EP0402112B1

EP0402112B1 - Formation of discrete, high active detergent granules using a continuous neutralization system

Info

Publication number: EP0402112B1
Application number: EP90306139A
Authority: EP
Inventors: Frank Joseph Mueller; Lester John Hollihan
Original assignee: Procter and Gamble Co
Current assignee: Procter and Gamble Co
Priority date: 1989-06-09
Filing date: 1990-06-06
Publication date: 1996-08-14
Anticipated expiration: 2010-06-06
Also published as: CN1048408A; AU5696590A; EP0402112A2; IE902074L; MX171874B; MA21868A1; ES2090102T3; TR26363A; NZ234000A; FI902874A0; CA2017922A1; EP0402112A3; BR9002720A; AR242985A1; DE69028043D1; JPH0372600A; PT94312A; CN1026596C; DE69028043T2; KR910001028A

Description

FIELD OF THE INVENTION

The present invention relates to a process for making discrete, high active detergent particles, and to detergent particles made by this process. More particularly, this process comprises the following steps:

(a) reacting alkyl sulfuric and/or alkyl benzene sulfonic acids with an alkali metal hydroxide solution (greater than or equal to 62 wt.% hydroxide) in a continuous neutralization system;
(b) adding polyethylene glycol of molecular weight 4,000 to 50,000 and/or certain ethoxylated nonionic surfactants during neutralization; and
(c) forming detergent particles.

BACKGROUND INFORMATION

There is currently interest in the detergent industry in concentrated detergent products. These products provide advantages to the consumer, who has a product which can be used in lower amounts and is more easily stored, and to the producer and intermediates, who have lower transportation and warehousing costs. A major difficulty, though, is finding an inexpensive and efficient way to produce a high active detergent particle for inclusion in a concentrated detergent product. By "high active" is meant greater than 50% active.
The traditional method for producing detergent granules is spray drying. Typically, detergent ingredients such as surfactant, builder, silicates and carbonates are mixed in a mix tank to form a slurry which is 35% to 50% water. This slurry is then atomized in a spray drying tower to reduce moisture to below 10%. It is possible to compact spray dried particles to make dense detergent granules. See U.S. Patent 4,715,979, Moore et al., issued December 29, 1987. However, the use of spray drying to make condensed granules has some disadvantages. Spray drying is energy intensive and the resulting granules are typically not dense enough to be useful in a concentrated detergent product. Spray drying methods generally involve a limited amount (less than 40%) of organic components such as surfactant for environmental and safety reasons.
One way to reduce the energy required to spray dry detergent granules is to reduce the moisture in the slurry which is atomized in the spray drying tower, i.e., by reducing the evaporative load. An alternative method for making a high active detergent particle is by continuous neutralization in, for example, a continuous neutralization loop. There are continuous neutralization loops available to which relatively concentrated caustic can be added. Using a caustic solution which is about 50% sodium hydroxide allows reduction of moisture in the resulting neutralized surfactant paste to about 16% water. However, caustic of greater than 50% solids cannot easily be added to existing continuous neutralization systems because the systems cannot reliably accommodate the viscous surfactant paste nor are the systems designed to accomodate the high temperatures necessary to handle concentrated caustic solutions. It has heretofore not been practical to use a continuous neutralization system to attain moisture levels below 12% in the paste so that free-flowing, high active detergent granules can be made from the paste without drying.
The following publications describe ways to make free-flowing high active particles without drying, using surfactant paste, and made with a continuous neutralization system.
Japanese Patent 61-118500, Hara et al., laid-open June 5, 1986, discloses a method for the manufacture of concentrated detergent compositions characterized by kneading the materials of the detergent composition continuously, and feeding these materials, which contain at least 30% by weight of surfactant, into an airtight-type kneader with a controlled pressure of 0.01-5 kg/cm²G.
Japanese Patent 60-072999, Satsusa et al., laid open April 25, 1985, discloses a production method for a highly concentrated powder detergent where sulfonate and/or sulfate is mixed with sodium carbonate and water in a high shear mixer, cooled below 40°C, and then pulverized with a zeolite powder and other detergent components.
U.S. Patent 4,515,707, Brooks, issued May 7, 1985 discloses anhydrous fatty alcohol sulfuric acid or ethoxylated fatty alcohol sulfuric acid which is neutralized with dry sodium carbonate powder in the presence of powdered sodium tripolyphosphate in a high shear mixer. The dry, powdered, neutralized reaction product is stored until required for use in the manufacture of a detergent bar.
U.S. Patent 4,162,994, Kowalchuk, issued July 31, 1979 discloses a non-spray dried, built laundry detergent composition comprising the calcium salt of a non-soap, organic anionic surfactant, an ethoxylated alcohol nonionic surfactant, an alkali-metal salt of a certain builder, and, optionally, calcium carbonate.
European Patent 266847-A discloses production of an organic acid containing pliable, pasty detergent composition comprising dry mixing a linear alkyl benzene sulphonic acid with sodium carbonate, neutralizing the mixture with caustic solution to form a pasty mass, and blending with active organic acid and filler. It is claimed that these compositions are useful for incorporation into multiple use scrubbing pads for bathroom use, etc., for removing soap scum and lime scale.
The use of polyethylene glycol and ethoxylated nonionic surfactants in granular detergent compositions is known in the art. For example, Japanese Patent 61-231099, Sai et al., laid-open October 15, 1986, discloses concentrated powdered detergents containing (a) anionic surfactant, (b) polycarboxylic acid polymer or their salts, (c) polyethylene glycol, in certain percentages and weight ratios. The detergent also contains 0-10% by weight of a water-soluble neutral inorganic salt.
Japanese Patent 62-263299, Nagai et al., laid-open November 16, 1987, discloses a method for the preparation of granular nonionic detergent composition by first kneading and mixing 20-50 weight % of nonionic surfactant at a temperature not above 40°C, and 50-80 weight % of a mixture of zeolite, and lightweight sodium carbonate in a specified ratio, followed by granulation.
U.S. Patent 4,639,326, Czempik et al., issued January 27, 1987 discloses a process for the preparation of a nonionic surfactant containing powdered detergent composition including spraying onto a spray-dried base powder further nonionic.
U.S. Patent 3,838,072, Smith et al., patented September 24, 1974 discloses particulate detergent compositions made by a process including spraying over the surfaces of spray-dried base particles, while in motion, from about 2 to 20%, by weight of the detergent composition, of droplets of a nonionic compound.
The following patents describe processes and/or surfactant compositions comprising viscosity modifiers such as polyethylene glycol and ethoxylated (E_20-60) alkyl (C_6-12) phenol.
U.S. Patent 4,482,470, Reuter et al., issued November 13, 1984 discloses a process for reducing the viscosity of aqueous concentrates of anionic surfactants by adding a small quantity of a compound containing polyglycol ether groups; and the aqueous concentrates prepared thereby. Example 5 describes the addition of polyethylene glycol of molecular weight 2,000 to an alkyl benzene sulfonate paste with 59 weight % active ingredients to modify viscosity. The aqueous anionic surfactant concentrate has a viscosity of 10,000 mPas or less at a temperature in the range of 50° to 90°C. From about 0.1 to about 10%, by weight of the concentrate, of viscosity modifier is added to the anionic surfactant component. Polyethylene glycol having a molecular weight of from about 600 to about 6,000 and ethoxylated (E_20-80) alkyl (C_6-12) are named as viscosity modifiers.
U.S. Patent 4,495,092, Schmid et al., issued January 22, 1985 discloses the addition of C_8-40 alcohols, or C_8-40 alcohols containing one or more hydroxyl groups and 20 moles of ethylene oxide and/or propylene oxide, to aqueous industrial anionic surfactants in order to significantly improve the rheological behavior thereof. The alcohols are apparently added in quantities of from about 1 to about 15% by weight, based on the quantity of surfactant, whereupon the viscosity of the surfactant concentrate becomes at most 10,000 mPas at 70°C.
U.S. Patent 4,532,076, Schmid et al., issued July 30, 1985 discloses an aqueous anionic surfactant concentrate with certain low molecular weight organic compounds as viscosity regulators, and a method of regulating the viscosity of highly viscous concentrates. The viscosity regulators are selected from:

(a) certain C_1-6 alkyl monocarboxylic acids,
b) certain C_1-6 alkylene acid dicarboxylic acids,
(c) nitrilotriacetic acid and its salts,
(d) certain ether alcohols,
(e) and mixtures thereof.

U.S. Patent 4,675,128, Linde et al., issued June 23, 1987 discloses certain alkali metal alkane sulfonates which are used as viscosity regulators for aqueous anionic surfactant concentrates. The viscosity regulators are apparently used in quantities of from 0.5 to 10% by weight, based on the surfactant content, so that the concentrates have a viscosity at 40°C of at most 10,000 mpas.
U.S. Patent 4,772,426, Koch et al., issued September 20, 1987 discloses an ester sulfonate-containing liquid surfactant concentrate comprising:

(a) about 50-70 weight % of one or more surfactants selected from the group consisting of (i) alkali metal salts of α-sulfonated fatty acid alkyl esters of C₁₆ and/or C₁₈ fatty acids and alcohols containing from 1 to 8 carbon atoms in the alkyl group and (ii) linear aliphatic fatty alcohol polyglycol ethers containing from 10 to 20 carbon atoms in the alkyl group of the alcohol and from 3 to 15 ethoxy groups in the molecule, the ratio between said surfactant components (i) and (ii) being from 1:0.3 to 1:3;
(b) about 10-30 weight % of one or more saturated and/or unsaturated linear aliphatic C_8-22 carboxylic acid; and
(c) 0 to about 10 weight % water.

None of the above disclose the instant process for making discrete, high active detergent particles from the high active paste made by reacting alkyl sulfuric and/or alkyl benzene sulfonic acids with concentrated caustic in a continuous neutralization system in which polyethylene glycol and/or certain ethoxylated nonionics are added during neutralization in specified proportions.

SUMMARY OF THE INVENTION

The present invention relates to a process for producing high active detergent particles, comprising the steps of:

(a) reacting in a continuous neutralization system C_12-18 alkyl sulfuric acid, or C_10-16 alkyl benzene sulfonic acid, or mixtures thereof with an alkali metal hydroxide solution, which is greater than or equal to 62% by weight of the hydroxide, to produce a neutralized product having less than or equal to 12% by weight of water;
(b) adding to said continuous neutralization system during formation of said neutralized product, polyethylene glycol of a molecular weight between 4,000 and 50,000; ethoxylated nonionic surfactant of the formula R(OC₂H₄)_nOH, wherein R is a C_12-18 alkyl group or a C_8-16 alkyl phenol group and n is from 9 to 80, with a melting point of greater than or equal to (120°F) 48.9°C; or mixtures thereof;
wherein the weight ratio of the additive of step (b) to the product of step (a) is from 1:5 to 1:20; and
(c) forming detergent particles.

DESCRIPTION OF THE INVENTION

This invention includes a process for making firm, high active detergent particles, and detergent particles made by this process. By "high active" is meant more than 50% active. The steps of the process are as follows. I.

I. Addition of Acid and Caustic

The first step of this process is neutralizing in a continuous neutralization system C_12-18 alkyl sulfuric acid, or C_10-16 alkyl benzene sulfonic acid, or mixtures thereof with an alkali metal hydroxide solution, which is greater than or equal to 62% by weight of the hydroxide, to produce a neutralized product having less than or equal to 12% by weight of water.
The C_12-18 alkyl sulfuric acid and C_10-16 alkyl benzene sulfonic acid can be made by any sulfation/sulfonation process, but preferably are sulfonated with S0₃ in air in a falling film reactor. See Synthetic Detergents, 7th ed., A.S. Davidson & B. Milwidsky, John Wiley & Sons, Inc., 1987, pp. 151-168.
C_12-18 alkyl sulfuric acid, and mixtures of it and C_10-16 linear alkyl benzene sulfonic acid, are preferred for use herein. Mixtures of the two are most preferred because of improved dispersibility of detergent particles formed from a paste made with the mixture. The two acids can be added as separate streams to the continuous neutralization system or mixed before addition. Alternatively, pastes made from each separate acid can be mixed after neutralization.
In this process, it is preferred that the final ratio of C_12-18 sodium alkyl sulfate to C_10-16 sodium linear alkyl benzene sulfonate be between 75:25 and 96:4, preferably between 80:20 and 95:5.
An 88:12 ratio of C_14-15 sodium alkyl sulfate to C_12-13 sodium linear alkyl benzene sulfonate is most preferred because the neutralized paste is not unacceptably sticky, yet the particles formed from the paste are dispersible in (60°F) 15.5°C water. Paste made from about 100% alkyl sulfuric acid (including impurities) is in contrast not very dispersible in cool (60°F) 15,5°C water despite its desirable consistency. Paste made from alkyl benzene sulfonic acid alone is soft and sticky and therefore difficult to form into nonsticky, discrete surfactant particles.
C_14-16 alkyl sulfuric acid is preferred for use in step (a) of this process over C_12-18 alkyl sulfuric acid. C_14-15 alkyl sulfuric acid is most preferred.
C_11-14 linear alkyl benzene sulfonic acid is preferred over C_10-16 alkyl benzene sulfonic acid. C_12-13 linear alkyl benzene sulfonic acid is most preferred for use herein.
The alkali metal hydroxide used in step (a) to neutralize the alkyl sulfuric acid and/or alkyl benzene sulfonic acid is greater than or equal to 62%, preferably greater than or equal to 68%, by weight of the hydroxide. This highly concentrated caustic solution melts at a high temperature so the caustic feed system must be carefully maintained at the required temperature to prevent "cold spots". A "cold spot" is any point in the feed system, pumps, metering systems, pipes or valves where the system has reached a temperature below the melting point of the caustic (155°F, or 68.3°C for 70% caustic, for example). Such a "cold spot" can cause crystallization of the caustic and blockage of the feed system. Typically "cold spots" are avoided by hot water jackets, electrical tracing, and electrically heated enclosures.
Sodium hydroxide, preferably 70% solids, is the preferred alkali metal hydroxide.
The neutralized product formed by the acid and caustic is in the form of a molten paste. When 62% active caustic is used, the molten paste ordinarily has about 12% by weight of water. When 70% active caustic is used, the molten paste ordinarily has between 8 and 10% by weight of water. It is most preferred that the alkali metal hydroxide be 70% by weight of hydroxide and that the molten paste be between 8% and 10% by weight water.
The alkali metal hydroxide is preferably present in slight excess of the stoichiometric amount necessary to neutralize the acid. If reserve alkalinity (excess caustic) in the neutralization system exceeds 1.5% M₂O (where M is metal), the paste is difficult to circulate through the continuous neutralization system because of its high viscosity. If reserve alkalinity drops below 0.1%, the alkyl paste may not be stable long term because of hydrolysis. It is therefore preferred that reserve alkalinity, which can be measured by titration with acid, of the molten paste in the neutralization system be between 0.1% and 1.5%, more preferably between 0.2% and 1.0%, most preferably between 0.3% and 0.7%.
The acid and caustic are put into the continuous neutralization system separately, preferably at the high shear mixer so that they mix together as rapidly as possible.
Generally, in a continuous neutralization loop, the ingredients enter the system through a pump (typically centrifugal) which circulates the material through a heat exchanger in the loop and back through the pump, where new materials are introduced. The material in the system continually recirculates, with as much product exiting as is entering. Product exits through a control valve which is usually after the pump. The recirculation rate of a continuous neutralization loop is between 1:1 and 50:1. The temperature of the neutralization reaction can be controlled to a degree by adjusting the amount of cooling by the heat exchanger. The "throughput" can be controlled by modifying the amount of acid and caustic introduced.
The continuous neutralization loop should be modified as follows to practice this process:

(1) Insulate the loop;
(2) Change the centrifugal pump to a positive displacement pump, which is better able to handle very viscous material;
(3) Install a caustic feed system which can handle concentrated caustic (greater than 50% solids);
(4) Introduce materials through a high shear mixer installed in-line;
(5) Install a metering system for the polyethylene glycol and/or ethoxylated nonionic surfactant, preferably after the high shear mixer; and
(6) Position the incoming streams of acid and caustic at the high shear mixer so that the highest degree of mixing possible takes place.
(7) The temperature of the loop should be sufficiently high to maintain the lowest possible viscosity of the paste to insure adequate recirculation and mixing. Typical paste temperatures in the loop are between (180°F) 82.2°C and (230°F) 110°C, preferably (200°F) 93.3°C to (210°F) 98.9°C.

II. Addition of Polyethylene Glycol and/or Ethoxylated Nonionic Surfactant

The second step of this process is adding to the continuous neutralization system during formation of the neutralized product polyethylene glycol of a molecular weight between 4,000 and 50,000 and/or ethoxylated nonionic surfactant of the formula R(OC₂H₄)_nOH, wherein R is a C_12-18 alkyl group or a C_8-16 alkyl phenol group and n is from 9 to 80, with a melting point greater than or equal to (120°F) 48.9°C. The weight ratio of the additive of step (b) to the mixture of step (a) is from 1:5 to 1:20.
The polyethylene glycol and/or the ethoxylated nonionic surfactant can be added separately or as a mixture to the continuous neutralization system at any point. In a neutralization loop, these additive(s) preferably enter the loop after the high shear mixer and before the recirculation pump. The additives must be melted before addition to the neutralization system, so that they can be metered in.
These two additives are chosen because they enhance detergent performance and are solid at below (120°F) 48.9°C, so that a detergent particle which is firm at ambient temperature can be made from the neutralized paste. Each additive also acts as a process aid by reducing the viscosity of the high active paste in the neutralizer loop.
Polyethylene glycol of a molecular weight between 4,000 and 50,000 is preferred over the ethoxylated nonionic surfactants. Polyethylene glycol of a molecular weight between 7,000 and 12,000 is more preferred, and most preferred is polyethylene glycol with a molecular weight of 8,000 ("PEG 8,000"). In this invention, the preferred weight ratio of polyethylene glycol to the acid/caustic mixture of step (a) is from 1:8 to 1:12. For polyethylene glycol with a molecular weight of 8,000, the preferred weight ratio is one part PEG 8,000 to ten parts acid/caustic mixture.
Polyethylene glycol is formed by the polymerization of ethylene glycol with ethylene oxide in an amount sufficient to provide a compound with a molecular weight between 4,000 and 50,000. It can be obtained from Union Carbide (Danbury, CT).
The preferred ethoxylated nonionic surfactant material is of the formula R(OC₂H₄)_nOH, wherein R is a C_12-18 alkyl group and n is from 12 to 30. Most preferred is tallow alcohol ethoxylated with 18 moles of ethylene oxide per mole of alcohol ("TAE 18"). The preferred melting point for the ethoxylated nonionic surfactant is greater than (140°F) 60°C.
Examples of other ethoxylated nonionics herein are the condensation products of one mole of decyl phenol with 9 moles of ethylene oxide, one mole of dodecyl phenol with 16 moles of ethylene oxide, one mole of tetradecyl phenol with 20 moles of ethylene oxide, or one mole of hexadecyl phenol with 30 moles of ethylene oxide.

III. Formation of Particles

The third and final step of this process is forming detergent particles from the product of step (b). Detergent particles can be formed in various ways from the neutralized product exiting the continuous neutralization system. A desirable detergent particle size distribution has a range of 100 to 1200 microns, preferably 150 to 600 microns, with an average of 300 microns.
The molten paste from a continuous neutralization loop can be atomized into droplets in a prilling (cooling) tower. To avoid prilling at all, the molten paste can be simultaneously cooled and extruded, and cut or ground into desirable particle sizes.
A third and preferred choice is to allow the molten paste to cool on a chill roll, or any heat exchange unit until it reaches a doughy consistency, at which point other detergent ingredients can be kneaded in. The resulting dough can then be granulated in a high shear mixer using a fine powder of less than 200 microns average particle diameter, or it can be granulated by mechanical means.
A fourth and most preferred choice is to allow the molten paste to cool completely on a chill roll or chilled belt unit until it is solid. The thin, hardened layer of solidified product can then be scraped off the chill roll or belt and broken into flakes.
The resulting detergent particles can be used as is, but are preferably admixed into a full detergent composition. For example, the instant detergent particles can be admixed with spray dried linear alkyl benzene sulfonate particles (with or without detergency builder) to make a granular detergent product which cleans well.
Appropriate full detergent compositions contain from 5 to 95% by weight of the instant high active detergent particles, from 0 to 95% by weight of additional detergent surfactant, from 0 to 85% by weight of detergency builder, from 0 to 50% by weight of fabric care agent, and from 0 to 20% by weight of percarboxylic acid bleaching agents.
The additional detergent surfactant referred to immediately above is selected from the group consisting of anionic, cationic, nonionic, amphoteric, and zwitterionic surfactants, and mixtures thereof. Examples of surfactants of these types are described in U.S. Patent 3,579,454, Collier, issued May 18, 1971, from Column 11, line 45 through Column 13, line 64. An extensive discussion of surfactants is contained in U.S. Patent 3,936,537, particularly Column 11, line 39 through Column 13, line 52. Anionic synthetic surfactants are particularly preferred.
Cationic surfactants can also be included in such full detergent compositions. Cationic surfactants comprise a wide variety of compounds characterized by one or more organic hydrophobic groups in the cation and generally by a quaternary nitrogen associated with an acid radical. Pentavalent nitrogen ring compounds are also considered quaternary nitrogen compounds. Suitable anions are halides, methyl sulfate and hydroxide. Tertiary amines can have characteristics similar to cationic surfactants at washing solution pH values less than about 8.5. A more complete disclosure of these and other cationic surfactants useful herein can be found in U.S. Patent 4,228,044, Cambre, issued October 14, 1980.
Other optional ingredients which may be included in the full detergent compositions herein include detergency builders, chelating agents, bleaching agents, antitarnish and anticorrosion agents, perfume and color additives, and other optional ingredients enumerated in the Baskerville patent, U.S. Patent 3,936,537, from Column 19, line 53 through Column 21, line 21. Chelating agents are also described in U.S. Patent 4,663,071, Bush et al., from Column 17, line 54 through Column 18, line 68. Suds modifiers are also optional ingredients and are described in U.S. Patents 3,933,672, issued January 20, 1976 to Bartoletta et al., and 4,136,045, issued January 23, 1979 to Gault et al.. Detergency builders are enumerated in the Baskerville patent from Column 13, line 54 through Column 16, line 16, and in U.S. Patent 4,663,071, Bush et al., issued May 5, 1987 . Such builders include, for example, phosphates, aluminosilicates, silicates, carbonates. C₁₀-C₁₈ alkyl monocarboxylates, polycarboxylates, and polyphosphonates, and mixtures thereof.
Fabric care agents are optionally included in such full detergent compositions. These include known fabric softeners and antistatic agents, such as those disclosed in U.S. Patent 4,762,645, Tucker et al., issued August 9, 1988 . The smectite clays described therein may also be included in the full detergent compositions.
Percarboxylic acid bleaching agents, or bleaching compositions containing peroxygen bleaches capable of yielding hydrogen peroxide in an aqueous solution and bleach activators at specific molar ratios of hydrogen peroxide to bleach activator, may also be included. These bleaching agents are fully described in U.S. Patent 4,412,934, Chung et al., issued November 1, 1983, and in U.S. Patent 4,483,781, Hartman, issued November 20, 1984.
The following nonlimiting examples illustrate the process and detergent particles of the present invention. All parts, percentages and ratios herein are by weight unless otherwise specified.

EXAMPLE I

Preparation of a high active detergent material suitable for granulation to a free flowing particulate is as follows.

Equipment

A falling film SO₃ reactor is used to prepare the acid form of C_14-15 alkyl sulfate. The acid is fed to a high active neutralization system supplied by Chemithon Corporation of Seattle, Washington. This customized neutralization system consists of a recycle loop containing a heat exchanger for cooling, a recirculation pump suitable for highly viscous fluids, and a high shear mixer with which the reactants are introduced.
In order to attain the very low moisture levels necessary for a free-flowing, high active particles, the neutralization loop is modified to handle 70% sodium hydroxide melt rather than the 38-50% normally used with the neutralization loop. This modification consists of hot water jackets and electrical heating of the caustic feed system to maintain the 70% caustic above the caustic melting point of about (155°F) 68.3°C.
Another necessary modification is the addition of a metering system which injects the polyethylene glycol into the neutralization loop at the discharge side of the high shear mixer. The presence of the polyethylene glycol facilitates pumping of the paste in the recirculation loop and reduces stickiness of the finished material. Polyethylene glycol having a molecular weight of about 8000 is added as a melt (about (160°F) or 71.1°C at a rate of about 1 part polyethylene glycol 8000 to 10 parts C_14-15 sodium alkyl sulfate active.

Operation

At start up, the neutralization loop is filled with water and the system is maintained at (180-230°F) 82.2-110°C by using hot water in the heat exchanger and in the double wall pipe comprising the recycle loop. The recycle pump and high shear mixer are started.
The 70% sodium hydroxide and C_14-15 alkyl sulfuric acid are introduced into the high shear mixer and allowed to react. The sodium hydroxide and C_14-15 alkyl sulfuric acid are metered to allow a slight excess of sodium hydroxide. Material displaced from the recirculation loop is discharged through a back pressure control valve.
As operation continues, the water is displaced from the loop and the concentration of the sodium C_14-15 alkyl sulfate is increased to over 70% active. Operation is continued until the desired amount of high active, low moisture material is produced. The reactant feed is then shut off and the reaction loop is washed with hot water.
Results The molten paste produced is cooled and manually ground to a free-flowing particulate product having the following composition.

Sodium C_14-15 alkyl sulfate 74.9%

Polyethylene glycol 8000 8.5

Water 9.1

Sodium hydroxide 0.6

Unreactants/miscellaneous 6.9

EXAMPLE II

Polyethylene glycol with a molecular weight of about 8000 is added to sodium C_14-15 alkyl sulfate to reduce its stickiness and make it suitable for granulating into free-flowing particles with low stickiness. The test sample is prepared by incorporating the polyethylene glycol 8000 into a quantity of sodium C_14-15 alkyl sulfate paste (made according to Example I) containing about 65% water, by mixing and then drying the product on a steam heated roll drier to less than 10% moisture. The polyethylene glycol 8000 is added at a ratio of 1 part of polyethylene glycol 8000 to 10 parts of sodium C_14-15 alkyl sulfate active. A control sample without polyethylene glycol is prepared in a similar manner. The material falls off the roll drier as dried flakes, which are manually ground and sieved through 14 mesh or 65 mesh.
Stickiness is measured by compressing 64mm (2-1/2") diameter x 64 mm (2-1/2") long cylinder of granules for 1 minute with a 9 kg (20 pound) weight. A force gauge is used to collapse the cylinder of granules. The force required, referred to as "cake grade", is measured and recorded as a measure of stickiness.

CAKE GRADES (Pounds of Force)
	Temperature
	(80°F) 26.6°C	(140°F) 60°C
Composition A	0.6	0.9
Composition B	12.4	22.2

These data show that the addition of polyethylene glycol 8000 results in a significantly lower cake grade, demonstrating that it reduces stickiness of the detergent particles.

EXAMPLE III

Polyethylene glycol with a molecular weight of about 8000 is added to sodium C_14-15 alkyl sulfate paste (made according to Example I) in a manner similar to Example II except that the polyethylene glycol 8000 is added at a ratio of 3 parts of polyethylene glycol 8000 to 10 parts of C_14-15 sodium alkyl sulfate active. Samples are roll dried and ground in the manner described in Example II. The samples are tested for caking as described in Example II, with the following results.

CAKE GRADES (Pounds of Force)
	Temperature
	(80°F) 26.6°C	(140°F) 60°C
Composition containing 3/10 ratio of polyethylene glycol/sodium C_14-15 alkyl sulfate	1.1	2.2
Control sample without polyethylene glycol 8000	12.4	22.2

These data show that the addition of polyethylene glycol 8000 results in a significantly lower cake grade, demonstrating that it reduces stickiness of the detergent particles. The ratio of 3:10 polyethylene glycol:alkyl sulfate is not significantly better at reducing cake grade than the 1:10 ratio of Example II.

EXAMPLE IV

In this example the falling film SO₃ reactor is used to prepare the acid form of C_12.3 linear alkyl benzene sulfonate. The acid is fed to the modified neutralization loop as described in Example I for neutralization with 70% caustic. PEG 8000 is added to the neutralization loop as described in Example I. A concentrated sodium C_12.3 linear alkyl benzene sulfonate is produced. The paste composition is 77.5% active, 8% PEG 8000, 9% water, the balance being excess caustic, unreacted material and miscellaneous.
The cooled sodium C_12.3 linear alkyl benzene sulfonate with polyethylene glycol is solid in nature but much more sticky than the sodium C_14-15 alkyl sulfate with polyethylene glycol prepared in Examples I and II.

EXAMPLE V

In this example high active sodium C_14-15 alkyl sulfate prepared as in Example I is mixed with the high active C_12.3 sodium linear alkyl benzene sulfonate prepared in Example IV in various ratios to study the dispersibility of the mixtures. All samples comprise polyethylene glycol 8000 in a 1:10 polyethylene glycol to alkyl sulfate or alkyl benzene sulfonate. To insure thorough mixing and simulate a co-neutralization of the two surfactants, the various ratios are mixed in a laboratory Sigma type mixer for 2 hours at a temperature of about (190°F) 87.8°C.
The mixtures are allowed to cool and are formed into granules by forcing through a 14 mesh screen. Each sample is tested for dispersibility by agitation in (60°F) 15.5°C water for 10 minutes. The wash water is then filtered through a black cloth filter to determine the amount of undissolved surfactant.
The deposits on the cloth are graded on a 1 to 10 scale; 10 representing no visible deposit.
As demonstrated by the data, a small amount of linear alkyl benzene sulfonate greatly improves the dispersibility of the detergent particle. As the level of linear alkyl benzene sulfonate is increased, the softness and stickiness of the particle increases. At high linear alkyl benzene sulfonate levels the particles are less suitable for use as detergent particles because of their stickiness. According to these data, the best compromise between low stickiness and good dispersibility is an alkyl sulfate/alkyl benzene sulfonate ratio of about 88/12.

Claims

process for producing detergent particles, having a surfactant activity of more than 50% by weight, comprising the steps of:
(a) reacting in a continuous neutralization system C_12-18 alkyl sulfuric acid, or C_10-16, preferably C_11-14 linear, alkyl benzene sulfonic acid, or mixtures thereof with an alkali metal hydroxide solution, preferably sodium hydroxide, which is greater than or equal to 62%, preferably 70%, by weight of the hydroxide, to produce a neutralized product having less than or equal to 12%, preferably between 8% and 12%, by weight of water;

(b) adding to said continuous neutralization system during formation of said neutralized product, polyethylene glycol of a molecular weight between 4,000 and 50,000; ethoxylated nonionic surfactant of the formula R(OC₂H₄)_nOH, wherein R is a C_12-18 alkyl group or a C_8-16 alkyl phenol group and n is from 9 to 80, with a melting point of greater than or equal to (120°F) 48.9°C; or mixtures thereof; wherein the weight ratio of the additive of step (b) to the product of step (a) is from 1:5 to 1:20, preferably 1:10; and

(c) forming detergent particles.
A process for producing high active detergent particles according to Claim 1 wherein step (a) comprises reacting said C_12-18 alkyl sulfuric acid, or a mixture of said C_12-18 alkyl sulfuric acid and C_10-16 linear alkyl benzene sulfonic acid, with said alkali metal hydroxide solution, preferably reacting said mixture in a weight ratio of C_12-18, preferably C_14-16, alkyl sulfuric acid to C_10-16, preferably C_11-14, linear alkyl benzene sulfonic acid between 75:25 and 96:4, preferably between 80:20 and 95:5.
A process for producing high active detergent particles according to Claims 1 or 2 wherein step (a) comprises reacting C_14-16 alkyl sulfuric acid with said alkali metal hydroxide solution.
A process for producing high active detergent particles according to Claims 1, 2 or 3 wherein said neutralized product has a reserve alkalinity of between 0.2% and 1.0%, preferably between 0.3% and 0.5%, Na₂O.
A process for producing high active detergent particles according to Claims 1, 2, 3 or 4 wherein said continuous neutralization system is a continuous neutralization loop which is preferably insulated and which preferably comprises a high shear mixer, positive displacement pump and a caustic feed system for caustic which is greater than or equal to 62%, preferably 70%, by weight of the hydroxide, and preferably wherein incoming acid and caustic streams are positioned at the high shear mixer, and step (b) additives are metered in after said high shear mixer and before said positive displacement pump.
A process for producing high active detergent particles according to Claims 1, 2, 3, 4 or 5 wherein said additive of step (b) is polyethylene glycol of a molecular weight between 6,000 and 50,000, preferably between 7,000 and 12,000.
A process for producing high active detergent particles according to Claims 1, 2, 3, 4, 5 or 6 wherein R is a C_12-18 alkyl group and n is from 12 to 30.
A process for producing high active detergent particles according to Claims 1, 2, 3, 4, 5, 6 or 7 wherein step (c) comprises cooling said product of step (b) on a chill roll until it has solidified, and scraping said solidified product off said chill roll into detergent flakes.