FIELD OF THE INVENTION
[0001] 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 about 62 wt.% hydroxide) in a continuous
neutralization system;
(b) adding polyethylene glycol of molecular weight about 4,000 to 50,000 and/or certain
ethoxylated nonionic surfactants during neutralization; and
(c) forming detergent particles.
BACKGROUND INFORMATION
[0002] 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 about 50% active.
[0003] 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 about 35% to 50% water. This slurry is then
atomized in a spray drying tower to reduce moisture to below about 10%. It is possible
to compact spray dried particles to make dense detergent granules. See U.S. Patent
[0004] 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.
[0005] 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 about 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 about 12% in the paste so that free-flowing, high active detergent granules
can be made from the paste without drying.
[0006] The following publications describe ways to make free-flowing high active particles
without drying, using surfactant paste, and made with a continuous neutralization
system.
[0007] 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.
[0008] 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.
[0009] 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.
[0010] 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.
[0011] 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.
[0012] 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.
[0013] 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 grnaulation.
[0014] 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.
[0015] 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.
[0016] The following patents describe processes and/or surfactant compositions comprising
viscosity modifiers such as polyethylene glycol and ethoxylated (E₂₀₋₆₀) alkyl (C₆₋₁₂)
phenol.
[0017] 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 CPS 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 (E₂₀₋₈₀) alkyl (C₆₋₁₂) are named
as viscosity modifiers.
[0018] U.S. Patent 4,495,092, Schmid et al., issued January 22, 1985 discloses the addition
of C₈₋₄₀ alcohols, or C₈₋₄₀ 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.
[0019] 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 C₁₋₆ alkyl monocarboxylic acids,
b) certain C₁₋₆ alkylene acid dicarboxylic acids,
(c) nitrilotriacetic acid and its salts,
(d) certain ether alcohols,
(e) and mixtures thereof.
[0020] 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.
[0021] 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
C₈₋₂₂ carboxylic acid; and
(c) 0 to about 10 weight % water.
[0022] 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
[0023] The present invention relates to a process for producing high active detergent particles,
comprising the steps of:
(a) reacting in a continuous neutralization system C₁₂₋₁₈ alkyl sulfuric acid, or
C₁₀₋₁₆ alkyl benzene sulfonic acid, or mixtures thereof with an alkali metal hydroxide
solution, which is greater than or equal to about 62% by weight of the hydroxide,
to produce a neutralized product having less than or equal to about 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 about 4,000 and 50,000;
ethoxylated nonionic surfactant of the formula R(OC₂H₄)nOH, wherein R is a C₁₂₋₁₈ alkyl group or a C₈₋₁₆ alkyl phenol group and n is from
about 9 to about 80, with a melting point of greater than or equal to about 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 about 1:5 to about 1:20; and
(c) forming detergent particles.
DESCRIPTION OF THE INVENTION
[0024] 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
about 50% active. The steps of the process are as follows.
I. Addition of Acid and Caustic
[0025] The first step of this process is neutralizing in a continuous neutralization system
C₁₂₋₁₈ alkyl sulfuric acid, or C₁₀₋₁₆ alkyl benzene sulfonic acid, or mixtures thereof
with an alkali metal hydroxide solution, which is greater than or equal to about 62%
by weight of the hydroxide, to produce a neutralized product having less than or equal
to about 12% by weight of water.
[0026] The C₁₂₋₁₈ alkyl sulfuric acid and C₁₀₋₁₆ alkyl benzene sulfonic acid can be made
by any sulfation/sulfonation process, but preferably are sulfonated with SO₃ 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.
[0027] C₁₂₋₁₈ alkyl sulfuric acid, and mixtures of it and C₁₀₋₁₆ 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.
[0028] In this process, it is preferred that the final ratio of C₁₂₋₁₈ sodium alkyl sulfate
to C₁₀₋₁₆ sodium linear alkyl benzene sulfonate be between 75:25 and 96:4, preferably
between 80:20 and 95:5.
[0029] An 88:12 ratio of C₁₄₋₁₅ sodium alkyl sulfate to C₁₂₋₁₃ 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) 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.
[0030] C₁₄₋₁₆ alkyl sulfuric acid is preferred for use in step (a) of this process over
C₁₂₋₁₈ alkyl sulfuric acid. C₁₄₋₁₅ alkyl sulfuric acid is most preferred.
[0031] C₁₁₋₁₄ linear alkyl benzene sulfonic acid is preferred over C₁₀₋₁₆ alkyl benzene
sulfonic acid. C₁₂₋₁₃ linear alkyl benzene sulfonic acid is most preferred for use
herein.
[0032] 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 about 62%, preferably
greater than or equal to about 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.
[0033] Sodium hydroxide, preferably 70% solids, is the preferred alkali metal hydroxide.
[0034] The neutralized product formed by the acid and caustic is in the form of a molten
paste. When about 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 about 8 and 10% by weight of water. It is most preferred that the alkali
metal hydroxide be about 70% by weight of hydroxide and that the molten paste be between
8% and 10% by weight water.
[0035] 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 about 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 about 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 about 0.1% and 1.5%, more preferably between about
0.2% and 1.0%, most preferably between about 0.3% and 0.7%.
[0036] 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.
[0037] 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 about 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.
[0038] 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
about 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 about 180°F (82.2°C) and 230°F (110°C),
preferably about 200°F (93.3°C) to 210°F (98.9°C).
II. Addition of Polyethylene Glycol and/or Ethoxylated Nonionic Surfactant
[0039] 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 about 4,000 and 50,000 and/or ethoxylated nonionic surfactant of the formula
R(OC₂H₄)
nOH, wherein R is a C₁₂₋₁₈ alkyl group or a C₈₋₁₆ alkyl phenol group and n is from
about 9 to about 80, with a melting point greater than or equal to about 120°F (48.9°C).
The weight ratio of the additive of step (b) to the mixture of step (a) is from about
1:5 to about 1:20.
[0040] 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.
[0041] These two additives are chosen because they enhance detergent performance and are
solid at below about 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.
[0042] Polyethylene glycol of a molecular weight between about 4,000 and 50,000 is preferred
over the ethoxylated nonionic surfactants. Polyethylene glycol of a molecular weight
between about 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
about 1:8 to about 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.
[0043] 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
about 4,000 and 50,000. It can be obtained from Union Carbide (Danbury, CT).
[0044] The preferred ethoxylated nonionic surfactant material is of the formula R(OC₂H₄)
nOH, wherein R is a C₁₂₋₁₈ alkyl group and n is from about 12 to about 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 about 140°F (60°C).
[0045] 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
[0046] 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 about 100 to 1200 microns, preferably about 150 to
600 microns, with an average of 300 microns.
[0047] 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.
[0048] 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 about 200 microns average particle
diameter, or it can be granulated by mechanical means.
[0049] 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.
[0050] 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.
[0051] Appropriate full detergent compositions contain from about 5 to 95% by weight of
the instant high active detergent particles, from 0 to about 95% by weight of additional
detergent surfactant, from 0 to about 85% by weight of detergency builder, from 0
to about 50% by weight of fabric care agent, and from 0 to about 20% by weight of
percarboxylic acid bleaching agents.
[0052] 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, incorporated herein by reference,
from Column 11, line 45 through Column 13, line 64. An extensive discussion of surfactants
is contained in U.S. Patent 3,936,537, incorporated herein by reference, particularly
Column 11, line 39 through Column 13, line 52. Anionic synthetic surfactants are particularly
preferred.
[0053] 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, incorporated herein by reference.
[0054] 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, incorporated herein by reference. Chelating agents
are also described in U.S. Patent 4,663,071, Bush et al., from Column 17, line 54
through Column line 68, incorporated herein by reference. 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.,
both incorporated herein by reference. 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, both incorporated herein by reference. Such builders
include, for example, phosphates, aluminosilicates, silicates, carbonates. C₁₀-C₁₈
alkyl monocarboxylates, polycarboxylates, and polyphosphonates, and mixtures thereof.
[0055] 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, incorporated herein by reference.
The smectite clays described therein may also be included in the full detergent compositions.
[0056] 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, both of which are incorporated herein by reference.
[0057] 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
[0058] Preparation of a high active detergent material suitable for granulation to a free
flowing particulate is as follows.
Equipment
[0059] A falling film SO₃ reactor is used to prepare the acid form of C₁₄₋₁₅ 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.
[0060] 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).
[0061] 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 C₁₄₋₁₅ sodium
alkyl sulfate active.
Operation
[0062] 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.
[0063] The 70% sodium hydroxide and C₁₄₋₁₅ alkyl sulfuric acid are introduced into the high
shear mixer and allowed to react. The sodium hydroxide and C₁₄₋₁₅ 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.
[0064] As operation continues, the water is displaced from the loop and the concentration
of the sodium C₁₄₋₁₅ 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
[0065] The molten paste produced is cooled and manually ground to a free-flowing particulate
product having the following composition.
Sodium C₁₄₋₁₅ alkyl sulfate |
74.9% |
Polyethylene glycol 8000 |
8.5 |
Water |
9.1 |
Sodium hydroxide |
0.6 |
Unreactants/miscellaneous |
6.9 |
EXAMPLE II
[0066] Polyethylene glycol with a molecular weight of about 8000 is added to sodium C₁₄₋₁₅
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 C₁₄₋₁₅ 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 C₁₄₋₁₅
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.
[0067] Stickiness is measured by compressing a 2-1/2" diameter x 2-1/2" long cylinder of
granules for 1 minute with a 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.
|
Composition A |
Composition B |
Sodium C₁₄₋₁₅ alkyl sulfate |
67 |
80 |
Polyethylene glycol 8000 |
7 |
0 |
Water |
7 |
6 |
Unreacted sodium hydroxide and miscellaneous |
Balance |
Balance |
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 |
[0068] 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
[0069] Polyethylene glycol with a molecular weight of about 8000 is added to sodium C₁₄₋₁₅
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 C₁₄₋₁₅ 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 C₁₄₋₁₅ alkyl sulfate |
1.1 |
2.2 |
Control sample without polyethylene glycol 8000 |
12.4 |
22.2 |
[0070] 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
[0071] 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.
[0072] The cooled sodium C
12.3 linear alkyl benzene sulfonate with polyethylene glycol is solid in nature but much
more sticky than the sodium C₁₄₋₁₅ alkyl sulfate with polyethylene glycol prepared
in Examples I and II.
EXAMPLE V
[0073] In this example high active sodium C₁₄₋₁₅ 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).
[0074] 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.
[0075] The deposits on the cloth are graded on a 1 to 10 scale; 10 representing no visible
deposit.
Ratio |
Black Fabric Grade |
Alkyl sulfate/alkyl benzene sulfonate |
|
100/0 |
5.5 |
94/6 |
9.0 |
88/12 |
9.5 |
75/25 |
10 |
50/50 |
10 |
25/75 |
10 |
0/100 |
10 |
[0076] 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.
1. A process for producing high active detergent particles comprising the steps of:
(a) reacting in a continuous neutralization system C₁₂₋₁₈ alkyl sulfuric acid, or
C₁₀₋₁₆, preferably C₁₁₋₁₄ 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 C₁₂₋₁₈ alkyl group or a C₈₋₁₆ 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.
2. A process for producing high active detergent particles according to Claim 1 wherein
step (a) comprises reacting said C₁₂₋₁₈ alkyl sulfuric acid, or a mixture of said
C₁₂₋₁₈ alkyl sulfuric acid and C₁₀₋₁₆ linear alkyl benzene sulfonic acid, with said
alkali metal hydroxide solution, preferably reacting said mixture in a weight ratio
of C₁₂₋₁₈, preferably C₁₄₋₁₆ alkyl sulfuric acid to C₁₀₋₁₄ preferably C₁₁₋₁₄ linear
alkyl benzene sulfonic acid between 75:25 and 96:4, preferably between 80:20 and 95:5.
3. A process for producing high active detergent particles according to Claims 1 or
2 wherein step (a) comprises reacting C₁₄₋₁₆ alkyl sulfuric acid with said alkali
metal hydroxide solution.
4. 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.
5. 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.
6. 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.
7. A process for producing high active detergent particles according to Claims 1,
2, 3, 4, 5 or 6 wherein R is a C₁₂₋₁₈ alkyl group and n is from 12 to 30.
8. 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.
9. A detergent particle made according to Claims 1, 2, 3, 4, 5, 6, 7 or 8.
10. A granular detergent composition comprising detergent particles made according
to Claims 1, 2, 3, 4, 5, 6, 7 or 8.