MXPA99003200A - Process for making a detergent composition by non-tower process - Google Patents

Abstract

A non-tower process for continuously preparing granular detergent composition having a density of at least about 600 g/l is provided. The process comprises the steps of:(a) dispersing a surfactant, and coating the surfactant with fine powder in a mixer, wherein first agglomerates are formed;(b) spraying finely atomized liquid onto the first agglomerates in a mixer, wherein second agglomerates are formed;and (c) granulating the third agglomerates in one or more fluidizing apparatus. The process can also comprise further step (b'), i.e., thoroughly mixing the second agglomerates in a mixer, between step (b) and step (c).

Description

PROCEDURE TO MAKE A COMPOSITION DETERGENT BY A PROCEDURE THAT IS NOT A TOWER FIELD OF THE INVENTION In general terms, the present invention relates to a non-tower process for producing a particulate detergent composition. More particularly, the invention is directed to a continuous process during which detergent agglomerates are produced by introducing a surfactant and coating materials into a series of mixers. The process produces a free-flowing detergent composition, the density of which can be adjusted for a wide range of consumer needs, and which can be sold commercially.

BACKGROUND OF THE INVENTION Recently, there has been considerable interest within the detergent industry for "compact" laundry detergents and, therefore, having low dosage volumes. To facilitate the production of these so-called low dosage detergents, many attempts have been made to produce high density global detergents, for example, with a density of 600 g / l or more. Low dosage detergents are currently in high demand because they conserve resources and can be marketed in small packages that are more convenient for consumers. However, the degree to which modern detergent products need to be "compact" in nature remains variable. In fact, many consumers, especially in developing countries, continue to prefer higher dosage levels in their respective laundry operations. In general, there are two main types of procedures by which granules or detergent powders can be prepared. The first type of process involves spray drying an aqueous detergent suspension in a spray drying tower to produce highly porous detergent granules (eg, tower process for low density detergent compositions). In the second type of process, the different detergent components are mixed dry, after which they are agglomerated with a binder such as anionic or nonionic surfactant to produce high density detergent compositions (e.g., agglomeration process). to produce high density detergent compositions). In the two previous processes, the important factors that determine the density of the resulting detergent granules are the shape, porosity and particle size distribution of said granules, the density of the different starting materials, the shape of the different starting materials. , and its respective chemical composition. There have been many attempts in the art to provide methods that increase the density of detergent granules or powders. Particular attention has been given to the densification of spray-dried granules by post-drying treatment in the tower. For example, an attempt involves an intermittent procedure in which granular or spray-dried detergent powders containing sodium tripolyphosphate and sodium sulfate are densified and spheronized in a Marumerizer®. This apparatus comprises a rotating table, made rough and substantially horizontal, located inside and at the base of a substantially vertical smooth wall cylinder. However, this process is essentially an intermittent process and is therefore less convenient for the large-scale production of detergent powders. More recently, other attempts have been made to provide continuous processes to increase the density of spray-dried or post-tower detergent granules. Typically, said processes require a first apparatus that pulverizes or crushes the granules, and a second apparatus that increases the density of the pulverized granules by agglomeration. Although these procedures achieve the desired increase in density by treating or densifying spray-dried or post-tower granules, are limited in their ability to go further at the surfactant level without a subsequent coating step. In addition, the treatment or densification by "post tower" treatment is not favorable in terms of economy (high cost of capital) and complexity of operation. In addition, all of the aforementioned processes are directed primarily to densify or otherwise process spray-dried granules. Currently, the relative amounts and types of materials subjected to spray drying processes in the production of detergent granules have been limited. For example, it has been difficult to achieve high levels of surfactant in the resulting detergent composition, a feature that facilitates the production of detergents more efficiently. Thus, it would be convenient to have a method by which detergent compositions can be produced without having the limitations imposed by conventional spray drying techniques. To that end, the technique is also replete with descriptions of procedures involving agglomerating detergent compositions. For example, attempts have been made to agglomerate builders by mixing zeolite and / or layered silicates in a mixer to form free flowing agglomerates. Although such attempts suggest that their process can be used to produce detergent agglomerates, they do not provide a mechanism by which starting detergent materials in the form of pastes, liquids and dry materials can effectively agglomerate into crisp and free-flowing detergent agglomerates.

Accordingly, there remains a need in the art to have an agglomeration process (other than tower) to continuously produce a detergent composition having high density produced directly from the starting detergent ingredients, and preferably that the density can be achieved adjusting the conditions of the procedure. Likewise, there is a need for such a process that is more efficient, flexible and economical to facilitate the large-scale production of detergents (1) for flexibility in the final density of the final composition and (2) for flexibility in terms of incorporating Several different types of detergent ingredients (especially liquid ingredients) in the procedure. The following references are directed to densify spray-dried granules: Appel et al., US patent. No. 5,133,924 (Lever); Bortolotti et al., Patent of E.U. No. 5,160,657 (Lever); Johnson et al., British Patent No. 1,517,713 (Unilever); and Curtis, European patent application 451.894. The following references are directed to producing detergents by agglomeration: Beujean et al., Document open to the public No. WO93 / 23,523 (Henkel), Lutz et al., US patent. No. 4,992,079 (FMC Corporation), Porasik et al., U.S. Patent. No. 4,427,417 (Korex); Beerse et al., Patent of E.U. No. 5,108,646 (Procter &Gamble); Capeci et al., Patent of E.U. No. 5,366,652 (Procter &Gamble); Hollingsworth et al., European patent application 351,937 (Unilever); Swatling et al., US patent. No. 5,205,958; Dhalewadikar et al., Open document No. WO96 / 04359 (Unilever). For example, open document No. WO93 / 23,523 (Henkel) describes the process comprising pre-agglomeration by means of a low speed mixer and an additional agglomeration step by means of a high speed mixer to obtain a high density detergent composition, in where less than 25% by weight of the granules have a diameter greater than 2 mm. The patent of E.U.

No. 4,427,417 (Korex) describes a continuous process for agglomeration that reduces the formation of cake and agglomerates of very large size. None of the documents of the existing technique provides all the advantages and benefits of the present invention.

BRIEF DESCRIPTION OF THE INVENTION The present invention meets the aforementioned needs in the art by providing a process that allows to produce a low density granular detergent composition. The present invention also satisfies the aforementioned needs in the art, by providing a process that allows to produce a granular detergent composition for flexibility in the final density of the final composition from an agglomeration process (for example, that is not tower) . The process does not make use of conventional spray drying towers, which is currently limited to produce high load compositions of surfactants. In addition, the process of the present invention is more efficient, economical and flexible with respect to the variety of detergent compositions that may be produced in the process. In addition, the procedure is more amenable to environmental aspects, because it does not use spray-drying towers that typically emit particles and volatile organic compounds into the atmosphere. As used herein, the term "agglomerates" refers to particles formed by agglomerating raw materials with binder, such as surfactants and / or inorganic solutions / organic solvents and polymer solutions. As used herein, the term "average residence time" refers to the following definition: mean residence time (hr) = mass (kg) / flow out (kg / hr) All percentages used herein they are expressed as "percent by weight", unless otherwise indicated. All relationships are weight ratios unless otherwise indicated. As used in the present, "comprises" means that other steps and other ingredients may be added that do not affect the result. This term encompasses the terms "consisting of" and "consisting essentially of". According to one aspect of the invention, there is provided a process for preparing a granular detergent composition having a density of at least about 600 g / l. The method comprises the steps of: (a) dispersing a surfactant and coating the surfactant with fine powders having a diameter of 0.1 to 500 microns, in a mixer in which the conditions include (i) from about 2 to about 50 seconds of average residence time, (i) from about 4 to about 25 m / s of tip speed and (iii) from about 0.15 to about 7 kj / kg of energy condition, where first are formed agglomerated; (b) sprinkling finely atomized liquid on the first agglomerates in a mixer, wherein the conditions of the mixer include (i) from about 0.2 to about 5 seconds of average residence time, (ii) from about 10 to about 30 m / s of tip speed, and (ii) from about 0.15 to about 5 kj / kg of energy condition, where second agglomerates are formed; and (c) granulating the agglomerated seconds in one or more fluidization apparatuses, wherein the conditions of each of the fluidization apparatuses include: (i) from about 1 to about 10 minutes of average residence time, (ii) from about 100 to about 300 mm of non-fluidized bed thickness, (iii) not more than about 50 microns of spray droplet size, (iv) from about 175 to about 250 mm of spray height, (v) from about 0.2 to about 1.4 m / s of fluidization velocity, and (vi) from about 12 to about 100 ° C bed temperature. Also provided is a process for preparing a granular detergent composition having a density of at least 600 g / l; the method comprises the steps of: (a) dispersing a surfactant and coating the surfactant with fine powders having a diameter of 0.1 to 500 microns, in a mixer in which the conditions include (i) from about 2 to about 50 seconds of average residence time, (i) from about 4 to about 25 m / s peak speed and (m) from about 0.15 to about 7 kj / kg of energy condition, where first are formed agglomerates; (b) sprinkling finely atomized liquid on the first agglomerates in a mixer, wherein the conditions of the mixer include (i) from about 0.2 to about 5 seconds of average residence time, (ii) from about 10 to about 30 m / s of tip speed, and (ii) from about 0.15 to about 5 kj / kg of energy condition, where second agglomerates are formed; (b ') completely mixing the agglomerated seconds in a mixer where the conditions of the mixer include (i) from about 0.5 to about 15 minutes of average residence time and (i) from about 0.15 to about 7 kj / kg condition of energy, where agglomerated third parties are formed; and (c) granulating the agglomerated third in one or more fluidization apparatuses, wherein the conditions of each of the fluidization apparatuses include: (i) from about 1 to about 10 minutes of average residence time, (i) ) from about 100 to about 300 mm of non-fluidized bed thickness, (iii) no more than about 50 microns of spray droplet size, (iv) from about 175 to about 250 mm of spray height, (v) ) from about 0.2 to about 1.4 m / s of fluidization velocity, and (vi) from about 12 to about 100 ° C bed temperature. Granular detergent compositions having a density greater than at least about 600 g / l, produced by any of the process modalities described in the present specification, are also provided. Accordingly, an object of the invention is to provide a method for continuously producing a detergent composition having flexibility with respect to the density of the final products, controlling the energy input, residence time condition, and tip speed condition in the mixers. It is also an object of the invention to provide a process that is more efficient, flexible and economical to facilitate large-scale production. These and other concomitant objects, features and advantages of the present invention will become apparent to those skilled in the art upon reading the following detailed description of the preferred embodiment and the appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a flow chart of a process according to one embodiment of the invention, including the agglomeration process with the first mixer, followed by the second mixer, then the fluidizing apparatus, to produce a granular detergent composition which It has a density of at least 600 g / l. Figure 2 is a flow diagram of a process according to an embodiment of the invention, including the agglomeration process with the first mixer, followed by the second mixer, then the third mixer and finally the fluidizing apparatus, to produce a granular detergent composition having a density of at least 600 g / l. Figure 3 is a flow chart of a process that is suitable for performing a variety of agglomeration processes, selected from the group consisting of agglomeration in the first mixer, the second mixer, the third mixer, the fluidization apparatus, and the combination thereof, to produce a granular detergent composition.

DETAILED DESCRIPTION OF THE PREFERRED MODALITY The present invention is directed to a process that produces free flowing granular detergent agglomerates having a density of at least about 600 g / l. The process produces granular detergent agglomerates from an aqueous and / or non-aqueous surfactant which is then coated with fine powders having a diameter of 0.1 to 500 microns, to obtain low density granules.

Procedure Reference is now made to Figure 1, which presents a flow chart illustrating an embodiment of the present invention, ie, a method comprising the first step, the second step (i) and the third step below; and Figure 2 which presents a flow chart illustrating an embodiment of the present invention, ie, a method comprising the first step, the second steps (i) and (ii) and the third step below. Another reference is made to Figure 3, which presents a flow chart illustrating various embodiments included by the present invention.

First step fStep In the first step of the process, one or more surfactants, 11, aqueous and / or non-aqueous surfactants, which are in the form of powder, paste and / or liquid, are introduced into a first mixer, 13. and fine powders, 12, having a diameter of 0.1 to 500 microns, preferably of about 1 to about 100 microns, to make agglomerates (The definition of surfactants and fine powders is given in detail below). , in addition to the fine powders, a stream of internal recirculation of powders, having a diameter of about 0.1 to about 300 microns can be introduced into the mixer, which can be generated from a fluidization apparatus, 27 which is described below in step 3. The amount of said internal powder recirculation stream 30, can be from 0 to about 60% by weight of the final product, 29. In another embodiment of the invention, the surfactant (s) 1 1, can be initially introduced into a mixer or pre-mixer (eg, a conventional worm extruder or other similar mixer) before the above, after which the mixed detergent materials are introduced into the mixer of the first step as described in the present to achieve agglomeration. Generally speaking, preferably the average residence time in the first mixer is on the scale of about 2 to about 50 seconds, and the tip speed of the first mixer is on the scale of about 4 m / s to about 25 m / s, the energy per unit mass of the first mixer (energy condition) is about 0.15 kj / kg to about 7 kj / kg, most preferably, the average residence time of the first mixer is on the scale of about 5 to approximately 30 seconds, and the tip speed of the first mixer is on the scale of about 6 m / s to about 18 m / s, the energy per unit mass of the first mixer (power condition) is on the scale of about 0.3 kj / kg at about 4 kj / kg, and most preferably, the average residence time of the first mixer is on the scale of about 5 to about 20 seconds, and the tip speed of the first mixer is on the scale of about 8 m / s at approximately 18 m / s, and the energy per unit mass of the first mixer (energy condition) is on the scale of about 0.3 kj / kg to about 4 kj / kg. Examples of mixers for the first step can be any type of mixer known to those skilled in the art, as long as the mixer can maintain the conditions mentioned above for the first step. An example can be the Lódige CB mixer, manufactured by the company Lódige (Germany). As a result of the first step, the product 16 is obtained (first agglomerates having fine powders on the surface thereof).

Second step fStep (bVStep (b ') 1 As a preferred modality, there are two types of options, that is, the second step (i) alone, or the second step (i) followed by the second step (i). step (i) Step (b): The resulting product 16, ie, the first agglomerates, are introduced into a second mixer, 17, and then finely atomized liquid, 18, is sprinkled on the first agglomerates in the mixer 17. Optionally, the fine powders in excess formed in the first step are added to the second step If optionally added in the second step (i) excess fine powders, it is useful to spray the finely atomized liquid to bind the excess fine powders on the agglomerate surface 17 about 0-10%, most preferably about 2-5% powdered detergent ingredients of the type used in the first step, and / or other detergent ingredients can be added to the mixer 17.

Generally speaking, preferably, the average residence time of the second mixer is on the scale of about 0.2 to about 5 seconds and the tip speed of the second mixer is on the scale of about 10 m / s to about 30 m / s, the energy per unit mass of the second mixer (energy condition) is on the scale of about 0.15 kj / kg to about 5 kj / kg, most preferably, the average residence time of the second mixer is on the scale of about 0.2 to about 5 seconds, and the tip speed of the second mixer is in the range of about 10 m / s to about 30 m / s, the energy per unit mass of the second mixer (power condition) is in the scale of about 0.15 kj / kg to about 5 kj / kg, and most preferably, the average residence time of the second mixer is on the scale of about 0.2 to about 5 seconds, the speed of The tip of the second mixer is on the scale of about 15 m / s to about 26 m / s, the energy per unit mass of the second mixer (energy condition) is on the scale of about 0.2 kJ / kg to about 3 kj / kg. The examples of the second mixer 17 can be any type of mixer known to those skilled in the art, provided that the mixer can maintain the conditions mentioned above for the second step (i). An example can be the Flexomic model manufactured by the company Schugi (Holland). As a result of the second step, the resulting product 20 is obtained. The resulting product (second agglomerates) is then subjected to either the second step (ii) or the third step. Second step (ii) [Step (b ') 1: The resulting product 20 (second agglomerates of the second step (i) is introduced into a third mixer 21. Namely, the product resulting from the second mixer is mixed and subjected to shear completely to round and grow the agglomerates in the third mixer 21. Optionally, about 0-10%, most preferably about 2-5%, of powdered detergent ingredients of the type used in the second step can be added to the second step (ii). the first step and / or the second step (i), and / or other detergent ingredients Preferably, grinders that can be fixed to the third mixer can be used to break up and separate the undesirable larger sized agglomerates. The process including the third mixer 21 with grinders is useful for obtaining a reduced quantity of agglomerates of larger size as final products, and said process is a preferred embodiment of the present invention. In general terms, preferably the average residence time of the third mixer is on the scale of about 0.5 to about 15 minutes, and the energy per unit mass of the second mixer (energy condition) is on the scale of about 0.15 to about 7 kj / kg, most preferably, the average residence time of the third mixer is on the scale of about 3 to about 6 minutes and the energy per unit mass of the second mixer (energy condition) is on the scale of about 0.15 to approximately 4 kj / kg. The examples of the third mixer 21 can be any type of mixer known to those skilled in the art., provided that the mixer can maintain the conditions mentioned above for the second step (ii). An example can be the Lódige KM mixer manufactured by the company Lódige (Germany). As a result of the second step (ii), the product 24 is obtained, that is, rounded granules.

Step Three Step (c) l In the third step of the process, the product resulting from the second step, i.e., a resulting product 20 or a resulting product 24, is introduced into a fluidization apparatus 27, such as a fluidized bed, for improve the granulation to produce high density granules of free flow. The third step can proceed in one or more fluidized bed apparatus (e.g., by combining different types of fluidization apparatus, such as a fluid bed dryer and a fluid bed cooler). In the third step, the product resulting from the second step is completely fluidized so that the granules of the third step acquire a round shape. Optionally, about 0 to about 10%, preferably about 2-5%, of powdered detergent materials of the type used in the first step and / or other detergent ingredients can be added to the third step. Also optionally, about 0 to about 20%, preferably about 2 to about 10%, of liquid detergent materials of the type used in the first step, the second step and / or other detergent ingredients can be added in this step to improve the granulation and the coating on the surface of the granules. Generally speaking, to achieve the density of at least about 600 g / l, preferably more than 650 g / l, the conditions of a fluidization apparatus may be: Average residence time: from about 1 to about 10 minutes. Thickness of the non-fluidized bed: from approximately 100 to approximately 300 mm. Spray drop size: no more than about 50 microns. Spray height: from approximately 175 to approximately 250 mm. Fluidized speed: from about 0.2 to about 1.4 m / s Bed temperature: from about 12 to about 100 ° C, most preferably: Average residence time: from approximately 2 to approximately 6 minutes. Thickness of the non-fluidized bed: from about 100 to about 250 mm. Spray drop size: less than about 50 microns. Spray height: from approximately 175 to approximately 200 mm. Fluidized speed: from approximately 0.3 to approximately 1.0 m / s. Bed temperature: from about 12 to about 80 ° C. If two different types of fluidized apparatuses are used, the average residence time of the third step can be in total from about 2 to about 20 minutes, most preferably about 2 to 12 minutes. A coating agent may be added to improve the flowability and / or minimize over-agglomeration of the detergent composition, at one or more of the following points of the present process: (1) the coating agent may be added directly after use the fluid bed cooler, or the fluid bed dryer; (2) the coating agent can be added between the fluid bed dryer and the fluid bed cooler; and / or (3) the coating agent can be added directly to the third mixer 21 and the fluid bed dryer. The coating agent is preferably selected from the group consisting of aluminosilicates, silicates, carbonates, and mixtures thereof. The coating agent not only improves the free fluidity of the resulting detergent composition, which is desirable by consumers since it allows easy evaluation of the detergent during use, but also serves to control the agglomeration, preventing or minimizing over agglomeration. As those skilled in the art will know, over-agglomeration can lead to very inconvenient flow and aesthetic properties of the final detergent product. In case the process of the present invention is carried out using (1) a CB mixer having flexibility to inject at least two liquid ingredients; (2) a Schugi mixer that has the flexibility to inject at least two liquid ingredients; (3) a KM mixer having flexibility to inject at least one liquid ingredient; (4) A fluidized bed (fluid) having flexibility to inject at least two liquid ingredients, the process can incorporate seven different types of liquid ingredients therein. Therefore, the proposed method is beneficial for the person skilled in the art to incorporate in a granule manufacturing process, starting detergent materials that are in liquid form and are rather expensive and sometimes more difficult in terms of handling and / or storage than solid materials. The proposed invention is also useful in view of the industrial requirement, because the person skilled in the art can establish a series of apparatuses in a plant (e.g., shown in Figure 3), and using diverters that can be connected / disconnected. between each apparatus, so that one skilled in the art can select process variations to satisfy the desired property (e.g., particle size, density, formula design) of the final product. Said variations include not only the method of the present invention, ie, as shown in Figure 3, (i) first mixer 13- (line 16) - second mixer 17- line (26) - fluidizing apparatus 27-line 28) - final product 29, (ii) first mixer 13 - (line 16) - second mixer 17 - (line 20) - third mixer 21 - (line 24) - fluidising apparatus 27 - (line 28) - final product 29 , but also include (iii) first mixer 17 - (line 16) - third mixer 21 - (line 24) - fluidizing apparatus 27 - (line 28) - end product 29, (iv) first mixer 13 - (line 16 ' ) - third mixer 21 - (line 23) - second mixer 17 - (line 26) - fluidizing apparatus 27 - (line 28) - final product 29, and (v) first mixer 13 - (line 16") - apparatus fluidized 27 - (line 28) - final product 29.

Starting Detergent Materials The total amount of the surfactants in the products prepared by the present invention, which include the following finely atomized liquid detergent materials and auxiliary detergent ingredients, is generally from about 5% to about 60%, more preferably from about 12% to about 40%, most preferably from about 15% to about 35%, on percentage scales. The surfactants that are included in the above can be from any point in the process of the present invention, for example, any of the first step, the second step and / or the third step of the present invention.

Detergent surfactant (aqueous / non-aqueous) The amount of the surfactant of the present process can be from about 5% to about 60%, more preferably about 12% to about 40%, most preferably from about 15% to about 35%, in the total amount of the final product obtained by the process of the present invention. The surfactant of the present process, which is used as the starting detergent material mentioned above in the first step, is in the form of powder, paste or liquid raw material. The surfactant itself is preferably selected from anionic, nonionic, zwitterionic, amphoteric and cationic classes, and compatible mixtures thereof. Detergent surfactants useful herein are described in the U.S. patent. 3,664,961, Norris, issued May 23, 1972, and the US patent. 3,929,678, Laughlin et al., Issued December 30, 1975, which are incorporated herein by reference. Useful cationic surfactants also include those described in the US patent. 4,222,905, Cockrell, issued September 16, 1980, and in the US patent. 4,239,659, Murphy, issued December 16, 1980, which are also incorporated herein by reference. Of the surfactants, anionics and nonionics are preferred, with anionics being more preferred. Non-limiting examples of the preferred anionic surfactants, useful in the present invention, include the C-alkyl-alkyl sulfonates; «| -C- | 8 conventional (" LAS "), C-10-C20 (" AS ") alkyl sulfates primary, branched chain and random, secondary alkyl sulfates (2,3) of C- | o-C < | 8 of the formula CH3 (CH2) x (CHOSO3-M +) CH3 and CH3 (CH2) and (CHOS? 3-M +) CH2CH3j where xy (y +1) are integers of at least about 7, preferably of at least about 9, and M is a cation of solubilization in water, especially sodium, unsaturated sulfates such as oleyl sulfate and the alkylalkoxy sulfates of C "| rj-C- | 8 (" AEXS ", especially ethoxysulfates EO 1-7). Useful anionic surfactants also include water-soluble salts of 2-acyloxy-alkan-1-sulfonic acids containing from about 2 to 9 carbon atoms in the acyl group, and from about 9 to about 23 carbon atoms in the alkane portion; water-soluble olefin sulphonates containing about 12 to 24 carbon atoms, and beta-alkyloxy alkan sulfonates containing from about 1 to about 3 carbon atoms in the alkyl group, and about 8 to 20 carbon atoms in the alkane portion. Other examples of Useful surfactants in the paste of the invention include C- * alkylalkoxycarboxylates? o-C- | 8 (especially the ethoxycarboxylates EO 1-5), the glycerol ethers of C10-C18. Alkyl polyglycosides of C- | () - C "| 8 and their corresponding sulfated polyglycosides, and alphasulfonated fatty acid esters of C- | 2-Ci8- If desired, conventional amphoteric and nonionic surfactants such as alkyl ethoxylates of C12-C18 ("AE") including the so-called narrow peak alkyl ethoxylates and the C6-C12 alkylphenolalkoxylates (especially ethoxylates and ethoxy / mixed propoxy), amine oxides of C <;? o-C- | 8, and the like, can also be included in the global compositions. The N-alkyl polyhydroxy fatty acid amides of C-jo-C-iß- can also be used. Typical examples include C-12-C18 N-methylglucamides. See WO 9,206,154. Other surfactants derived from sugar include the N-alkoxy polyhydroxy fatty acid amides, such as N-3-methoxypropyl) glucamide of C-10-C- | 8- The glucamides of N-propyl to N-hexyl of C12- C18 can be used for low foam formation. Conventional C-JO-C20 soaps can also be used. If high foaming is desired, branched chain C-iQ-C-iß soaps can be used. Mixtures of anionic and nonionic surfactants are especially useful. Other conventional useful surfactants are mentioned in the normal texts. Cationic surfactants may also be used as a detergent surfactant herein, and suitable quaternary ammonium surfactants are selected from N-alkyl or alkenyl ammonium mono- or cycloalkyl surfactants, preferably Cg-C-io, wherein the remaining N positions are substituted with methyl, hydroxyethyl or hydroxypropyl groups. Ampholytic surfactants may also be used as the detergent surfactant herein, which include aliphatic derivatives of heterocyclic secondary and tertiary amines; zwitterionic surfactants including derivatives of aliphatic quaternary ammonium, phosphonium and sulfonium compounds; water-soluble salts of esters of fatty acids alphasulfonated; alkyl ether sulfates; water-soluble salts of olefin sulfonates; beta-alkyloxy-alcansulfonates; betaines having the formula R (R1) 2N + R2COO "- wherein R is a hydrocarbyl group of CQ-C Q, preferably an alkyl group of C-jo-C-iß or alkylacylamido group of C- | oC * | 6> R1 is typically C1-C3 alkyl, preferably methyl, and R2 is a C-1-C5 hydrocarbyl group, preferably C-1-C3 alkylene group, more preferably an alkylene group of C1- C2 Examples of suitable betaines include coconut acrylamidopropyldimethylbetaine, hexadecyldimethylbetaine, C-12-C14-acylamidopropylbetaine, C8-C14-acylamidohexyldiethylbetaine, 4-C- [4-i6] -1-carboxybutane [acylmethylamidodiethylammonium], [beta] -C ^ acylamidodimethylbetaine The C-12-C16 acrylamidopentanodiethylbetaine and C-2-C6 acylmethylamidodimethylbetaine The preferred betaines are dimethylammonium hexanoate of C-12-I8 and acetylamidopropane (or ethane) dimethyl (or diethyl) betaines of C- 10-C18; and 'sultaines having the formula R (RI) 2N + R2S03"wherein R is a hydrocarbyl group of CQ-C- Q, preferably a C10-C16 alkyl group, more preferably a C-12-C13 alkyl group, each R ^ is typically C1-C3 alkyl, preferably methyl, and R2 is a Ci-Cß hydrocarbyl group, preferably a C 1 -C 3 alkylene or, preferably, a C 1 -C 3 hydroxyalkylene group. Examples of suitable sultaines include dimethylammonium-2-hydroxypropyl sulphonate of C - ^ - CH, amidopropylammonium-2-hydroxypropyl-sultaine of C-12-C14, dihydroxyethylammonium propanesulfonate of C-12-C14 and dimethylammonium hexansulfonate of Ci6-C- | 8 > the amidopropylammonium-2-hydroxypropyl sultaine of C-12-C14 being preferred.

Fine powders The amount of fine powders of the present process, which are used in the first step, may be from about 94% to 30%, preferably from 86% to 54%, in a total amount of the starting material for the first step . The starting fine powders of the present process are preferably selected from the group consisting of ground soda ash, powdered sodium tripolyphosphate (STPP), hydrated tripolyphosphate, ground sodium sulphates, aluminosilicates, layered crystalline silicates, nitrilotriacetates (NTA), phosphates, precipitated silicates, polymers, carbonates, citrates, pulverized surfactants (such as pulverized alkanesulfonic acids) and internal recirculating powder from the process of the present invention, wherein the average diameter of the powder is from 0.1 to 500 microns, preferably from 1 to 500 microns. 300 microns, more preferably 5 to 100 microns. In case of using STPP hydrated as fine powders of the present invention, STPP which is hydrated to a level of not less than 50% is preferred: The aluminosilicate ion exchange materials used herein as builder have a high capacity of calcium ion exchange and a high exchange rate. Without being intended to be limited by theory, it is thought that said high capacity and rate of calcium ion exchange are a function of several interrelated factors that derive from the method by which the aluminosilicate ion exchange material is produced. In this regard, the aluminosilicate ion exchange materials used herein are preferably produced in accordance with Corkill et al., U.S. Pat. No. 4,605,509 (Procter &Gamble), the disclosure of which is incorporated herein by reference. Preferably, the aluminosilicate ion exchange material is in the "sodium" form, since the potassium and hydrogen forms of the present aluminosilicate do not exhibit a capacity and an ion exchange rate as high as provided by the sodium form. Additionally, preferably the aluminosilicate ion exchange material is in a very dry form to facilitate the production of crisp detergent agglomerates as described herein. The aluminosilicate ion exchange materials used herein preferably have particle size diameters that optimize their effectiveness as builders. The term "particle size diameter", as used herein, represents the average diameter of particle size of a given aluminosilicate ion exchange material determined by conventional analytical techniques, such as microscopic and scanning electron microscopy determination. (SEM). The preferred particle size diameter of the aluminosilicate is from about 0.1 microns to about 10 microns, more preferably from about 0.5 microns to about 9 microns. Most preferably, the diameter of particle size is from about 1 miera to about 8 micras. Preferably, the aluminosilicate ion exchange material has the formula: Naz [(AIO2) z (Si? 2) and] xH2O where z and y are integers of at least 6, the molar ratio z.y is from about 1 to about 5, and x is from about 10 to about 264. More preferably, the aluminosilicate has the formula: Na12 [(Al? 2) i2 (Si? 2) i2] xH20 wherein x is from about 20 to about 30, preferably about 27. These preferred aluminosilicates are commercially available, for example, under the designations Zeolite A, Zeolite B and Zeolite X. Alternatively, naturally occurring aluminosilicate ion exchange materials. or which are synthetically derived and suitable for use herein, can be obtained as described in Krummel et al., US Pat. No. 3, 985,669, the disclosure of which is incorporated herein by reference. The aluminosilicates used herein are further characterized by their ion exchange capacity which is at least about 200 mg hardness equivalents of CaC 3 / g, calculated on an anhydrous basis, and which is preferably on a scale around from 300 to 352 mg hardness equivalents of CaC? 3 / g. Additionally, the aluminosilicate ion exchange materials of the present are further characterized by their calcium ion exchange rate, which is at least about 2 grains of Ca ++ / 3.785 liters / minute / gram / 3.785 liters, and more preferably on a scale of about 2 grains of Ca ++ / 3.785 liters / minute / gram / 3.785 liters to about 6 grains of Ca ++ / 3.785 liters / minute / gram / 3.785 liters.

Finely atomized liquid The amount of the finely atomized liquid of the present process can be from about 1% to about 10% (active base), preferably from about 2% to about 6% (active base) in a total amount of the product final obtained by the process of the present invention. The finely atomized liquid of the present process can be selected from the group consisting of liquid silicate, anionic or cationic surfactants which are in liquid form, aqueous or non-aqueous polymer solutions, water, and mixtures thereof. Other optional examples for the finely atomized liquid of the present invention may be a solution of sodium carboxymethylcellulose, polyethylene glycol (PEG) and dimethylenetriaminepentamethylphosphonic acid (DETMP) solutions. Preferable examples of the anionic surfactant solutions that can be used as the finely atomized liquid in the present invention are HLAS of about 88 to 97% concentration, NaLAS of about 30 to 50% concentration, AE3S solution of about 28 % concentration, liquid silicate of approximately 40 to 50% concentration, etc.

Cationic surfactants may also be used as the finely atomized liquid herein, and suitable quaternary ammonium surfactants are selected from N-alkyl or alkenyl ammonium surfactants of Cß-C-io. wherein the remaining N positions are substituted with methyl, hydroxyethyl or hydroxypropyl groups. Preferable examples of the aqueous or non-aqueous polymer solutions that can be used as the finely atomized liquid in the present invention are modified polyamines comprising a polyamine skeleton corresponding to the formula: H [H2N-R] n + 1- [N-R] m- [N-R] n-NH2 which has a modified polyamine formula V (n + "|) WmYnZ or a polyamine skeleton corresponding to the formula: H R [H2N-R] n-k + 1- [N-R] m- [N-] n- [N-R] k-NH2 having a modified polyamine formula V (n.k + i) WmYnY'k Z, wherein k is less than or equal to n, said polyamine backbone, before modification, has a molecular weight greater than about 200 daltons, in where: i) units V are terminal units that have the formula: E X "O E-N-R- E-N + -R- E-N-R- ii) the units W are skeleton units that have the formula: E X "O I I -N-R- or -N + -R- or -N-R- iii) Y units are branching units having the formula: E X "O I I -N-R- or -N + -R- or -N-R-; and iv) and the Z units are terminal units having the formula: X "-NR- or N + wherein the skeletal linker units R are selected from the group consisting of C2-C-12 alkylene-C4-C12 alkenylene, C3-C12 hydroxyalkylene, C4-C dihydroxyalkylene. 2> C 8 -C 12 dialkylarylene - (R 1?) X R 1 -, - (R 10) x R 5 (OR 1) X, - (CH 2 CH (OR 2) CH 2 O) z (R 0) and R 1 - (OCH 2 CH (OR 2) CH 2) W ". C (O) (R4) rC (O) -, -CH2CH (OR2) CH2", and mixtures thereof, wherein R1 is C2-C6 alkylene, and mixtures thereof, R is hydrogen, - (R1) ?) xB, and mixtures thereof, R-3 is CjC-is alkyl, C7-C12 arylalkyl, aryl substituted with C7-C12 alkyl, C6-C12 aryl and mixtures thereof, R4 is alkylene C < | -C < 2, C 4 -C 12 alkenylene, C 8 -C 12 arylalkylene, C 1 -C 1 arylene, and mixtures thereof; R 5 is C 1 -C alkylene; 2. C3-C-12 hydroxyalkylene, C4-C12 dihydroxyalkylene, C8-C12 dialkylarylene, -C (O) -, -C (O) NHR6NHC (O) -, -R1 (OR1) -, - C (O) (R4) rC (O) -, CH2CH (OH) CH2-, CH2CH (OH) CH2O- (R1?) And R1OCH2CH (OH) CH2- and mixtures thereof; R * -5 is C2 alkylene -C 12 or C 1 -C 4 arylene, the E units are selected from the group consisting of hydrogen, C 1 -C 22 alkyl, C 3 -C 22 alkenyl, C 7 -C 22 arylalkyl, C 2 -C 22 hydroxyalkyl. ) pC? 2M, - (CH2) qSO3M, -CH (CH2C? 2M) C? 2M, - (CH2) pP? 3M, - (R1O) xB, -C (O) R3, and mixtures thereof; gone; B is hydrogen, C -CQ alkyl, - (CH2) qS03M, - (CH2) pC02M, - (CH2) q (CHS03M) CH2S03M, - (CH2) q- (CHSO2M) CH2S? 3M, - (CH2 ) pP03M, -PO3M and mixtures thereof; M is hydrogen or a cation soluble in water in an amount sufficient to satisfy the balance of the charge; X is a water soluble anion; m has the value of 4 to about 400; n has the value from 0 to about 200; p has the value of 1 to 6, q has the value of 0 to 6; r has the value of 0 or 1; w has the value of 0 or 1; x has the value of 1 to 100; "y" has the value of 0 to 100; z has the value of 0 or 1. An example of the most preferred polyethylene imines would be a polyethylenimine having a molecular weight of 1800, which is further modified by ethoxylation to a degree of about 7 ethyleneoxy residues per nitrogen (PEI 1800, E7 ). It is preferred that the above polymer solution be premixed with an anionic surfactant such as NaLAS. Other preferred examples of the aqueous or non-aqueous polymer solutions which can be used as the finely atomized liquid in the present invention are polymeric polycarboxylate dispersants which can be prepared by polymerizing or copolymerizing suitable unsaturated monomers, preferably in their acid form. Unsaturated monomeric acids which can be polymerized to form suitable polymeric polycarboxylates include acrylic acid, maleic acid (or maleic anhydride), fumaric acid, itaconic acid, aconitic acid, mesaconic acid, citraconic acid and methylenemalonic acid. The presence, in the polymeric polycarboxylates of the present, of monomer segments which do not contain carboxylate radicals such as vinyl methyl ether, styrene, ethylene, etc., is adequate, provided that said segments do not constitute more than about 40% by weight of the polymer. Preferred are homopolymeric polycarboxylates having molecular weights greater than 4000, such as those described below. Particularly suitable homopolymeric polycarboxylates can be derived from acrylic acid. Said polymers based on acrylic acid, which are useful herein, are the water-soluble salts of polymerized acrylic acid. The average molecular weight of said polymers in acid form preferably ranges from more than 4,000 to 10,000, preferably from more than 4,000 to 7,000, and most preferably from more than 4,000 to 5,000. The water-soluble salts of said acrylic acid polymers may include, for example, the alkali metal, ammonium and substituted ammonium salts. Copolymeric polycarboxylates such as a copolymer based on acrylic acid / maleic acid can also be used. Such materials include the water-soluble salts of the copolymer of acrylic acid and maleic acid. The average molecular weight of said copolymers in acid form preferably ranges from about 2,000 to 100,000, more preferably from about 5,000 to 75,000, and most preferably from about 7,000 to 65,000. The ratio of acrylate: maleate segments in said copolymers will generally vary from about 30: 1 to about 1: 1, more preferably from about 10: 1 to 2: 1. The water-soluble salts of said copolymers of acrylic acid: maleic acid may include, for example, the alkali metal, ammonium and substituted ammonium salts. It is preferred that the above polymer solution be premixed with an anionic surfactant such as LAS.

Auxiliary detergent ingredients The starting detergent material in the present process may include additional detergent ingredients, and / or any number of additional ingredients may be incorporated into the detergent composition during the subsequent steps of the present process. These auxiliary ingredients include other detergency builders, bleaches, bleach activators, foaming enhancers, or foam suppressors, anti-rust and anti-corrosion agents, soil suspending agents, soil removal agents, germicides, pH adjusting agents, alkalinity sources without detergency builder, chelating agents, smectite clays, enzymes, enzyme stabilizing agents, and perfumes. See the US patent. 3,936,537, issued February 3, 1976 to Baskerville, Jr., et al., Incorporated herein by reference. Other detergency builders can generally be selected from the various water-soluble alkali metal, ammonium or ammonium phosphates, polyphosphates, polyphosphonates, carbonates, borates, polyhydroxysulfonates, polyacetates, carboxylates and polycarboxylates substituted. Alkali metal, especially sodium, salts of the above are preferred. Preferred for use herein are the phosphates, carbonates, fatty acids of C-? Or-18-polycarboxylates, and mixtures thereof. More preferred are sodium tripolyphosphate, tetrasodium pyrophosphate, citrate, tartrate, mono- and di-succinates, and mixtures thereof (see below). Compared to the amorphous sodium silicates, the crystallized sodium silicate laminates exhibit a clearly increased calcium and magnesium ion exchange capacity. In addition, stratified sodium silicates prefer magnesium ions over calcium ions, a feature necessary to ensure that substantially all of the "hardness" is removed from the wash water. However, these layered crystalline sodium silicates are generally more expensive than amorphous silicates, as well as other detergency builders. Consequently, in order to provide an economically feasible laundry detergent, the proportion of the crystalline layered sodium silicates used must be judiciously determined. Said stratified sodium silicates are described in Corkill et al., U.S. No. 4,605,509, previously incorporated herein by reference. Specific examples of inorganic phosphate builders are sodium and potassium tripolyphosphate, pyrophosphate, polymeric metaphosphate having a degree of polymerization of about 6 to 21, and orthophosphates. Examples of polyphosphonate builders are the sodium and potassium salts of ethylene diphosphonic acid, the sodium and potassium salts of ethane-1-hydroxy-1,1-diphosphonic acid, and the sodium and potassium salts of acid ethane-1, 1, 2-triphosphonic. Other phosphorus builder compounds are described in the U.S. Patents. 3,159,581; 3,213,030; 3,422,021; 3,422,137; 3,400,176 and 3,400,148, all of which are incorporated herein by reference. Examples of inorganic builders without phosphorus are tetraborate decahydrate and silicates having a weight ratio of SiO 2: alkali metal oxide of about 0.5 to about 4.0, preferably about 1.0 to about 2.4. The water-soluble organic builders without phosphorus useful herein include the various alkali metal, ammonium and substituted ammonium polyacetates, carboxylates, polycarboxylates and polyhydroxysulfonates. Examples of polyacetate and polycarboxylate builders are the sodium, potassium, lithium, ammonium and substituted ammonium salts of ethylenediaminetetraacetic acid, nitrilotriacetic acid, oxydisuccinic acid, melific acid, benzene polycarboxylic acids, and citric acid. Polycarboxylate polymeric detergency builders are described in the U.S. patent. 3,308,067, Diehl, issued March 7, 1967, the disclosure of which is incorporated herein by reference. Such materials include the water-soluble salts of homo- and co-polymers of aliphatic carboxylic acids such as maleic acid, itaconic acid, mesaconic acid, fumaric acid, aconitic acid, citraconic acid and methylenemalonic acid. Some of these materials are useful as the water-soluble anionic polymer as described below, but only if they are in intimate admixture with the non-soap anionic surfactant. Other polycarboxylates suitable for use herein are the polyacetal carboxylates described in the U.S. patent. 4,144,226, issued March 13, 1979 to Crutchfield et al., And the US patent. 4,246,495, issued March 27, 1979 to Crutchfield et al., Which are incorporated herein by reference. These polyacetal carboxylates can be prepared by bringing together a glyoxylic acid ester and a polymerization initiator under polymerization conditions. The resulting polyacetal carboxylate ester is then attached to chemically stable end groups to stabilize the polyacetal carboxylate against rapid depolymerization in alkaline solution, converted to the corresponding salt, and added to a detergent composition. Particularly preferred polycarboxylate builders are ether carboxylate builder compositions which comprise a combination of tartrate monosuccinate and tartrate disuccinate described in the US patent. 4,663,071, Bush et al., Issued May 5, 1987, the disclosure of which is incorporated herein by reference. Bleaches and activators are described in the U.S. patent. 4,412,934, Chung et al., Issued November 1, 1983, and in the US patent. 4,483,781, Hartman, issued November 20, 1984, which are incorporated herein by reference. Chelating agents are also described in the U.S. patent. 4,663,071, Bush et al., In column 17, line 54 to column 18, line 68, incorporated herein by reference. Foam modifiers are also optional ingredients, and are described in the US patents. 3,933,672, issued January 20, 1976 to Bartolotta et al., And 4,136,045, issued January 23, 1979 to Gault et al., Which are incorporated herein by reference. Smectite clays suitable for use herein are described in the U.S. patent. 4,762,645, Tucker et al., Issued August 9, 1988, column 6, line 3 to column 7, line 24, incorporated herein by reference. Other builders suitable for use herein are indicated in the Baskerville patent, column 13, line 54 to column 16, line 16, and in the U.S. patent. 4,663,071, Bush et al., Issued May 5, 1987, which are incorporated herein by reference.

Optional steps of the method Optionally, the method may comprise the step of spraying an additional binder in one or more of the first, second and / or third mixers for the present invention. A binder is added for the purpose of improving agglomeration by providing a "binder" or "adherent" agent for the detergent components. The binder is preferably selected from the group consisting of water, anionic surfactants, nonionic surfactants, liquid silicates, polyethylene glycol, polyvinylpyrrolidone, polyacrylates, citric acid, and mixtures thereof. Other suitable binding materials including those included herein are described in Beerse et al., U.S. No. 5,108,646 (Procter &Gamble Co.), the disclosure of which is incorporated herein by reference. Other optional steps contemplated by the present method include screening the larger size detergent agglomerates in a screening apparatus that can take various forms including, but not limited to, conventional screens selected for the desired particle size of the finished detergent product. Other optional steps include conditioning the detergent agglomerates by subjecting them to further drying, by the apparatus described above. Another optional step of the present process is to terminate the resulting detergent agglomerates by various methods including spraying and / or mixing with other conventional detergent ingredients. For example, the finishing step encompasses the spraying of perfumes, brighteners and enzymes onto the finished agglomerates to provide a more complete detergent composition. Such techniques and ingredients are well known in the art. Another optional step in the process includes a method of structuring surfactant paste, for example, curing an aqueous anionic surfactant paste, incorporating a paste hardening material by using an extruder prior to the process of the present invention. The details of the surfactant paste structuring process are described in the associated application No. PCT / US96 / 15960 (filed October 4, 1996). To make the present invention more easily understood, reference is made to the following examples, which are intended to be illustrative only and not to limit the scope of the present invention.

EXAMPLES EXAMPLE 1 The following is an example for obtaining agglomerates having high density, using the Lódige CB mixer (CB-30), followed by the Schugi FX-160 mixer, then the Lódige KM mixer (KM-600), and finally using the fluid bed for additional granulation. [Step 1] 250 - 270 kg / hr of aqueous surfactant paste of coconut fatty alcohol sulfate are dispersed (C <; | 2-C < | 8. concentration 71.5%) by means of the shank instruments of a CB-30 mixer together with 220 kg / hr of pulverized STPP (average particle size of 40 to 75 microns), 160-200 kg / hr of soda ash milled (average particle size 15 microns), 80-120 kg / hr of ground sodium sulphate (average particle size of 15 microns) and 200 kg / hr of recirculating internal powder stream. The surfactant paste is introduced at approximately 40-52 ° C, and the powders are introduced at room temperature. The conditions of the CB-30 mixer are as follows: Average residence time: 10-18 seconds Peak speed: 7.5 to 14 m / s Power condition: 0.5 - 4 kj / kg Mixer speed: 550 - 900 rpm the shirt: 30 ° C [Step 2 (i)] The agglomerates of the CB-30 mixer are introduced to the Schugi FX-160 mixer. 30 kg / hr of HLAS (an acid precursor of C- | - | -C- | 8 alkylbenzenesulfonate, 95% cntration) are dispersed as a finely atomized liquid in the Schugi mixer at about 50-60 ° C. Schugi mixer is added with 20-80 kg / hr of soda ash (average particle size of approximately 10-20 microns). The conditions of the Schugi mixer are the following: Average residence time: 0.2-5 seconds Peak speed: 16-26 m / s Power condition: 0.15 - 2 kj / kg Mixer speed: 2000 - 3200 rpm [Step 2 (ii)] The agglomerates of the Schugi mixer are introduced into the mixer KM-600 for additional agglomeration, for rounding and growth of the agglomerates.

KM 30 kg / hr of zeolite is also added to the mixer. Crushers can be used in the KM mixer to reduce the amount of agglomerates of larger size. The conditions of the KM mixer are the following: Average residence time: 3-6 minutes Energy condition: 0.15 - 2 kj / kg Mixer speed: 100 - 150 rpm Sleeve temperature: 30-40 ° C [Step 3] The agglomerates of the KM mixer are introduced into a fluid bed drying apparatus to dry, round and grow the agglomerates. 20-80 kg / hr of liquid silicate can also be added to the fluid bed drying apparatus (43% solids, 2.0 R) at 35 ° C. The conditions of the fluid bed drying apparatus are the following: Average residence time: 2-4 minutes. Thickness of the non-fluidized bed: 200 mm. Spray drop size: less than 50 microns. Spray height: 175-250 mm (above the distributor plate). Fluidized speed: 0.4-0.8 m / s. Bed temperature: 40-70 ° C. The granules resulting from step 3 have a density of approximately 700 g / l and can optionally be subjected to an optional cooling, sizing and / or grinding process.

EXAMPLE 2 The following is an example for obtaining agglomerates having high density, using the Lódige CB mixer (CB-30), followed by the Schugi FX-160 mixer, then the Lodige KM mixer (KM-600), and finally using the fluid bed for additional granulation.

[Step 1] 15 kg / hr-30 kg / hr of HLAS (an acid precursor of alkylbenzenesulfonate of C «| - | -C- | 8, cntration, 95%) are dispersed at about 50 ° C, and 250-270 kg / hr of aqueous paste of coconut fatty alcohol sulfate surfactant (C12-C * | 8, cntration 71.5%), by means of the instruments of a CB-30 mixer together with 220 kg / hr of pulverized STPP (average size) particle size from 40 to 75 microns), 160-200 kg / hr of ground soda ash (average particle size 15 micras), 80-120 kg / hr of ground sulphate (average particle size of 15 micras) and the 200 kg / hr of powder from the internal recirculation stream. The surfactant paste is introduced at approximately 40-52 ° C, and the powders are introduced at room temperature. The conditions of the CB-30 mixer are the following: Average residence time: 10-18 seconds Peak speed: 7.5 to 14 m / s Energy condition: 0.5 - 4 kj / kg Mixer speed: 550 - 900 fm the shirt: 30 ° C [Step 2 (i)] The agglomerates of the CB-30 mixer are introduced to the Schugi mixer FX-160. 35 kg / hr of neutralized liquid AE3S (cntration, 28%) is dispersed as a finely atomized liquid in the Schugi mixer at about 30 to 40 ° C. 20-80 kg / hr of soda ash are added to the Schugi mixer. The conditions of the Schugi mixer are as follows: Average residence time: 0.2 - 5 seconds Top speed: 16 - 26 m / s Power condition: 0.15 - 2 kj / kg Mixer speed: 2000 - 3200 rpm [Step 2 (ii)] The agglomerates of the Schugi mixer are introduced into the KM-600 mixer for further agglomeration, for rounding and growth of the agglomerates. KM 60 kg / hr of milled soda ash (average particle size of 15 microns) is also added to the mixer. Crushers can be used in the KM mixer to reduce the amount of agglomerates of larger size. The conditions of the KM mixer are the following: Average residence time: 3-6 minutes Energy condition: 0.15 - 2 kj / kg Mixer speed: 100 - 150 rpm Sleeve temperature: 30-40 ° C [Step 3] The agglomerates of the KM mixer are introduced into a fluid bed drying apparatus to dry, round and grow the agglomerates. 20-80 kg / hr of liquid silicate can also be added to the fluid bed dryer apparatus (43% solids, 2.0 R) at 35 ° C. The conditions of the fluid bed drying apparatus are the following: Average residence time: 2-4 minutes. Thickness of the non-fluidized bed: 200 mm. Spray drop size: less than 50 microns. Spray height: 175-250 mm (above the distributor plate). Fluidized speed: 0.4-0.8 m / s. Bed temperature: 40-70 ° C. The resulting granules of the fluid bed dryer apparatus are introduced to a fluid bed cooler apparatus. The conditions of the fluid bed cooler apparatus are as follows: Average residence time: 2-4 minutes. Thickness of the non-fluidized bed: 200 mm. Fluidized speed: 0.4-0.8 m / s. Bed temperature: 12-60 ° C. The granules resulting from step 3 have a density of approximately 700 g / l and can optionally be subjected to optional sizing and / or grinding processes.

EXAMPLE 3 The following is an example for obtaining agglomerates having high density, using the Lódige CB mixer (CB-30), followed by the Schugi FX-160 mixer, followed by the fluid bed apparatus for further granulation.

[Step 1] 250-270 kg / hr of aqueous surfactant fatty alcohol sulfate coconut paste (C < 2-C- | 8, concentration 71.5%) are dispersed by means of the tang instruments of a CB-mixer 30 together with 220 kg / hr of pulverized STPP (average particle size of 40 to 75 microns), 160 - 200 kg / hr of ground soda ash (average particle size 15 microns), 80 - 120 kg / hr of sulphate of milled sodium (average particle size of 15 microns) and 200 kg / hr of internal recirculation powder flow. The surfactant paste is introduced at approximately 40-52 ° C, and the powders are introduced at room temperature. The conditions of the CB-30 mixer are the following: Average residence time: 10-18 seconds Peak speed: 7.5 to 14 m / s Power condition: 0.5 - 4 kj / kg Mixer speed: 550 - 900 m the shirt: 30 ° C [Step 2 (i)] The agglomerates of the CB-30 mixer are introduced to the Schugi FX-160 mixer. 30 kg / hr of HLAS (an acid precursor of C- | i-C- | 8 alkylbenzenesulfonate, concentration 94-97%) are dispersed as a finely atomized liquid in the Schugi mixer at about 50-60 ° C. Schugi mixer is added 20-80 kg / hr of soda ash. The conditions of the Schugi mixer are the following: Average residence time: 0.2-5 seconds Peak speed: 16-26 m / s Power condition: 0.15 - 2 kj / kg Mixer speed: 2000 - 3200 rpm [Step 3] The agglomerates of the Schugi mixer are introduced into a fluid bed drying apparatus to dry, round and grow the agglomerates. 20-80 kg / hr of liquid silicate can also be added to the fluid bed dryer apparatus (43% solids, 2.0 R) at 35 ° C. The conditions of the fluid bed drying apparatus are the following: Average residence time: 2-4 minutes. Thickness of the non-fluidized bed: 200 mm. Spray drop size: less than 50 microns. Spray height: 175-250 mm (above the distributor plate). Fluidized speed: 0.4-0.8 m / s. Bed temperature: 40-70 ° C. The granules resulting from step 3 have a density of about 600 g / l, and can optionally be subjected to optional cooling, dimen- sioning and / or grinding processes. Having thus described the invention in detail, it will be apparent to those skilled in the art that various changes can be made without departing from the scope of the invention, and that the latter should not be considered to be limited to what is described in the specification.

Claims (10)

NOVELTY OF THE INVENTION CLAIMS

1. - A non-tower process for preparing a granular detergent composition having a density of at least about 600 g / l, comprising the steps of: (a) dispersing a surfactant and coating the surfactant with fine powders that have a diameter of 0.1 to 500 microns, in a mixer in which conditions include (i) from about 2 to about 50 seconds of average residence time, (ii) from about 4 to about 25 m / s of speed of tip and (iii) from about 0.15 to about 7 kj / kg of energy condition, where first agglomerates are formed; (b) sprinkling finely atomized liquid on the first agglomerates in a mixer, wherein the conditions of the mixer include (i) from about 0.2 to about 5 seconds of average residence time, (ii) from about 10 to about 30 m / s of tip speed, and (ii) from about 0.15 to about 5 kj / kg of energy condition, where second agglomerates are formed; and (c) granulating the agglomerated seconds in one or more fluidization apparatuses, wherein the conditions of each of the fluidization apparatuses include: (i) from about 1 to about 10 minutes of average residence time, (ii) from about 100 to about 300 mm of non-fluidized bed thickness, (iii) not more than about 50 microns of dew drop size, (iv) from about 175 to about 250 mm of dew height, (v) from about 0.2 to about 1.4 m / s of fluidization velocity, and (vi) from about 12 to about 100 ° C bed temperature.

2. A non-tower process for preparing a granular detergent composition having a density of at least 600 g / l; the method comprises the steps of: (a) dispersing a surfactant and coating the surfactant with fine powders having a diameter of 0.1 to 500 microns, in a mixer in which the conditions include (i) from about 2 to about 50 seconds of average residence time, (ii) from about 4 to about 25 m / s peak speed and (iii) from about 0.15 to about 7 kj / kg energy condition, where first agglomerates are formed; (b) sprinkling finely atomized liquid on the first agglomerates in a mixer, wherein the conditions of the mixer include (i) from about 0.2 to about 5 seconds of average residence time, (ii) from about 10 to about 30 m / s of tip speed, and (iii) from about 0.15 to about 5 kj / kg of energy condition, wherein second agglomerates are formed; (b ') completely mixing the agglomerated seconds in a mixer wherein the conditions of the mixer include (i) from about 0.5 to about 15 minutes of average residence time and (ii) from about 0.15 to about 7 kj / kg condition of energy, where agglomerated third parties are formed; and (c) granulating the agglomerated third in one or more fluidization apparatuses, wherein the conditions of each of the fluidization apparatuses include: (i) from about 1 to about 10 minutes of average residence time, (ii) from about 100 to about 300 mm of non-fluidized bed thickness, (iii) not more than about 50 microns of dew drop size, (iv) from about 175 to about 250 mm of dew height, (v) from about 0.2 to about 1.4 m / s of fluidization velocity, and (vi) from about 12 to about 100 ° C bed temperature.

3. The process according to claim 1 or 2, characterized in that said surfactant is selected from the group consisting of anionic surfactant, nonionic surfactant, cationic surfactant, zwitterionic surfactant., ampholytic surfactant and mixtures thereof.

4. The process according to claim 1 or 2, characterized in that said surfactant is selected from the group consisting of alkylbenzenesulfonates, alkylalkoxy sulfates, alkylethoxylates, alkyl sulfates, coconut fatty alcohol sulfates and mixtures thereof.

5. The process according to claim 1 or 2, characterized in that in step (a) fine powders are formed in excess, and the fine powders in excess are added in step (b).

6. The process according to claim 1 or 2, characterized in that an aqueous or nonaqueous polymeric solution is dispersed with said surfactant in step (a).

7. The process according to claim 1 or 2, characterized in that the fine powders are selected from the group consisting of soda ash, powdered sodium tripolyphosphate, hydrated tripolyphosphate, sodium sulfates, aluminosilicates, layered crystalline silicates, phosphates, precipitated silicates, polymers, carbonates, citrates, nitrilotriacetates, pulverized surfactants and mixtures thereof.

8. The process according to claim 1 or 2, characterized in that the finely atomized liquid is selected from the group consisting of liquid silicates, anionic surfactants, cationic surfactants, aqueous polymer solutions, non-aqueous polymer solutions, water and mixtures thereof.

9. The process according to claim 1 or 2, further characterized in that a stream of internal recirculating powder from the fluidization apparatus is added in step (a).

10. - A granular detergent composition prepared according to the method of claim 1 or 2.