US3112274A - Process for making a bleach composition - Google Patents

Process for making a bleach composition Download PDF

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US3112274A
US3112274A US855139A US85513959A US3112274A US 3112274 A US3112274 A US 3112274A US 855139 A US855139 A US 855139A US 85513959 A US85513959 A US 85513959A US 3112274 A US3112274 A US 3112274A
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bed
particles
sodium
polychlorocyanurate
range
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John H Morgenthaler
Thomas D Parks
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Procter and Gamble Co
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Procter and Gamble Co
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Priority to US855139A priority patent/US3112274A/en
Priority to FR844789A priority patent/FR1274163A/fr
Priority to GB40490/60A priority patent/GB953655A/en
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D17/00—Detergent materials or soaps characterised by their shape or physical properties
    • C11D17/0039—Coated compositions or coated components in the compositions, (micro)capsules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D11/00—Special methods for preparing compositions containing mixtures of detergents
    • C11D11/0082—Special methods for preparing compositions containing mixtures of detergents one or more of the detergent ingredients being in a liquefied state, e.g. slurry, paste or melt, and the process resulting in solid detergent particles such as granules, powders or beads
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11D—DETERGENT COMPOSITIONS; USE OF SINGLE SUBSTANCES AS DETERGENTS; SOAP OR SOAP-MAKING; RESIN SOAPS; RECOVERY OF GLYCEROL
    • C11D3/00—Other compounding ingredients of detergent compositions covered in group C11D1/00
    • C11D3/395—Bleaching agents
    • C11D3/3955—Organic bleaching agents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00141—Coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00212—Plates; Jackets; Cylinders
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S118/00—Coating apparatus
    • Y10S118/05—Fluidized bed
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S159/00—Concentrating evaporators
    • Y10S159/03—Fluidized bed

Definitions

  • This invention relates to a process for making a dry bleach composition. More particularly, it is a process for coating a chlorinated organic bleaching compound with inorganic salts in a fluidized bed in order to obtain a dry bleach composition having outstanding characteristics.
  • Dry chlorine bleach compositions have advantages over the widely used liquid hypochlorite solution which include ease in packaging, handling and shipping. Moreover, dry chlorine bleach compositions can be combined advantageously with dry products such as granular detergents whereas liquid bleaches cannot.
  • the polychlorocyanurates i.e. triand di-chloro cyanuric acids and the alkali metal salts of dichlorocyanuric acid, have found wide acceptance as stable and efiicient dry organic bleaching compounds.
  • the polychlorocyanurates are usually mixed with dry inorganic salts, preferably alkaline salts, as carrier agents to provide bulk for ease in measuring and for prevention of localized overconcentration and preferably to provide alkalinity when the bleaching compound is dissolved in water. It has been found that p olychlorocyanurates provide the greatest bleaching activity in water under alkaline conditions.
  • aqueous slurries of the polychlorocyanurate and the carrier agent have been dried, usually by spray drying. Forming and drying such aqueous slurries, particularly spray drying, have caused substantial difficulties.
  • the polychlorocyanurate in dry bleach compositions dried in accordance with the usual methods, such as by spray drying, are not protected or are only partially protected from moisture and air which are known to increase the tendency of such compounds to decompose.
  • the process of spray drying a homogeneous aqueous slurry of a polychlonocyanurate and an inorganic carrier agent effects a combination of the two ingredients in a granule which is usually hollow.
  • Polychlorocyanurate in a spray dried granule will be exposed on the entire surface of the granule. Only the polychlorocyanurate in the interior of the granule will be protected by the carrier agent. Thus, the exposed polychlorocyanurate is subject ice Isl
  • Exposed polychlorocyanurate also provides a distinct chlorine odor to which some people might object and which would interfere with desired perfuming.
  • organic coating materials such as waxes, soaps, parafins, fatty alcohols and the like is undesirable because of the reactivity of such materials with the polychlorocyanurates, because coating with such materials is diflicult, and because such materials tend to leave a residue in the water in which the p olychlorocyanurate is used.
  • It is another object of this invention to provide a process for making a homogeneous, dry bleach composition comprising a polychlorocyanur-ate having an inorganic coating which protects the polychlorocyanurate from attack from moisture, air, and reactive organic materials.
  • the process involves low temperature and low moisture conditions relative to the usual drying processes, such as spray drying, thereby markedly reducing the loss of available chlorine during the processing of the polycyanurates.
  • the process involves a lesser amount of equipment which is subject to corrosive attack than spray-drying processes.
  • Polychlorocyanurates have the formula wherein X is Cl (trichlorocyanuric acid), H (dichlorocyanuric acid), or an alkali metal such as Na (sodium dichlorocyanurate) or K (potassium dichlorocyanurate). Tautomeric forms of polychlorocyanurates and methods for making polychlorocyanurates are discussed in US. Patents 2,607,738 and 2,913,460. The preferred polychlorocyanurates are sodium and potassium dichlorocyanurates since they are more stable than the polychlorocyanuric acids.
  • the inorganic material which is used to coat the polychlorocyanurate particles in the fluidized bed comprises aqueous slurries of inorganic salts which are dried to form a protective film around the particles.
  • inorganic salts are sodium and potassium sulfates, phosphates, carbonates and borates. Slurries of such salts should have a pH in the range of about 4 to about 11. A slurry having a pH higher than about 11 undosirably decreases the stability of the polychlorocyanurate particles on which it is sprayed.
  • the halides and ammonium compounds are not suitable since they tend to cause decomposition or degradation of the polychlorocyanurates.
  • Sodium tripolyphosphate and mixtures of sodium tripolyphosphate and sodium sulfate wherein the amount of sodium sulfate is up to three times the amount of sodium tripolyphosphate are extremely useful in the process of this invention since they provide a good coating and the desired buffered alkalinity for the optimum bleaching activity of the polychlorocyanurate.
  • Other examples of inorganic salts useful in the process of this invention are sodium carbonate, sodium tetraborate, potassium sulfate, sodium pyrophosphate, sodium bicarbonate, potassium tripolyphosphate, sodium hexametaphosphate, sodium sesquicarbonate, sodium orthophosphate (monoand di-basic) and potassium bicarbonate.
  • Such detergents are soap and non-soap synthetic detergents of the sulfuric and sulfonic ester type which also contain in their molecular structure an alkyl or acyl radical containing from 8 to 18 carbon atoms.
  • Such detergents should not contain amine or amide groups because of the reactivity of the nitrogen in these groups with the polychlorocyanurates.
  • amine soaps and acyl taurides are undesirably reactive with the polychlorocyanurates.
  • Non-ionic detergents such as higher fatty acid monoand (ii-ethanol amides, are also undesirable.
  • soaps are examples of useful additions to the slurry of coating material used in the process of this invention: sodium and potassium salts of the higher fatty acids of naturally occurring plant or animal fats and oils (e.g. palm oil, coconut oil, soybean oil, castor oil, tall oil, tallow, whale and fish oils, grease and lard) or of synthetically produced fatty acids.
  • Sodium and potassium soaps can be made by direct saponiflcation of the fats and oils or the neutralization of the free fatty acids.
  • water-soluble, anionic, organic, nonsoap, synthetic detergents are examples of useful additions to the slurry of coating material used in the process of this invention: sodium and potassium alltyl glyceryl ether sulfonates, especially those others of higher fatty alcohols derived by the reduction of coconut oil; the reaction product of higher fatty acids with sodium or potassium isethionate, where, for example, the fatty acids are derived from coconut oil; sodium or potassium alkyl benzene sulfonates in which the alkyl group contains from about 9 to about carbon atoms in either a straight chain or preferably a branched chain which is derived from polymers of propylene; dialliyl esters of sodium or potassium salts of sulfosuccinic acid, for example the dihexyl ester; sodium and potassium alkyl sulfonates and sulfates, especially those alkyl sulfates derived by sulfation of higher fatty alcohols produced
  • Fluidization is a technique widely used in catalytic cracking. Fluidization involves the formation of a bed of a dense phase of finely divided solids suspended in an up flowing gaseous stream under such conditions that the solids are in turbulent, random motion within the bed, while the bed maintains an upper free surface re scmbling that of boiling liquid.
  • the vessel in which a fluidized bed is maintained has provision at the bottom for providing the even distribution of the up-fiowing gas over the cross section of the vessel such as the use of a porous plate.
  • the velocity of the gas is sufficiently high to buoy the finely divided solids in a turbulent, fluidlike motion.
  • the gas velocity must be sufficient to buoy the solids in this manner but must not be so great that the bed will be swept out of the container or that the bed will lose its upper free surface.
  • the variables of fluidized beds i.e. kinetics, particle size, gas velocity, apparatus, etc., have been extensively studied and reported. See, for example, Fluidization edited by D. F. Othmer (Reinhold, 1956) and Fluidization by Max Leva (McGraw-Hill, 1959).
  • the slurry of inorganic coating material is sprayed onto the particles of polychlorocyanurate in the fluidized bed.
  • This method of spray coating has advantages over other methods which might be used for spray coating such as methods in which the particles to be sprayed are in a falling stream, a tumbling drum or on a screen.
  • a very large amount of particle surface is exposed and the drying efliciency of the fluidizing gas and the coating completeness are very great.
  • the treated particles are easily removed and transported since the fluidized solids behave similar to a liquid.
  • the process of this invention in more specific terms involves forming a fluidized bed consisting of a dense phase bounded by an upper free surface by passing a distributed ascending current of gas at a predetermined velocity through a mass of solid particles of a polychlorocyanurate, heating the bed to a temperature in the range of about F. to about F. and spraying onto the particles in the thus formed bed an aqueous slurry of an inorganic coating material selected from the group consisting of sodium and potassium sulfates, phosphates, borates and carbonates to coat the particles in the bed.
  • Sufficient coating is sprayed on the particles to obtain coated particles having a weight ratio on an anhydrous basis of polychlorocyanurate to coating material in the range of about 3:1 to about 1:5.
  • the bed is maintained in the temperature range of about 100 F. to about 170 F. until the free moisture content of the coated particles is in the range of about 1% to about 15%.
  • the coated particles are then dried at a temperature in the range of about F. to about 240 F. to a free moisture content of 0% to about 2%.
  • the final drying step can be effected in the same vessel as the earlier steps by increasing the temperature of the fluidized bed. Drying can also be effected by fiuidizi-ng the partially dried coated particles in a second fluidized bed, by imble drying them in a rotary drum drier, or by drying the particles on a moving belt in an oven.
  • the process can be made continuous by continuously supplying the fluidized bed with uncoated polychlorocyanurate powder, continuously spraying on the slurry of inorganic coating material and continuously drawing olf partially dried coated particles which are then dried continuously, preferably in fluidized bed in a second fluidizing vessel, where finished dried product is continuously drawn off.
  • free moisture means moisture other than that of the water of hydration existing in inorganic salt hydrates which are stable (retain their water of hydration) at least up to 120 F.
  • the water in sodium sulfate decahydrate is classed herein as free moisture because sodium sulfate decahydrate is stable only up to about 90 F. where its water of hydration is liberated.
  • the water in sodium tripolyphosphate hexahydrate is not classed as free moisture because that hydrated salt is stable up to about 220 F.
  • the polychlorocyanurate powder is introduced from its storage 3 into the fluidizing vessel 1 in a quantity predetermined to form a fluidized bed of the desired size. Valve 8 is then closed. The powder is then formed into a fluidized bed by forcing a gas which is substantially inert to the powder such as air or nitrogen, through the grid 5.
  • the grid 5 is preferably a porous plate but any grid can be used which provides substantially even distribution of the upward flowing gas over the cross section of the fluidizing vessel 1.
  • porous plate If a porous plate is used, it should be porous enough to permit upward passage of air without an unduly large pressure drop but should not be so porous that substantially even distribution of the fluidizing gas is not obtained.
  • the porous plate can be made of sintered stainless steel or of a porous ceramic material.
  • porous plates finely perforated plates, fine screens or bubble cap plates of the type used in distilling and deodorizing columns can be used as grids.
  • a grid can be dispensed with in smaller iiuidizing vessels which have a conical bottom which evenly distributes the fiuidizing gas.
  • the velocity of the fiuidizing gas should be suflicient to buoy the polychlorocyanurate particles into a fluidized bed but should not be so great that the upper free surface of the bed is lost either by extreme bubble formation or slugging within the bed (severe vertical surging of the bed) or by sweeping the particles out of the vessel.
  • Polychlorocyanurate powders having a particle size in the range of about 5 to about 5 mm., preferably 20 to 85%., can be formed into the fluidized beds which are useful in the process of this invention. Particles smaller in size than about 5 are too fine to form properly into a bed. It has been found that gas velocities in the range of about 1 ft./sec.
  • velocities and the velocities hereinafter mentioned are measured after the fluidizing air has risen above the upper free surface of the bed and are more useful figures than velocities measured below or within the bed.
  • the height of the fluidized bed does not appear to be a critical factor in the practice of this invention; however, the best fluidization and processing results occur when the bed height is between 1 and 2 feet. Practical fluidizing vessel diameters range from about 1 to about 5 feet. Bed heights higher than 2 feet can be used in vessels having a diameter of about 3 to 5 feet.
  • the temperature within the fluidized bed should be maintained in the range of about 100 F. to about 170 F.
  • the fluidizing gas can be heated or a heating coil 6 or heated rods can be placed in the bed or a heating jacket can be placed around the portion of the fiui-dizing vessel within which the bed is located.
  • the bed temperature is maintained partially with heated fluidizing air and partially with a heating means in or around the bed. Heating of the bed is easier to control if both methods of heating are used since each method uses a lower temperature than if only one method were used.
  • the slurry of coating material from crutcher 2 is sprayed on to the bed through spray nozzle 4 from a point above the upper free surface of the bed.
  • the spray nozzle is a conventional atomizing nozzle using pressure atomization or preferably a two fluid nozzle using air or other inert gas as the atomiziug fluid.
  • Liquid spray pressures can be in the range of about 10 p.s.i. to about 100 p.s.i. with air or gas pressures in the range of about 10 p.s.i. to about 100 p.s.i.
  • the slurry of coating material should have a water content in the range of about 30% to about Less than about 30% water results in a viscous slurry which is hard to spray, increases the tendency of the slurry to spray dry and makes difiicult the coating of the polychlorocyanurate powder. More than about 85% water in the slurry results in poor coating characteristics and a high evaporative load in the process.
  • the preferred range is 55% to 75%.
  • the slurry temperature should be high enough to obtain a purnpable viscosity but not be so high that there is undesirable spray drying on atomization. Satisfactory slurry temperatures vary with slurry composition but the preferred temperatures for slurries containing sodium tripolyphosphate and/ or sodium sulfate are in the range of about 70 F. to about 140 F.
  • the temperature maintained within the bed during the coating step is in the range of about F. to about 170 F.
  • a temperature within this range coupled with the evaporative effect of the fluidizing gas results in the formation of the inorganic coating around the polychlorocyanurate particles and in the partial drying of this coating.
  • the temperature should not be less than about 100 F. in order to prevent the buildup of so much water in the coated particles that proper fluidization is prevented. If the temperature exceeds about 170 F. the atomized slurry of coating material has a tendency to be spray dried, which prevents efiective coating of the polychlorocyanurate particles.
  • the preferred temperature range is F. to F.
  • Sufficient coating material should be sprayed on the polychlorocyanurate particles to obtain a weight ratio of coating material to polychlorocyanurate in the finished product in the range of about 1:3 to about 5:1, preferably 121.5 to 2:1, on an anhydrous basis.
  • the tendency of the coated particles to agglomerate with each other in the form of clumps of coated particles can be increased by adding a small amount of an anionic organic detergent to the slurry of coating material.
  • the detergent imparts a stickiness to the coated particles causing increased agglomeration.
  • the slurry can contain from 0% to about 1.5% anionic detergent for agglomeration purposes with the size of the agglomerate increasing with increasing amounts of detergent. Amounts greater than about 1.5 result in an undesirably large increase in the size of the agglomerates making the operation of the fluidized bed difficult. 0.5% to 1% is the preferred amount of detergent in the slurry.
  • the amounts of anionic detergent present in the slurry necessarily determine the amounts of anionic detergent present in the coating (on anhydrous basis) since the range of water content in the slurry has hereinbefo-re been given. Since the solids in the slurry provide the coating '7 for the polychlorocyanurate particles, a simple ratio balance will give the percentage range of anionic detergent in the coating.
  • the coating comprises, on an anhydrous basis, to about anionic detergent, perferably 0.7% to 6.7%.
  • the fluidized bed is maintained in the above tempera ture range until the free moisture content of the coated particles is in the range of about 1% to about
  • the coated particles are dried in this step to a free moisture content in the range of 0% to about 2%.
  • the finished product should not contain more than about 2% free moisture, preferably not more than about 1%, since more than this amount decreases the stability of the prodnot and makes the product sticky with a tendency to cake.
  • the preferred free moisture content of the final product is 0%. If a hydrated inorganic salt which is stable up to at least about 120 F.
  • the final product is used as a coating material, it is desirable to drive off a portion of the water of hydration during the drying step to a point where the final product contains as low as about 2% total water. This permits the final product to take up some moisture from the atmosphere, if it is so exposed, without the water so taken up becoming free moisture.
  • the final drying step can be effected in several ways depending on the type of operation desired.
  • the coated particles can be retained in fiuidizing vessel 1 while the bed temperature is increased from a temperature in the range of about 100 F. to about 170 F. to a temperature in the drying range of about 190 F. to about 240 F.
  • valve 9 is opened and the finished product is discharged through discharge 7.
  • the partially dried coated particles can be run through valve 9, discharge 7, inlet 12. and valve 16 into another fluidizing vessel 11.
  • the partially dried coated particles are formed into a fluidized bed in the same manner that a bed is formed in the first fiuidizing vessel 1.
  • the bed is maintained at a temperature in the range of about 190 F. to about 240 F. with either heated fiuidizing gas passing through grid 14 or a heating coil 13 or jacket or, as explained above, preferably both.
  • a temperature in this range is maintained until the coated particles are dried to a free moisture content in the range of 0% to about 2% at which time valve 17 is opened and the finished product is discharge-cl through discharge 15.
  • the final drying can be effected by drying means other than a second fluidized bed such as by tumble drying in a low speed rotary drum drier or by drying on a moving belt in an oven. Drying in a fiuidized bed is preferred because it is eflicient, it is an enclosed system and the fluidizing air facilitates removal of fines.
  • valves 8, 9, 16, and 17 are left open and there is a continuous input of polychlorocyanurate powder from its source 3 to maintain the bed, continuous spray-on from spray nozzle 4-, continuous discharge of coated, partially dried particles from discharge 7, continuous input of these particles through inlet 12, continuous drying of these particles in fluidizing vessel 11 and continuous discharge of the finished dried particles through discharge 15
  • valve 8 is below the upper free surface of the bed.
  • valve 9 is preferably located at the lowest portion of the fluidized bed in the coating operation to minimize the proportion of uncoated or partially coated particles drawn off. Then in fluidizing vessel 11, the dried coated particles, being lighter than the partially dried coated particles entering in the lower portion of the fluidized bed, will migrate to the upper portion of the fluidized bed where they can be drawn off through valve 17 and discharge 15.
  • a continuous process can also be obtained if the final drying step is performed by drying means other than a second fluidized bed such as by continuous passage through a rotary drum drier or an oven.
  • Example I A slurry consisting of 35% sodium tripolyphosphate and 65% water was added to a crutcher and heated to 92 F.
  • the vessel had a grid which consisted of a plate of sintered powdered stainless steel. The plate was inch thick and had a porosity grade of D as described in an article by I. E. Campbell on pages 98101 of Materials and Methods, April 1955.
  • the powder was formed into a fluidized bed by passing air, evenly distributed by the grid over the cross-section of the vessel, at 168 F. upward through the grid. The velocity of the air as measured above the bed was 2.27 feet per second. The air had sufficient velocity to buoy all of the particles of powder in a fluidized bed having an upper free surface. Heating coils located within the bed area of the vessel were heated to 368 F. with steam.
  • the slurry was sprayed downward onto the bed through a two-fluid spray nozzle located 24 inches above the upper free surface of the bed. Air at 50 p.s.i. was the atomizing fluid and the slurry was pumped through the nozzle at 27 p.s.i.
  • the bed temperature was F.
  • the slurry was sprayed onto the bed until a coating of sodium tripolyphosphate had formed around the sodium dichlorocyanurate particles in the weight ratio, on an anhydrous basis, of coating to sodium dichlorocyanurate of 1.2: 1.
  • the coated particles had a free moisture content of 1.4%.
  • the coated particles were then dried by increasing the bed temperature to 205 F.
  • the heating coil temperature was 368 F. and the fluidizing air temperature was 171 F. The drying was stopped when the free moisture of the coated particles was completely eliminated.
  • the final product had the following composition:
  • This product was a stable granular dry bleach composition which when dissolved in water provided active and efficient bleaching, sterilizing and disinfecting properties.
  • the sodium tripolyphosphate provided the solution with the desired buffered alkalinity and sequestered water hardness ions.
  • the coating of sodium tripolyphosphate around the sodium dichloroey-anur-ate salt particles provided greater storage stability and resistance to attack from air or moisture than either the untreated salt or the salt spray dried with an equivalent amount of sodium tripolyphosphate.
  • the granules had only a very slight chlorine odor.
  • the granules were substantially uniform in composition throughout the product and there was no noticeable tendency for the ingredients of the composition to segregate.
  • a mixture of equal parts by weight of sodium tripolyphosphate and sodium suliate can be substituted for the sodium tripolyplrosphate in an equal amount by weight in Example "I with substantially the same results.
  • Example 11 A slurry consisting of 34.2% sodium sulfate, 0.7% sodium coconut oil alcohol sulfate and 65.1% water was added to a crutcher and heated to 100 F.
  • Example I pounds of the sodium dichlorocyanurate described in Example I were added to the fluidizing vessel and formed into a fluidized bed as described in Example I except that the air temperature was 178 F. and the heating coil temperature was 370 F.
  • the slurry was sprayed on to the bed as described in Example I except that the air was at 50 p.s.i. and the slurry pressure was 18 p.s.i.
  • the bed temperature was 116 F. Spraying continued until a sodium sulfate coating had formed around the sodium dichlorocyanurate in a ratio of coating to sodium dichlorocyanurate of 1:1.1 on an anhydrous basis.
  • the coated particles had a free moisture content of 12.4%.
  • the coated particles were then dried by increasing the bed temperature to 235 F.
  • the heating coil temperature was 370 F. and the fiuidizing air temperature was 173 F. The drying was stopped when the free moisture content of the coated particles was 0.7%.
  • the final product had the following composition:
  • the final product was an outstanding granular dry bleach composition having characteristics substantially the same as the product described in Example I except that the sodium sulfate provided no buffered alkalinity or sequestration in solution.
  • potassium tripolyphosphate, tetrasodium pyrophosphate, sodium tetraborate or potassium bicarbonate can be substituted in equal amounts by weight for the sodium sulfate with substantially equal results.
  • These compounds provide alkaline solutions and/or sequestering properties.
  • Example HI A slurry consisting of 34.43% sodium tripolyphosphate, 0.35% sodium coconut oil alcohol sulfate, 0.22% ultramarine blue (for coloring purposes) and 65% water was added to a crutcher and heated to 90 F.
  • Example I 20 pounds of the sodium dichlorocyanurate powder havin the particle size described in Example I was added to a circular iluidizing vessel having the diameter and grid characteristics described in Example I.
  • the powder was formed into a fluidized bed by passing air at 220 F. upward through the grid.
  • the velocity of the air as measured above the bed was 3.19 feet per second (150 cubic feet per minute).
  • the air had sufficient velocity to buoy all of the particles of powder in a fluidized bed having an upper free surfiace.
  • Heating coils located within the bed area of the vessel were heated to 350 F. with steam.
  • the slurry was sprayed downward on to the bed through a two-fluid spray nozzle located 18 inches above the upper free surface of the bed. Air at 30 p.s.i. was the atomizing fluid. The slurry was pumped through the nozzle at 10 p.s.-i. at the rate of 6-6 pounds per hour. The bed temperature was E. Additional sodium dichlorocyanurate was introduced into the fluidizin-g vessel continuously at the rate of 23 pounds per hour. Sodium dichlorocyanurate particles with a sodium tripolyphosphate coating and containing 1.5% free moisture were continuously drawn oil" from the lower portion of the fluidized bed. The particles had a coating to sodium dichlorocyanurate ratio of 1:1.04 of an anhydrous basis.
  • the thusly coated particles were continuously led into a second lluidizing vessel having the same characteristics as the first vessel and formed into a fluidized bed.
  • the fluidizing air had a temperature of 220 F. and a velocity of 3.82 it. per second (180 cubic feet per minute).
  • Steam heated coils Within the bed were at a temperature of 300 F.
  • the bed temperature was 220 F.
  • Coated particles having no free moisture and a total moisture content of 5% were continuously drawn oil from the upper part of the bed at the rate of 39 pounds per hour. (A small amount of product was lost as dust through the cyclones at the top or" the iluidizing vessels.)
  • the final product had the following composition:
  • This product was a stable granular dry bleach having the outstanding characteristics described in Example I except that the particle size was greater because of the agglomeration of the coated particles resulting from the alkyl sulfate in the slurry of coating material.
  • potassium dichlorocyanurate, dichlorocyanuric acid and trichlorocyanuric acid can be substituted for the so dium dichlorocyanurate in equal amounts by weight with substantially equal results except that the amounts of available chlorine in the final product will vary slightly.
  • sodium coconut oil alcohol glyce-ryl ether sulfonate, potassium laurate and sodium polypropylene benzene sulfonate (the polypropylene averaging 12 carbon atoms) can be substituted for the sodium coconut oil alcohol sulfate in equivalent amounts with substantially equal results.
  • coated polychlorocyanurate particles obtained in the process of this invention are more stable and have less chlorine odor than either uncoated polychlorocyanurate particles or granular products having the same composition but dried by different processes. Other drying processes do not provide the protective coating that is obtained in the process of the present invention.
  • This coating comprises a substantially complete film of inorgarlic salt around the polychlorocyanurate particles.
  • Example III The coated sodium dichlorocyanuratc particles obtained in Example III, uncoated sodium dichlorocyanurate and a spray dried sodium dichlorocyanurate composition were compared for relative stability.
  • Example 111 35 parts of the coated sodium dichlorocyanurate particles obtained in Example 111 were mechanically mixed with 65 parts of a spray dried composition which contained 1.85% sodium coconut oil alcohol sulfate, 53.8% P121 304, 40.3% sodium tripolyphosphate, 0.15% optical brightener, 0.3% ultramarine blue and 3.6% water.
  • B. 16.4 parts of uncoated sodium dichlorocyanurate were mechanically mixed with 1.5 parts sodium polypropylene benzene sulfonate (the polypropylene averag ing 12 carbon atoms), 41.3 pants sodium tripolyphosphate, 38.2 parts Na SO 0.1 part optical brightener,
  • composition A coated particles of Example Ill (composition A) had lost only 5.5% the original available chlorine while the uncoated particles (composition 3) and the spray dried particles (composition C) lost 14% and 14.3% respectively of the original available chlorine.
  • coated polychlorocyanurate particles of the present invention are useful per so as a source of available chlorine in aqueous solution for bleaching, disinfecting and sterilizing purposes.
  • a composition containing about to about 25% available chlorine is more desirable and permits the use of readily available measuring cups to measure the amount of bleaching composition that should be placed in the washing machine.
  • Compositions containing available chlorine in this range can be obtained by using the appropriate amount of coating material in the process or a lesser amount of coating material can be used and the final dry product from the fluidized bed can be diluted with additional dry inorganic material to provide the desired available chlorine content.
  • a composition containing about available chlorine can be obtained by mixing about 35 parts of the product obtained in Example III with about 65 parts of a spraydried mixture of sodium tripolyphosphate and sodium sulfate having about the same particle size as the fluidized bleach product.
  • a bleach containing detergent product is obtained by mixing about parts of the product of Example 111 with about 80 parts of a conventional spraydried, heavy-duty granular detergent.
  • the process of this invention is useful for coating dry chlorinated organic bleaching compounds other than the polychlorocyanurates which are preferred and which are emphasized herein because of their excellent stability and bleaching efliciency characteristics.
  • dry N-chlorinated organic bleaching compounds are: 1,3- dichloro-5,5-dimethyl hydantoin; N,N-dic lorobenzoyleneurea; paratoluene sulfondichloroamide; trichloromelamine; ILchloroammeline; N-chloro succinimide; N,N-dichloroazodicarbonamidine; N-cllloro acetyl urea; N,N- dichlorobiuret; chlorinated dicyandiamide.
  • a dry granular bleach composition comprising the steps of (1) forming a fluidized bed consisting of a dense phase bounded by an upper free surface by passing a distributed ascending current of gas at a predetermined velocit ranging from about '1 ft./ sec. to about 10 ft./sec. measured above said free surface, through a mass of solid particles of a polychlorocyanurate, having a particle size of from about S to about 5 mm., (2) heating said bed to a temperature in the range of about 100 F.
  • said slurry containing from about 30% to about Water, (4) maintaining said bed in said temperature range until the free moisture content of said coated particles is from about 1% to about 15%, (5) drying said coated particles to a free moisture content of 0% to about 2% at a temperature in the range of about 190 F. to about 240 F.
  • step (5) The process of claim 1 wherein the drying of the coated particles in step (5) is effected in a fluidized bed of said particles.
  • polychlorocyanurate is selected from the group consisting of sodium and potassium dichlorocyanurates
  • the aqueous slurry contains from 0% to about 1.5% of an anionic organic detergent and the coating material is sodium tripolyphosphate.
  • the polychlorocyanurate is selected from. the group consisting of sodium and potassium dichlorocyanura-tes
  • the aqueous slurry contains from 0% to 1.5% of an anionic organic detergent
  • the coating material is a mixture of sodium tripolyphosphate and sodium sulfate wherein the amount of sodium sulfate is up to three times the amount of sodium tripolyphosphate.
  • a dry granular bleach composition comprising the steps of (1) forming a fluidized bed consisting of a dense phase bounded by an upper free surface by passing a distributed ascending current of air at a predetermined velocity, ranging from about 1 ft./sec. to about 10 ft./sec. measured above said free surface, through a mass of solid particles of a polychlorocyanurate having a particle size of from about 5/.L to about 5 mm. selected from the group consisting of sodium and potassium dichlorocyanurates, (2) heating said bed to a temperature in the range of r -F.
  • the process of continuously making a granular bleach composition comprising the steps of (1) forming an initial fluidized bed consisting of a dense phase bounded by an upper free surface by passing a distributed ascending current of air at a predetermined velocity, ranging from about 1 ft./sec. to about 10 ft./sec. measured above said free surface, through a mass of solid particles of a polychlorocyanurate having a particle size of from about 5a to about 5 mm, (2) heating said bed to a temperature in the range of 120 F.

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US3248330A (en) * 1963-05-24 1966-04-26 Monsanto Co Process for preparing a stable, freeflowing dishwashing composition
US3289312A (en) * 1964-03-17 1966-12-06 Fmc Corp Drying of chlorinated isocyanurates and salts thereof
US3303104A (en) * 1963-12-12 1967-02-07 Lever Brothers Ltd Compositions containing discoloration inhibitors
US3330766A (en) * 1963-11-08 1967-07-11 Lever Brothers Ltd Discoloration inhibitors
US3346502A (en) * 1962-02-09 1967-10-10 Colgate Palmolive Co Bleaching composition
US3350318A (en) * 1964-02-18 1967-10-31 Fmc Corp Method of producing detergent composition
US3356612A (en) * 1965-02-01 1967-12-05 Petrolite Corp Stable detergent compositions
US3364053A (en) * 1963-10-12 1968-01-16 Polymer Corp Method of coating articles
US3441507A (en) * 1965-07-03 1969-04-29 Henkel & Cie Gmbh Bleaching detergents and washing adjuvants
US3459665A (en) * 1965-03-27 1969-08-05 Henkel & Cie Gmbh Bleaching detergents and washing adjuvants
US3475195A (en) * 1964-12-01 1969-10-28 Potasse & Engrais Chimiques Process and apparatus for granulating paste
US3639256A (en) * 1970-05-27 1972-02-01 Ncr Co Encapsulation process by complex coacervation using inorganic polymers
US3800740A (en) * 1972-12-14 1974-04-02 Int Nickel Co Apparatus for decomposition of metal carbonyls
US3819526A (en) * 1970-12-23 1974-06-25 Philadelphia Quartz Co Coated detergent compositions
US3872024A (en) * 1970-05-27 1975-03-18 Ncr Co Encapsulation process by simple coacervation using inorganic polymers
US3908045A (en) * 1973-12-07 1975-09-23 Lever Brothers Ltd Encapsulation process for particles
US3983254A (en) * 1973-12-07 1976-09-28 Lever Brothers Company Encapsulation particles
US4237814A (en) * 1972-12-13 1980-12-09 Laszlo Balla Apparatus for the continuous production and coating of granulates in fluidized layer
US4279764A (en) * 1980-06-30 1981-07-21 Fmc Corporation Encapsulated bleaches and methods of preparing them
US4427417A (en) 1982-01-20 1984-01-24 The Korex Company Process for preparing detergent compositions containing hydrated inorganic salts
US4464281A (en) * 1983-07-28 1984-08-07 Lever Brothers Company Stabilized bleach-sensitive dyes in automatic dishwasher detergent compositions
US4526699A (en) * 1983-10-17 1985-07-02 Fmc Corporation Encapsulated bleach composition and method of preparation
US4655780A (en) * 1985-12-31 1987-04-07 Lever Brothers Company Encapsulated bleach particles coated with a mixture of C16 -C18 and C12 -C14 fatty acid soaps
US4657784A (en) * 1986-03-10 1987-04-14 Ecolab Inc. Process for encapsulating particles with at least two coating layers having different melting points
US4681696A (en) * 1984-06-19 1987-07-21 Chemed Corporation Solid stabilized active halogen-containing detergent compositions and methods
US4707160A (en) * 1985-12-31 1987-11-17 Lever Brothers Company Particles containing active halogen bleach in a diluted core
US4759956A (en) * 1987-05-22 1988-07-26 Lever Brothers Company Process for encapsulating particles using polymer latex
US4863632A (en) * 1986-11-14 1989-09-05 Lever Brothers Company Encapsulated bleach particles for machine dishwashing compositions
US4909956A (en) * 1988-09-09 1990-03-20 Olin Corporation Chlorine bleach compositions with reduced fabric dye attack
WO1990002832A1 (en) * 1988-09-01 1990-03-22 Olin Corporation Chlorine bleach compositions with reduced fabric dye attack
US5213705A (en) * 1985-04-30 1993-05-25 Ecolab Inc. Encapsulated halogen bleaches and methods of preparation and use
US5614485A (en) * 1990-07-10 1997-03-25 The Procter & Gamble Company Process for making a granular dishwashing composition by agglomerating ingredients and admixing solid alkali metal silicate
US5616277A (en) * 1991-08-13 1997-04-01 The Procter & Gamble Company Incorporating nonionic surfactant into silicate for granular automatic dishwashing detergent composition

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SE424739B (sv) * 1977-05-26 1982-08-09 Elektrokemiska Ab Granuler ravara for maskindiskmedel-, avfettningsmedel-, och rengorings-medelskomposition och forfarande for dess framstellning
GB2182864B (en) * 1985-11-14 1989-10-04 Nickerson Seed Company Limited Coating of flowable granular material
US4713079A (en) * 1985-12-31 1987-12-15 Lever Brothers Company Particles containing dihalohydantoin bleach in a diluted core
EP0436971B1 (en) * 1989-11-15 1997-12-17 Unilever N.V. Wax encapsulated bleach particles and method for making same
GB9712583D0 (en) 1997-06-16 1997-08-20 Unilever Plc Production of detergent granulates
GB9712580D0 (en) * 1997-06-16 1997-08-20 Unilever Plc Production of detergent granulates
GB9713748D0 (en) * 1997-06-27 1997-09-03 Unilever Plc Production of detergent granulates

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US2308992A (en) * 1937-10-03 1943-01-19 Procter & Gamble Method for producing washing, cleansing, bleaching, and rinsing agents containing percompounds
US2465346A (en) * 1943-07-15 1949-03-29 Lever Brothers Ltd Dedusting process and product thereof
US2561392A (en) * 1945-08-11 1951-07-24 Donald E Marshall Process and apparatus for treating solutions to recover and coat solid particles
US2586818A (en) * 1947-08-21 1952-02-26 Harms Viggo Progressive classifying or treating solids in a fluidized bed thereof
USRE24412E (en) * 1948-06-25 1957-12-31 Bleaching
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US2776943A (en) * 1951-05-14 1957-01-08 Procter & Gamble Treatment of soap particles
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US2795556A (en) * 1954-07-26 1957-06-11 Theobald Ind Composition providing available chlorine and process of making same
BE551308A (el) * 1955-05-09
US2889283A (en) * 1956-04-23 1959-06-02 Procter & Gamble Process for making detergent composition
US2897154A (en) * 1956-07-30 1959-07-28 Purex Corp Ltd Bleaching and disinfecting compositions
US2913460A (en) * 1956-09-10 1959-11-17 Procter & Gamble Composition having bleaching, sterilizing and disinfecting properties, and method of preparation thereof
US2921911A (en) * 1958-01-10 1960-01-19 Pennsalt Chemicals Corp Oxidizing compositions

Cited By (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3346502A (en) * 1962-02-09 1967-10-10 Colgate Palmolive Co Bleaching composition
US3248330A (en) * 1963-05-24 1966-04-26 Monsanto Co Process for preparing a stable, freeflowing dishwashing composition
US3364053A (en) * 1963-10-12 1968-01-16 Polymer Corp Method of coating articles
US3330766A (en) * 1963-11-08 1967-07-11 Lever Brothers Ltd Discoloration inhibitors
US3303104A (en) * 1963-12-12 1967-02-07 Lever Brothers Ltd Compositions containing discoloration inhibitors
US3350318A (en) * 1964-02-18 1967-10-31 Fmc Corp Method of producing detergent composition
US3289312A (en) * 1964-03-17 1966-12-06 Fmc Corp Drying of chlorinated isocyanurates and salts thereof
US3475195A (en) * 1964-12-01 1969-10-28 Potasse & Engrais Chimiques Process and apparatus for granulating paste
US3356612A (en) * 1965-02-01 1967-12-05 Petrolite Corp Stable detergent compositions
US3459665A (en) * 1965-03-27 1969-08-05 Henkel & Cie Gmbh Bleaching detergents and washing adjuvants
US3441507A (en) * 1965-07-03 1969-04-29 Henkel & Cie Gmbh Bleaching detergents and washing adjuvants
US3639256A (en) * 1970-05-27 1972-02-01 Ncr Co Encapsulation process by complex coacervation using inorganic polymers
US3872024A (en) * 1970-05-27 1975-03-18 Ncr Co Encapsulation process by simple coacervation using inorganic polymers
US3819526A (en) * 1970-12-23 1974-06-25 Philadelphia Quartz Co Coated detergent compositions
US4237814A (en) * 1972-12-13 1980-12-09 Laszlo Balla Apparatus for the continuous production and coating of granulates in fluidized layer
US3800740A (en) * 1972-12-14 1974-04-02 Int Nickel Co Apparatus for decomposition of metal carbonyls
US3983254A (en) * 1973-12-07 1976-09-28 Lever Brothers Company Encapsulation particles
US3908045A (en) * 1973-12-07 1975-09-23 Lever Brothers Ltd Encapsulation process for particles
US4279764A (en) * 1980-06-30 1981-07-21 Fmc Corporation Encapsulated bleaches and methods of preparing them
US4427417A (en) 1982-01-20 1984-01-24 The Korex Company Process for preparing detergent compositions containing hydrated inorganic salts
US4464281A (en) * 1983-07-28 1984-08-07 Lever Brothers Company Stabilized bleach-sensitive dyes in automatic dishwasher detergent compositions
US4526699A (en) * 1983-10-17 1985-07-02 Fmc Corporation Encapsulated bleach composition and method of preparation
US4681696A (en) * 1984-06-19 1987-07-21 Chemed Corporation Solid stabilized active halogen-containing detergent compositions and methods
US5213705A (en) * 1985-04-30 1993-05-25 Ecolab Inc. Encapsulated halogen bleaches and methods of preparation and use
US4707160A (en) * 1985-12-31 1987-11-17 Lever Brothers Company Particles containing active halogen bleach in a diluted core
US4655780A (en) * 1985-12-31 1987-04-07 Lever Brothers Company Encapsulated bleach particles coated with a mixture of C16 -C18 and C12 -C14 fatty acid soaps
US4657784A (en) * 1986-03-10 1987-04-14 Ecolab Inc. Process for encapsulating particles with at least two coating layers having different melting points
US4731195A (en) * 1986-03-10 1988-03-15 Ecolab Inc. Encapsulated bleach particles with at least two coating layers having different melting points
US4863632A (en) * 1986-11-14 1989-09-05 Lever Brothers Company Encapsulated bleach particles for machine dishwashing compositions
US4759956A (en) * 1987-05-22 1988-07-26 Lever Brothers Company Process for encapsulating particles using polymer latex
WO1990002832A1 (en) * 1988-09-01 1990-03-22 Olin Corporation Chlorine bleach compositions with reduced fabric dye attack
US4909956A (en) * 1988-09-09 1990-03-20 Olin Corporation Chlorine bleach compositions with reduced fabric dye attack
WO1990002833A1 (en) * 1988-09-09 1990-03-22 Olin Corporation Chlorine bleach compositions with reduced fabric dye attack
US5614485A (en) * 1990-07-10 1997-03-25 The Procter & Gamble Company Process for making a granular dishwashing composition by agglomerating ingredients and admixing solid alkali metal silicate
US5616277A (en) * 1991-08-13 1997-04-01 The Procter & Gamble Company Incorporating nonionic surfactant into silicate for granular automatic dishwashing detergent composition

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