FIELD The present disclosure relates to a regenerative adsorbent composition for removal of chlorides from chloride containing hydrocarbon feed and a process for its preparation.

DEFINITION

As used in the present disclosure, the following terms are generally intended to have the meaning as set forth below, except to the extent that the context in which it is used indicates otherwise.

Chemisorption refers to adsorption method wherein the adsorbed material(s) is/are held by chemical bonds.

Extruding aid refers to an additive which reduces or eliminates surface defects that appear during extrusion process. Adsorption capacity refers to the amount of adsorbate taken up by the adsorbent per unit mass (or volume) of the adsorbent. With reference to the present disclosure, the adsorption capacity of the adsorbent composition refers to the amount of the chloride ions that is adsorbed per gram of the adsorbent composition till the chloride content in the treated hydrocarbon feed is < 1 ppm. Layered double hydroxides (LDH) refers to a class of ionic solids, typically minerals characterized by a layered structure with the generic layer sequence [ACBZACB]n, where C represents layers of metal cations, A and B are layers of hydroxide (HO ) anions, and Z are layers of other anions and neutral molecules (such as water).

Ion exchanged Zeolite refers to the zeolites wherein the metal cations present in the zeolite are exchanged with other ions such as alkali metal, alkaline earth metal, hydronium ions and ammonium ions or mixture thereof. The zeolite framework is open, contain channels and interconnected voids filled with exchangeable cations to balance the negative charge of zeolite lattice. BACKGROUND

The background information herein below relates to the present disclosure but is not necessarily prior art.

Organo-chlorine compounds, such as carbon tetrachloride and perchloroethylene are added continuously in the process to maintain the chlorine level on the Continuous Catalytic reforming (CCR) catalyst. In many instances, the organic chlorides may become a part of the hydrocarbon product during the reaction of the hydrocarbon streams from which the hydrocarbon product is produced. If chemically-combined chlorines, such as organic chlorides, are not removed from the hydrocarbon streams, the presence of organic chlorides in the resultant hydrocarbon products, particularly gasoline or other fuels, can cause corrosion of processing equipment and engine parts, as well as other detrimental effects like loss in the activity of the metal-containing reforming catalysts to such an extent that the catalyst loses its ability to promote the various individual reforming reactions. In addition, the catalyst may lose its ability to promote the desired reforming reactions such that the catalyst loses the desired selectivity for desired products. Chloride contamination is particularly harmful in the processes involving disproportionation and alkylation of toluene to para-xylene and para- ethyl toluene over ZSM-5 zeolite catalysts which also contain magnesium.

Conventionally, methods such as catalytic hydro -dechlorination is used for the removal of chloride compounds. This method involves the transformation of organic chloride compounds to hydrogen halide, which is subsequently removed by caustic treatment. However, this technique has disadvantages like loss of unsaturated or oxygenated compounds, moreover this method is complex and expensive.

Therefore, there is felt a need for an adsorbent capable of removing chloride compounds from hydrocarbon. OBJECTS

Some of the objects of the present disclosure, which at least one embodiment herein satisfies, are as follows:

It is an object of the present disclosure to ameliorate one or more problems of the prior art or to at least provide a useful alternative. An object of the present disclosure is to provide an adsorbent composition for removing chloride compounds from the chloride containing hydrocarbon feed.

Another object of the present disclosure is to provide an adsorbent composition that can be regenerated. Still another object of the present disclosure is to provide a process for preparing an adsorbent composition for removing chloride compounds from the chloride containing hydrocarbon feed.

Other objects and advantages of the present disclosure will be more apparent from the following description, which is not intended to limit the scope of the present disclosure. SUMMARY

The present disclosure relates to a regenerative adsorbent composition for removal of chlorides from the chloride containing hydrocarbon feed and a process for its preparation.

In first aspect, the present disclosure provides a regenerative adsorbent composition comprising an ion exchanged zeolite; bauxite; a layered double hydroxide; and a binder. Typically, the regenerative adsorbent composition comprising an ion exchanged zeolite in an amount in the range of 30 to 50 wt% of the total mass of the composition on dry basis; bauxite in an amount in the range of 1 to 20 wt% of the total mass of the composition on dry basis; a layered double hydroxide in an amount in the range of 40 to 60 wt% of the total mass of the composition on dry basis; and a binder in an amount in the range of 1 to 20 wt% of the total mass of the composition on dry basis.

In second aspect, the present disclosure provides a process for preparing an adsorbent composition for removal of chlorides from chloride containing hydrocarbon feed. The process comprises dry mixing the ion exchanged zeolite with bauxite, a layered double hydroxide, and a binder to obtain a dry mixture. The mixture is kneaded in a fluid medium, at least one surfactant and at least one extruding aid. The kneaded mixture is extruded to form shaped articles, followed by drying and calcining the shaped articles to obtain the adsorbent composition.

In third aspect, the present disclosure provides a process for removal of chlorides from chloride containing hydrocarbon feed using the regenerative adsorbent composition. The process involves passing chloride containing hydrocarbon feed through a bed consisting of the adsorbent composition comprising an ion exchanged zeolite, bauxite, a layered double hydroxide, and a binder to obtain a treated hydrocarbon feed having chloride content less than 1 ppm. In fourth aspect, the present disclosure provides a process for regeneration of an adsorbent composition by purging the adsorbent composition with a stream selected from air, nitrogen, and carbon dioxide at a temperature in the range of 250-550 °C and for a time period in the range of 4 to 6 hours. The regeneration of the adsorbent composition can also be carried out by purging the adsorbent composition with a stream at a temperature in the range of 100-150 °C for a time period in the range of 4 to 6 hours. The process further comprises calcining at a temperature in the range of 300 to 600 °C for a time period in the range of 3 to 5 hours to obtain a regenerated adsorbent composition.

The adsorbent composition of the present disclosure can be regenerated at last 5 times and can be used effectively to remove chlorides from the chloride containing hydrocarbon feed. BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWING

The present disclosure will now be described with the help of the accompanying drawing, in which:

Figure 1 illustrates a schematic representation of a set up for removal of the chloride content from the hydrocarbon feed using the adsorbent composition of the present disclosure. DETAILED DESCRIPTION

Embodiments, of the present disclosure, will now be described with reference to the accompanying drawing.

Embodiments are provided so as to thoroughly and fully convey the scope of the present disclosure to the person skilled in the art. Numerous details are set forth, relating to specific components, and process, to provide a complete understanding of embodiments of the present disclosure. It will be apparent to the person skilled in the art that the details provided in the embodiments should not be construed to limit the scope of the present disclosure. In some embodiments, well-known processes, well-known apparatus structures, and well-known techniques are not described in detail. The terminology used, in the present disclosure, is only for the purpose of explaining a particular embodiment and such terminology shall not be considered to limit the scope of the present disclosure. As used in the present disclosure, the forms "a,” "an," and "the" may be intended to include the plural forms as well, unless the context clearly suggests otherwise. The terms "comprises," "comprising,"“including,” and“having,” are open ended transitional phrases and therefore specify the presence of stated features, integers, steps, operations, elements, modules, units and/or components, but do not forbid the presence or addition of one or more other features, integers, steps, operations, elements, components, and/or groups thereof. The particular order of steps disclosed in the process and process of the present disclosure is not to be construed as necessarily requiring their performance as described or illustrated. It is also to be understood that additional or alternative steps may be employed.

Presence of chlorides in hydrocarbon products has an adverse effect on downstream processes as well as it causes corrosion of the processing equipments. Catalytic and adsorption techniques are usually employed for removal of chlorides from refinery/ hydrocarbon products. Conventional techniques used for the removal of chloride compounds are complex and expensive.

In first aspect, the present disclosure provides a regenerative adsorbent composition capable of removing low levels of chlorides from the diverse hydrocarbon feeds.

The adsorbent composition comprises an ion exchanged zeolite; bauxite; a layered double hydroxide; and a binder.

The adsorbent composition typically comprises an ion exchanged zeolite in an amount in the range of 30 to 50 wt% of the total mass of the composition on dry basis, preferably 36 to 44 wt%; bauxite in an amount in the range of 1 to 20 wt% of the total mass of the composition on dry basis, preferably 4 to 6 wt%; a layered double hydroxide in an amount in the range of 40 to 60 wt% of the total mass of the composition on dry basis, preferably 48 to 52 wt%; and a binder in an amount in the range of 1 to 20 wt% of the total mass of the composition on dry basis, preferably 4 to 6 wt%.

In accordance with an exemplary embodiment of the present disclosure, the adsorbent composition comprises an ion exchanged zeolite in an amount in the range of 40 wt% of the total mass of the composition on dry basis; bauxite in an amount in the range of 5 wt% of the total mass of the composition on dry basis; a layered double hydroxide in an amount in the range of 50 wt% of the total mass of the composition on dry basis; and a binder in an amount in the range of 5 wt% of the total mass of the composition on dry basis.

The adsorbent composition has bulk density in the range of 0.5 to 0.7 g/cc; a BET Surface area in the range of 200 to 500 m 2 /g; a crushing strength in the range of 2.5 to 3.5 Kgf/cm 2 ; and a particle size in the range of 1 to 6 mm. In accordance with an exemplary embodiment, the adsorbent composition has a bulk density of 0.6 g/cc; a BET Surface area of 213 m /g; and a crushing strength in the range of 3.0 Kgf/cm .

In accordance with the present disclosure, when ion exchanged zeolites are used in combination with bauxite and layered double hydroxides, organic chlorides present in the hydrocarbon feed get decomposed into a corresponding unsaturated hydrocarbon molecules, and molecule of hydrogen chloride, which is later picked up by the adsorbent. The metal ions present in the zeolite contribute both in providing the acidity of the adsorbent composition along with the adsorption of hydrogen chloride, leading to the formation of respective chloride salt. Overall, both physical and chemisorption occurs, thereby indicating the renewability of the adsorbent, as physio-sorption is reversible in nature.

Typically, the ion exchanged zeolite is faujasite zeolite having Si/Al ratio in the range of 1.4 to 3.0; and the cation of the zeolite being partially exchanged with at least one metal selected from copper and indium. The particle size of the ion exchanged zeolite is in the range of 0.2 to 0.5 pm, preferably 0.3 pm.

Typically, bauxite comprises aluminium oxide (Al ₂ 0 ₃ ) in an amount in the range of 40 to 60 wt% of the total mass of bauxite; iron oxide (Fe ₂ 0 ₃ ) in an amount in the range of 5 to 15 wt% of the total mass of bauxite; silica (Si0 ₂ ) in an amount in the range of 2 to 10 wt% of the total mass of bauxite; titanium oxide (Ti0 ₂ ) in an amount in the range of 1 to 5 wt% of the total mass of bauxite; calcium oxide (CaO) in an amount in the range of 1 to 5 wt% of the total mass of bauxite; and water in an amount in the range of 15 to 30 wt% of the total mass of bauxite. The particle size of bauxite is in the range of 0.2 to 0.3 pm, preferably 0.25 pm.

The layered double hydroxide is hydrotalcite having magnesium oxide (MgO) to aluminium oxide (Al ₂ 0 ₃ ) ratio in the range of 4 to 5, a BET surface area in the range of 10 to 20 m /g and a particle size in the range of 0.30 to 0.60 pm. The particle size of the layered double hydroxide is in the range of 0.2 to 0.4 pm, preferably 0.3 pm. The binder is at least one selected from bentonite clay and kaolinite clay. In accordance with the exemplary embodiment of the present disclosure, the binder is bentonite clay and the particle size of the bentonite clay is in the range of 0.1 to 0.2 pm, preferably 0.15 pm.

The chloride adsorption capacity of the adsorbent composition is in the range of 20 to 30 wt%.

In accordance with the exemplary embodiment of the present disclosure, the adsorbent composition comprises faujasite zeolite in an amount of 44 wt% and having particle size of 0.3 pm; bauxite in an amount of 5 wt% and having particle size of 0.25 pm; hydrotalcite in an amount of 50 wt% and having particle size of 0.3 pm; and bentonite clay in an amount of 5 wt% and having particle size of 0.15 pm.

In second aspect, the present disclosure provides a process for preparing an adsorbent composition for removal of chlorides from the chloride containing hydrocarbon feed. The process is described in detail herein below:

Initially, the ion exchanged zeolite is mixed with a layered double hydroxide, bauxite and a binder to obtain a dry mixture. The so obtained mixture is kneaded in a fluid medium comprising a pre-determined amount of water, at least one surfactant and at least one extruding aid. The kneaded mixture is then extruded to form shaped articles; followed by drying under inert atmosphere at a temperature in the range of 80 °C to 150 °C for a time period in the range of 1 hour to 5 hours. The dried articles are further calcined under inert atmosphere at a temperature in the range of 300 °C to 600 °C for a time period in the range of 3 hours to 6 hours to obtain the adsorbent composition.

Typically, the fluid medium used for kneading the mixture is a combination of ethanol and water. The amount of water in the fluid medium is in the range of 70 to 80 wt%.

Typically, the amount of extruding aid in the fluid medium is in the range of 1 to 10 wt% and the extruding aid is at least one selected from the group consisting of stearic acid, palmetic acid, oleic acid, calcium stearate and zinc stearate.

The surfactant is used in an amount in the range of 1 to 10 wt% and the surfactant is at least one fatty acid selected from the group consisting of behenic acid, lauric acid, and lignoceric acid. In accordance with the exemplary embodiment of the present disclosure, the process comprises dry mixing the faujasite zeolite with hydrotalcite, bauxite and bentonite clay to obtain a dry mixture. A fluid medium consisting of a mixture of ethanol and water, along with 5 wt% of calcium stearate and 5 wt% of lauric acid are added to the dry mixture to obtain a resultant mixture. The resultant mixture is kneaded to obtain a kneaded mixture; followed by extruding the kneaded mixture to form shaped articles. The so obtained shaped articles are dried at 150 °C for 2 hours, followed by calcining at 550 °C for 5 hours to obtain the adsorbent composition.

In third aspect, the present disclosure provides a process for removal of chlorides from the chloride containing hydrocarbon feed. The process involves the step of passing chloride containing hydrocarbon feed through a bed consisting of the adsorbent composition comprising an ion exchanged zeolite, bauxite, a layered double hydroxide, and a binder to obtain a treated hydrocarbon feed having substantially reduced chloride content.

Typically, the chloride containing hydrocarbon feed is passed through a bed consisting of the adsorbent composition at a temperature in the range of 30 to 50 °C, under a pressure in the range of 30 to 40 kg/cm ; and at a liquid hourly space velocity (LHSV) in the range of 0.5 per hour to 5 per hour.

In accordance with an exemplary embodiment of the present disclosure, the chloride containing hydrocarbon feed is contacted with an adsorbent composition at 40 °C, under a pressure of 35 kg/cm ; and at a liquid hourly space velocity (LHSV) in the range of 2 per hour.

In accordance with the embodiment of the present disclosure, the chloride containing hydrocarbon feed is pre-heated at a temperature in the range of 30 to 50 °C so that a uniform temperature is obtained through out the bed consisting of the adsorbent composition.

The hydrocarbon feed treated in accordance with the present disclosure has chloride content of less than 1 ppm.

In fourth aspect, the present disclosure provides a process for regeneration of an adsorbent composition. The process comprises purging the adsorbent composition with a stream selected from air, nitrogen, and carbon dioxide at a temperature in the range of 250-550 °C and for a time period in the range of 4 to 6 hours. Further the regenerated catalyst is activated by calcining at a temperature in the range of 300 to 600 °C for a time period in the range of 3 to 5 hours.

In accordance with an embodiment of the present disclosure, the regeneration of the adsorbent composition can also be carried out by purging the adsorbent composition with steam at a temperature in the range of 100-150 °C for a time period in the range of 4 to 6 hours. The process further comprises calcining at a temperature in the range of 300 to 600 °C for a time period in the range of 3 to 5 hours to obtain a regenerated adsorbent composition.

Further, the regenerated adsorbent is capable of 100% adsorption after I ^st regeneration. Still further, the physicochemical properties of the regenerated adsorbent are similar to the fresh adsorbent, further no leaching of active metal ions present in the zeolite is observed. The adsorbent of the present disclosure can be re-generated at least 5-6 time/cycles and has an adsorption capacity up to 60 % to 70 % of the fresh adsorbent composition.

The present disclosure is further illustrated with help of the figure.

Figure-1 discloses a schematic representation of the process for removal of chlorides from the chloride containing hydrocarbon feed. Typically, the assembly used in the process for the removal of chlorides comprises a nitrogen source (2), a storage tank (3) and a feed tank (4) adapted to store the chloride containing hydrocarbon feed, a preheater (5) adapted to preheat the chloride containing hydrocarbon feed, a packed bed column (7) loaded with adsorbent composition, an electric heater furnace (6) and a condenser (9). The chloride containing hydrocarbon feed is passed through the packed bed column at a liquid hourly space velocity (LHSV) in the range of 0.5 per hour to 5 per hour with the help of the pump. The temperature of the fixed bed column is maintained in the range of 200 to 350 °C with the help of an electric furnace and further passed through condenser to obtain the treated hydrocarbon feed. In accordance with the embodiment of the present disclosure, the chloride containing hydrocarbon feed is pre-heated using an electric heater furnace (6) at a temperature in the range of 30 to 50 °C so that a uniform temperature is obtained through out the bed consisting of the adsorbent composition.

The adsorbent composition of the present disclosure provides the following advantages:

It has high chloride pick-up capacity without any side reaction. It is sensitive to the fluctuation in chloride content and variations in the process conditions, i.e., the adsorbent is capable of detecting variation in the chloride content in an ongoing process and remove chloride accordingly.

Since the adsorbent composition can be regenerated and reused for a number of cycles, it needs to be disposed of after 3-4 years as compared to yearly disposal in case of existing commercial adsorbents.

Use of the adsorbent composition of the present disclosure minimizes changeover and thereby increases overall production.

It is capable of protecting the downstream catalyst poisoning and thereby enhancing the downstream hydrocarbon yield.

It protects the process equipment from corrosion thereby enhancing the life of plant.

The process for preparing the adsorbent composition is cost effective as it involves easily available raw material. Moreover, the adsorbent composition can process feed which is 30-40 times its own weight. - The adsorbent composition has a purification capacity >99% thereby improving its life cycle as well as protecting the process equipment.

Loss of unsaturated or oxygenated compounds is not observed when the adsorbent of the present disclosure is used for the removal of chlorides from hydrocarbon.

The adsorbent composition is capable of being operated at mild conditions. It is capable of dehydrochlorination (mild catalytic activity) followed by adsorption and can simultaneously remove both organic and inorganic chlorides from diverse hydrocarbon streams.

The foregoing description of the embodiments has been provided for purposes of illustration and not intended to limit the scope of the present disclosure. Individual components of a particular embodiment are generally not limited to that particular embodiment, but, are interchangeable. Such variations are not to be regarded as a departure from the present disclosure, and all such modifications are considered to be within the scope of the present disclosure. The present disclosure is further described in light of the following experiments which are set forth for illustration purpose only and not to be construed for limiting the scope of the disclosure. The following experiments can be scaled up to industrial/commercial scale and the results obtained can be extrapolated to industrial scale. EXPERIMENTAL DETAILS

Experiment- 1: Preparation of the adsorbent composition in accordance with the present disclosure

Ion exchanged zeolite (40 g) having particle size of 0.3 pm was mixed hydrotalcite having stearate and hydroxide as counter ions (50 g) having particle size of 0.3 pm, bauxite (5 g) having particle size of 0.25 pm and bentonite (5 g) having particle size of 0.15 pm to obtain a mixture. The mixture was kneaded using a mixture of water (75 wt%), ethanol (25 wt%), calcium stearate (5 wt%)and lauric acid (5 wt%). The formed dough was extruded using an extruder to obtain extrudates having the size 2 mm. The so obtained extrudates were air dried at 150 °C for 2 hours; followed by calcination at 550 °C for 5 hours to obtain the adsorbent composition.

Physiochemical properties of the adsorbent composition are given in Table 1 below.

Experiment-2: Preparation of the adsorbent composition (Comparative Example)

Layered double hydroxide powder having stearate and hydroxide as counter ions (70 g) having particle size of 0.3 pm was mixed with bauxite (20 g) having particle size of 0.2 pm and a bentonite (10 g) having particle size of 0.2 pm to obtain a mixture. The mixture was kneaded using a mixture of water (75 wt%), ethanol (25 wt%), calcium stearate (5 wt%) and lauric acid (5 wt%). The formed dough was then extruded using an extruder to obtain extrude having size of 2 mm. The so obtained extrudates were air dried at 150 °C for 2 hours; followed by calcination at 550 °C for 5 hours to obtain the adsorbent composition. The mechanical properties of the adsorbent were measured.

Physiochemical properties of the adsorbent composition are given in Table 1 below.

Table 1:

From Table 1, it is evident that the adsorbent composition of the present disclosure has increased surface area as compared to the adsorbent composition without ion exchanged zeolite. Experiment 3: Treatment of the chloride containing hydrocarbon feed using adsorbent composition of experiment 1

The dynamic adsorption capacity of the prepared adsorbents was measured using the experimental set up illustrated in Figure-1.

26 g adsorbent was loaded in a fixed bed column and the temperature of the column was maintained at 40 °C and the pressure was maintained at 35 kg/cm ² . Chloride containing feed from recovery plus unit (3.5ppm) was passed through this bed at LHSV = 2 h ¹ .

800 ltr. of the feed could be purified when the chloride content of the treated feed reached a value of lppm. 1 ppm was considered the breakthrough point as chloride content above 1 ppm is considered to be lethal for the health of downstream catalyst and adsorbents. The chloride adsorption capacity of the adsorbent was determined to be 11 wt%.

Experiment 4: Treatment of the chloride containing hydrocarbon feed using adsorbent composition of experiment 2

The dynamic adsorption capacity of the prepared adsorbents was measured using the experimental set up illustrated in Figure-1. 25 g adsorbent was loaded in a fixed bed column and the temperature of the column was maintained at 40 °C and the pressure was maintained at 35 kg/cm ² . Chloride containing feed from recovery plus unit (3.5 ppm) was passed through this bed at LHSV = 2 h ¹ .

597 ltr of the feed could be purified till the chloride content of the treated feed at outlet reached a value of lppm. 1 ppm was considered the breakthrough point as chloride content above 1 ppm is considered to be lethal for the health of downstream catalyst and adsorbents.

The chloride adsorption capacity of the adsorbent was determined to be 8 wt%.

Experiment 5: Measuring chloride adsorption capacity of the adsorbent composition

The chloride adsorption capacity of the adsorbent was measured by contacting lg of the adsorbent with 10 g of chloride containing hydrocarbon feed containing organic and inorganic chloride (3.5 ppm) in vials. The vial was kept overnight.

The chloride measurement was carried out with help of chloride analyzer working on the principle of colorimetric titration.

The chloride content of the treated hydrocarbon feed was found to be 0 ppm. Experiment 6: Measuring chloride adsorption capacity of the adsorbent composition of experiment 2

The chloride adsorption capacity of the so obtained adsorbent composition was measured by contacting lg of the adsorbent with 10 g of chloride containing hydrocarbon feed containing organic and inorganic chloride (3.5 ppm) in vials. The vial was kept overnight. The chloride measurement was carried out with help of chloride analyzer working on the principle of colorimetric titration.

The chloride content of the treated hydrocarbon feed was found to be 0 ppm.

Experiment 7: Measuring chloride adsorption capacity of the adsorbent composition of experiment 1 The adsorbent was kept in contact with a mixture of nitrogen + HC1 (500 ppm) overnight for 12 hours. Chloride analysis of spent adsorbent was done using Mohr’s method.

The chloride adsorption capacity of the adsorbent was 25 wt%. Experiment 8: Measuring chloride adsorption capacity of the adsorbent composition of experiment 2

Further, the adsorbent was kept in contact with a mixture of nitrogen + HC1 (500 ppm) overnight for 12 hours. Chloride analysis of the spent adsorbent was done using Mohr’s method.

The chloride adsorption capacity of the adsorbent was determined to be 20 wt%.

Experiment 9: Regeneration of the spent adsorbent prepared in accordance with the present disclosure

The spent adsorbents were regenerated in-situ using hot air at 250 °C. Hot air was passed through the spent bed for 5-6 hours at 250 °C, followed by activating at 350 °C for 3-5 hours.

Experiment 10: Treatment of the chloride containing hydrocarbon feed using the regenerated adsorbent composition of the present disclosure

Dynamic adsorption capacity of the regenerated adsorbents was measured using the experimental set up illustrated in Figure-1. 25g adsorbent was loaded in a fixed bed column and the temperature of the column was maintained at 40 °C and the pressure was maintained at 35 kg/cm ² . Chloride containing feed from recovery plus unit (3.5 ppm) was passed through this bed at LHSV = 2 h ¹ .

597 ltr of the feed could be purified when the chloride content of the treated feed reached a value of 1 ppm. TECHNICAL ADVANCEMENTS

The present disclosure described herein above has several technical advantages including, but not limited to, the realization of an adsorbent composition that has:

- has high adsorption capacity, long life, high stability and no side effects;

- can be regenerated; and is economical. The embodiments as described herein above, and various features and advantageous details thereof are explained with reference to the non-limiting embodiments in the following description.

The embodiments herein and the various features and advantageous details thereof are explained with reference to the non-limiting embodiments in the following description. Descriptions of well-known components and processing techniques are omitted so as to not unnecessarily obscure the embodiments herein. The examples used herein are intended merely to facilitate an understanding of ways in which the embodiments herein may be practiced and to further enable those of skill in the art to practice the embodiments herein. Accordingly, the examples should not be construed as limiting the scope of the embodiments herein.

The foregoing description of the specific embodiments so fully reveal the general nature of the embodiments herein that others can, by applying current knowledge, readily modify and/or adapt for various applications such specific embodiments without departing from the generic concept, and, therefore, such adaptations and modifications should and are intended to be comprehended within the meaning and range of equivalents of the disclosed embodiments. It is to be understood that the phraseology or terminology employed herein is for the purpose of description and not of limitation. Therefore, while the embodiments herein have been described in terms of preferred embodiments, those skilled in the art will recognize that the embodiments herein can be practiced with modification within the spirit and scope of the embodiments as described herein.

The use of the expression“at least” or“at least one” suggests the use of one or more elements or ingredients or quantities, as the use may be in the embodiment of the disclosure to achieve one or more of the desired objects or results.

Any discussion of documents, acts, materials, devices, articles or the like that has been included in this specification is solely for the purpose of providing a context for the disclosure. It is not to be taken as an admission that any or all of these matters form a part of the prior art base or were common general knowledge in the field relevant to the disclosure as it existed anywhere before the priority date of this application.

The numerical values mentioned for the various physical parameters, dimensions or quantities are only approximations and it is envisaged that the values higher/lower than the numerical values assigned to the parameters, dimensions or quantities fall within the scope of the disclosure, unless there is a statement in the specification specific to the contrary.

While considerable emphasis has been placed herein on the components and component parts of the preferred embodiments, it will be appreciated that many embodiments can be made and that many changes can be made in the preferred embodiments without departing from the principles of the disclosure. These and other changes in the preferred embodiment as well as other embodiments of the disclosure will be apparent to those skilled in the art from the disclosure herein, whereby it is to be distinctly understood that the foregoing descriptive matter is to be interpreted merely as illustrative of the disclosure and not as a limitation.