixture by gas chromatography indicated the formation of 74% wt 3- dodecyloxy-1-propanol, 24% wt of 1,3-propanediol, didodecyl ether and 2% wt dodecene dimer. Analysis of the bottom layer showed 98% wt unreacted 1,3-propanediol and 2% wt linear dimer of 1,3-propanediol (3- hydroxypropyleneoxy-1-propanol).

Example 3: Addition of 1,3-propanediol to 1-dodecene is provided using another homogeneous catalyst, trifluoromethanesulphonic acid, as catalyst.

The reaction in example 2 was repeated using 1 gram (0.0067 moles) of trifluoromethanesulphonic acid as catalyst instead of p-toluenesulphonic acid. The reaction mixture was cooled to room temperature. The reaction mixture consisted of two phases. Dodecene was removed from the upper phase via distillation affording 23 grams of a clear oil. Analysis of this product mixture by gas chromatography indicated the formation of 69% w 3-dodecyloxy-1-propanol, 22% w of 1,3-propanediol, didodecyl ether and 9% w dodecene dimer. Analysis of the bottom layer showed 93% w unreacted 1,3-propanediol and 7% w linear dimer of 1,3-propanediol (3- hydroxypropyleneoxy-1-propanol).

Example 4: Reaction of 1-dodecene with 1,3-propanediol is provided using a heterogeneous catalyst, beta H+ zeolite as catalyst.

To a 500 ml round bottom with an overhead stirrer, condenser and N2 inlet system was added 100 grams (0.6 moles) of 1-dodecene (acquired from Aldrich Chemical Company) and 137 grams (1.8 moles) of 1,3-propanediol

(obtained from Shell Chemical Company) and 10 grams of beta zeolite powder, H+ form (obtained from Zeolyst Corporation). The mixture was heated to 150°C for two hours at which time the reaction mixture was cooled to room temperature.

The reaction mixture consisted of two phases, with the powdered zeolite catalyst suspended in the bottom phase. The reaction mixture was diluted with 250 ml of heptane and 250 ml of distilled water, mixed well and the two phases separated using a separatory funnel. The top phase was isolated, and the heptane was removed by rotary evaporation affording 23.2 grams of clear oil.

Analysis of this product indicated the formation of 94% wt 3-dodecyloxy-1-propanol, 4% wt 3-dodecyoxypropyloxy- 1-propanol and 2% w dodecene dimers. C13 NMR analysis indicated that the 3-dodecyloxy-1-propanol was a mixture of isomers with 95% wt of the hydroxypropyl group attached at the 2-carbon position (relative to the alpha carbon atoms) of the dodecyl moiety to produce a methyl branched product (I1) and 5% wt of the hydroxypropyl group attached at the 3-carbon position to produce an ethyl branched product (12). There was <1% w of attachment at the 4 (I3) and the higher carbon positions. The isomers have the following structural formulae, respectively:

Example 5: Reaction of NEODENE 14 Olefin (NEODENE is a trademark of Shell group of companies) with 1,3- propanediol, using beta H+ zeolite as catalyst, is provided. /+ HOOH belite CH3 CH3 The reaction of Example 4 was repeated except that 118 grams (0.6 moles) of NEODENE 14 Olefin (1-tetradecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin. After the reaction mixture was cooled to room temperature, there resulted two discrete phases, each of which was analysed by gas chromatography. The upper phase indicated the formation

of 70% w unreacted tetradecenes, 27% w of isomers of 3- tetradecyloxy-l-propanol,-3% w of the 3- tetradecyloxypropyloxy-1-propanol. Analysis of the bottom phase showed 94% w unreacted 1,3-propanediol, 5% w hydroxypropyloxy-1-propanol and a trace of higher trimer of 1,3-propanediol (i. e. oligomer).

Example 6: Reaction of NEODENE 16 Olefin with 1,3-propanediol, using beta Zeolite as catalyst, is provided. + HO"'OH beta H+ CH3 CHs The reaction of Example 4 was repeated except that 135 grams (0.6 moles) of 16 Olefin (1-hexadecene obtained from Shell Chemical Company) was used in place of 1- dodecene as the olefin. After the reaction mixture was cooled to room temperature, both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation of 72% w hexadecenes, 25% w of isomers of 3-hexadecyloxy-l-propanol,-3 %w of the 3- hexadecyloxypropyloxy-1-propanol. Analysis of the bottom phase showed 96% w unreacted 1,3-propanediol, 4% w hydroxypropyloxy-1-propanol and a trace of higher trimer of 1,3-propanediol (i. e. oligomer).

Example 7: Reaction of NEODENE 12 Olefin with 1,3-propanediol using another heterogeneous catalyst, CBV-500 Zeolite, as the catalyst is provided.

The reaction of Example 4 was repeated except that 100 grams (0.6 moles) of NEODENE @ 12 Olefin (1-dodecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin and 10 grams of CBV-500 zeolite as catalyst. CBV-500 zeolite is a Y-type zeolite obtained from Zeolyst International. After about 3.5 hours of reaction time, the reaction mixture was cooled to room temperature, and both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation of 90% w unreacted dodecenes, 9% w of isomers of 3-dodecyloxy-1-propanol product, and trace amounts of the 3-dodecyloxypropyloxy- 1-propanol. Analysis of the bottom phase showed 98% w unreacted 1,3-propanediol and 2% w 3-hydroxypropyloxy-1- propanol.

Example 8: A reaction of NEODENE 12 Olefin with 1,3-propanediol using another heterogeneous catalyst, CBV-780 Zeolite, as catalyst is provided.

The reaction of Example 4 was repeated except that 100 grams (0.6 moles) of NEODENE 12 Olefin (1-dodecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin and 10 grams of CBV-780 Zeolite as catalyst. This catalyst is a modified Y-type zeolite obtained Zeolyst International. After the reaction mixture was cooled to room temperature, both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation

of 90% w dodecenes, 9% w of isomers of 3-dodecyloxy-1- propanol product, and trace amounts of the 3- dodecyloxypropyloxy-1-propanol. Analysis of the bottom phase showed 98% w unreacted 1,3-propanediol and 2% w 3- hydroxypropyloxy-1-propanol.

Example 9: A reaction of NEODENE 12 Olefin with 1,3-propanediol using another heterogeneous catalyst, CBV-740 Zeolite, as catalyst is provided.

The reaction of Example 4 was repeated except that 100 grams (0.6 moles) of NEODENE 12 Olefin (1-dodecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin and 10 grams of CBV-740 Zeolite as catalyst. CBV-740 zeolite is a modified Y- zeolite obtained from Zeolyst International. After the reaction mixture was cooled to room temperature, both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation of 91% w dodecenes, 8% w of isomers of 3-dodecyloxy-1- propanol product, and trace amounts of the 3- dodecyloxypropyloxy-1-propanol. Analysis of the bottom phase showed 98% w unreacted 1,3-propanediol and 2% w 3- hydroxypropyloxy-1-propanol.

Example 10: A reaction of NEODENE 12 Olefin with 1,3-propanediol using another heterogeneous catalyst, 13X Molecular Sieve, as catalyst is provided.

The reaction of Example 4 was repeated except that 100 grams (0.6 moles) of NEODENE 12 Olefin (1-dodecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin and 10 grams of 13X Molecular Sieve obtained from PQ Corporation as catalyst. After

the reaction mixture was cooled to room temperature, both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation of 82% w dodecenes, 16% w of isomers of 3-dodecyloxy-1- propanol product, and 2% w of the 3-dodecyloxypropyloxy-1- propanol. Analysis of the bottom phase showed 96% w unreacted 1,3-propanediol and 4% w 3-hydroxypropyloxy-1- propanol.

Example 11: A reaction of NEODENE 12 Olefin with 1,3-propanediol using another heterogeneous catalyst, a H+ Y Zeolite, as catalyst is provided.

The reaction of Example 4 was repeated except that 100 grams (0.6 moles) of NEODENE @ 12 Olefin (1-dodecene obtained from Shell Chemical Company) was used in place of 1-dodecene as the olefin and 10 grams of H+ Y Zeolite prepared by treatment of a Na-Y Zeolite (CBV-100 obtained from Zeolyst International) with ammonium nitrate followed by calcination at 500°C in air for 8 hours was used as the catalyst. After the reaction mixture was cooled to room temperature, both phases from the product mixture were analysed by gas chromatography. The upper phase indicated the formation of 94% w dodecenes and 6% w of isomers of 3-dodecyloxy-1-propanol product. No appreciable 3-dodecyloxypropyloxy-1-propanol was observed. Analysis of the bottom phase showed 96% w unreacted 1,3-propanediol and 4% w 3-hydroxypropyloxy-1- propanol.

Example 12: A reaction of C15/C16 internal olefins with 1,3- propanediol (PDO) using a homogeneous catalyst, p- toluenesulphonic acid, is provided.

To a 500 ml Zipperclave autoclave was added 44 grams (0.2 moles) of a mixture of C15/C16 internal olefins obtained from Shell Chemical Company, 76 grams (1 mole) of 1,3-propanediol (acquired from Shell Chemical Company) and 0.38 grams (0.002 moles) of p-toluene sulphonic acid in 100 ml of tetrahydrofuran. The autoclave system was placed under N2 atmosphere after removal of air by repeated pressurisation and depressurisation with N2. Then the pressure of the Zipperclave was adjusted to 345 kPa g (50 psig) N2. The reaction was heated to 100°C for 18 hours. The reaction was cooled to 25°C. The tetrahydrofuran solvent was removed by rotary evaporation producing two phases. The two phases were separated by separatory funnel.

Each phase was analysed by gas chromatography. The upper phase indicated the formation of about 6% wt of the 1,3-propanediol adduct of the mixture of C15/C16 olefins.

The balance was isomerised C15/C16 olefins. The lower phase consisted of 98% wt 1,3-propanediol and 2% wt 3- hydroxypropyl-1-propanol.

Example 13: A reaction of C15/C16 internal olefins with PDO using p-toluenesulphonic acid as catalyst.

Example 12 was repeated except that 88 grams (0.4 moles) of a mixture of an internal C15/C16 olefin mixture obtained from Shell Chemical Company and 100 ml of dimethoxyethane was used as solvent. After the reaction was cooled to 25 C. the dimethoxyethane solvent was removed by rotary evaporation producing two phases. The phases were separated by separatory funnel. Each phase was analysed by gas chromatography. The upper phase indicated the formation of-8% w of the 1,3-propanediol

adduct of the mixture of C15/C16 olefins. The balance was isomerised C15/C16 olefins. The lower phase consisted of 98% w 1,3-propanedioll and 2% w 3- hydroxypropyl-1-propanol.

Example 14: A reaction of isomerised C15/C16 Olefins obtained from Shell Chemical Company with PDO using a homogeneous catalyst, trifluoromethane sulphonic acid is provided.

Example 13 was repeated except 0.3 grams (0.002 moles) of trifluoromethanesulphonic acid was used as catalyst. After the reaction was cooled to 25 C. The dimethoxyethane solvent was removed by rotary evaporation producing two phases. Each phase was analysed by gas chromatography. The upper phase indicated the formation ouf-low of the 1,3-propanediol adduct of the mixture of C15/C16 olefins and 2% w of the hydroxypropoxypropyloxy adduct of the mixture of C15/C16 olefins. The balance was isomerised C15/C16 olefins. The lower phase consisted of 98% w 1,3-propanediol and 2% w 3- hydroxypropyl-1-propanol.

Example 15: A reaction of 1-Dodecene with 1,3-propanediol using p-toluenesulphonic acid as catalyst and dimethoxyethane as solvent is provided.

To a 500 ml Zipperclave autoclave was added 67.2 grams (0.4 moles) of 1-dodecene [acquired from Aldrich Chemical Company], 76 grams (1 mole) of 1,3-propanediol [acquired from Shell Chemical Company] and 0.38 grams (0.002 moles) of p-toluene sulphonic acid in 100 ml of dimethoxyethane. The autoclave system was placed under N2 atmosphere after removal of air by repeated pressurisation and depressurisation with N2. Then the

pressure of the Zipperclave was adjusted to 345 kPa g (50 psig) N2. The reaction was heated to 150°C for 3 hours.

The reaction was cooled to 25°C The dimethoxyethane solvent was removed by rotary evaporation producing two phases. Each phase was analysed by gas chromatography.

The upper phase indicated the formation of-11% w of 3- dodecyloxy-1-propanol and 89% w mixed dodecenes. The lower phase consisted of 97% w 1,3-propanediol and 3% w 3- hydroxypropyl-1-propanol.

Example 16: A reaction of 1-Dodecene with 1,3-propanediol using trifluoromethanesulphonic acid as catalyst and dimethoxyethane solvent is provided.

Example 14 was repeated using 0.3 grams (0.002 moles) of trifluoromethanesulphonic acid as catalyst.

The reaction was cooled to 25°C. The dimethoxyethane solvent was removed by rotary evaporation producing two phases. The dodecene was removed from the upper phase by distillation affording 2.3 grams of clear oil. Analysis indicated this product to be 3-dodecyloxy-1-propanol.

Example 17: A reaction of 1-Dodecene with 1,3-propanediol using trifluoromethanesulphonic acid as catalyst without a solvent is provided.

Example 14 was repeated using 0.3 grams (0.002 moles) of trifluoromethanesulphonic acid as catalyst but no solvent. The reaction was cooled to 25°C, producing two phases. The dodecene was removed from the upper phase by distillation affording 9.4 grams of clear oil.

Analysis indicated this product to be 3-dodecyloxy-1- propanol.

Example 18: A Reaction of NEODENE 12 Olefin with PDO using a heterogeneous catalyst, CBV-500 Zeolite, as catalyst is provided.

To a 500 ml round bottom flask equipped with an overhead stirrer, condenser and N2 inlet system was added 100 grams (0.6 moles) of NEODENE 12 Olefin (obtained from Shell Chemical Company) and 137 grams (1.8 moles) of 1,3- propanediol (obtained from Shell Chemical Company) and 10 grams of CBV-500 Zeolite, a Y zeolite obtained from Zeolyst International. The mixture was heated to 150°C for two hours at which time the reaction mixture was cooled to room temperature. The reaction mixture consisted of two phases and each phase was analysed by gas chromatography. Analysis of the top phase indicated the formation of 4% w of 3-dodecyloxy-1-propanol and 96% w mixed dodecenes. Analysis of the bottom phase indicated 99owt unreacted 1,3-propanediol with-1% wt linear dimer.

Example 19: A reaction of NEODENE 12 Olefin with PDO using another heterogeneous catalyst, CBV-712 Zeolite, is provided.

Example 18 was repeated using 10 grams of CBV-712 Zeolite as catalyst. CBV-712 zeolite is a modified Y- zeolite obtained from Zeolyst International. Analysis of the top phase indicated the formation of 3% w of 3- dodecyloxy-1-propanol and 97% w mixed dodecenes. Analysis of the bottom phase indicated 99% wt unreacted 1,3- propanediol with-1% wt linear dimer Example 20: Experiments were conducted using a fixed bed reactor system consisting of a 20mm x 220 mm 316 stainless steel

tubular reactor which was fitted with a thermowell transversing the centre of the tube and containing three temperature control/indicator thermocouples at the top, middle and bottom of the reactor. The tube was filled with 20 ml of CP861E beta zeolite extrudate obtained from Zeolyst International which had been calcined at 500° C for 6 hours. The catalyst system was purged with N2.

NEODENE 12 Olefin and 1,3-propanediol were pumped separately to the reactor system at 20ml/hr each initially at 25 °C and 1 atmosphere of N2. The reactor system was heated to 150° C and pumping continued for 8 hours. The product mixture separated into two clear, colourless phases at 25° C and was analysed by gas chromatography. Analysis of the upper phase showed the formation of 21% w 3-(2-methylundecyloxy)-1-propanol, 4% w 3- (2-ethyldecyloxy)-1-propanol and-1% dodecene dimers.

The remainder was a mixture of dodecenes. The lower phase contained 94% w unreacted 1,3-propanediol and 6% w linear dimer of PDO.

Example 21 A larger scale reaction of NEODENE 12 Olefin with PDO Using beta H+ Zeolite Catalyst is provided.

A total of 2352 grams (14 moles) of NEODENE 12 Olefin obtained from Shell Chemical Company, 3192 grams (42 moles) of 1,3-propanediol and 200 grams of beta H+ Zeolite obtained from Zeolyst International were added to a 12 litre resin vessel fitted with overhead stirrer, thermowell, condenser and N2 gas inlet/outlet system.

The mixture was mixed well and heated to 150° C for 5 hours. The reaction mixture was cooled to 25°C, resulting in the formation of two phases. The two phases were separated by separatory funnel. Each phase was

analysed by gas chromatography. Analysis of the top phase indicated the formation of 25.2% w of the 1-PDO adduct of NEODENE 12 Olefin, 2.0 % w of the linear di-PDO adduct of NEODENE 12 Olefin, 4.4% w dodecene dimers and 68.4% w isomerised dodecenes. Analysis of the bottom phase indicated 90% w unreacted 1,3-propanediol, and 10% w linear di-PDO dimer. Distillation of the dodecenes from the upper phase afforded 858 grams of a clear, fluid liquid. Analysis of this material by C13 NMR indicated the formation of 94% of the 1-PDO adduct of NEODENE 12 Olefin (of which 95% w was 3-(2-methylundecyloxy)-1- propanol and 5% w was 3- (3-ethyldecyloxy)-l-propanol) and 6% w was the linear PDO dimer (or PDO-2) adduct of NEODENE 12 Olefin.

Example A-C Examples of sulphated products derived from Cl2, C14, and C16 branched primary alcohols, prepared in a manner similar to Example 6, respectively Examples A, B, and C, were produced according to the following method.

0.666 moles of the respective branched primary alcohol were dissolved in 300 mls of methylene chloride in a 500 ml multineck round bottom flask equipped with an addition funnel and stirring bar. The reaction mixture was cooled to 0°C. 0.7 moles of chlorosulphonic acid was transferred to the addition funnel and added dropwise over a 15 minute period. The product was neutralised by pouring the reaction mixture into a well stirred aqueous solution of 0.7 moles of sodium hydroxide dissolved in approximately 800 mls of distilled water. The methylene chloride was removed from the mixture by reduced pressure. This produced an approximately 25 weight percent active solution of the desired sulphated products

of the branched primary alcohols. The products were all clear fluid pale yellow liquids. Example A is Cl2- PDOS. Example B is C14-1 PDOS and Example C is Cl6- PDOS.

For comparison, the properties of a primary alcohol sulphate produced by sulphation of NEODOL 23 Alcohol (mixture of C12 and C13 having typical hydroxyl number of 289 mg/gKOH) in a similar manner to those above obtained from Shell Chemical Co. and Witconate 1260, a 60% aqueous solution of Cl2 linear alkyl sulphate (Cl2 LAS) from Witco Corp. are provided.

RELATIVE STRENGTHS Physical Property C 12 N23-S C12-1 C14-1 C16-1 Attributes LAS PDOS PDOS PDOS Solubility °C (+) (-) (+) (+) (-) Critical Micelle Conc. (-) (-) (+) (+) (++) (CMC)@25°C Hardness Tolerance (-) (-) (+++) (++) (+) Ca +'- Interfacial Tension (++) (++) (-) (-) (+) 4/1 Cetane/oleic acid InterfacialTension (+) (+) (-) (-) (+) Hexadecane Other IFT in (-) None (+) (+) (+) Seawater 4/1 above Solubility in (-) (-) (+) (+) (-) Seawater

ACTUAL VALUES Physical Property C 12 N23-S C12-1 C14-1 C16-1 Attributes LAS PDOS PDOS PDOS Solubility °C 0 29 0 0 22 Krafft 1. 0% Solution Critical Micelle Conc. 0.070 0.140 0.062 0.029 0.0063 (CMC) 25°C Wt % Wt % Wt % Wt % Wt % Surface Tension 34 25 28 30 33 (Dynes/Cm.) @ CMC Foam Rate (cc/min) 110 100 100 133 102 Foaming Stability * 14 20 10 14 16 Hardness Tolerance 140 18 > 120, 000 30,200 1,800 Ca ++ PPM PPM ppm ppm Interfacial Tension 0.5 0.5 5.3 2.5 1.4 4/1 Cetane/oleic acid Interfacial Tension 6.4 5.7 13.6 9.3 6.3 HexadecaneI Other IFT in 0.5 None 0.12 0.11 0.17 Seawater 4/1 above Solubility in Cloudy Cloudy Clear Clear Cloudy Seawater X Ppt. Ppt. Ppt.

* Centimetre of foam remaining after 20 minutes in DI water @ 25 °C and 0 ppm hardness.

Average Dynes/Centimetre in 0.1 % solution at 25°C over more than one hour. m Seawater is 3.589 % synthetic salt that contains every major, minor and trace element found in original seawater. Parts per million concentration, ppm, is 35,890ppm.

Example D-F Examples of ethoxylated products derived from Cl2, C14 and C16 branched primary alcohols, prepared in a manner similar to Example 6, respectively Examples D, E, and F, were produced according to the following method.

7 moles of Ethylene oxide was introduced into a pressure reactor containing 1 mole of the respective branched primary alcohol reactant and KOH as catalyst at a partial pressure of 207 kPa g (30 psig) and diluted with Nitrogen gas to a total pressure of 414 kPa g (60 psig). The reaction was carried out at a temperature of 160°C for a period of 2 hours. The ethylene oxide- alcohol adduct produced had an average 7 EO repeating units.

For comparison, the properties of an alcohol ethoxylate having an average of 7 ethoxylate repeat units prepared by ethoxylation of NEODOL 25 alcohol obtained from Shell Chemical Co. is provided.

Cloud point and phase behaviour were measured as follows: A temperature scan is normally completed on a 1% solution of a nonionic alcohol ethoxylate to first determine the exact cloud point and secondly to determine the other phases that are inherent to the alcohol ethoxylate. This is accomplished by use of the dipping probe instrument, which measures the turbidity change in the ethoxylate as the temperature is increased from room temperature to 90°C. Each surfactant will have its own unique trace or"fingerprint"as the changes of temperature and turbidity are recorded and noted.

The solubilisation rates of hexadecane and 4/1 hexadecane/oleic acid into 1% solutions were measured at 25°C using the dipping probe colorimeter system.

Hexadecane models a nonpolar lubricating oil while 4/1 hexadecane/oleic acid models a polar sebum-like soil.

The rates were calculated by measuring the time required for 10y1 samples of oil to completely dissolve into the well-stirred solution as indicated by the disappearance of turbidity. The results for 4/1 hexadecane/oleic acid are given as an average value for five sequential injections while the data for hexadecane are based on a single injection.

As shown in the data table, the 7-EO PDO adduct provided faster solubilisation on average than the commercial 7-EO ethoxylate having the same cloud point temperature. This result was true for both the nonpolar hexadecane oil as well as the nonpolar/polar oil blend containing oleic acid. Rapid solubilisation of oil is indicative of good-cleaning surfactant systems that provide enhanced removal rates of oily soils from various solid substrates.

ACTUAL VALUES Physical Property N25-7 C12-1 C14-1 C16-1 PDO Attributes PDO 7EO PDO 7EO 7EO Cloud Point UP (°C) 52.6 53.6 47 42.7 DOWN (°C) 53.4 53.7 47.7 43 AVERAGE (°C) 53.0 53. 7 47.4 42.9 L a Phase (°C range) 91-86 72.6-79 71-82 Short @ 70 L Phase (°C range)-83-85. 9 86.5-88.4-80 L2 Phase (°C range) - - - double cloud Solubilisation* (µL/ minute) 4/1 Hexadecane/oleic acid 10 » L 50.0 200.0 26.7 0.2 10µL 40.0 66.7 20.0 0.2 10µL 28.6 40.0 20.0 None 10itL 28.6 28.6 33.3 None 10µL 20.0 20.0 11.4 None average 33.4 71.1 22.3 0.2 Hexadecane 10µL 0.083 0. 333 0.089 0.064 10yL None None None None 10L None None None None * 25°C Solubility Solubility Key Result Time, Seconds Min. 100 0. 1 6 50 0. 2 12 5 2 120 0.5 20 1200 0.05 200 12000