A plant and a process for producing a surfactant product

Abstract

A plant (10) for producing a surfactant product (11), in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product, in which in particular said surfactant product (11) is obtained by neutralization of an intermediate product, i.e., of a non-stable surfactant product (111), comprises means, or apparatus, (16) for withdrawing dioxane from a corresponding surfactant product (11), i.e., from a neutralized or stabilized surfactant product (11).

Description

[0001] A PLANT AND A PROCESS FOR PRODUCING A SURFACTANT PRODUCT

[0002] Field of application of the present invention

[0003] The present invention relates to a plant and a process for producing a surfactant product.

[0004] State of the art

[0005] Plants for producing a surfactant product containing Sodium Laureth Sulfate in an amount ranging between 70% and 90% of the same surfactant product are known, which plants allow obtaining said surfactant product by neutralization of an intermediate product, i.e., of a non-stable surfactant product, in particular in the form of a corresponding sulphonic acid.

[0006] However, the thus-obtained surfactant product has a degree of harmfulness to humans and to the environment that is highly undesirable.

[0007] In particular, during the corresponding sulfation reaction, dioxane is formed by a side reaction in the bulk of said surfactant product, which dioxane is a substance considered potentially carcinogenic to humans and, in any case, harmful to the environment.

[0008] In the field, there is moreover a continuing need to have a high-quality surfactant product available.

[0009] In the field, there is also a need to operate, in order to produce said surfactant product, at costs that are as low as possible.

[0010] Summary of the invention

[0011] With the present invention, it is therefore intended to propose a novel and alternative solution to the solutions known so far, and in particular to overcome one or more of the above-mentioned drawbacks or problemsand / or to meet one or more of the above-mentioned needs and / or, in any case, needs felt in the art, and in particular as may be inferred from the foregoing.

[0012] A plant is thus provided, for producing a surfactant product, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product; especially said surfactant product being obtained by neutralization of an intermediate product of said surfactant product; the plant being characterized in that it comprises means, or apparatus, for withdrawing dioxane from said surfactant product, i.e., from said neutralized or stabilized surfactant product.

[0013] In this manner, it is possible to obtain a surfactant product having a degree of harmfulness to humans and to the environment that is advantageously reduced.

[0014] In particular, a surfactant product may be obtained, having a dioxane amount in the same surfactant product that is particularly low, especially being of less than 10 ppm, preferably being less than 5 ppm, and optimally that is less than 2 ppm.

[0015] According to another aspect, a process is provided, for producing a surfactant product, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product; especially said surfactant product being obtained by neutralization of an intermediate product of said surfactant product; the process being characterized in that it is provided for withdrawing dioxane from said surfactant product, i.e., from said neutralized or stabilized surfactant product.

[0016] In this manner, it is possible to obtain a surfactant product having a degree of harmfulness to humans and to the environment that is advantageously reduced.

[0017] In particular, a surfactant product may be obtained, having a dioxaneamount in the same surfactant product that is particularly low, especially being of less than 10 ppm, preferably being less than 5 ppm, and optimally less than 2 ppm.

[0018] Brief description of the drawings

[0019] This and other novel aspects, i.e., respective and specific advantageous embodiments, are in any case set forth in the appended claims, the specific technical features of which can be found, together with corresponding advantages achieved, in the following description illustrating in detail merely exemplary and non-limiting embodiments of the invention, and which is made with reference to the appended drawings, in which:

[0020] Fig. 1 illustrates a schematic view of a first preferred embodiment of a plant according to the present invention;

[0021] Fig. 2 illustrates a perspective, schematic view of a portion of the scraping means that are used in the first preferred embodiment of a plant according to the present invention;

[0022] Fig. 3 illustrates a schematic view of a second preferred embodiment of a plant according to the present invention;

[0023] Fig. 4 illustrates a schematic view of a third preferred embodiment of a plant according to the present invention;

[0024] Fig. 5 illustrates a schematic view of a fourth preferred embodiment of a plant according to the present invention.

[0025] Detailed description of preferred embodiments of the invention

[0026] In FIGS. 1 and 2, a first preferred embodiment 10 of a plant for producing a surfactant product is illustrated.

[0027] In particular, said surfactant product contains Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product, especially, said Sodium Laureth Sulfate exhibiting adegree of ethoxylation ranging between 0,5 moles and 30 moles of Ethylene Oxide (EO).

[0028] In particular, said surfactant product is in the form of a product having a pasty texture.

[0029] Especially, the surfactant product is obtained by neutralization of an intermediate product 111 of said surfactant product, especially in the form of sulphonic acid, i.e., in the form of a non-neutralized, non-stable product and that is neutralized, i.e., made stable, via a neutralization agent 144’, in particular in the form of an alkaline agent, preferably in the form of caustic soda.

[0030] In particular, said intermediate product 111 is obtained, in 12, as will be best understood from the following of the present description, by sulfation preferably via sulfuric anhydride, i.e., sulfuric acid, of an ethoxylate, in turn obtained by ethoxylation of an organic substance, i.e., of corresponding fatty alcohols, with ethylene oxide.

[0031] Advantageously, as illustrated, the plant 10 comprises means, or apparatus, 16 for withdrawing dioxane from a corresponding surfactant product, i.e., from a neutralized or stabilized surfactant product 11 , especially which was obtained as will be best understood from the following of the present description from said intermediate product 111, and which, however, in particular has a high dioxane content.

[0032] In this manner, it is possible to obtain a surfactant product 11’ having a degree of harmfulness to humans and to the environment that is advantageously reduced.

[0033] In particular, a surfactant product may be obtained, 11’ having a dioxane amount in the same surfactant product that is particularly low, especially being of less than 10 ppm, preferably being less than 5 ppm, i.e., as will be best understood from the following of the present description, a surfactant product 11” having a dioxane amount in the same surfactantproduct that is even lower, in particular until reaching a content of less than 2 ppm.

[0034] It is pointed out that, in the present patent text, by surfactant product is meant a stable surfactant product, i.e., a surfactant product that has already been subjected to a neutralization process with a corresponding agent, in particular in the form of an alkaline agent, preferably in the form of caustic soda, while by intermediate product 111 is meant an intermediate product of said non-stable surfactant, i.e., an intermediate product of said surfactant that has not already been subjected to a neutralization process, and in particular that is in the form of a sulphonic acid.

[0035] Advantageously, as is clear from said Figures, said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 are in the form of means 16 for stripping dioxane from said surfactant product 11.

[0036] As is clear from said Figures, in a particularly advantageous manner, said means 16 for stripping dioxane from said surfactant product 11 are in the form of means 16 for evaporating water from said surfactant product 11.

[0037] In this manner, in order particularly reduced costs can be achieved when obtaining said surfactant.

[0038] Advantageously, as is clear from said Figures, said means 16 for stripping dioxane from said surfactant product 11, i.e., said means 16 for evaporating water from said surfactant product 11 , are in the form of an evaporator 16.

[0039] Advantageously, as is clear from said Figures, said evaporator 16 for withdrawing dioxane from said surfactant product is an evaporator of the wiped film type.

[0040] As is clear from said Figures, in an appreciably advantageous manner, said evaporator 16 for withdrawing dioxane from said surfactant product has a containment body 160, in particular vertically elongated, having a circumferentially extended inner surface 161, which delimits, or defines, acorresponding process chamber 162, in particular vertically extended.

[0041] Advantageously, as is clear from said Figures, said evaporator 16 for withdrawing dioxane from said surfactant product has, inside said process chamber 162, corresponding scraping means 163 that are adapted to spread said surfactant product 11 along said circumferential inner surface 161 , which said scraping means 163 are movable in rotation inside the same process chamber 162 and preferably comprise a plurality of blades 164 carried by a corresponding frame 165 and arranged according to respective groups, vertically distributed and in which the respective blades 164 are circumferentially distributed, with the blades 164 of the respective group that are staggered relative to the blades of the adjacent group.

[0042] Advantageously, the tangential peripheral speed of said scraping means 163 preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

[0043] In this manner, it is possible to improve the stripping of dioxane from said surfactant product 11.

[0044] As is clear from said Figures, with appreciable advantage, said evaporator 16 for withdrawing dioxane from said surfactant product comprises means 166 for inputting said surfactant product 11 to be processed into said process chamber 162.

[0045] Advantageously, as is clear from said Figures, said means 166 for inputting said surfactant product 11 to be processed into said process chamber 162 are provided at the head, i.e., in an upper position, to said containment body 160.

[0046] In this manner, a particularly advantageous distribution of said surfactant product 11 can be achieved.

[0047] Advantageously, as is clear from said Figures, said means 166 for inputting said surfactant product 11 to be processed into said process chamber 162 comprise a single inputting inlet, or mouth, 166 into saidcontainment body 160.

[0048] As is clear from said Figures, with advantage, said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 comprise means 167 to input process water, in particular said evaporator 16 for withdrawing dioxane from said surfactant product comprises means 167 to input process water, especially into said process chamber 162.

[0049] Advantageously, as is clear from said Figures, said means 167 to input process water into said process chamber 162 comprise a plurality of inlets, especially distributed, in particular vertically, along said containment body 160, and adapted to input said process water into said process chamber 162 at corresponding distributed positions, in particular vertically, of said same process chamber 162.

[0050] In this manner, a particularly advantageous distribution of water in said surfactant product 11 can thus be achieved.

[0051] Advantageously, as is clear from said Figures, said evaporator 16 for withdrawing dioxane from said surfactant product comprises means 168 for the exit of said processed surfactant product 1 T from said evaporator 16, i.e. , from said process chamber 162.

[0052] As is clear from said Figures, in an advantageous manner, said means for the exit of said processed surfactant product 1 T from said evaporator 16, i.e., from said process chamber 162, comprise a single exit mouth 168 opening, in particular vertically, downwardly at the lower end of said evaporator 16, i.e., of said containment body 160.

[0053] Advantageously, as is clear from said Figures, said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 comprise means 169 that are adapted to create a vacuum, or depression, condition, in particular inside said process chamber 162 of said evaporator 16 for withdrawing dioxane from said surfactant product.

[0054] Advantageously, as is clear from said Figures, said means that areadapted to create a vacuum, or depression, condition, inside said process chamber 162, of said evaporator 16 for withdrawing dioxane from said surfactant product, comprise a corresponding suctioning device 169, in particular mounted on top, i.e., superiorly, to said containment body 160.

[0055] In a particularly advantageous manner, said means 169 that are adapted to create a vacuum, or depression, condition, in particular into said process chamber 162 of said evaporator for withdrawing dioxane from said surfactant product 11, are adapted to create a vacuum condition ranging between 5 mbar and 100 mbar and that is preferably about 50 mbar.

[0056] In this manner, it is thus possible to improve the stripping of dioxane from said surfactant product 11.

[0057] Advantageously, as is clear from said Figures, said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 comprise means 1610 for thermally heating said surfactant product 11 subjected to dioxane withdrawal, and in particular said evaporator 16 for withdrawing dioxane from said surfactant product comprises thermal heating means 1610, in particular to heat said process chamber 162.

[0058] Advantageously, as is clear from said Figures, said thermal heating means 1610, in particular to heat said process chamber 162 comprise a jacket for a heating fluid provided in said containment body 160 externally to said circumferentially extended inner surface 161, defining said process chamber 162.

[0059] In an appreciably advantageous manner, said thermal heating means 1610, in particular to heat said process chamber 162 are adapted to induce, especially inside the same process chamber 162, a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e., which is of about the latter temperature range.

[0060] In this manner, the stripping of dioxane can be increased, without inany case reducing the quality of said surfactant product 11. Advantageously, as is clear from said Figures, means, or apparatus, 14 are also provided in the plant, which are adapted to make said surfactant product 11 stable, in particular carrying out the neutralization of the corresponding intermediate product 111.

[0061] Advantageously, as is clear from said Figures, said means, or apparatus, adapted to make said surfactant product 11 stable comprise, or consist in, a corresponding neutralization reactor 14.

[0062] As is clear from said Figures, with appreciable advantage, said neutralization reactor 14 is defined by an evaporator of the wiped film type (wiped film evaporator).

[0063] In this manner, particularly reduced costs can be achieved when obtaining said surfactant.

[0064] Advantageously, as is clear from said Figures, said neutralization reactor 14 has a containment body 140, in particular vertically elongated, having an inner surface 141, circumferentially extended, which delimits, or defines, a corresponding reaction chamber 142, in particular vertically extended.

[0065] Advantageously, as is clear from said Figures, said neutralization reactor 14 comprises means 143 for inputting said intermediate product 111 to be processed into said neutralization chamber 142.

[0066] As is clear from said Figures, with advantage, said means 143 for inputting said intermediate product to be processed 111 are provided on top, i.e. , in an upper position, to said containment body 140.

[0067] Advantageously, as is clear from said Figures, said means for inputting said intermediate product to be processed 111 comprise a single inlet, or mouth, 143 for the input into said containment body 140.

[0068] Advantageously, as is clear from said Figures, said neutralization reactor 14 comprises means 144 for inputting a neutralization agent 144’, inparticular in the form of an alkaline agent.

[0069] As is clear from said Figures, in an advantageous manner, said means for inputting said neutralization agent 144’ are provided on top, i.e., in an upper position, to said containment body 140.

[0070] Advantageously, as is clear from said Figures, said means for inputting said neutralization agent 144’ comprise a single inlet, or mouth, 144 for the input into said containment body 140.

[0071] Advantageously, as is clear from said Figures, said neutralization reactor 14 comprises means 145 for the exit of said surfactant product, i.e., of said stabilized or neutralized surfactant product.

[0072] As is clear from said Figures, in a particularly advantageous manner, said means for the exit of said surfactant product comprise a single exit mouth 145, opening, in particular vertically, downwardly at the lower end of said evaporator 14, i.e., of said containment body 140.

[0073] Advantageously, as is clear from said Figures, means 1460 are provided, to heat the product being processed in the same neutralization chamber 142 of said neutralization reactor 14.

[0074] Advantageously, as is clear from said Figures, said means 1460 to heat the product being processed in the same neutralization chamber 142 of said neutralization reactor 14 define means for evaporating water from said product being processed in the same neutralization chamber 142 of said neutralization reactor 14.

[0075] As is clear from said Figures, in an appreciably advantageous manner, said means 1460 to heat the product being processed in the same neutralization chamber 142 of said neutralization reactor 14 operate in a vacuum condition.

[0076] Advantageously, as is clear from said Figures, means 146 are provided, which are adapted to create a vacuum, or depression, condition, during the neutralization, in particular into said neutralization chamber 142 ofsaid neutralization reactor 14.

[0077] Advantageously, as is clear from said Figures, said means that are adapted to create a vacuum, or depression, condition, into said neutralization chamber 142 of the neutralization reactor 14, comprise a corresponding suctioning device 146, in particular mounted on top, i.e., superiorly, to said containment body 140 of the same neutralization reactor 14.

[0078] As is clear from said Figures, with appreciable advantage, means 148 for supplying water into said neutralization chamber 142 are provided for.

[0079] Advantageously, as is clear from said Figures, said means 148 for supplying water into said neutralization chamber 142 comprise a plurality of water inlets, especially distributed, in particular vertically, along said containment body 140, and adapted to input said process water into said process chamber 142 at corresponding distributed positions, in particular vertically, of said same process chamber 142.

[0080] Advantageously, as is clear from said Figures, said means, or apparatus, 14 adapted to make said intermediate product 111 stable, i.e., said neutralization reactor 14, are, or is, adapted to withdraw dioxane from the same product being processed.

[0081] With advantage, said means 146 that are adapted to create a vacuum, or depression, condition, into said neutralization chamber 142, of said neutralization reactor 14, are adapted to create a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

[0082] In this manner, it is thus possible to obtain an advantageous primary stripping of dioxane from said product being processed in the same neutralization chamber 142 of said neutralization reactor 14.

[0083] Advantageously, as is clear from said Figures, said neutralization reactor 14 has, inside said neutralization chamber 142, corresponding scraping means that are adapted to spread said surfactant product 11 along said circumferential inner surface 141, which said scraping means, while notbeing particularly illustrated in attached figures, are nonetheless similar to the scraping means of said evaporator 16 for withdrawing dioxane from said surfactant product, illustrated in Fig. 2, and are movable in rotation inside the same neutralization chamber 142 and preferably comprise a plurality of blades carried by a corresponding frame and arranged according to respective groups, vertically distributed, and in which the blades are circumferentially distributed, with the blades of the respective group being staggered relative to the blades of the adjacent group.

[0084] Advantageously, the tangential peripheral speed of said scraping means of said neutralization reactor 14 into said neutralization chamber 142 of said neutralization reactor 14 preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

[0085] In this manner, the primary stripping of dioxane from said surfactant product being stabilized or neutralized 11 is also improved.

[0086] In an advantageous manner, said means 1460 to heat the product being processed in the same neutralization chamber 142 of said neutralization reactor 14 are adapted to induce, especially inside the same neutralization chamber 142 of said neutralization reactor 14, a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e., which is of about the latter temperature range.

[0087] In this manner, the stripping of dioxane can be increased, without in any case reducing the quality of said surfactant product 11.

[0088] Advantageously, in said neutralization chamber 142, of the neutralization reactor 14, a surfactant product 11 is provided for, having a water concentration ranging between 70% and 95%, preferably between 72% and 90%.

[0089] In this manner, it is thus possible to operate within said neutralizationreactor with said intermediate product being processed in a more concentrated form, further promoting the stripping of dioxane from the same surfactant product.

[0090] Advantageously, as is clear from said Figures, said thermal heating means, in particular to heat said process chamber 142 comprise a jacket 1460 for a heating fluid provided for in said containment body 140 externally to said inner surface 141, circumferentially extended, defining said process chamber 142.

[0091] Advantageously, as is clear from said Figures, connecting means 15 are provided, which are adapted to transfer said surfactant product 11 between said means, or apparatus, 14 adapted to make said surfactant product 11 stable and said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11.

[0092] Advantageously, as is clear from said Figures, said connecting means between said means, or apparatus, 14 adapted to make said surfactant product 11 stable and said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 comprise a conduit 15 connecting said means, or mouth, 145 for the exit of said surfactant product, of said neutralization reactor 14, with said means 166 for inputting said surfactant product 11 to be processed into said process chamber 162 of said evaporator 16 for withdrawing dioxane from said surfactant product.

[0093] In a particularly advantageous manner, said neutralization reactor 14 is configured to process, and in particular to output, a surfactant product 11 having a water concentration ranging between 0% and 60%, preferably between 10% and 30%.

[0094] In this manner, it is thus possible to operate within said neutralization reactor 14 with said product being processed in the same neutralization chamber 142 of said neutralization reactor 14 that is more concentrated, further promoting the stripping of dioxane from the same surfactant product.Advantageously, as is clear from said Figures, means 15’ are provided, for supplying water to said surfactant product 11 into said means 15 for the connection between said means, or apparatus, 14 that are adapted to make said surfactant product 11 stable and said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11.

[0095] In this manner, said surfactant product 11 containing Sodium Laureth Sulfate can be brought to aa concentration of Sodium Laureth Sulfate ranging between 70% and 90% of the same surfactant product, and thus easily operate within said evaporator for withdrawing dioxane from said surfactant product.

[0096] In the subsequent Fig. 3, a second preferred embodiment 100 is illustrated of a plant for producing a surfactant product 11, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product.

[0097] In this second preferred embodiment 100 of a plant, components that are similar or equivalent to those in the first preferred embodiment are marked by the same reference numerals as used in the preceding preferred embodiment and, in order not to unduly burden the present description, are not commented in detail again.

[0098] Advantageously, as is best understood from said Fig. 3, in this second preferred embodiment, means, or apparatus, 18 are provided, for an additional withdrawing dioxane from said surfactant product 1 T.

[0099] In this manner, a surfactant product 11” can be obtained, having an extremely low dioxane amount, in particular unit being less than 2 ppm.

[0100] As is best understood from said Fig., in an appreciably advantageous manner, said means, or apparatus, 18 for an additional withdrawing dioxane from said surfactant product 11 ’ receive the surfactant product 11 ’ that was processed by said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 1 T.Advantageously, as is best understood from said Fig., said means, or apparatus, 18 for an additional withdrawing of dioxane from the surfactant product 1 T are downstream of said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 1 T and are connected with the exit 168 for said surfactant product 11’ of said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 1 T.

[0101] Advantageously, as is best understood from said Fig., in a preferred manner, said means, or apparatus, 18 for an additional withdrawing of dioxane from said surfactant product 11 ’ are in the form of means 18 adapted to perform an additional stripping of dioxane from said surfactant product 1 T.

[0102] As is best understood from said Fig., with appreciable advantage, in a particularly preferred manner, said means 18 for an additional stripping of dioxane from said surfactant product 11’ are in the form of means 18 for evaporating water from said surfactant product 1 T.

[0103] In this manner, particularly reduced costs can be achieved when obtaining said surfactant.

[0104] Advantageously, as is best understood from said Fig., said means 18 for an additional stripping of dioxane from said surfactant product 11, i.e., said means 18 for evaporating water from said surfactant product 11’, are defined by a corresponding evaporator 18.

[0105] Advantageously, as is clear from said Figures, in a preferred manner, said evaporator 18 for the additional stripping of dioxane from said surfactant product is an evaporator of the wiped film type (wiped film evaporator).

[0106] As is best understood from said Fig., with advantage, said evaporator 18 for the additional stripping of dioxane from said surfactant product has a containment body 180, in particular vertically elongated, having a circumferentially extended inner surface 181, which delimits, or defines, a corresponding additional process chamber 182, in particular vertically extended.Advantageously, as is best understood from said Fig., said evaporator 18 for the additional stripping of dioxane from said surfactant product 11 ’ has, inside said additional process chamber 182, corresponding scraping means that are adapted to spread said surfactant product 11’ along said circumferential inner surface 181 , which said scraping means, while not being particularly illustrated in attached figures, are nonetheless similar to the scraping means of said evaporator 16 for withdrawing dioxane from said surfactant product, illustrated in Fig. 2, and are movable in rotation inside said same additional process chamber 182, and preferably comprise a plurality of blades carried by a corresponding frame and arranged according to respective groups, vertically distributed, and in which the blades are circumferentially distributed, with the blades of the respective group being staggered relative to the blades of the adjacent group.

[0107] Advantageously, the tangential peripheral speed of said scraping means of said evaporator 18 for the additional stripping of dioxane from said surfactant product preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

[0108] As is best understood from said Figure, in an advantageous manner, said evaporator 18 for the additional stripping of dioxane from said surfactant product comprises means 186 for inputting said surfactant product 1 T to be additionally processed into said additional process chamber 182.

[0109] Advantageously, as is best understood from said Figure, said means 186 for inputting said surfactant product 1 T to be additionally processed into said process chamber 182 are provided on top, i.e., in an upper position, to said containment body 180 of the same evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0110] Advantageously, as is best understood from said Figure, said means 186 for inputting said surfactant product 1 T to be additionally processed into said additional process chamber 182 comprise a single inlet, or mouth, 186for the input into said containment body 180 of the evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0111] As is best understood from said Figure, in a particularly advantageous manner, said evaporator 18 for the additional stripping of dioxane from said surfactant product comprises means 188 for the exit of said additionally processed surfactant product 11 ” from the same evaporator for the additional stripping of dioxane from said surfactant product 18, i.e., from the corresponding additional process chamber 182.

[0112] Advantageously, as is best understood from said Figure, said means for the exit of said surfactant product 11” additionally processed from said evaporator for the additional stripping of dioxane from said surfactant product 18, i.e., from the corresponding additional process chamber 182, comprise a single exit mouth 188 opening, in particular vertically, downwardly provided at the lower end of the same evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0113] Advantageously, as is best understood from said Figure, said means, or apparatus, 18 for an additional withdrawing of dioxane from said surfactant product 11’ comprise means 187 to input process water, in particular said evaporator 18 for the additional stripping of dioxane from said surfactant product comprises means 187 to input process water into said additional process chamber 182.

[0114] As is best understood from said Figure, in an appreciably advantageous manner, said means 187 to input process water into said additional process chamber 182 comprise a plurality of inlets, especially distributed, in particular vertically, along said containment body 180, and adapted to input said process water into said additional process chamber 182 at corresponding distributed positions, in particular vertically, of said same additional process chamber 182.

[0115] Advantageously, as is best understood from said Figure, saidevaporator 18 for the additional stripping of dioxane from said surfactant product comprises means 189 that are adapted to create a vacuum, or depression, condition, into said additional process chamber 182 of said evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0116] Advantageously, as is best understood from said Figure, said means 189 that are adapted to create a vacuum, or depression, condition, into said additional process chamber 182, of said evaporator 18 for the additional stripping of dioxane from said surfactant product, comprise a corresponding suctioning device, in particular mounted on top, i.e., superiorly, to the containment body 180 of the same evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0117] With appreciable advantage, said means 189 that are adapted to create a vacuum, or depression, condition, into said additional process chamber 182 of said evaporator 18 for the additional stripping of dioxane from said surfactant product are adapted to create a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

[0118] Advantageously, as is best understood from said Figure, said means, or apparatus, 18 for an additional withdrawing of dioxane from said surfactant product 11’ comprises means 1810 for thermally heating said surfactant product 11’, in particular said evaporator 18 for the additional stripping of dioxane from said surfactant product comprises thermal heating means 1810, in particular to heat said additional process chamber 182.

[0119] Advantageously, as is best understood from said Figure, said thermal heating means 1810, i.e., to heat said additional process chamber 182, comprise a jacket for a heating fluid provided for in said containment body 180, of said evaporator 18 for the additional stripping of dioxane from said surfactant product, externally to said inner surface 181, circumferentially extended, defining said additional process chamber 182.With advantage, said thermal heating means 1810, in particular to heat said additional process chamber 182, are adapted to induce, especially inside the same additional process chamber 182, a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e. , which is of about the latter temperature range.

[0120] Advantageously, as is best understood from said Fig. 3, in the second preferred embodiment 100 of a plant, connecting means 17 are provided, which are adapted to transfer said surfactant product 11 between said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 and said means, or apparatus, 18 for an additional withdrawing of dioxane from surfactant product 11.

[0121] Advantageously, as is best understood from said Figure, said means for a connection, between said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11 and said means, or apparatus, 18 for an additional withdrawing of dioxane from surfactant product 1 T, comprise a conduit 17 connecting said means, or mouth, 168 for the exit of said surfactant product 11’, of said evaporator 16 for withdrawing dioxane from said surfactant product, with said means 186 for inputting said surfactant product 1 T to be additionally processed into said additional process chamber 182 of said evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0122] As is clear from said Figures, in an advantageous manner, in the present plant, means, or reactor, 12 are provided, for the production of said intermediate product 111, which comprise an elongated body, or reactor, 120 having an inlet per the organic substance, an inlet 122 for sulphuric anhydride, or for a similar reaction substance, and an exit 123 for said intermediate product 111.

[0123] Advantageously, as is clear from said Figures, in the present plant,connecting means 13 are provided, which are adapted to transfer an intermediate product 111 between the means, or reactor, 12 for the production of said intermediate product 111 and the means, or apparatus, 14 adapted to make the same surfactant product stable.

[0124] Advantageously, as is clear from said Figures, said connecting means between the means, or reactor, 12 for the production of said intermediate product 111 and said means, or apparatus, 14 adapted to make the same surfactant product stable comprise a conduit 13 connecting said means, or mouth, 123 for the exit of said intermediate product 111, from said means, or reactor, 12 for the production of said intermediate product 111, with said means, or mouth, 143 for inputting said intermediate product 111 into said neutralization reactor 14, i.e., into said neutralization chamber 142 of said neutralization reactor 14.

[0125] Advantageously, as is clear from said Figures, means 1210’ for quenching the product being processed in said means, or reactor, 12 for the production of said intermediate product 111 are provided for.

[0126] In this manner, less dioxane is produced in said intermediate product. Advantageously, as is clear from said Figures, said means 1210’ for quenching the product being processed in said means, or reactor, 12 for the production of said intermediate product 111, are adapted to cool the product between 5° C and 40° C, and preferably between 20° C and 30° C.

[0127] In this manner, less dioxane is produced in said intermediate product. Advantageously, as is clear from said Figures, said means 1210’ for quenching the product being processed in said means, or reactor, 12 for the production of said intermediate product 111, are in the form of corresponding means 1210' operating in the lower portion of the same means, or reactor, 12 for the production of said intermediate product 111, i.e., in the proximity of the outlet 123 thereof.

[0128] In this manner, less dioxane is produced in said intermediate product.in particular, as is clear from said Figures, the means 1210 for cooling the product being processed in said means, or reactor, 12 for the production of said intermediate product 111, comprise respective cooling sections, respectively, a lower quenching section 1210’, having a respective inlet 121 T and a respective outlet 1212’ of cooling fluid, in particular water, an intermediate quenching section 1210”, having a respective inlet 1211” and a respective outlet 1212” of cooling fluid, in particular water, and an upper quenching section 1210’”, having a respective inlet 121 T” and a respective outlet 1212’” of cooling fluid, in particular water.

[0129] With advantage, said means for quenching the product being processed in said means, or reactor, 12 for the production of said intermediate product 111, are defined by the cooling section 1210' that operates in the lower portion of the same means, or reactor, 12 for the production of said intermediate product 111, i.e., in the proximity of the outlet 123 thereof.

[0130] From said Figures 1 to 5, preferred embodiments are inferred, of a process for producing a surfactant product 11 , in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product, which is a product having a pasty texture.

[0131] In particular, as already stated above, said surfactant product 11 is obtained by neutralization of an intermediate product 111, i.e., of a non-stable surfactant product, in particular in the form of a sulphonic acid, which is neutralized, i.e., made stable, via a neutralization agent 144’, in particular in the form of an alkaline agent, preferably in the form of caustic soda, said intermediate product 111 being preferably obtained by sulfation preferably via sulfuric anhydride, i.e., sulfuric acid, of an ethoxylate, in turn obtained by ethoxylation of an organic substance, i.e., of corresponding fatty alcohols, with ethylene oxide.

[0132] In a particularly advantageous manner, as illustrated, according to theprocess, it is provided for withdrawing dioxane from said surfactant product 11 , i.e. , from said neutralized or stabilized surfactant product 11.

[0133] In this manner, it is possible to obtain a surfactant product 11 having a degree of harmfulness to humans and to the environment that is advantageously reduced.

[0134] In particular, a surfactant product may be obtained, having a dioxane amount in the same surfactant product that is particularly low, especially being of less than 10 ppm, preferably being less than 5 ppm, and optimally less than 2 ppm.

[0135] Advantageously, according to the process, the withdrawing of dioxane from said surfactant product 11 occurs by stripping of dioxane from said surfactant product 11.

[0136] Advantageously, according to the process, the stripping of dioxane from said surfactant product 11 occurs by evaporation of water from said surfactant product 11.

[0137] In an appreciably advantageous manner, according to the process, the stripping of dioxane from said surfactant product 11 , is carried out by using an evaporator 16, in particular an evaporator of the wiped film type (wiped film evaporator).

[0138] Advantageously, according to the process, said evaporator 16 has, inside the process chamber 162, corresponding scraping means 163 that are adapted to spread said surfactant product 11 along the circumferential inner surface 161 of said evaporator 16 for withdrawing dioxane from said surfactant product, which preferably have a tangential peripheral speed of said scraping means 163 that preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

[0139] In this manner, the stripping of dioxane from said surfactant product being stabilized or neutralized 11 is thus also improved.Advantageously, according to the process, for withdrawing dioxane from said surfactant product 11 process water is inputted into the same surfactant product 11, in particular, as needed, into said evaporator 16 for withdrawing dioxane from said surfactant product comprises means 167 to input process water, especially into said process chamber 162.

[0140] Advantageously, as stated above, according to the process, it is provided for creating a vacuum, or depression, condition, in particular inside the process chamber 162 of said evaporator for withdrawing dioxane from said surfactant product 16, and preferably a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

[0141] In this manner, the stripping of dioxane from said surfactant product being stabilized or neutralized 11 is thus improved.

[0142] With appreciable advantage, as stated above, according to the process, that, in order to withdraw dioxane from said surfactant product 11 , i.e. , from said neutralized or stabilized surfactant product 11 , it is provided for heating said surfactant product 11, in particular by heating the process chamber 162 of said evaporator 16 for withdrawing dioxane from said surfactant product, in particular to a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e., which is of about the latter temperature range.

[0143] Advantageously, according to the process, it is provided for making the surfactant product 11 stable, in particular operating the neutralization of the corresponding intermediate product 111.

[0144] Advantageously, according to the process, in order to make said surfactant product 11 stable, a neutralization reactor 14 is used, in particular in the form of an evaporator of the wiped film type.

[0145] In an appreciably advantageous manner, according to the process, during the stabilization of said surfactant product 11, i.e., during theneutralization of said intermediate product 111, it is provided for heating the product being processed, in particular providing for an evaporation of water from said intermediate product being processed, preferably operating in a vacuum, or depression, condition, in particular inside the neutralization chamber 142 of said neutralization reactor 14.

[0146] Advantageously, according to the process, it is provided for supplying water into said intermediate product 111, in particular into the same neutralization chamber 142.

[0147] Advantageously, according to the process, during the stabilization of said intermediate product 111, i.e., during the neutralization of said intermediate product 111, in particular in said neutralization chamber 142 of said neutralization reactor 14, it is provided for withdrawing dioxane from the same intermediate product being processed.

[0148] With appreciable advantage, according to the process, a vacuum, or depression, condition is provided, in particular inside the neutralization chamber 142 of said neutralization reactor 14, which vacuum, or depression, condition ranges between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

[0149] Advantageously, according to the process, said neutralization reactor 14 has, inside said neutralization chamber 142, corresponding scraping means that are adapted to spread said surfactant product 11 along the circumferential inner surface 141 of the same neutralization chamber 142, which scraping means are rotating with a tangential peripheral speed ranging between 6 m / sec and 10 m / sec and that is preferably about 8 m / sec.

[0150] In this manner, the stripping of dioxane from said surfactant product being stabilized or neutralized 11 is thus also improved.

[0151] Advantageously, according to the process, the heating of the intermediate product being processed inside the neutralization chamber 142 of said neutralization reactor 14, is kept at a temperature ranging between30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e. , which is of about the latter temperature range.

[0152] In this manner, the stripping of dioxane can be increased, without in any case reducing the quality del surfactant product that is thus obtained.

[0153] Advantageously, according to the process, in said neutralization chamber 142, of the neutralization reactor 14, a surfactant product 11 is provided, having a water concentration ranging between 70% and 95%, preferably between 72% and 90%.

[0154] In this manner, it is thus possible to operate within said neutralization reactor with said intermediate product being processed in a more concentrated form, further promoting the stripping of dioxane from the same surfactant product.

[0155] Advantageously, according to the process, water is supplied to said surfactant product 11 during the transfer between said means, or apparatus, 14 adapted to make said surfactant product 11 stable and said means, or apparatus, 16 for withdrawing dioxane from said surfactant product 11.

[0156] In this manner, said surfactant product 11 containing Sodium Laureth Sulfate can be thus brought to a concentration di Sodium Laureth Sulfate ranging between 70% and 90% of the same surfactant product, and thus easily operate within said evaporator for withdrawing dioxane from said surfactant product.

[0157] Advantageously, according to the process, following said withdrawing of dioxane from said surfactant product 11, in particular inside said evaporator 16 for withdrawing dioxane from said surfactant product, an additional withdrawing of dioxane from said surfactant product 11’ can be provided for, in particular inside a corresponding evaporator 18 for said additional withdrawing of dioxane from said surfactant product.

[0158] In this manner, a surfactant product 11” can be obtained, having anextremely low dioxane amount, in particular until being less than 2 ppm. As is best understood from said Fig. 3, with advantage, according to the process, the additional withdrawing of dioxane from said surfactant product 1 T occurs via an additional stripping of dioxane from said surfactant product 1 T.

[0159] Advantageously, according to the process, said additional stripping of dioxane from said surfactant product 1 T occurs by evaporation of water from said surfactant product 1 T.

[0160] In this manner, particularly reduced costs can be achieved when obtaining said surfactant.

[0161] Advantageously, according to the process, said additional stripping of dioxane from said surfactant product 11, is carried out by using a corresponding evaporator 18, in particular an evaporator of the wiped film type (wiped film evaporator).

[0162] As is best understood from said Fig. 3, with advantage, according to the process, said evaporator 18 for the additional stripping of dioxane from said surfactant product has, inside said additional process chamber 182, corresponding scraping means that are adapted to spread said surfactant product 11’ along said circumferential inner surface 181, which preferably have a tangential peripheral speed of said scraping means ranging between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

[0163] Advantageously, as is clear from the corresponding Figures, for an additional withdrawing of dioxane from said surfactant product 11’, process water is inputted into the same surfactant product, in particular into said evaporator 18 for the additional stripping of dioxane from said surfactant product.

[0164] Advantageously, according to the process, it is provided for creating a vacuum, or depression, condition, in particular into said additional processchamber 182 of said evaporator 18, for the additional stripping of dioxane from said surfactant product, and preferably a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

[0165] Advantageously, as is clear, according to the process, in order to provide for an additional withdrawing of dioxane from said surfactant product 11’, it is provided for thermally heating said surfactant product 11’, in particular to a temperature ranging between 30° C and 95° C, preferably to a temperature ranging between 40° C and 90° C, and optimally to a temperature ranging between 70° C and 80° C, i.e. , which is of about the latter temperature range.

[0166] As is clear from said Figures, according to the process, said intermediate product 111 is produced, or made, in particular in corresponding means, or reactor, 12 for the production of the same intermediate product 111.

[0167] Advantageously, according to the process, the product being processed is quenched, in particular in said means, or reactor, 12, for the production of said intermediate product 111.

[0168] Advantageously, according to the process, said quenching of the product being processed, in particular in said means, or reactor, 12, for the production of said intermediate product 111, provides for cooling the product between 5° C and 40° C, and preferably between 20° C and 30° C.

[0169] Advantageously, according to the process, said quenching of the product being processed, in particular in said means, or reactor, 12, for the production of said intermediate product 111, is operated in the lower portion of the same means, or reactor, 12 for the production of said intermediate product 111, i.e., in the proximity of the outlet 123 thereof.

[0170] In this manner, a surfactant product 11” can be obtained, having an extremely low dioxane amount, in particular until being less than 2 ppm.

[0171] In the subsequent Fig. 4, a third preferred embodiment 200 isillustrated, of a plant for producing a surfactant product, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product, in which especially said surfactant product is obtained by neutralization of an intermediate product 111 of said surfactant product, which is fed to the plant portion illustrated in Fig. 4 coming from a reactor 12, which however is not particularly illustrated in this Fig. 4. In Fig. 4, the components of this third preferred embodiment 200 that are similar or equivalent to those of the preceding preferred embodiments are not commented in detail again in order not to unduly burden the present description.

[0172] Advantageously, this third preferred embodiment 200 of a plant differs, in particular from the preceding second preferred embodiment 100, in that a vacuum flash chamber apparatus 18’, in which water is evaporated from the product by virtue of the heat of neutralization and the heat that is obtained by a corresponding heat exchanger 18” are used as means, or apparatus, for an additional withdrawing of dioxane from said surfactant product 1 T.

[0173] In particular, as is best understood from said Fig. 4, the heat exchanger 18” is outside the chamber 182’ of the apparatus 18’ in a corresponding loop, or recirculation, circuit, 18’”, in which a water supply 187’ is also present.

[0174] In the subsequent Fig. 5, a fourth preferred embodiment 300 is illustrated, of a plant for producing a surfactant product, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product, in which especially said surfactant product is obtained by neutralization of an intermediate product 111 of said surfactant product, which is fed to the plant portion illustrated in Fig. 5 coming from a reactor 12, which however is not particularly illustrated in this Fig. 5. In Fig. 5, the components of this fourth preferred embodiment that are similar or equivalent to those of the preceding preferredembodiments are not commented in detail again in order not to unduly burden the present description.

[0175] Advantageously, this fourth preferred embodiment 300 of a plant differs, in particular from the preceding second preferred embodiment 100, in that a vacuum flash chamber apparatus 14’, in which the water is evaporated from the product by virtue of the heat of neutralization and the heat that is obtained from a corresponding heat exchanger 14” are used as means, or apparatus, that are adapted to make said surfactant product 11 stable, in particular carrying out the neutralization of the corresponding intermediate product 111 of said surfactant product.

[0176] In particular, as is clear from Fig. 5, the heat exchanger 14” is outside the chamber 142’ of the apparatus 14’ in a corresponding loop, or recirculation, circuit, 14’”, in which a water supply 148’ is also present.

[0177] In practice, as is clear, the technical characteristics illustrated above allow, individually or in a respective combination, achieving one or more of the following advantageous results:

[0178] - A surfactant product can be obtained, having a degree of harmfulness to humans and to the environment that is advantageously reduced;

[0179] - A surfactant product can be obtained, having a dioxane amount in the same surfactant product that is particularly low, especially being less than 10 ppm, preferably being less than 5 ppm, and optimally less than 2 ppm;

[0180] - The stripping of dioxane from said surfactant product is improved; - A particularly advantageous composition of said surfactant product can thus be obtained;

[0181] - A particularly advantageous distribution of water in said surfactant product inside the corresponding reactor or evaporator can thus be obtained;

[0182] - The stripping of dioxane can be increased, without in any case reducing the quality of said surfactant product;- An advantageous stripping of dioxane from said surfactant product being stabilized or neutralized is obtained;

[0183] - It is thus possible to operate within said neutralization reactor with said product being processed that is more concentrated, further promoting the stripping of dioxane from the same surfactant product;

[0184] - A surfactant product having an extremely low dioxane amount, in particular unit being less than 2 ppm can also be obtained;

[0185] - Particularly reduced costs can be achieved to produce said surfactant product.

[0186] The present invention is susceptible of evident industrial application. Those skilled in the art may also envisage a number of modifications and / or variations to be made to the same invention, while remaining within the scope of the inventive concept as broadly set forth. Furthermore, those skilled in the art may envisage further preferred embodiments of the invention comprising one or more of the features illustrated above with reference to the aforesaid preferred embodiment, in particular as set forth in the appended claims. Moreover, it is also to be understood that all the details of the invention may be replaced with technically equivalent elements.

Claims

CLAIMS1. A plant (10) for producing a surfactant product, in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product; especially said surfactant product being obtained by neutralization of an intermediate product (111 ) of said surfactant product; the plant (10) being characterized in that it comprises means, or apparatus, (16) for withdrawing dioxane from a surfactant product (11), i.e., from a neutralized or stabilized surfactant product (11).

2. The plant according to claim 1 , characterized in that said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (11 ) are in the form of means (16) for stripping dioxane from said surfactant product (11), in particular said means (16) for stripping dioxane from said surfactant product (11) are in the form of means (16) for evaporating water from the same surfactant product (11 ).

3. The plant according to claim 2, characterized in that said means (16) for stripping dioxane from said surfactant product (11), i.e., said means (16) for evaporating water from said surfactant product (11 ), are in the form of an evaporator (16), in particular of the so-called scraped film type.

4. The plant according to claim 3, characterized in that said evaporator (16) for withdrawing dioxane from said surfactant product has, within said process chamber (162), corresponding scraping means (163) that are adapted to spread said surfactant product (11) along said circumferential inner surface (161), which scraping means (163) are movable in rotation inside the same process chamber (162).

5. The plant according to claim 4, characterized in that the tangential peripheral speed of said scraping means (163) preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

6. The plant according to any one of the preceding claims, characterizedin that said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (11) comprise means (167) to input process water, in particular said evaporator (16) for withdrawing dioxane from said surfactant product comprises means (167) to input process water, especially into said process chamber (162), and preferably in that said means (167) to input process water into said process chamber (162) comprise a plurality of inlets, especially distributed, in particular vertically, along said containment body (160), and adapted to input said process water into said process chamber (162) at corresponding distributed positions, in particular vertically, of said same process chamber (162).

7. The plant according to any one of the preceding claims, characterized in that said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (11) comprise means (169) that are adapted to create a vacuum, or depression, condition, in particular into said process chamber (162) of said evaporator (16) for withdrawing dioxane from said surfactant product.

8. The plant according to claim 7, characterized in that said means (169) that are adapted to create a vacuum, or depression, condition, in particular into said process chamber (162) of said evaporator (16) for withdrawing dioxane from said surfactant product, are adapted to create a vacuum condition ranging between 5 mbar and 100 mbar and that is preferably about 50 mbar.

9. The plant according to any one of the preceding claims, characterized in that said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (11) comprise means (1610) for thermally heating said surfactant product (11) subjected to dioxane withdrawal, in particular said evaporator (16) for withdrawing dioxane from said surfactant product comprising thermal heating means (1610), in particular to heat said process chamber (162).

10. The plant according to claim 9, characterized in that said thermal heating means (1610), in particular to heat said process chamber (162), comprise a jacket for a heating chamber provided in said containment body (160) externally to said circumferentially extended inner surface (161), defining said process chamber (162).

11. The plant according to any one of the preceding claims 9 and 10, characterized in that said thermal heating means (1610), in particular to heat said process chamber (162), are adapted to induce, especially inside the same process chamber (162), a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70°C and 80° C, i.e. , which is about the latter temperature range.

12. The plant according to any one of the preceding claims or according to the pre-characterizing part of claim 1, characterized in that means, or apparatus, (14) are provided for, which are adapted to make said surfactant product (11) stable, in particular carrying out the neutralization of the corresponding intermediate product (111 ) of said surfactant product.

13. The plant according to claim 12, characterized in that said means, or apparatus, adapted to make said surfactant product (11) stable comprise, or consist in, a corresponding neutralization reactor (14); in particular in that said neutralization reactor (14) is defined by an evaporator of the scraped film type.

14. The plant according to claim 13, characterized in that said neutralization reactor (14) comprises means for the inlet (144) of said neutralization agent, in particular in the form of an alkaline agent.

15. The plant according to any one of the preceding claims 12 to 14, characterized in that means (1460) for heating the product being processed are provided for inside the same neutralization chamber (142) of said neutralization reactor (14); in particular in that said means (1460) for heatingthe product being processed inside the same neutralization chamber (142) of said neutralization reactor (14) define means for evaporating water from said intermediate product being processed, and / or in that said means (1460) for heating the product being processed inside the same neutralization chamber (142) of said neutralization reactor (14) operate under a vacuum condition.

16. The plant according to any one of the preceding claims 12 to 15, characterized in that means (148) for supplying water into said neutralization chamber (142) are provided for.

17. The plant according to claim 16, characterized in that said means (148) for supplying water into said neutralization chamber (142) comprise a plurality of water inlets, especially distributed, in particular vertically, along said containment body (140), and adapted to input said process water into said process chamber (142) at corresponding distributed positions, in particular vertically, of said same process chamber (142).

18. The plant according to any one of the preceding claims 12 to 17, characterized in that said means, or apparatus, (14) adapted to make said intermediate product (111) stable, i.e. , said neutralization reactor (14), are, or is, adapted to withdraw dioxane from the same intermediate product being processed.

19. The plant according to any one of the preceding claims 12 to 18, characterized in that means (146) are provided for, which are adapted to create a vacuum, or depression, condition, into said neutralization chamber (142), of said neutralization reactor (14), being adapted to create a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

20. The plant according to any one of the preceding claims 12 to 19, characterized in that said neutralization reactor (14) has, within said neutralization chamber (142), corresponding scraping means that are adapted to spread said product being processed inside the sameneutralization chamber (142) of said neutralization reactor (14) along said circumferential inner surface (141), which said scraping means are movable in rotation inside the same neutralization chamber (142).

21. The plant according to claim 20, characterized in that the tangential peripheral speed of said scraping means of said neutralization reactor (14) into said neutralization chamber (142) of said neutralization reactor (14) preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

22. The plant according to any one of the preceding claims 15 to 21, characterized in that said means (1460) for heating the product being processed inside the same neutralization chamber (142) of said neutralization reactor (14) are adapted to cause, in particular inside the same neutralization chamber (142) of the same neutralization reactor (14), a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e., which is about the latter temperature range.

23. The plant according to any one of the preceding claims 13 to 22, characterized in that said neutralization reactor (14) is configured to process, and in particular to output, a surfactant product (11) having a concentration in water ranging between 0% and 60%, preferably between 10% and 30%.

24. The plant according to any one of the preceding claims, characterized in that means, or apparatus, (18) are provided for, for an additional dioxane withdrawal from said surfactant product (1 T).

25. The plant according to claim 24, characterized in that said means, or apparatus, (18) for an additional dioxane withdrawal from said surfactant product (1 T) receive the surfactant product (1 T) that has been processed by said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (1 T).

26. The plant according to claim 25, characterized in that said means, orapparatus, (18) for an additional dioxane withdrawal from surfactant product (11’) are downstream of said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (11’) and are connected to the outlet (168) for said surfactant product (11’) of said means, or apparatus, (16) for withdrawing dioxane from said surfactant product (1 T).

27. The plant according to any one of the preceding claims 24 to 26, characterized in that said means, or apparatus, (18) for an additional dioxane withdrawal from said surfactant product (1 T) are in the form of means (18) adapted to perform an additional stripping of dioxane from said surfactant product (1 T).

28. The plant according to claim 27, characterized in that said means (18) for an additional stripping of dioxane from said surfactant product (1 T) are in the form of means (18) for evaporating water from said surfactant product (11).

29. The plant according to any one of the preceding claims 24 to 28, characterized in that said means (18) for the additional stripping of dioxane from said surfactant product (1 T), i.e. , said means (18) for evaporating water from said surfactant product (1 T), are defined by a corresponding evaporator (18).

30. The plant according to claim 29, characterized in that said evaporator (18) for the additional withdrawal of dioxane from said surfactant product is an evaporator of the scraped film type.

31. The plant according to claim 30, characterized in that the tangential peripheral speed of the scraping means of said evaporator (18) for the additional withdrawal of dioxane from said surfactant product preferably ranges between 2 m / sec and 20 m / sec, especially between 8 m / sec and 12 m / sec, and optimally is about 10 m / sec.

32. The plant according to any one of the preceding claims 29 to 31 , characterized in that said evaporator (18) for the additional withdrawal ofdioxane from said surfactant product comprises means (189) that are adapted to create a vacuum, or depression, condition, into said additional process chamber (182) of said evaporator (18) for the additional withdrawal of dioxane from said surfactant product.

33. The plant according to claim 32, characterized in that said means (189) that are adapted to create a vacuum, or depression, condition, into said additional process chamber (182) of said evaporator (18) for the additional withdrawal of dioxane from said surfactant product are adapted to create a vacuum condition ranging between 5 mbar and 100 mbar and that is preferably about 50 mbar.

34. The plant according to any one of the preceding claims 24 to 33, characterized in that said means, or apparatus, (18) for an additional dioxane withdrawal from said surfactant product (1 T) comprise means (1810) for thermally heating said surfactant product (11’), in particular said evaporator (18) for the additional withdrawal of dioxane from said surfactant product comprises thermal heating means (1810), in particular to heat said additional process chamber (182).

35. The plant according to claim 34, characterized in that said thermal heating means (1810), in particular to heat said additional process chamber (182), are adapted to cause, in particular inside the same additional process chamber (182), a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70°C and 80° C, i.e. , which is about the latter temperature range.

36. The plant according to any one of the preceding claims 34 and 35, characterized in that said means, or apparatus, (18) for an additional withdrawal of dioxane from said surfactant product (1 T) comprise means (187) to input process water, in particular said evaporator (18) for the additional withdrawal of dioxane from said surfactant product comprisesmeans (187) to input process water into said additional process chamber (182).

37. The plant according to any one of the preceding claims or according to the pre-characterizing part of claim 1, characterized in that means, or reactor, (12) are provided for, for the production of said intermediate product (111).

38. The plant according to claim 37, characterized in that means (1210’) for quenching the product being processed in said means, or reactor, (12) for the production of said intermediate product (111) are provided for.

39. The plant according to claim 38, characterized in that said means (1210’) for quenching the product being processed in said means, or reactor, (12) for the production of said intermediate product (111), are adapted to cool the product between 5° C and 40° C, and preferably between 20° C and 30° C.

40. The plant according to any one of the preceding claims 37 and 38, characterized in that said means for quenching the product being processed in said means, or reactor, (12) for the production of said intermediate product (111), are in the form of corresponding means (1210') that operate in the lower part of the same means, or reactor, (12) for the production of said intermediate product (111), i.e., in the proximity of the outlet (123) thereof.

41. A process for producing a surfactant product (11), in particular containing Sodium Laureth Sulfate, preferably in an amount ranging between 70% and 90% of the same surfactant product; especially said surfactant product (11 ) being obtained by neutralization of an intermediate product (111) of said surfactant product; the process being characterized in that it is provided for withdrawing dioxane from said surfactant product (11 ), i.e., from said neutralized or stabilized surfactant product (11).

42. The process according to claim 41, characterized in that the withdrawal of dioxane from said surfactant product (11) occurs by strippingdioxane from said surfactant product (11), in particular by evaporating water from said surfactant product (11), especially, said stripping of dioxane from said surfactant product (11) is performed by using an evaporator (16), in particular an evaporator of the scraped film type.

43. The process according to any one of the preceding claims 41 and 42, characterized in that the creation of a vacuum, or depression, condition, is provided for inside the process chamber (162) of said evaporator (16) for withdrawing dioxane from said surfactant product, and preferably a vacuum condition ranging between 5 mbar and 100 mbar, and which is preferably about 50 mbar.

44. The process according to any one of the preceding claims 41 to 43, characterized in that , in order to withdraw dioxane from said surfactant product (11), i.e., from said neutralized or stabilized surfactant product (11), the heating of said surfactant product (11) is provided for, in particular by heating the process chamber (162) of said evaporator (16) for withdrawing dioxane from said surfactant product, preferably at a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70°C and 80° C, i.e., which is about the latter temperature range.

45. The process according to any one of the preceding claims 41 to 44 or according to the pre-characterizing part of claim 41 , characterized in that it is provided to make the surfactant product (11) stable, in particular by carrying out the neutralization of the corresponding intermediate product (111); in particular, in order to make said surfactant product (11) stable, a neutralization reactor (14) is used, in particular in the form of an evaporator of the scraped film type.

46. The process according to claim 45, characterized in that, during the stabilization of said intermediate product (111), i.e., during the neutralization of said intermediate product (111), in particular in said neutralization chamber(142) of said neutralization reactor (14), a withdrawal of dioxane from the same intermediate product being processed is provided for.

47. The process according to any one of the preceding claims 45 and 46, characterized in that a vacuum, or depression, condition is provided for, in particular inside the neutralization chamber (142) of said neutralization reactor (14), which vacuum, or depression, condition ranges between 5 mbar and 100 mbar, and preferably is of about 50 mbar.

48. The process according to any one of the preceding claims 45 to 47, characterized in that, during the stabilization of said surfactant product (11), i.e., during the neutralization of said intermediate product (111), the heating of the intermediate product being processed is provided for, in particular by providing an evaporation of water from said intermediate product being processed, preferably operating under a vacuum, or depression, condition, in particular inside the neutralization chamber (142) of said neutralization reactor (14).

49. The process according to claim 48, characterized in that the heating of the intermediate product being processed, in particular inside the neutralization chamber (142) of said neutralization reactor (14), is maintained at a temperature ranging between 30° C and 95° C, preferably a temperature ranging between 40° C and 90° C, and optimally a temperature ranging between 70° C and 80° C, i.e., which is about the latter temperature range.

50. The process according to any one of the preceding claims 41 to 49, characterized in that, following said withdrawal of dioxane from said surfactant product (11), in particular inside said evaporator (16) for withdrawing dioxane from said surfactant product, an additional withdrawal of dioxane from said surfactant product (1 T) can be provided, in particular inside a corresponding evaporator (18) for said additional withdrawal of dioxane from said surfactant product.

51. The process according to any one of the preceding claims 41 to 50 oraccording to the pre-characterizing part of claim 41 , characterized in that the product being processed is quenched for producing an intermediate product (111), in particular in that said quenching of the product being processed for the production of said intermediate product (111) provides for a cooling of the product between 5° C and 40° C, and preferably between 20° C and 30° C; and / or in that said quenching of the product being processed for the production of said intermediate product (111) is carried out in the lower part of the same means, or reactor, (12) for the production of said intermediate product (111), i.e., in the proximity of the outlet (123) thereof.

52. A plant and a process, each being respectively characterized in that it is made according to any one of the preceding claims and / or as described and illustrated with reference to the attached drawings.

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