MXPA98010535A - System of adsorbent and / or catalyst and agglomerante enhanced by contact with ac - Google Patents

Abstract

This invention relates to a process for producing an enhanced absorbent particle, comprising contacting a porous, porous, crystalline, non-ceramic, non-amorphous particle of aluminum produced by calcination at a particle temperature of 300. §C to 700§C, with one acid for a sufficient time to increase the adsorbent properties of the particle. A process for producing an enhanced adsorbent particle comprising contacting a porous, non-ceramic, porous, adsorptive particle with an acid for a time sufficient to increase the adsorbent properties of the particle is also presented. Particles prepared by the process of the present invention and particle feeds are also provided as, for example, correction of waste streams. The invention also relates to a method for the production of an adsorbent and / or catalyst and binder system. The invention also relates to particles made by the process, binders and methods for correcting contaminants in a stream. The invention also relates to an anchor system of adsorbent and / or catalyst and agglomerates

Description

SYSTEM OF ADSORBENT AND / OR CATALYST AND AGGLOMERANTE ENHANCED BY CONTACT WITH ACID BACKGROUND OF THE INVENTION RELATED REQUESTS (I) This relationship is (i) a continuation in part of the US application Serial No. 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of the US application No. of series 08 / 351,600, filed on December 7, 1994, abandoned; (2) a continuation in part of the US application Serial No. 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of PCT / US95 / 1582, filed on December 6, 1995, which is a continuation in part of the North American application no. of series 08 / 351,600, filed on December 7, 1994, abandoned; (3) a continuation in part of the US application Serial No. 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of the US application Serial No. 08 / 426,981, filed on April 21, 1995, abandoned; and (4) a continuation in part of the US application Serial No. 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of PCT / US96 / 05303, filed on October 17, 1996. April 1996, which is a continuation in part of the North American application Na. series 08 / 426,981, filed on April 21, 1995, abandoned. (II) This application is also (i) a continuation in part of the US application Serial No. 08 / 734,331, filed on October 21, 1996, pending, which is a continuation in part of the US application Ha. series 08 / 662,331, filed on June 12, 1996, pending, which is (a) a continuation in part of the US application Serial No. 08 / 351,600, filed on December 7, 1994, abandoned, ( b) a continuation in part of PCT / US95 / 15829, filed on December 6, 1995, which is a continuation in part of the US application Serial No. 08 / 351,600, filed on December 7, 1994, abandoned , (c) a continuation in part of the North American patent application Na. in series 08 / 426,981, filed on April 21, 1995, abandoned, and (d) a continuation in part of PCT / US96 / 05303, filed on April 17, 1996, which is a continuation in part of the North American application ericana Serial No. 08 / 426,981, filed on April 21, 1995, abandoned and (2) a continuation in part of the North American application No, series 08 / 734,331, filed on October 21, 1996, pending, which is a continuation in part of PCT / US95 / 1582, filed on June 12, 1995, which is a continuation in part of the US application Serial No. 08 / 351,600 filed on December 7, 1994, abandoned. (III) This application is also (1) a continuation in part of the US application Serial No. 08 / 734,330, filed on October 21, 1996, pending, which is a continuation in part of PCT / US96 / 05303, filed on April 17, 1996, pending, which is a continuation in part of the US application Serial No. 08 / 426,981, filed on April 21, 1995, pending; (2) a continuation in part of the North American application Serial No. 08 / 734,330, filed on October 21, 1996, pending, which is a continuation in part of the North American request Na. of series 08 / 426,981, filed on April 21, 1995, pending; (3) a continuation in part of the North American application Na. of series 08 / 734,330, filed on October 21, 1996, pending, which is a continuation in part of the North American application Na. series 08 / 662,331, filed on June 12, 1996, pending, which is (a) a continuation in part of the US application Serial No. 08 / 351,600, filed on December 7, 1994, abandoned, (b) a continuation in part of PCT / US95 / 15829, filed on December 6, 1995, which is a continuation in part of the US application Serial No. 08 / 351,600, filed on December 7 1994, abandoned, (c) a continuation in part of the US application Serial No. 08 / 426,981, filed on April 21, 1995, abandoned, and (d) a continuation in part of PCT / US96 / 05303, filed on April 17, 1996, which is a continuation of part of the US application Serial No. 08 / 426,981, filed on April 21, 1995, abandoned; and (4) a continuation in part of the US application Serial No. 08 / 734,330, filed on October 21, 1996, pending, which is a continuation in part of PCT / US95 / 15829, filed on June 12. of 1995, pending, which is a continuation in part of the American application Serial No. 08 / 351,600, filed on December 7, 1994, abandoned. All the aforementioned applications will be incrapated here by reference in their entirety regarding all their teachings. FIELD OF THE INVENTION This invention relates, in general terms, to enhanced adsorbent particles, particularly particles that have been enhanced in terms of their adsorbent property by contacting them with an acid. This invention also relates generally to an adsorbent / catalyst particle having improved adsorbent properties and / or improved or newly existing catalytic properties by using the particle in combination with a particle binder to produce a particle / binder system. The binder can be either cross-linked with the particle, crosslinked in itself and envalver the particle or both. This invention also relates to a binder / adsorbent system and / or catalyst that can be used as an anchored catalyst system. BACKGROUND OF THE ART Oxides of metals and some non-metals are known to be useful for removing constituents of a gas or liquid stream by adsorbent mechanisms. For example, the use of activated alumina is considered an economic method of water treatment for the removal of various pollutants, gases and some liquids. Its highly porous structure allows the capacity of preferential adsorption of moisture and contaminants contained in gases and some liquids. It is useful as a drying agent for gases and vapors in the petroleum industry, and has also been used as a catalyst or catalyst-vehicle, in chromatography and in water purification. The removal of contaminants, such as phosphates by activated alumina, is known in the art. See, for example, Yee, W., "Selective Remaval of Mixed Phosphates by Activated Alumina" (Selective Removal of Mixed Phosphates by Activated Alumina), J. Amer. Water arks Assoc., Val, 58, pages 239-247 (1996). The North American patent Na. 4,795,735 to Liu et al. presents an activated carbon / aluminum compound and a process for the production of the compound. The compound is prepared by mixing powdered activated carbon and activated alumina. After complete mixing, an aqueous solution is added to allow the activated alumina to be rehydratablely bound to the carbon particles. The amount of water added must not exceed the amount that prevents the explosion or agglomeration of the mixture. After the addition of the water, the mixture is subjected to a formation process using extrusion, agglomeration or pelletization in order to obtain a green body. The green body is then heated to a temperature of 25-100 ° C or is. The compound can be reinforced by peptization by addition of nitric acid to the mixture. It is indicated that alumina can serve as a binder as well as an absorbent. This patent does not make use of calcined alumina. Liu et al. shows an amorphous alumina trihydrate powder such as CP2 obtained in Alcoa and an amorphous alumina trihydrate powder as for example CP-1 to good CP-7, indicated in US patent No. 4,579,839, which is incorporated by reference in Liu et al. The use by Liu et al. The term "active" refers to the dried surface water and does not refer to a calcined particle. Liu et al., Use acid to reinforce the particle and increase its adsorbent properties. Liu et al., Have an alumina percursor, which is absorbent and not adsorbent. U.S. Patent No. 3,360,134 to Pullen presents a composition having adsorption properties and catalytic properties. Example 2 shows an alumina hydrate formed by partial dehydration of a-alumina trihydrate in a rotary dryer by countercurrent flow with a heated gas and an inlet temperature of approximately 1200 ° F and an outlet temperature of approximately 300 ° F. The resulting product was washed with 57% sulfuric acid, rinsed with water and dried to a free water content of about 2.7 .. Solid sucrose was mixed with the hydrate and the mixture was heated. Example 4 indicates that the procedure of example 2 was repeated except that calcined alumina was used. The product was not adequate when calcined alumina was used. Thus, the acid washed product of example 2 na was calcined alumina. U.S. Patent No. 4,051,072 to Bedford et al. presents a ceramic alumina that can be tratrated with very dilute acid to neutralize the free alkali metal, mainly Na20, to allow impregnation with catalytic material at a controlled depth of at least 90 to about 250 microns. This patent does not employ a crystallized aluminum oxide that has been calcined in accordance with the present invention. This patent calcines the particle at a temperature of about 1700 ° F to about 50 ° C (927 ° C to 1016 ° C) to form a ceramic material, specifically what is referred to herein as an alumina. U.S. Patent No. 5,242,879 to Abe et al. it indicates that activated carbon materials subjected to carbonization and activation treatment, and then further subjected to an acid treatment and a heat treatment, have a high catalyst activity and are suitable as catalysts for the decomposition of hydrogen peroxide, hydrazines or else water contaminants such as organic acids, quaternary ammonium salts, and sulfur-containing compounds. The acid is used to remove impurities and na to increase the adsorbing characteristics. This patent also does not employ a particle of the present invention. Adsorbent particles of the prior art have achieved the ability to remove particulate contaminants from a liquid to gas stream, such as a waste stream or potable water, to acceptably low levels. In addition, the adsorbent particles of the prior art have been able to be fixed firmly with particulate contaminants in such a way that the adsorbent / contaminant particle composition can be easily removed in a sanitary container. Here, there is a need for an adsorbent technique that has the improved ability to adsorb atheryl and particulates, particularly contaminants from a gas or liquid stream, to purify said stream in this manner. In the art there is a need for adsorbent particles that bind tightly to adsorbed aminants. Salts have discovered that particles enhanced with acid solve the aforementioned problems. The American patent Ha. 5,422,323 to Banerjee et al. presents the preparation of a pumpable refractory insulator composition. The composition consists of the combination of a wet component of colloidal silica (40%) in water, and a dry component consisting of standard refractory material. Examples of refractory materials include clay, kaolinite, mulite, alumina and alumina silicates. The resulting insulating composition was cast, dried and baked to form an insulating layer. Japanese Patent No. 63264125 to Fumikazu et al. presents the preparation of dry dehumidifying materials. Moisture is removed from the ambient air or from a gas as it passes through a dehumidifying rotor of zeolite (70% by weight) and an inorganic binder (2-30% by weight). The inorganic binder includes colloidal silica, colloidal alumina, silicates, aluminates and bentonite. The moist air passes through the dehumidifying rotor, and the amount of dry air is evaluated. Japanese Patent No. 60141680 to Kanbe et al. presents the preparation of a refractory lining preparation material. The material prepared by the addition of a solution of phosphoric acid with an ultra fine silica powder to a mixture of refractory clay and refractory aggregates composed of calcined and crushed clay, alumina, silica, zirconium and pyrophyllite. The refractory material has an improved bond strength and a tiny structure, it is useful for metal castings in bed melt for example casting, tundish and electric ovens. Adsorbent particles of the. Prior art has not achieved the ability to remove contaminants and particles from a liquid or gas stream, such as a waste stream or potable water at acceptably low levels. In addition, the adsorbent particles of the prior art have not been able to be firmly fixed on particulate contaminants in such a way that the adsorbent / contaminant particle composition can safely be removed in a sanitary landfill. Thus, there is a need for adsorbents having the improved ability to adsorb particulate materials, particularly contaminants from a gas or liquid stream, in order to purify the current in this way. There is a need in the art for the adsorbent particles to be firmly fixed on the adsorbed contaminant. There is also a need for a catalyst technique that has the ability or has an improved ability to catalyze the reaction of contaminants in non-polluting byproducts. Typically, in the art, binders block active sites in absorbent and catalyst particles, thus reducing the effectiveness of such particles. In addition, there is a need in the art for a binder system that binds adsorbent and / or catalytic particles together without reducing the performance of the particles. Applicants have discovered that by using a special binder for adsorbent and / or catalytic particles, new or improved adsorbent and / or catalytic properties can be achieved due to the synergy between the binder and the adsorber and / or catalyst particle. None of the aforementioned documents presents the process compositions described and claimed herein. COMPENDIUM OF THE INVENTION In accordance with the purpose (s) of this invention, exemplified and described in general terms herein, this invention, in one aspect, relates to a process for the production of an enhanced absorbent particle comprising the contacting a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous produced by calcination at a particle temperature of 300 * C at 700 ° C, with an acid for a sufficient time to increase the properties of adsorbency of the particle. The invention further provides a process for the production of an enhanced adsorbent particle comprising contacting an oxide, porous, ceramic, adsorbent particle with an acid for a sufficient time to increase the adsorption properties of the particle. In yet another aspect, the invention offers a composition comprising the particles of the invention. In another aspect, the invention relates to a method for the production of an adsorbent and / or catalyst and binder system comprising i) the mixture of components comprising a) a binder comprising a colloidal metal oxide or colloidal metalloid oxide; b) an oxide adsorbent and / or catalyst particle, and c) an acid, ii) removal of a sufficient amount of water from the mixture to cross link components a and b to form an adsorbent system and / or catalyst and binder. In another aspect, the present invention offers a system. adsorbent and / or catalyst made by the processes of the invention. In one aspect, the invention features an adsorbent and / or catalyst and binder system comprising a binder that has been cross-linked with at least one type of oxide and / or catalyst adsorbent particles. In another aspect, the invention provides a method for reducing or eliminating the amount of a contaminant from a liquid or gas stream comprising contacting the adsorbent binder system and / or catalyst with the contaminant in the stream during a enough time to reduce or eliminate the amount of contaminants in the stream. In another aspect, the invention offers a method to catalyze the degradation of an organic compound that / comprises contacting the organic compound with the adsorbent and / or catalyst system for a sufficient time to catalyze the degradation of an organic compound.

In another aspect, the invention provides a method for reducing or eliminating the amount of contaminants from a gas stream by catalysis, comprising contacting the adsorbent binder system and / or catalyst with a gas stream containing a contaminant. comprising a nitrogen oxide, a sulfur oxide, a carbon monoxide, hydrogen sulfide or mixtures thereof for a sufficient time to reduce or eliminate the amount of contaminants. In another aspect, the invention provides a method for the production of an adsorbent and / or catalyst and binder system, comprising i) the mixture of components comprising a) a binder comprising a colloidal metal oxide or a metalloid oxide colloidal, b) a first adsorbent and / or catalytic particle that does not react in a heavy way with the binder, and c) an acid, ii) the removal of a sufficient amount of water to crosslink the component to itself, thereby trapping and maintaining the component b within the crosslinked binder, to form an adsorbency system and / or catalyst and binder. In another aspect, the invention relates to a composition for agglomerating adsorbent particles and / or catalysts to produce an agglomerated particle comprising (a) a colloidal metal oxide or colloidal metalloid oxide and (b) an acid. In another aspect, the invention relates to a set of elements for agglomerating adsorbent and / or catalyst particles to produce an agglomerated particle comprising (a) a colloidal metal oxide or colloidal metalloid oxide and (b) an acid. In another aspect, the invention provides a method for agglomerating adsorbent and / or catalyst particles, which comprises the steps of: (a) colloidal alumina or colloidal silica mixtures with the particles and an acid; (b) stirring the mixture until homogeneous; (c) heating the mixture for a sufficient time to cause crosslinking of the aluminum oxide in the mixture. In another aspect, the invention relates to an adsorbent and / or catalyst and binder system, comprising: (a) a binder substituted or either substituted with pendant ligand, and (b) a particle of oxide adsorbent and / or oxide catalyst unsubstituted or substituted by pending ligand. wherein at least one of components (a) and (b) is a substituted pending ligand, and wherein component (a) is crosslinked with a component (b).

In another aspect, the invention relates to a method for using the aforementioned system with a catalyst support system comprising the agglomeration of the above system with a second catalyst particle. In another aspect, the invention relates to an anchored binder and / or catalyst and adsorbent system, comprising: (a) a binder unsubstituted or substituted by pending ligand pair, and (b) a particle of oxide adsorbent and / or unsubstituted oxide catalyst or substituted by pendant ligand, and (c) a csmple or of metal, wherein at least one of the camponents (a) and (b) is substituted pendant ligand, where component (a) is crosslinked with a component (b) and where the metal complex (c) is attached to the component ( a) and / or (b). In another aspect, the invention relates to a method for the production of an adsorbent system and / or catalyst substituted with ligand pendiepte, comprising: (i) mixing components, comprising: (a) a binder substituted or unsubstituted with ligand slope consisting of a colloidal metal oxide or a colloidal metalloid oxide, (b) a particle of oxide adsorbent and / or oxide catalyst substituted or unsubstituted by pendant ligand, and (c) an acid, where at least Lt of the components (a) and (b) is replaced by pending ligand, and (ii) the removal of a sufficient amount of water from the mixture to crosslink the components (a) and (b) to form a catalyst and / or adsorbent system replaced by pendant ligand and binder. This method may further comprise (iii) the binding of a metal complex in the system resulting from step (ii) to form an anchored catalyst system. In another aspect, the invention relates to a method for the production of an adsorbent / catalyst and binder system, comprising: (i) mixing components comprising: (a) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, (b) a particle of oxide and / or catalyst adsorbent, and (c) an acid, (ü) removing a sufficient amount of water from the mixture to crosslink components a and b to form a catalyst system and / or adsorbents and binder and (iii) reacting the oxide adsorbent particle and / or Resolutive oxide catalyst and the binder system of step (ii) with a hydroxyl-reactive compound to form an oxide adsorbent system and / or an oxide catalyst substituted by pendant ligand and binder. In another aspect, the invention relates to the aforementioned method which further comprises after step (iii) the binding of a metal complex in the system resulting from step (iii) to form an anchored catalyst system. In another aspect, the invention relates to an adsorbent LO system and / or anchored catalyst and binder, which comprises: (a) a binder, and (b) a particle of oxide adsorbent and / or oxide catalyst, and (c) a metal complex where component (a) is crosslinked with component (b), and where the metal complex (b) is directly attached to component (a) and / s (b). In another aspect, the invention relates to a method for the production of an anchored adsorbent and / or catalyst system, comprising: (i) mixing components, comprising: (a) a binder comprising an oxide of colloidal metal or a colloidal metalloid oxide, 25 (b) a particle of oxide adsorbent and / or oxide catalyst, and (c) an acid, (ii) remove a sufficient amount of water from the mixture to crosslink the components (a) and (b) to form a system of catalyst and / or adsorbents and binder, and (iii) joining a metal complex directly on the system resulting from step (ii) to form the anchored catalyst system. In another aspect, the invention relates to a method for encapsulating a contaminant within an adsorbent particle, comprising heating the particle of the invention that has adsorbed a contaminant at a temperature sufficient to close the pores of the particle and encapsulate it. form the pollutant within the particle. In another aspect, the invention relates to a method for regenerating adsorbent particles that has adsorbed a contaminant. Further advantages of the invention will be presented in part in the following description, and in part will be apparent from the description, or may be derived from the practice of the invention. The advantages of the invention will be realized and obtained by means of the elements and I combinations particularly indicated in the appended claims. It is understood that both the foregoing general description and the following detailed description are intended to explain and exemplify said invention but not to limit it. BRIEF DESCRIPTION OF THE FIGURES Figure 1 is a graph showing the reduction of concentration of lead ions by the use of a particle of the invention. Figure 2 is a graph that shows the surface area versus curing temperature of aluminaalumin compounds. Figure 3 is a graph showing the oxidation of CO over time using a binder of Cu0 / Mn02 / A1203-colloidal alumina. Figure 4 is a graph showing the reduction of NOx with the passage of time using a Cu0 / Ga203 / A1203-colloidal alumina binder. DETAILED DESCRIPTION The present invention can be more easily understood with reference to the following detailed description of the preferred embodiments of the invention and the examples included therein. Before presenting and describing the present compositions of matter and methods, it should be understood that this invention is not limited to specific synthetic methods or particular formulations since this can obviously vary. It should also be understood that the terminology used herein is for the sole purpose of describing particular modalities and is not intended to limit the invention. In this specification and in the following claims, reference will be made to several terms that will be defined with the following meanings: the singular forms "one", "some", "the" and "the" include plural elements to which the context indicates clearly the opposite. The terms "optional" to "optionally" refer to the fact that the event or the circumstance subsequently described may occur and that the description includes cases in which said event or circumstance occurs and cases in which it does not occur. The term "particle" as used herein is used interchangeably throughout the document to refer to a particle in singular form or a combination of smaller particles grouped together in a larger particle, such as agglomeration of particles.

The term "ppm" refers to parts per million and the term "ppb" refers to parts per billion. The term "and / or" in "adsorbent and / or catalyst" refers to a particle that acts either as a catalyst, either as an adsorbent, or that can act as an adsorbent and catalyst under different circumstances due, for example, to the composition and the type of pollutant. I. ADSORBENT PARTICLE OF OXIDE AND / OR CATALYZER INCREASED BY ACID In accordance with the purpose or purposes of this invention, as shown and described in general terms herein, this invention, in one aspect, refers to a process for the production of an enhanced adsorbent particle comprising the contact pad of a particle of calcined, porous, crystalline, nacreous, amorphous aluminum oxide produced by calcination at a particle temperature of 300 ° C to 700 ° C, with an acid for a sufficient time to increase the adsorption properties of the particle. This process may also consist essentially of either the particular process raisins described above or else includes the additional characteristics described below. The invention further provides a process for the production of an enhanced adsorbent particle comprising contacting a porous, porous, naphthalic adsorbent particle with an acid for a time sufficient to increase the adsorption properties of the particle. This process can also consist essentially of either the particular process steps described above or it also includes the additional features described below. In one embodiment, this particle is calcined. In another aspect, the invention offers particles made by the process of the present invention. In another aspect, the invention provides a process for the reduction to elimination of the amount of contaminants in a stream, comprising contacting the particle of the invention with the current for a sufficient time to reduce to eliminate the contamination of said current. In another aspect, the invention provides a composition comprising the particles of the invention. The particles of this invention have improved or enhanced adsorption characteristics. The particles of this invention can adsorb a larger amount of adsarbate per unit volume or weight of adsorbent particles than non-enhanced particle Lina. Also, the particles of this invention can reduce the concentration of contaminants or adsorption material in a stream to an absolute value less than what is possible with a "non-enhanced particle." In particular embodiments, the particles of this invention can reduce the concentration of contaminants in a stream at levels below detectable levels, which is believed to have never been reached with particles of the technique? previous. Enhanced adsorption features are intended to particularly include iapes capture and ion exchange mechanisms. Ion capture refers to the ability of a particle to bind irreversibly with other atoms through covalent or ionic interactions. In this invention, ion capture typically predominates in comparison to the ion exchange property, and is typically the enhanced ion capture property that increases the adsorbent performance of the particle. Adsorption is a term well known in the art and should be distinguished from adsorption. The adsorbent particles of this invention are chemically bonded to adsorbate material and retain it very tightly. These chemical bonds are ionic and / or cavalent bonds. Without wishing to be bound by any theory, it is believed that the contact of acid with the particle enhances the adsorption capacity of the particle by including the number of hydroxyl groups in the particle. With cationic and anionic contaminants, the hydroxyl groups provide sites for chemical bonding to be replaced, so that contaminants are irreversibly bound to the particle. In general, the increased amount of hydroxyl groups generates more active sites for the contaminant to bind to these sites.

The invention captures the use of adsorbent and / or catalyst particle of the prior art or particle composed of two or more types of particles. In a preferred embodiment, the particle comprises an oxide particle, with an even greater preference, a porous, non-ceramic oxide particle. In one embodiment the particle comprises a metal oxide to metalloid particle. Examples of such particles include, but are not limited to, oxide complexes such as transition metal oxides, lanthanide oxides, thorium oxide, as well as Group IIA oxides (Mg, Ca, Sr, Ba), Group IIIA ( A, Al, Ga, In, Tí), Group IVA (Yes, Ge, Sn, Pb), and Group VA (As, Sb, Bi). In another embodiment, the particle comprises an oxide of aluminum, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconia, tungsten, renia, arsenic, magnesium, thorium, silver, cadmium, tin, lead, antimony, ruthenia, osmium, cobalt or nickel or zeolite. Typically, any oxidation state of the oxide complexes may be useful for the present invention. The oxide may be a mixture of at least two metal oxide particles having the same metal with a variable stoichiometry and varying oxidation states. In one embodiment, the particle comprises A120, Ti02, CuO, Cu02, V205, Si02, Mn02, Mn203, Mn304, ZnO, W02, 03, Re207, As203, As205, MgO, ThO, Ag20, AgO, CdO, Sn02, PbO , FeO, Fe203, Ru.203, RuO, 0s04, Sb203, CaO, Co203, NiO or else zeolite. In a further embodiment, the particle further comprises a second type of adsorbent particles and / or catalyst of an aluminum oxide, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, tungsten, rhenium, arsenic, magnesium, thorium, silver, cadmium, tin, lead, antimony, ruthenium, osmium, cobalt or nickel or zeolite, activated carbon, including coal and coconut coal, peat, zinc or tin. In another embodiment, the particle further comprises a second type of adsorber particle and / or aluminum oxide catalyst, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc, zeolite, activated carbon, peat, zinc or tin particle. Typical zeolites employed in the present invention include "Y" type, "beta" type, ardenite, and ZsM5. In a preferred embodiment, the particle comprises calcinated, porous, crystalline, non-ceramic, non-amorphous aluminum oxide produced by calcination of the precursor to obtain the calcined aluminum oxide at a particle temperature of 300 to 400 ° C at 700 ° C. , preferably in gamma, chi-rho, or eta form. The precursor of the calcined aluminum oxide may include, but is not limited to, boehmite, bauxite, pseudo-bahemite, oxide layer, A1 (0H) 3, and alumina hydrates. In the case of other metal oxide complexes, these complexes can also be found in the calcined or uncalcined state. In another embodiment of the invention, in the particle of this invention, typically any adsorbent particle that is a porous, non-ceramic oxide may be employed. Such particles of the invention are found in a crystalline drug and therefore are not amorphous. Rigid or hard adsorbent particles, dissolved in a negative degree by the acid, and having initially high adsorption properties before enhancement are preferred. Examples of such particles include, but are not limited to, metal oxides such as transition metal oxides and metal oxides from Group IIA, Group IIIA, and Group IVA (Group entry according to CAS), and metal oxides. such as silicon and germanium. Preferred adsorbents include oxides of aluminum, silicon, including zeolites, natural and synthetic, manganese, copper, vanadium, zirconis, iron and titanium. Even more preferred adsorbents include aluminum oxide (A1203), silicon dioxide (Si02), manganese oxides (MnO, Mn02, Mn203, and Mn304), copper oxides (CuO and Cu20), vanadium pentaoxide (V205), zirconium oxide (Zr02), iron oxides (FeO, Fe203, and Fe304), and titanium dioxide (Ti02). In a preferred embodiment, the particle is microparous, in an even more preferred embodiment, the particle is substantially icraparase with an average micron size preferably within a range of 3.5 n to 35 nm (35 A to 350-5) in diameter. In an even more preferred embodiment, the oxide is aluminum oxide (A1203) produced by the calcination of a particle at a temperature of 300 ° C to 700 ° C. In other embodiments, the lower limit of calcination temperature is 400 ° C, 450 ° C, 500 ° C, 550 ° C, 600 ° C, or 650 ° C and the upper limit of calcination is 650 ° C, 600 ° C, 55 ° C, 500 ° C, or 450 ° C. These preferred particles of aluminum oxide are preferably in the gamma, chi-rho, or eta form. The ceramic form of A1203, bed for example the alpha form, is included as part of this invention. In a preferred embodiment, the A1203 particles of this invention are substantially microporous with an average icropor size of 3.5 nm at 35 or 50 nm in diameter, preferably even greater than 60 nm, and with a BET surface area of 120 to 350 m2 / g. In one embodiment, the particle is aliminium oxide that has been pre-treated by a calcination process. Calcined aluminum oxide particles are well known in the art. They are particles that have been heated to a particular temperature to form a particular crystalline structure. Processes for making calcined aluminum oxide particles are well known in the art as presented, for example, in Physical and Chemical Aspects of Adsarbents and Catalyst, (Physical and chemical aspects of adsorbents and catalysts), ed. Linsen et al., Academic Press (1970), which is incorporated herein by reference. In one embodiment, the Bayer process can be used to prepare aluminum oxide precursors. Also, precalcined aluminum oxides, i.e., the aluminum oxide precursor (eg, A1 (0H) 3 or aluminum trihydrate, boehmite, pseudo-boehmite, bauxite), and calcined aluminum oxides can be easily obtained in trade. Calcined aluminum oxide can be used in this dry, activated form or it can be used in a partially to almost totally deactivated form allowing the adsorption of water on the surface of the particle. However, it is preferable to minimize deactivation to optimize the adsorbent capacity. In some references of the prior art, the term "activated" refers only to the removal of surface water from the particle to increase its adsorbent capacity. However, as is used with reference to the present invention, "activated" oxide particles refer to an oxide particle that has been first calcined and then, preferably but not necessarily, maintained in a dry state. Thus, as used herein, all the active particles of the invention have also been calcined. Na particles are limited to 3? a particular physical form and can be ep particle, dust, grab, pella, to similar. In another embodiment, in addition to acid enhancement, the adsorbent, catalyst, and adsorbent and catalyst particles embodied in this invention may be enhanced by other processes known in the art or described below. For example, the particles may be dried to be activated or they may be treated by processes presented in the related applications presented above and in the applicant's co-pending application filed on October 21, 1996, Serial No. 08 / 734,329, entitled "Enhapced Adsarbent and Roa Temperature Catalyst Particle and Methad of Making and Using Therefor", (Adsorbent and Catalyst Particle at Enhanced Ambient Temperature and Metada to Prepare and Use said Particle), which is a continuation in part of PCT / US96 / 05303, filed on April 17, 1996, pending, which is a continuation in part of the North American application Serial No. 08 / 426,981, filed on April 21, 1995, pending. These requests are incorporated here by reference. in their totalities for all their teachings. The acid which can be used in this invention can be any acid or mixture of acid that can catalyze the formation of hydroxyl groups on the surface of the pores of the oxide particle. Examples of such acids include, but are not limited to, nitric acid, sulfuric acid, hydrochloric acid, boric acid, acetic acid, formic acid, phosphoric acid, and mixtures thereof. In one embodiment, the acid is an aliphatic or aromatic carboxylic acid. In another embodiment, the acid is acetic acid. Examples of aliphatic or aromatic carboxylic acids include, but are not limited to, acetic acid, benzoic acid, butyl acid, citric acid, fatty acids, lactic acid, maleic acid, malonic acid, octyl acid, salicylic acid, stearic acid, acid succinic, tartaric acid, propionic acid, valeric acid, hexanaic acid, heptanoic acid, caprylic acid, pelargonic acid, capric acid, undecanaic acid, lauric acid, trideconic acid, myristic acid, piptadecanaic acid, palmitic acid, heptadetic acid, nonadecanic acid, arachidic acid, heneicasanoic acid, acidic behenica, triosanoic acid, lignoceric acid, pentacosanoic acid, ceric acid, heptasanoic acid, mantánica acid, nanacasanoic acid, melisic acid, phthalic acid, glutaric acid, adipic acid, azelaic acid, sebacic acid, cinnamic acid , acrylic acid, cratonic acid, lipaleic acid, or a mixture of them. In a preferred embodiment, the acid is acetic acid because it is relatively safer to handle than most other acids and because of its low cost. Typically the acid is diluted with water to avoid dissolution of a particle and to obtain a lower price. In general, it is reported that a diluted acid solution only reaches the maximum or saturated charge of the ion portions in the particle. For example, a solution of acetic acid at 0.5% by weight (0.09 N, pH of approximately 2.9) and even 0.1% by weight (0.02 N, pH of approximately 3.25) is effective. However, a wider range of acid concentrations ep this invention can be employed from very dilute concentrations to very concentrated concentrations according to the risks involved and the economic aspects of the production. However, if the acid is too concentrated, it will chemically attack the particle causing an increase in the macropores and eliminating the micropores, which is negative for the particles of this invention. Thus, the acid treatment is preferably of a concentration (ie, acid strength measured, for example, by normality or pH), acid type, temperature and duration greater than a simple surface wash but less than an attack chemical. In particular modalities, the chemical attack of the particle is minimized and it is only nominal by the selection of the acid treatment conditions co-no for example acid strength, acid type and temperature and treatment time in such a way that the reduction of the surface area overall, measured preferably by the BET method, is less than 20%, less than 15%, less than 10%, less than 5%, less than 2%, less than 1%, or less than 0.5%. For example, strong acids, such as hydrochloric, nitric or sulfuric acid, are preferably used at a concentration of strength greater than a weak acid, such as acetic acid, since the strong acid tends to chemically react with the particle and attack it chemically. to a much greater degree than a weak acid and at a comparable concentration. In a particular embodiment, the acid is of a higher force equivalent to an aqueous solution at 0.5 N (normality) of acetic acid. In other embodiments, the upper force of the acid is equivalent to an aqueous solution of acetic acid 0.25 N, 0.1 N, 0.09 N, 0.075 N, 0.05 N, 0.02 N, 0.01 N, 0. 05 N, or 0.001 N. The lower strength of the acid should be the force that provides more than a superficial wash but provides increased adsorbent effects to the particle. In particular embodiments, the lower strength of the acid is equivalent to an aqueous solution of acetic acid of 0.25 N, 0.1 N, 0.09 N, 0.075 N, 0.05 N, 0.02 N, 0.01 N, 0.005 N, 0.001 N, 0.0005 N, or O 0001 N. After the acid treatment, the resulting particle >;4 of the invention substantially retains the microporosa originally present and the acid does not chemically attack the particle appreciably and does not create any appreciable amount of new macrocraps (average pore diameter greater than about 35 nm). In a preferred embodiment, when the particle is aluminum oxide, the aluminum oxide treated with acid retains its microsaparous nature, with an average pore size of 3.5 nm to 35 nm in diameter and a BET surface area of 120 to 350 m2 / g. Additionally, the acid preferably has a certain amount of water present to offer OH- and / or H + ions that bind with the particle. Since the acid is diluted with water, the water is preferably distilled water to minimize the amount of impurities that come into contact with the particle. The particle of the invention is made by means of the following process. The particle comes into contact with an acid. The particle can come into contact with an acid in several ways, including the immersion of the particle in the acid, the extensive washing of the particle with acid, or the submergence in acid. The time during which the particle must be in contact csn the acid varies according to the capacity of the specific particle to generate hydroxyl groups on the surface and pores of the particle. The time can be 30 seconds, some minutes (three) • - •) minutes, at least 15 mint-hours, at least one hour, at least 6 hours, at least 12 hours, or at least one day, to achieve adequate adsorption results and / or to ensure saturation preference. The time must be sufficient to at least increase the adsorbent properties of the particle by adding groups with increasing hydroxyl index in the particle. In one embodiment, the particle is submerged in the acid, and saturation is typically reached when full absorption of the alumina pores with the acid solution is observed. The contacting must be sufficiently substantial to provide for the penetration of the acid into the pores of the particle thus increasing the number of hydroxyl groups on the pore surface of the particle. A simple washing of the outer surface of the particle to remove impurities is not sufficient to provide adequate penetration of the acid into the pores of the particle. Typically, contacting with acid is carried out at temperature biepte. The higher the acid temperature and the concentration, the more likely the acid will chemically negatively attack the particle. The particle contacted with the acid is then optionally rinsed, preferably with water. The rinsing of the particle in contact with the acid na reduces the enhanced adsorption capacity of the particle. When rinsing, the particle is preferably rinsed with distilled water to minimize contact with impurities. The rinsing of the particle has two purposes. First, any residual acid that remains on the surface or pores of the material is removed which makes the particle easier to handle when in dry form. Second, the rinsing of the particle removes the counter-ion of the acid that can be enriched on the surface or pores of the particle. Optionally, the particle is dried by means of a thermal treatment under woody to remove the excess of liquid, such as acid or water, from the rinse step thus increasing the adsorption activity. Typically, the drying is carried out at a temperature ranging from approximately 50 ° C to approximately 200 ° C. The drying of the particle also reduces the costs of particle transfer. However, preferably the particle is not calcined or recirculated after acid treatment and before the contact with a contaminant. Said recollection could negatively change the surface characteristics by closing the micropores. Nevertheless, the particle can be heated to calcination temperature or above after the particle has been in contact with a contaminant to encapsulate the contaminant in accordance with what is described below. In addition, the particles of the present invention are preferably not sintered, either before or after the acid treatment step, since this could negatively accept the microwaves, closing micro-pads and this would decrease negatively the pore volume and the area superficial Preference should preferably be given to any other process, such as thermal treatment, which increases the size or eliminates micro-pads, enlarges the size of macraparos, creates or destroys acroporos, or decreases the surface area available for absorption or catalysis, particularly after the acid treatment of the particle. The size of the particles employed in this invention can vary greatly depending on the end use. Typically, for adsorption applications or catalytic applications, a small particle size such as 20 μm is preferable because such small sizes provide a larger surface area per unit volume than large particles. Typically, for adsorption applications to well for catalytic applications, the particle size is within a range of 50 μm to 5000 μm. The particle of this invention can be used in any application of adsorption or capture of known ions by people with certain knowledge in the field. In one embodiment, the particle is used for environmental remedy applications. In this embodiment, the particle can be used to rebuff contaminants such as, but not limited to, heavy metals, organic substances, including hydrocarbons, chlorinated organic substances, including chlorinated hydrocarbons, inorganic substances or mixtures thereof. Specific examples of contaminants include, but are not limited to, acetone, microbial agents such as cryptosporidia, ammonia, benzene, clear, dioxane, ethanal, ethylene, formaldehyde, hydrogen cyanide, hydrogen sulfide, methanol, methyl ethyl ketone, methylene chloride, prapilena, styrene, sulfur dioxide, toluene, vipilo chlorine, arsenic, lead, iron, phosphates, selenium, cadmium, uranium bed pair example U308, radon, 1, 2-dibroma-3-claropropane (DBCP), chromium, smoke of tobacco, kitchen fumes, zinc, trichlorethylene, and PCBs. The particle can remedy an anion, an oxoanion, a cation, or a pali-axoapion. The particle of this invention can remediate individual pollutants to multiple singulators from a single source. In essence, in all the parts where adsorbents are employed to capture contaminants, this invention achieves an improved efficiency by adsorbing a larger amount of contaminants and by reducing the level of contamination to LI? much lower value than in the case of the use of non-enhanced particles. For environmental remediation applications, the particles of the present invention are typically placed in a container, such as a filter unit. The contaminated stream enters the container at the extreme Lin, comes into contact with the particles inside the container, and the purified stream exits at the other end of the container. The particles come in contact with the contaminants in the stream and bind to these pollutants and remove them from the stream. Typically, the particles become saturated with contaminants over a period of time, and the particles must be removed from the container and replaced with new particles. The stream with contaminants can be a gas stream or a liquid stream, such as an aqueous stream. The particles can be used to remedy, for example, waste water, production facility effluent, flue gas, automobile exhaust, drinking water and similar. The particle of the invention can be used alone, in combination with other particles prepared by the process of the present invention, and / or in combination, other adsorbent, catalytic or remediation particles of contaminants known in the art. The particles may be combined in a physical or agglomerated mixture using techniques known, for example, with an agglomerate to form a composite particle. The particle / binder system of the present invention can be preferably used as the catalytic adsorbent medium itself. In an alternative embodiment, the system is used as an adsorbent or catalytic support. In one embodiment, the acid-enhanced particle is used in combination with a particle that has been pretreated to improve its adsorbent properties and / or to implement or provide catalytic properties, such as an ionic or electronic enhancement, in accordance with Applicant's Candidate Application filed on October 21, 1996, US Serial No. 08 / 734,329, entitled "Enhanced Adsorbent and Raom Temperature Catalyst Particle and Method of Making and Using Therefor," (Enhanced Adsorbent and Catalyst Particulate at Ambient Temperature and Method for Making and Using said Particle), which is a continuation in part of the PCT document / US96 / 05303, filed on April 17, 1996, pending, which is a continuation in part of the North American patent application Serial No. 08 / 426,981, filed on April 21, 1995, pending, all these applications they are incorporated herein by reference ep as to all their teachings. In another embodiment, the acid-enhanced particle of the present invention is used in combination with a noble metal known in the art for its particular adsorbent or catalytic properties. Such noble metals include gold, silver, platinum, palladium, iridium, repio, rhodium, cobalt, copper, rt-tapeworm, and osmium, preferably gold, silver, platinum, and palladium. Such a combination can be used to take advantage of the adsorbent properties of the acid-enhanced particle and the catalytic properties of the noble metal. In one embodiment, the invention focuses on a composition comprising an aluminum oxide particle made by the acid enhancement process of the present invention. In another embodiment, this composition further comprises a co-particle. This co-particle is preferably an adsorbent or catalyst particle known in the art. Such ca-particles can be porous, preferably non-ceramic, oxide adsorptive particles, or activated carbon, more preferably silicon dioxide, or a metal oxide, such as, for example, manganese oxides (MnO, Mp02, Mn203, and Mn-304), copper oxides (CuO and Cu20), vanadium pentoxide (V205), zirconium oxide (Zr02), iron oxides (FeO, Fe203, and Fe304), titanium dioxide (Ti02) and zeolites, both natural and synthetic and activated carbon. The co-particle may be enhanced with acid or enhanced with acid. In a preferred embodiment, the co-particle is not initially enhanced with acid even though it may be in contact with acid during the binding step. In a preferred embodiment, the composition comprises aluminum oxide made by the acid enhancement process of the present invention, copper oxide, and manganese oxide. Preferably, these components are present in a proportion of 50-98 parts by weight, more preferably 80-95 parts by weight, preferably even greater than 88 parts by weight of aluminum oxide enhanced with acid; and 1-49 parts by weight, more preferably 4-19 parts by weight, preferably even more 6 parts by weight each of copper oxide and manganese oxide. Preferably, the copper oxide is CuO and the manganese oxide is Mn02. Preferably, the composition is held together using a colloidal alumina binder that has been cross-linked in accordance with what is described below. In a preferred embodiment, this composition can be used to remediate organic substances, including but not limited to hydrocarbons and clarinated organic substances, and even greater preference, triclaroeti lene (TCE). Without wishing to be bound by any theory, it is believed that at least a certain part and perhaps the entirety of the capacity of the aluminum oxide-enhanced embodiment of acid / co-particle of the invention described above for remediating organic contaminants is due to a catalytic degradation of the organic contamipant, even at room temperature. This catalytic activity is evident because the co-particle of the invention of example 5 was challenged with a high concentration of organic contaminants and non-organic contaminants were found in the residual solution after analysis with TCLP (see example 6). In a preferred embodiment, A1203 enhanced with acid in combination with one or more oxides of manganese, copper, and / or iron is especially suitable for catalytically degrading organic substances such as hydrocarbons, clarinated hydrocarbons, and chlorinated organic substances such as triclaraeti lena . With even greater preference, the catalytic composition comprises from 50 to 98 parts by weight, more preferably from 80 to 95 parts by weight, still more preferably 88 parts by weight of aluminum oxide enhanced with acid; and from 1 to 49 parts by weight, more preferably from 4 to 19 parts by weight, preferably even more than 6 parts by weight of each of copper oxide and mapganese oxide. Agglomerates for joining the individual particles in order to form an agglomerated particle are known in the art or are described herein. In a preferred embodiment, the binder may also act as an adsorbent and / or catalyst. A preferred binder that can be used with the particles of this invention is a colloidal metal oxide or colloidal metalloid oxide binder in accordance with the filings of the applicant's US application filed on October 21, 1996, No US Series 08 / 734,330, entitled "Adsorbent and / or Catalyst and Binder System and Method of Making and Using Therefor" (Adsorbent System and / or Catalyst and Binder thus Bed Method for Making and Using it), which is (i) a continuation in part of PCT / US96 / 05303, filed on April 17, 1996, pending, which is a continuation of part of the North American application Serial No. 08 / 426,981, filed on April 21, 1995, pending; (2) a continuation in part of the North American application Serial No. 08 / 426,981, filed on April 21, 1995, pending; (3) a continuation in part of the North American application Serial No. 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of PCT / US95 / 15829, filed on June 12, 1995, pending which is a continuation in part of the North American application Na. of series 08 / 351,600, filed on December 7, 1994, abandoned; and (4) a continuation in part of PCT / US95 / 15829, filed June 12, 1995, pending, which is a continuation in part of the North American application Serial No. 08 / 351,600, filed on December 7, 1994, abandoned. All applications are hereby incorporated by reference in their entirety in regard to all their teachings. This colloidal metal oxide or colloidal metalloid oxide binder and binder system is also described in detail below in the following section II. further, this colloidal metal oxide or colloidal metalloid oxide binder can be used with an untreated (na enhanced with acid) particle of the present invention and / or with an acid-treated (acid-enhanced) particle of the present invention described above in section I. This binder can be used in any of the particle compositions of this invention indicated above or below, enhanced with acid or not enhanced with acid. In addition, the particles and systems described below in section II and ep section III may be untreated or treated with acid (enhanced with acid) as described above in section I. A preferred binder for the agglomerated particle is colloidal alumina. or colloidal silica. The colloidal alumina passes through a transformation step and crosslinks with itself at a temperature comprised between 25 ° C and 400 ° C, preferably 250 ° C and / or crosslinked with the particle. The colloidal silica crosslinks itself if it is in a sufficiently dry state to remove water typically at temperatures between 25 ° C and 400 ° C. Preferably, from about 1 to 99% by weight, from 20% to 99%, or from 10% to 35% by weight of the total mixture is colloidal alumina or colloidal silica to provide the necessary crosslinking during heating to bond the agglomerated particle in a water resistant particle. The particle can then resist exposure to all types of water for a long time without disintegrating. The binder may be mixed with the particle before or after the acid treatment of this invention. In one embodiment, the agglomerated particle is made by mixing colloidal alumina with the adsorbent particles. Typically, from about 99.9% by weight, from 10 to 35% by weight, or from 20 to 99% by weight of the mixture is colloidal alumina. In another embodiment, the mixture of particles is mixed with an acidic solution such as, for example, nitric, sulfuric, hydrochloric, boric, acetic, formic, phosphoric acid, and mixtures thereof. In one embodiment, the acid is a 5% nitric acid solution. In another embodiment, the acid is an aliphatic or aromatic carbsylic acid. In a preferred embodiment, the acid is acetic acid. The colloidal alumina and the adsorbent and / or catalytic particles are mixed tatally in order to create a homogeneous mixture of all the elements. The additional acid solution is added and further mixing is carried out until the mixture reaches a suitable consistency for agglomeration. After finishing the agglomeration, the agglomerated particles are heated or dehydrated to cause crosslinking of the colloidal alumina. The particle of this invention binds with the contaminant in such a way that the particle and the contaminant are firmly attached. This link makes it difficult to remove the contaminant from the particle, allowing the waste to be discarded at any public sanitary landfill. Measurements of contaminants adsorbed on the particles of this invention using an EPA Taxicity Characteristic Leachability Procedure (TCLP) test known to experts in the art showed that there was a strong interaction between the particles of this invention and the contaminants in such a way that the pollutant is strongly stopped. II. AGGLOMERANT AND OXIDE ADSORBENT SYSTEMS AND / OR OXIDE CATALYST In accordance with the purpose of the invention or the purposes of the invention, as generally described and described herein, this invention in one aspect relates to a method for the production of an adsorbent and / or catalyst and binder system, comprising i) the mixture of components comprising a) binder comprising a colloidal metal oxide or a colloidal ethaloid oxide, b) an adsorbent particle of oxide and / or oxide catalyst, and c) an acid, ii) removing a sufficient amount of water from the mixture to crosslink the components "a" and "b" to form an adsorbent and / or catalyst and binder system. In another aspect, the invention offers an adsorbent and / or catalyst system made by the processes of the invention. In one aspect, the invention provides a system of adsorbent and / or catalyst and binder comprising a cross-linked binder with at least one particle type of oxide adsorbent and / or catalyst. In another aspect, the invention provides a method for reducing or eliminating the amount of a contaminant from a liquid or gas stream, comprising contacting the adsorbent system and / or catalyst and binder with the contaminant in the stream for a period of time. enough time to reduce or eliminate the amount of contaminant in the stream. In another aspect, the invention provides a method for catalyzing the degradation of an organic compound comprising contacting the organic compound with the adsorbent and / or catalyst system for a sufficient time to catalyze the degradation of an organic compound. In another aspect, the invention provides a method for reducing or eliminating the amount of a contaminant from a gas stream by catalysis comprising contacting the adsorbent and / or catalyst and binder system with a gas stream containing a gas. pollutant that comprises a nitrogen oxide, a oxide of sulfur, a carbon monoxide, hydrogen sulphide or mixtures thereof for a sufficient time to reduce to eliminate the amount of contaminant. In another aspect, the invention provides a method for producing an adsorbent system and a catalyst and binder, which comprises: i) mixing components comprising a) a binder comprising a colloidal metal oxide or a colloidal metallaid oxide, b) a first particle of adsorbent and / or catalyst that does not crosslink with the binder, and c) a acid, ii) rinsing a sufficient amount of water from the mixture to crosslink the component on itself, thereby trapping and holding the "b" member within the binder cross-linked to form an adsorbent and / or catalyst and binder system. In another aspect, the invention relates to a composition for binding adsorbent and / or catalyst particles to produce an agglomerated particle comprising (a) a colloidal metal oxide or colloidal metalaid oxide and (b) an acid. In another aspect, the invention relates to an assembly for joining adsorbent and / or catalytic particles to produce an agglomerated particle comprising (a) a colloidal metal oxide or a colloidal metalaid oxide and (b) an acid. In another aspect, the invention provides a method for joining adsorbent and / or catalyst particles, comprising the steps of: (a) mixing colloidal alumina or colloidal silica with the particles and an acid; (b) shake the mixture until homogeneous; and (c) heating the mixture for a sufficient time to cause crosslinking of the aluminum oxide in the mixture. When the system acts as an adsorbent, the adsorbent and agglomeration system of this invention has enhanced or removed adsorption characteristics. In one embodiment, the system of this invention can adsorb a greater amount of adsarbata per unit volume or weight of adsorber particles than a prior art system. In another embodiment, the adsorbent and binder system of this invention may reduce the concentration of contaminants or adsorb material in a stream to a lower absolute value than is possible with a non-bound particle or a bound particle of the previous technique. In particular embodiments, the adsorbent and binder system of this invention can reduce the conception of contaminant in a stream at levels below the detectable levels. Adsorption is a term well known in the art and should be distinguished from absorption. The adsorbent particles of this invention bind chemically to the attached material and hold it very firmly. These chemical bonds are ionic and / or covalent in nature. The binder catalyst system of the invention can also be used for the catalytic decomposition or remediation of contaminants. The catalyst system achieves an improved catalytic performance or catalytic properties never observed before for a specific contaminant. The adsorbent and / or catalyst and binder system can be prepared by techniques presented below to form a multifunctional composite particle. The catalysis can be carried out at room temperature in certain applications. The aglomerapte campido a particle of hearing that can 5? react, preferably crosslink with other oxide complexes. This binder can also react, preferably crosslink with it. The aglsmerapte forms cross-links with other oxide complexes upon drying by forming chemical bonds with it and with other oxides. Under acidic conditions, the binder has a large number of surface hydrosyl groups. In one embodiment, the binder which is known as B-OH, is cross-linked therewith by losing water to generate B-O-B. In addition to crosslinking with it, the B-QH binder can also be crosslinked with an oxide complex of adsorbent and / or catalyst (M-0) to a hydroxyl compound (M-OH) to produce B-O-M. The adsorbent / catalyst complexes are known herein as particles of the acid adsorbent and / or catalyst or as particles of oxide adsorbent and / or oxide catalyst., both expressions indicate that the particle, which can have adsorbent, catalytic or adsorbent and catalytic properties, has a complex oxidant and / or hydroxide. The resulting binder system consists of a three dimensional network or matrix where the component particles are bonded together with B-O-B and B-O-M bonds. The resulting system can be used as an adsorbent and / or catalyst system. The resulting system is sometimes known as an agglomerated particle.

The term "colloidal metal oxide binder or colloidal metalloid oxide (i.e., colloidal metal oxide or colloidal metal oxide)", as described herein, refers to a particle comprising a hydroxide, from hydride to fine particle.of mixed metal or metalloid oxide, such that the weight loss of the colloidal metal oxide or colloidal metalloid binder caused by the loss of water upon ignition is from 1 to 100%, 5 to 99%, 10 to 98%, or 50 to 95% of the loss of theoretical water weight, from pure metal or metalloid hydroxide to the corresponding metal oxide or pure metalloid. The loss of water when passing from pure metal or metalloid hydroxide to the corresponding pure metal or metalloid oxide (for example, the change of n M (0H) x to MnOm yy "H20" or more specifically to 2 A1 (0H) 3 to A1203 and 3H20) is defined as 10O% of the weight loss of water. Thus, weight loss is described ep the water loss based on the initial weight of the water (not the total weight of the initial binder). There is a continuous transition of metal to metalloid hydroxides, oxides of hydride, and oxides in a typical commercial product, such that the loss or removal of water from metal or metal hydroxides produces the corresponding hydroxides. of additional loss or removal of water provide the corresponding metal or metalloid oxides. Through this continuous transition, the loss or retreat of water produces eplaces M-0-M, where M is a metal or metalloid. The particles of this continuous transition, except in the case of metalloid or pure metal oxides, are suitable to serve as a metal oxide or colloidal metalloid binder in this invention. In another embodiment, the binder system includes the use of a binder in combination with a particle with few hydroxyl groups on the surface or without any surface hydroxyl group such that the particle is not crosslinked or cross-linked only with the hydroxyl group. binder Examples of particles possessing only nominal amounts that do not pass surface hydroxyl groups include metal particles such as, for example, not limited thereto, tin or zinc, or carbon. In another embodiment, the "b" compacter does not contain any oxide particles. Metal alloys such as bronze can also be used. In a preferred embodiment, the particle is activated carbon. In this embodiment, the binder is crosslinked therewith in the manner described above to form a three-dimensional network or matrix which physically traps or holds component "b" without being crosslinked or reticent only in a very limited manner with component "b". The resulting binder system can be sent as an adsorber and / or catalyst system. In another embodiment, the invention focuses on a method for the production of an adsorbent and / or catalyst and agglomerate system comprising i) the mixture of components comprising a) a binder comprising a colloidal metal oxide or an oxide of colloidal metalloid, b) a first particle of adsorbent and / or catalyst that is crosslinked with the binder, and c) an acid, ii) the removal of a sufficient amount of water from the mixture to crosslink the component "a" on itself same, thereby trapping and holding the component "b" within the crosslinked binder, to form an adsorbent and / or catalyst and binder system, further comprises a second particle of adsorbent and / or catalyst that is crosslinked with the binder, thus crosslinking the binder and the second particle and thereby trapping and holding the first particle within the crosslinked binder and / or within the crosslinked binder and second particle. In this embodiment, the system comprises a binder and particles of adsorbent and / or catalyst that are crosslinked with the binder as well as particles having a limited amount of surface hydroxy groups that do not crosslink with the binder. In this case, the binder is crosslinked thereon and on the oxide complex particles, and the agglomerate also forms a network or matrix around the particles having the limited number of surface hydroxyl groups. Binders that can be used in the present invention are complexes of colloidal metal oxide or of colloidal metalloid. The term colloidal as used herein is defined as an oxide group having a substantial number of hydroxyl groups which can form a dispersion ep an aqueous medium. This is distinguished from the other uses of the term colloid in relation to a size less than i μm. The binders here typically have a small size, for example, less than 150 μm, but do not have to be less than μm. Typically, the ag agglomerator is in the calcined state to optimize the availability of the hydroxyl group. In addition, they must have a substantial number of hydroxyl groups that can form a dispersion in aqueous medium, which is not always true of the colloid particles defined simply by having less than i μm. Examples of binders include, but are not limited to, any metal oxide or metalloid complex having a substantial number of hydroxy groups which can form a dispersion in an aqueous medium. In one embodiment, the binder is colloidal alumina, colloidal silica, colloidal metal oxide, where the metal is iron or a mixture thereof, preferably colloidal alumina or colloidal silica. In another embodiment, the binder is not colloidal alumina or colloidal silica. The colloidal alumina may be in the form of powder, sol, gel, or aqueous dispersion. The colloidal alumina can also be stabilized with an acid, preferably nitric acid, and even more preferably, with 3 to 4% nitric acid. In a preferred embodiment, the colloidal alumina is not found in the calcined state and has a sufficient number of hydrosyl groups in such a way that the total weight loss of the particle (as opposed to only the water loss discussed above) is understood to be between 5% and 34%, with greater preference between 20% and 31%. The size of the colloidal alumina is preferably 5 nm to 400 μm, preferably at least 30% is less than 25 μm in size and 95% by weight is less than 100 μm in size. The colloidal silica is preferably not calcined with a sufficient number of hydroxy groups in such a way that the total particle weight loss upon igniting is between 5% and 37%, preferably between 20% and 31%. The size of the colloidal silica is preferably 5 μm to 250 μm, preferably less than 30% by weight is of a size less than 25 μm and 95% by weight is less than 100 μm in size. In one embodiment, the binder is from 1% to 99.9% by weight of the mixture, preferably from 10% to 35% by weight. As used herein, the binder will be known as a "colloidal" bed to distinguish it from the "b" particle since the types of composition can be the same, for example both can contain aluminum oxide. Although agglomeration can be employed in the prior art in combination with the binder system of the present invention, these prior art binders do not have some advantages. In the present invention, the activity is not degraded when it is exposed to aqueous solutions. The system is also very durable and not subject to decomposition when exposed to a residual agent, unlike other adsorbent and / or catalyst and agglomerate systems of the prior art such as polyvinyl pyrrolidone, starch, or ce-lose. The invention contemplates the use of any particle of oxide and / or catalyst adsorbent or particle composed of two or more types of particle system and binder, but with replacement of the prior art aglomerapte with the binder of the present invention. In one aspect, the invention features an adsorbent / or catalyst and lamellar system comprising a binder that has been crosslinked with at least one type of adsorbent particles and / or oxide catalyst. In a modality, the companepte "b" comprises at least two different types of adsorbent particles and / or oxide catalyst, to form a crosslinking between the binder and both particles to thereby form a composite particle. In another embodiment, component "b" comprises at least three different types of adsorbent and / or catalyst particles. In a preferred embodiment, the component "b" comprises an oxide particle, preferably the metal oxide particle, or even more preferably a porous, non-ceramic metal oxide particle. Examples of such particles include, but are not limited to, complexes of oxide as exemplary transition metal oxides, lantipid oxides, thorium oxide, as well as oxides of HA Group (Mg, Ca, Sr, Ba), Group IIIA (B , Al, Ga, In, Ti), Group IVA (Yes, Ge, Sn, Pb), and Group VA (As, Sb, Bi). In general, any oxide complex that is a basic anhydride is decuads for component "b". In another embodiment, component "b" comprises an oxide of aluminum, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, tungsten, renia, arsenic, magnesium, thorium, silver, cadmium, tin, lead, antimony. , ruthenium, osmium, cobalt or nickel or zeolite. Typically any oxidation state of the oxide complexes may be useful for the present invention. The oxide may be a mixture of at least two metal oxide particles having the same metal with varying states of oxidation and stoichiometry. In one embodiment, component "b" comprises A1203, Ti02, CuO, Cu20, V205, Si02, Mn02, Mn203, Mp304, ZpO, W02, W03, Re207, As203, As205, MgO, Th02, Ag20, AgO, CdO, Sp02, PbO, FeO, Fe203, Fe304, Ru203, RuO, 0s04, Sb203, CoO, Co203, NiO or zeolite. In a further embodiment, the "b" component further comprises a second type of adsorbent and / or catalyst particles that an aluminum oxide, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, tungsten, rhenium, arsenic. , magnesium, sodium, silver, cadmium, tin, lead, antimynia, ruthenium, osmium, cobalt or nickel or zealite, activated carbon including charcoal and coconut coal, peat, zinc or tin. In another embodiment, component "b" further comprises a second type of adsorber particles / or aluminum oxide catalyst, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc oxide, zealite, activated carbon, peat, zinc or tin particle. Typical and pleated zeolites in the present invention include "Y" type, "Í3 :, mardenite and ZsM5." In a preferred maltida, component "b" comprises calcined, porous, crystalline, non-ceramic, non-amorphous aluminum oxide produced by the calcining of the precursor in the calcined aluminum oxide at a particle temperature of 300 or 400 ° C to 700 ° C, preferably in gamma, chi-rho or eta pharma The precursor of the calcined aluminum oxide may include, without limitation To these, boehmite, bauxite, pseudo-boemi ta, oxidized layer, A1 (0H) 3 and alumina hydrates, in the case of other complexes of metal oxide, these complexes may also be calcined or not calcined. The adsorbent and / or catalyst employed in this invention may be enhanced or enhanced by processes known in the art or described below, For example, the particles may be dried to be activated or be of a composition or treated. gives by means of processes of activation treatment to enhancement by acid or ionic or electronic beam presented in two applications of the applicants submitted on October 21, 1996 and entitled (1) "Ephanced Adsorption and Room Temperature Catalyst Particle and Method of Making and Using Therefar "(Catalyst particle at room temperature and adsorbent enhanced as well as method for making and using it) Serial No. US 08 / 734,329, which is a continuation in part of PCT / US96 / 05303, filed on 17 April 1996, pending, which is a coptinuaciónin part of the North American dl-d no. of series 08 / 426,981 filed on April 21, 1995, pending, and (2) "Acid Contained Ephanced Adsorbent Particle and Methad of Making and Using Therefor". { Adsorbent particle enhanced by contact with acid and method to elaborate and use it), na. series US 08 / 734,331, which is a continuation in part of the North American application na. of series 08 / 662,331, filed on June 12, 1996, pending, which is a continuation in part of PCT / US95 / 15829, filed on June 12, 1995, pending, which is a continuation in part of the request North American no. of series 08 / 351,600, filed on December 7, 1994, abandoned, the filings of both applications and all of their prior priority applications are hereby incorporated by reference in their entirety for all their teachings, including, but not limited to, , particle compositions and treatment method. The acid treatment or enhancement method and the particles are described above in section I. In one embodiment, the adsorbent and / or oxide catalyst particle has not been treated for acidic enhancement. An acid is required to crosslink the binder with the compapepte "b". The addition of an acid to the agglomerates or allows the reaction between the binder and the oxide particle. A strong or diluted acid may be used. A dilute acid is preferred to minimize chemical attack of certain particles. Typically, the acid is diluted with water to avoid dissolution of the particle and to reduce costs. The acid treatment is preferably carried out at a conception (ie the strength of the acid measured, eg, by normality or pH), type of acid, temperature, and period of time to crosslink the binder and the component "b" . In one embodiment, the acid comprises nitric acid, sulfuric acid, hydrochloric acid, boric acid, acetic acid, formic acid, phosphoric acid or mixtures thereof, preferably acetic acid or nitric acid. In another embodiment, the acid is an aliphatic or aromatic carbsylic acid, Examples of aliphatic and aromatic carboxylic acids include, but are not limited to, acetic acid, benzoic acid, butyric acid, citric acid, fatty acids, lactic acid, maleic acid, malonic acid, ophthalmic acid, salicylic acid, stearic acid, succinic acid, tartaric acid, propionic acid, valeric acid, hexanaic acid, heptansic acid, caprylic acid, pelargonic acid, capric acid, undecanoic acid, lauric acid, trideconaic acid , myristic acid, pentadecanaic acid, palitic acid, heptadecanoic acid, nonadecanoic acid, arachidics acid, heneicosanoic acid, behépico acid, triosanaic acid, lignacérico acid, pentacosanaic acid, peric acid, heptasanoic acid, montápico acid, napacosanoic acid, acid melisic, phthalic acid, glutaric acid, glutaric acid, adipic acid, azelaic acid, sebacic acid, cinnamic acid, acrylic acid, crotonic acid, linsleico acid, or a mixture thereof. In a preferred embodiment, the acid concentration is from 0.15 N to 8.5 N, preferably from 0.5 N to 1.7 N. The volume of dilute acid employed must be sufficiently high such that the particle of adsorber and / or catalyst of the The present invention can be used in the state or further processed, such as extruded or pressure filtered. In order to ensure efficient crosslinking between the binder comparator and the oxide particle, water is removed from the resulting binder system. This is typically carried out by using a drying agent or by heating the system. The crosslinking temperature as used herein is the temperature at which the crosslinking between the agglomerant and the component "b" of the oxide and / or catalyst adsorbent is carried out at an acceptable rate at or at a temperature at which the binder reacts with the same at an acceptable speed. In a modality, the crosslinking temperature is from 25 ° C to 400 ° C. Thus, in one embodiment, the crosslinking temperature for certain binders is room temperature and does not require heating, even when the crosslinking speed at this temperature is low. In various modalities, the reticution temperature, and therefore the heating step is 50 ° C, 60 ° C, 110 ° C, or 150 ° C at 200 ° C, 250 ° C, 300 ° C, a biep 350 ° C, preferably from 150 ° C to 300 ° C, preferably even higher than approximately 250 ° C. The crosslinking process can be carried out in open air, under an inert atmosphere or under reduced pressure. The crosslinking temperature can accept the activity of the adsorbent system and / or catalyst and binder. When the crosslinking is done in the open air, then the particle is more susceptible to oxidation as the crosslinking perature increases. Oxidation of the particle can reduce the activity of the particle. Preferably, during or after passage (i), the mixture of step (i) is not heated above the crosslinking temperature of the colloidal metal oxide or colloidal metalloid oxide. Preferably, during or after step (i), the mixture of step (i) is not heated to the calcining temperature either above the calcination temperature of the colloidal metal oxide or colloidal metalaid oxide. Preferably, during or after step (i), the mixture from step (i) na is heated to the calcination temperature of the particle or above the calcination temperature of the particle. In several embodiments, during a after the paase (i), the mixture of step (i) is not heated above 500 ° C, 450 ° C, 400 ° C, 350 ° C, 300 ° C, or 250 ° C , preferably pa is heated above 400 ° C. The crosslinking must be distinguished from the calcination. The calcination typically includes heating a particle to remove residual water that may be in the particle as well as to change the crosslinking structure of the particle to form a crystalline particle. For example, to produce a crystalline aluminum oxide particle, the calcination temperature is from about 300 or 400 ° C to about 700 ° C. The calcination also removes the hydroxyl groups in the binder that are required for crosslinking. Accordingly, heating the system during or after step (i) above the crosslinking temperature in the range of particle or binder calcination temperature or above said range is negative for the system. Thus, systems of the prior art, wherein mixtures of colloidal alumina and / or colloidal silica are (i) calcined or recalcinated (2) heated to form a refractory material forms part of this invention. In another aspect, the invention comprises an adsorbent and / or catalyst system made by the process of the invention. The binder system of the invention is made in one embodiment by the following general process. The (1) binder and (2) adsorbent and / or catalyst particles are pre-mixed in dry form. The colloidal binder can be added or prepared ip. For example, alum can be added in the form of a dry powder and can then be converted to colloidal alumina in situ. Other ep aluminum-based compounds can be used for in situ processing, such as for example aluminum chloride, secondary aluminum butoxide, and the like. A solution of the acid is added to the mixture, and the mixture is stirred, typically for 1 minute to 2 hours, preferably 10 minutes to 40 minutes, until the material has a homogeneous "mud" texture. The mixture is then ready for crosslinking or it can first be fed through an extruder and then shear in a final form, preferably spheres, pellets or full letes, typically from 0.2 mm to 3 mm in size, preferably from 0.2 to 3 mm. 0.5 to 1.5 mm. After finishing the final form, the product is transferred to a drying oven where the products are dried during a pearl from 15 minutes to 4 hours, preferably from 30 minutes to 2 hours. Once the binder is added to the adsorbent and / or catalyst particles (component b), the mixture is not heated to calcine or recalcitate the "b" particle or binder. Said calcination or recalcination would negatively change the surface characteristics of component "b" closing the micropores. In addition, the particles of the present invention preferably are sintered, since this would be negative for the micro-pads, closing the microporos and would negatively decrease the pore volume and the surface area. The particles and the binder system are also not heated above the calcination temperature to form a refractory material. Any other process that increases the size or eliminates the micropores, increases the size of acropsros or looks for macropores at the expense of micropores or destroys macropores, or decreases the surface area available for adsorption or catalysis should be avoided preferably. The size and the pharmacy of the pleated particles in this invention before the extrusion step can vary greatly depending on the end use. Typically, for adsorption applications or catalytic applications, a small bed particle size for example 5 μm or more up to about 250 μm is a preferred size because it provides a larger surface area than the larger particles. In another aspect, this invention provides a method for reducing or eliminating the amount of a contaminant present in a liquid or gas stream, said method comprising contacting the system of adsorber particles and / or catalyst and agglomerant with the contaminant. in the flow for a sufficient time to reduce or eliminate the amount of chanter found in the stream. In one embodiment, the stream is a liquid, preferably water. In another embodiment, the stream is a gas, preferably a gas comprising air or natural gas. The adsorbent and / or catalyst and agglomeration particle system of this invention can be used for environmental remediation applications. In this embodiment, contaminants from a liquid or gas stream can be reduced or eliminated by means of a catalysis reaction. In another embodiment, contaminants can be reduced or eliminated from a liquid or gas stream by an adsorption reaction. The particle can be used to remove contaminants such as, for example, without limitation, heavy metals, organic substances, including hydrocarbons, clarinated organic substances, including chlorinated hydrocarbons, inorganic substances, or mixtures thereof. Specific examples of contaminants include, but are not limited to, acetone, ammonia, bepcene, carbon monoxide, clear, hydrogen sulfide, triclarsethylene, 1,4-diaxana, ethanol, ethylene, fsmalmaldehyde, hydrogen cyanide, hydrogen sulfide. , methanal, methyl ethyl ketone, ethylene chloride, nitrogen oxides such as nitrogen oxide, propylene, styrene, sulfur oxides such as sulfur dioxide, toluene, vinyl chloride, arsenic, cadmium, chlorine, 1,2-dibromoclorspropane (DBCP), iron, lead, phosphate, radon, selenium, an anion, an axoanion, a poly-axanan or not uranium, as for example U308. The adsorbent and / or catalyst and binder particle system of this invention can remediate single contaminants or multiple contaminants from a single source. This invention achieves improved efficiency by adsorbing a higher amount of contaminants and by reducing the level of contamination to a much lower value than what is achieved by the use of non-enhanced particles. In another aspect, the invention provides a method for catalyzing the degradation of an organic compound comprising contacting the organic compound with the adsorbent and / or catalyst particle system for a sufficient time to catalyze the degradation of an organic compound. . In a modality, the catalysis reaction is carried out at room temperature. In one embodiment, the organic compound is a clarinated organic compound, such as for example triclaraethylene (TCE). In one embodiment, the catalyst and binder system catalyzes the hydrolysis of the chlorinated organic compounds. In another aspect, the invention provides a method for reducing or eliminating the amount of contaminant from a gas stream by catalysis, said method comprising contacting the adsorber particle system and / or catalyst and binder with a gas stream. that it has a contaminant comprising a nitrogen oxide, a sulfur oxide, carbon mop oxide, hydrogen sulfide, or mixtures thereof for a sufficient time to reduce or eliminate the amount of challamine. In one embodiment, the catalysis reaction is carried out at room temperature. In the case of environmental remediation applications, adsorbent particles and / or catalyst of the present invention are typically placed in a container, such as in a filtration unit. The contaminated stream enters the container at one end, comes into contact with the particles inside the container, and the purified stream exits through another end of the container. The particles come into contact with the contaminants in the stream and bind to the contaminants and remove them from the currents. Typically, the particles become saturated with contaminants over time, and the particles must be removed from the container and replaced by new particles. The contamipant carrier may be a gas stream or a liquid stream, such as an aqueous stream. The particles can be used to remedy, for example, waste water, production facility effluent, smoke exhaust gas, auto exhaust gas, drinking water, and the like.

The particle / binder system of the invention can preferably be used as the adsorbent or catalytic medium ep itself. In an alternative embodiment, the system is used as an adsorbent or catalytic support. In another embodiment, na is used as a catalyst support. When the particle adsorbs a contaminant, the particle of this invention binds with the contaminant such that the particle and the contaminant are firmly attached. This union makes it difficult to remove the contaminant from the particle, allowing waste to be disposed of in any public sanitary landfill. Measurements of the contaminants adsorbed on the particles of this invention by means of a test of EPA Toxicity Characteristic Leachability Prscedure (TCLP) known by part of the experts in the matter showed that there is a very strong interaction between the particles of this invetration and the contaminants of such way that the pollutant is retained very strongly. Even when the particle system binds firmly to the contaminant, the system of the invention can be regenerated by several techniques. In one embodiment, the acid-enhanced particle of section I above can be regenerated. In another embodiment, the catalyst system and oxide and / or catalyst adsorbent particles can be regenerated. In one embodiment, the particle can be regenerated by calcining it in air to resize the particle. In another embodiment, the contaminant can be removed by contacting the particle that has the contaminant adsorbed with a reactive wash. The reactive wash may include, but is not limited to, aqueous ammonia, phosphines or detergents. In another embodiment, the use of a pH change can remove the captaminant from the particle. Several pH ranges can be used to remove the contaminant from the particle according to the type of contaminant. In one embodiment, an acid solution can be used to remove a cation from the particle. In another embodiment, a basic solution can be used to remove an anion from the particle. In another embodiment, acids and Lewis bases can be used to remove the contaminant from the adsorbent particle. In one embodiment, component "b" comprises aluminum oxide, copper oxide and manganese dioxide. In this embodiment, the binder is preferably colloidal alumina. In this embodiment, the acid is preferably acetic acid. In this embodiment, the aglamerant is from 1 to 97 parts by weight, preferably from 5 to 35 parts by weight, the aluminum oxide is from 1 to 97 parts by weight, preferably from 55 to 85 parts by weight, the oxide The copper content is 97 parts by weight, preferably 1 to 20 parts by weight, and the manganese oxide is from 1 to 97 parts by weight, preferably 20 parts by weight. In another embodiment, the binder is 20 parts by weight, the aluminum oxide is 70 parts by weight, the copper oxide is 5 parts by weight, and the manganese dioxide is 5 parts by weight. In another embodiment, component "b" comprises aluminum oxide and activated carbon. In this embodiment, the binder is preferably colloidal alumina. In this embodiment, the acid is preferably acetic acid. In this embodiment, the binder is from 1 to 98 parts by weight, preferably from 5 to 35 parts by weight, the aluminum oxide is from 98 parts by weight, preferably from 45 to 75 parts by weight, and activated carbon is 98 parts by weight, preferably 35 to 55 parts by weight. In another embodiment, the binder is 20 parts by weight, the aluminum oxide is 60 parts by weight and the activated carbon is 5 parts by weight. In another embodiment, component "b" comprises copper oxide and manganese dioxide. In this embodiment, the binder is preferably colloidal alumina. In this embodiment, the acid is preferably acetic acid. In this mode, the agglomerate is from 1 to 98 parts by weight, preferably from 5 to 35 parts by weight, the copper oxide is from 1 to 98 parts by weight, preferably from 35 to 55 parts by weight, and the manganese dioxide is from 1 to 98 parts by weight, preferably from 25 to 55 parts by weight. In another embodiment, the binder is 20 parts by weight, the copper oxide is 40 parts by weight and the manganese dioxide is 40 parts by weight. In another embodiment, component "b" comprises aluminum oxide, copper oxide, manganese dioxide and active carbon. In this mode, the aglamer is preferably of colloidal alumina. In this embodiment, the acid is preferably acetic acid. In this mode, the binder is from 96 parts by weight, preferably from 5 to 35 parts by weight, the aluminum oxide is from 1 to 96 parts by weight, preferably from 45 to 75 parts by weight, the Copper is from 1 to 96 parts by weight, preferably from 1 to 20 parts by weight, manganese dioxide is from 1 to 96 parts by weight, preferably from 1 to 20 parts by weight, and activated carbon is from 96 to 100 parts by weight. parts by weight, preferably 25 parts by weight. In another embodiment, the aglo ester is 19.9 parts by weight, the aluminum oxide is 60 parts by weight, the copper oxide is 5.98 parts by weight, the manganese dioxide is 4.98 parts by weight, and the activated carbon is 9.95 parts by weight. in weigh. In another embodiment, the compsnept "b" comprises aluminum oxide, silicon dioxide and activated carbon. In a further embodiment, the particle comprises from 97 parts, preferably from 5 to 35 parts, more preferably 20 parts by weight of aluminum oxide, from 1 to 97 parts, preferably from 5 to 35 parts, more preferably 20 parts by weight of silicon dioxide and from 1 to 99 parts, preferably from 25 to 55 parts, more preferably 40 parts by weight of activated carbon. In this embodiment, the binder is preferably colloidal alumina and the acid is preferably acetic acid. The binder is from 1 to 97 parts by weight, preferably from 5 to 35 parts by weight. In another embodiment, the catalyst and binder system can be used as the oxidation catalyst. In one embodiment, the system comprises colloidal alumina as a binder, A1203, and one or more of the following oxide particles V205, W02, W03, Ti02, Re207, As203, As205, 0s04, or Sb203. In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, A12Q3 is from 1 to 90 parts by weight, and V205, W02, W03, Ri02, Re207, As203, As205, 0s04, or Sb203 are, each from 1 to 90 parts by weight »In another embodiment, the catalyst and binder system can be used as the Lewis acid catalyst. In one embodiment, the system contains colloidal alumina as a binder, A1203, and one or more of the following oxide particles of V205, Zr02, Ti02, MgO, Th02, or lanthanide oxides. In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, A1203 is from 1 to 90 parts by weight, and V205, Zr02, Ti02, MgO, Th02 or lanthanide oxides are each from 90 parts by weight. in weigh. In another embodiment, the catalyst and binder system can be used as a decomposition catalyst. In one embodiment, the system comprises colloidal alumina as an agatomer, 1203, and one or more of the following oxide particles of CuO, ZnO, Ag20, AgO, CdO, Sn02, PbO, V205, Zr02, MgO, Th02 or oxides of lanthanide In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, A1203 is from 1 to 90 parts in pess, and CuQ, ZnO, Ag20, AgO, CdO, Sn02, PbO, V205, Zr02, MgO, Th02 s lanthanide oxides each of 90 parts by weight. In another embodiment, the binder and catalyst system can be used as a reduction catalyst. In one embodiment, the system comprises colloidal alumina as binder, A1203, and one or more of the following oxide particles of Mn02, Fe203, Fe304, Ru203, 0s04, CoO, Co203, RuO or NiO. In another embodiment, colloidal alumina is from 10 to 30 parts by weight, A1203 is from 90 parts by weight, and Mn02, Fe203, Fe-304, Ru203, 0s04, CoO, Co203, Ru.0 or NiO are each one of the 90 parts by weight. In another modality, the catalyst and binder system can be used as a catalyst for the reduction and removal of nitrogen oxides. In one embodiment, the aglomraptre is colloidal alumina and the particle comprises aluminum oxide, gallium oxide and copper oxide. In another embodiment, the colloidal alumina is from 1 to 98% by weight, the aluminum oxide is from 98% ep weight, the gallium oxide is from 1 to 98% by weight, and the copper oxide is from 1 to 99% by weight. In another embodiment, the colloidal alumina is from 5 to 40% by weight, the aluminum oxide is from 40 to 99% by weight, the gallium oxide is from 1 to 10% by weight, and the copper oxide is from 1 to 10% by weight. to 10% by weight. In a preferred embodiment, the colloidal alumina is 20% by weight, A1203, preferepcia enhanced with acid, is 70% by weight, Ga203 is 5% by weight, and CuO is 5% by weight, where the particle is cross-linked with acid acetic acid at a temperature of 350 ° C. In another embodiment, the aglamer is colloidal alumina and the particle comprises oxides of aluminum, copper oxide and zirconium oxide. In another embodiment, the colloidal alumina is from 1 to 97% by weight, the aluminum oxide is from 1 to 97% by weight, and the copper oxide is from ia to 97% by weight, and the zirconium oxide is from ia 97% by weight. In a preferred embodiment, the colloidal alumina is from 10 to 40% ep weight, the aluminum oxide is from 30 to 70% by weight, the copper oxide is from 10 to 20% by weight, and the zircanium oxide is from 1 to 20% ep weight. In an even more preferred modal, colloidal alumina is 20% by weight, A1203, preferably enhanced with acid, is 70% by weight, CuO is 5% by weight and Zr02 is 5% by weight, where the particle is cross-linked with acetic acid at a temperature of 350 ° C. In another embodiment, the aglamer is colloidal alumina and the particle comprises aluminum oxide and silver nitrate. In another embodiment, the colloidal alumina is from 1 to 98% by weight, the aluminum oxide is from 1 to 98% by weight, and the silver nitrate is from 1 to 98% by weight. In a preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, and the silver nitrate is from 1 to 20% by weight. In a preferred embodiment, the colloidal alumina is 20% by weight, A1203, preferably enhanced with acid, is 75% by weight and AgN03 is 5% by weight, where the particle is cross-linked with acetic acid at 350 ° C. In another embodiment, the binder is colloidal alumina and the particle comprises aluminum oxide, a mixed oxide complex, and copper oxide. Mixed bed compound oxides are defined as particles comprising at least 2 or more oxide complexes. In another embodiment, the colloidal alumina is from 1 to 97% by weight, the aluminum oxide is from I to 97% by weight, the mixed oxide is from ia to 97% by weight, and the copper oxide is from 1 to 97 % in weigh. In a preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, the mixed oxide is from 1 to 20% by weight, and the copper oxide is from 1 to 20% by weight. to 20% by weight. A mixed oxide particle useful for this embodiment is M0LECULITE (mr), supplied by Molecular Products LTD, Essex, United Kingdom. M0LECULITE (mr) contains from 60 to 75% by weight of ores of manganese compounds, including Mn02, Mn203, and / or Mn304, from 11 to 14% by weight of copper oxide and approximately 10% by weight of lithium hydroxide. In the embodiment, the system comprises colloidal alumina as a binder, and the particle comprises aluminum oxide and goat oxide. In an even more preferred embodiment, the colloidal alumina is 20% by weight, the A1203, preferably enhanced with acid, is 70% by weight, the product MOLECULITE (mr) is 5% by weight, Cub is 5% by weight, where the particle is cross-linked with acetic acid at 350 ° C. In another embodiment, the binder is colloidal alumina and the particle comprises aluminum oxide, copper oxide, manganese dioxide, and magnesium oxide. In another embodiment, the colloidal alumina is from 1 to 96% by weight, the aluminum oxide is from 96% by weight, the manganese dioxide is from 1 to 96% by weight, the copper oxide is from 1 to 96 % by weight, and magnesium oxide is 96%. In preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, the manganese dioxide is from 1 to 20% ep weight, the copper oxide is from 1 at 20% ep weight, and the magnesium oxide is from 1 to 30%. In an even more preferred embodiment, the colloidal alumina is 20% by weight, A1203, preferably enhanced with acid, is 50% by weight, Mn02 is 5% by weight, CuO is 5% by weight, and MgO is 20%, where the particle is cross-linked with acetic acid at 350 ° C. In another embodiment, the colloidal alumina is from 1 to 98% by weight, the alumina oxide is from 1 to 98% ep weight, and the copper oxide is from 1 to 98% ep weight. In a preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight and the copper oxide is from 1 to 20% by weight. In an even more preferred embodiment, the colloidal alumina is 25% by weight, A1203, preferably enhanced with acid is 65% by weight, and CuO is 10% by weight, since the particle is cross-linked with acetic acid at SSO ^ C. In tying modality, the catalyst and binder system can be used as a catalyst for the oxidation of CQ and hydrocarbons. In one embodiment, the binder is colloidal alumina and the partylitol comprises aluminum oxide, a mixed oxide and copper oxide. In another embodiment, the colloidal moiety is from 1 to 98% by weight, the aluminum oxide is from 1 to 98% ep weight, and the mixed oxide is from 1 to 98% ep weight. In a preferred embodiment, the colloidal alumina is from 10 to 40% ep weight, the aluminum oxide is from 10 to 40% by weight, and the mixed oxide is from 20 to 70% by weight. A mixed metal oxide useful in this embodiment is CARULITE (r) 300, supplied by Carus Chemical Company, LaSalle, Illinois, USA. CARULILTE (mr) 300 contains 60 to 75% by weight of manganese dioxide, 11 to 14% of goat's oxide and 15 to 16% of aluminum oxide. In an even more preferred embodiment, the colloidal alumina is 20% by weight, A1203, preferably enhanced with acid, is 20% by weight, and CARULITE (mr) 300 is 60% by weight, where the particle is cross-linked with flft acid nitrate at a temperature of 350 ° C. In another embodiment, the catalyst and binder system can be used as an adsorbent for sulfur and oxygen compounds. In one embodiment, the system comprises colloidal alumina bed aglsmerapte, and the particle comprises aluminum oxide and copper oxide. In another embodiment, the colloidal alumina is from 1 to 98% by weight, the aluminum oxide is from 1 to 98% by weight, and the copper oxide is from 1 to 98% by weight. Ep In a preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, and the copper oxide is from 1 to 20% by weight. In another embodiment, the binder and oxide adsorbent system and / or oxide catalyst can remove hydrocarbons clarinets from a liquid stream. In one embodiment, the binder system and adsorbent oxide and / or catalyst • Acid-based (1) colloidal alumina, (2) aluminum oxide, (3) a mixed oxide, such as mixed manganese oxide oxides, for example, MOLECULITE (mr) and (4) carbon. In In a preferred embodiment, the composition comprises or consists of colloidal alumina of from 10 to 30%, preferably 20% by weight, A1203, preferably enhanced with acid, from 50 to 70%, preferably 60% by weight, M0LECULITE (mr ) from 5 to 15%, preferably 10% by weight and carbon from 5 to 15%, preferably 10% by weight. 8: In another embodiment, the catalyst and binder system can be used as the carbon gasification catalyst. In a modality, the system comprises colloidal alumina as a binder, A1203, and one or more of the following oxide particles of Fe203, Fe304, CaO or Ca203. In another embodiment, colloidal alumina is from 10 to 30 parts by weight, A1203 is l 90 parts by weight, and Fe203, Fe304, CoO, or biep Co203, ssp each from 1 to 90 parts by weight. In another embodiment, the catalyst and binder system can be used as a carbon gas reforming catalyst. In an embodiment, the system comprises colloidal alumina as a binder, I203, and one or more of the following oxide particles of Fe203, Fe304, CoO, or Co203. In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, 1203 is from 1 to 90 parts by weight, and Fe2Q3, Fe304, CoO, or Co203, are each from 1 to 90 parts by weight. In another embodiment, the catalyst and binder system can be employed as a hydrogenation catalyst. In one embodiment, the system comprises colloidal alumina co or binder, A1203, and one or several of the following oxide particles of Fe2Q3, Fe304, CaO or Co203. In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, 1203 is from 1 to 90 parts by weight and Fe203, Fe304, CsO or Co203 each from 1 to 90 parts by weight.

In another embodiment, the catalyst and binder system can be used as a drying bed. In one embodiment, the system comprises colloidal alumina as binder, A1203, and one or more of the following: zeolite oxide, MgO or Th02"In another embodiment, colloidal alumina is from 10 to 30 parts by weight, A1203 is from The 90 parts in pess, zeslite, MgO or Th02 are each 90 parts by weight. In another embodiment, the catalyst and binder system can be used as a catalyst support. In one embodiment, the system encamises colloidal alumina as agglomerate, A1203, and one or more of the following oxide particles of MgO or Th02. In another embodiment, the colloidal alumina is from 10 to 30 parts by weight, A1203 ss from 1 to 90 parts by weight, and MgO or Th02 each from 90 parts by weight. In another embodiment, the catalyst and binder system can be used to adsorb ions from a stream of gas to liquid. In one embodiment, the system comprises colloidal alumina as a binder, aluminum oxide and copper oxide. In another embodiment, the colloidal alumina is from 1 to 98% ep weight, the aluminum oxide is from 1 to 98% by weight, and the copper oxide is from 1 to 98% by weight. In a preferred embodiment, the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, and the copper oxide is from 1 to 20% by weight. The adsorbed ion includes, without being bound to them, an anian, an sxs-apiop, a poly-oxaanon, or a mixture thereof. In another embodiment, the system comprises a colloidal alumina aglamer and the particle comprises aluminum oxide, zinc oxide and copper oxide. In another embodiment, the system comprises a colloidal alumina binder and the particle catches aluminum oxide and oxide. coppermade. In another embodiment, the catalyst and binder system can encapsulate a contaminant within an adsorbent particle. The particle of adsorbent and / or catalyst enhanced by acid of section I above and the binder and the particle of oxide adsorbent and / or oxide catalyst of this section II may be used to encapsulate a contaminant. By heating the adsorbent particle that has adsorbed a contaminant at a sufficient temperature, the pores of the particle close and encapsulate the contaminant within the particle. In one embodiment, the curing temperature is from 450 ° C to 1200 * 0, preferably from 600 ° C to 1200 ° C. By heating the particle or the binder-particle system, the pores of the particle, binder or both are closed and encapsulate the contaminant. The oxide which is used to enhance the particle of section I above and the acid used to crosslink the binder and the oxide adsorbent particle and / or oxide catalyst of this section may also behave as a blowing agent. The term "blowing agent" is defined herein as any reagent that can modify a physical property of the particle. Examples of physical properties that can be modified include, without militarizing, surface area, pore area, bulk density, skeletal density, and porosity. In one embodiment, the blowing agent can be an acid, preferably acetic acid and nitric acid. Without being limited to one theory, it is believed that the acid can be attached to the particle of section I during acid treatment or enhanced with acid or biep that the acid can be bound to the binder and / or the oxide adsorbent and / or the catalyst oxide of this section during the kneading step and the extrusion step. The complex is then decomposed during the curing step to produce gases. The resulting gas leaves the particle which results in an increase in surface area, bulk density of para area, skeletal density and porosity. By varying the physical properties of the particle, the activity of the adsarbepte and / or the activity of the catalyst can be enhanced. In another embodiment, the invention relates to a composition for bonding adsorbent and / or catalytic particles to produce an agglomerated particle comprising (a) a colloidal metal oxide or a colloidal metalloid oxide and (b) an acid. In this composition, in one embodiment, the colloidal metal oxide or the colloidal metalloid oxide comprises colloidal or colloidal silica. In this composition, in one embodiment, the acid is acetic acid or nitric acid. In another application, the invention relates to a method for joining adsorbent and / or catalytic particles, comprising the steps of: (a) mixing colloidal alumina s colloidal silica with the particles and an acid; (b) stir the mixture until it reaches homogeneity; and (c) heating the mixture for a sufficient time to cause crosslinking of the aluminum oxide in the mixture. In Lina modality, colloidal alumina or colloidal silica is colloidal alumina. In another embodiment, the colloidal alumina is from 20% to 99% by weight of the mixture. In another form, the acid is nitric acid. III. ADSORBENT SYSTEM AND / OR ANCHORED CATALYST The use of organic and inorganic materials as catalyst systems is known in the art. These catalyst support systems can be linked with a homogeneous catalyst. A homogeneous catalyst is defined as a catalyst that is in the same phase as the reactants. There are two main advantages in relation to the use of a catalyst support system ep combined with LI? homogeneous catalyst. First, the homogeneous catalyst bound or complexed with the support can be recovered after the reaction has ended. Several of the homogeneous catalysts used in the art are expensive in their preparation; Therefore, the recovery of these materials is important. Second, the support can enhance the activity of the anchored hamagéneo catalyst. An anchored catalyst is defined as a catalyst attached to a support system. The formation of complexes of a catalyst with an inert support or, for example, a polymer like paliestirens has been the focus of extensive research in the prior art. The use of metal oxides as catalyst supports has also been used extensively in catalytic reactions. A review of the systems of -5 anchored catalysts is presented in Valentipe et al., "Technological Perspective for Anchored Catalysts Preparation" (Technocracy Perspective for the preparation of anchored catalysts), Am. Chem. Soc., Div. Pet. Chem., Volume 27 (3), pages 608-10, 1982; Pitt an et al., "Unusual Selectivi ties ip Hydroformy latiops Catalyzed by Polymer-Attached Carbonylhydrotris (triphey iphosphine) rhodium" (unusual selectivities in hydropharmamilations catalyzed by carbapilhydrotris (triphenylphasin) rodia fixed on polymer), J. Am. Chem. Soc. Volume 98 (17), pages 5402-5, 1976; Jacobsan et al., "Selective Hydragepatian of 4- Vinylcyclahexene Catalyzed by Polymer- nchored Carbsnylchlorobis (triphep Iphosphine) iridium" (selective hydrogenation of 4-vinylcyclshexeno catalyzed by carbsnilclarobis (triphenylphosphin (polymer-anchored iridium), J. Mol. 1 (1), pages 73-6, 1975; Pittman et al. "The Vinyl Reactivity of {5-Vinylcyclslpentadienyl) dicarbony Initrosy lchrsmium. A Novel Vinyl Organsmetal lie Manamer" (the vinyl reactivity of (5-vinylcyclapentadienyl) dicarbanilnitrasilcramo A novel vinyl oragnesmetical monomer), Macrsmolecules volume 11, pages 560-565, 1978, and Csttan et al., "Advanced Inorganic Chemistry, A Comprehensive Text", a 3rd edition, patinas 620- 801, 1962. Even though pu systems are known in the art, such systems are limited in extent to the extent that current polymer delivery systems are limited to the reaction conditions where the polymer is stable. Prior art support systems are composed of an organic polymer structure, or a single component metal oxide system. In one embodiment, the invention relates to a catalyst and binder adsorbent system, comprising: (a) a binder not SLtstituids or substituted by ligand pendiepte, and (b) a particle of oxide adsorbent and / or oxide catalyst unsubstituted or substituted by pendant ligand, wherein at least one of the camponents (a) and (b) is substituted by pendant ligand, and where the substance (a) is crosslinked with the component (b). The unsubstituted binder and the adsorbent particle of oxide and / or unsubstituted oxide catalyst is defined herein as a particle having free hydrosyl groups that have not been replaced by an organic or inorganic pending ligand portion. The binder and the oxide adsorbent and / or oxide catalyst and system particles discussed in the previous section entitled "binder and oxide adsorbent system and / or oxide catalyst" can be employed as the unsubstituted agglomerator and the adsorbent particles of oxide and / or unsubstituted oxide catalyst and systems. In a modality, the binder may be a colloidal metal oxide or a colloidal metalloid oxide, preferably colloidal alumina, colloidal silica, a metal oxide colloidal metal is iron, or a mixture thereof, and preferably even higher, alumina colloidal, colloidal silica, or a mixture thereof, and preferably even higher colloidal alumina. In one embodiment, the oxide and / or oxide catalyst adsarbent particle is replaced by pending ligand. In another embodiment, the binder is substituted with pending ligand. In another embodiment, the oxide adsorbent particle and / or the oxide catalyst and the binder are both substituted with pendant ligand.

The substituted binder and the oxide adsorbent system and / or the independently substituted oxide catalyst contain a pending ligand in the mepas. A pending ligand ss is defined herein as a portion having at least one campleta forming group and optionally a fixing end. The complex formation group is typically the portion of the pending ligand employed to attach or bind to a metal complex, where the metal complex may be a homogeneous catalyst known in the art and presented, for example, Coliman et al-, "Principles and Applications of Organotransition Metal Chemistry", Chapter 2, 1987, can be used here. In one embodiment, the complex formation group is a group with an isolated pair of electrons. In this case, the camplejo formation group can be linked with another portion by means of a Lewis acid-base interaction. Examples of groups possessing isolated pairs of electrons and which may behave as complex formation sites include, but are not limited to, a hydroxyl group, an ether, a thiol, a thioether, an amine, a monssubstituted or disubstituted amine, a fasfina, a more substituted or disubstituted phosphine or a mixture thereof. Typically, the pending ligand has a fixing group (or "fixation end"), but here there are dopde modalities of the complex formation group can be attached directly on the agomerapte / oxide adsorbent system and / or the oxide catalyst without need for a fixation. In another embodiment, the complex formation group may be an unsaturated organic moiety. The unsaturated organic portion may be, without limitation, a cyclic, acyclic or aromatic portion. In one embodiment, the acyclic unsaturated organic moiety may include, but is not limited to, an olefin, an allyl, a diene, a triene, or a mixture thereof. In another embodiment, the acyclic unsaturated organic moiety has the f? RmL-la - (CH = CH) n CH = CH2, where n is from I to 5, preferably from ia 3. In another embodiment, the complex formation group it can be a cyclic unsaturated organic portion. Examples of cyclic unsaturated organic moieties include, but are not limited to, cyclopeptadiene, cycloheptatriene, cyclooctadiene, cyclalactetraens, or a mixture thereof. In another embodiment, the complexing agent may be an aromatic unsaturated organic portion. Examples of aromatic unsaturated organic portions include, but are not limited to, benzene, naphthalene, anthracepa or mixtures thereof. The pending ligand portion may also have a fixing end. The attachment end connects the complexing group end of the ligand over the binder or biep on the oxide adsorbent particle and / or oxide catalyst. If no fixation is present, the complex formation group is fixed directly on the binder or on the particle of oxide adsorbent and / or oxide catalyst. The binding end may comprise an amino group, an aromatic group, a silyl group, a siloxy group or a combination thereof or an oligomer or polymer thereof. The length of the fixing end may vary according to the end use. In an embodiment, the attachment end may be an aliphatic rump or an aromatic rump of 1 to 20 carbon atoms, preferably 1 to 10 carbon atoms, and preferably even greater than 1 to 5 carbon atoms. The fixing end may be branched or unbranched, and substituted or unsubstituted. In another embodiment, the fixing end may be a silane, a palisalace, a hydrocarbon-if mixed, a hydrocarbon-whether or not, or a mixture thereof. In another embodiment, the invention relates to an adsorbent and / or anchored catalyst and binder system, comprising (a) an unsubstituted binder or substituted with pendant ligand, and (b) a particle of oxide adsorbent and / or unsubstituted or unsubstituted oxide catalyst csn pending ligand, and (c) a metal complex, wherein at least one of components (a) and (b) is it is substituted with pendant ligand, where the campspente (a) is crosslinked with the component (b), and dande the metal complex (c) is attached to the component (a) and / or (b). The binder substituted by the pending ligand and the oxide and / or oxide catalyst adsorbents system described above can be incorporated with the metal complex. As previously mentioned, the pending ligand has a complex formation group that can be linked to a metal complex (c). Examples of metal complexes that can be attached to the binder system and / or substituted catalyst include, but are not limited to, a metal salt, a metal carbonyl complex, a metal phosphine complex, a metal amine complex , a metal hydride complex, a metal olefin complex, a metal acetylene complex, a metal polyene complex, a metal halide complex, or a mixture thereof. In this modality, the etals that can be used are metal carbopyl complexes, metal phosphine complexes, metal amine complexes, metal olefin complexes, metal acetylene complexes, metal polyene complexes, and metal complexes. Metal halide include transition metals, metals of the lanthanide and actinide series. In one embodiment, the metal salt may be a halide, a carbonate, an oxalate, a bicarbonate, or a carboxylate as contracted and lithia, sodium, potassium, rubidium, cesium, francis, magnesium, calcium, strontium, barium, radon, the transition metals, the metalss of the lanthanide series, or the metals of the actinide series as the metal portion. In another embodiment, the metal carbspile may be a mononuclear or polynuclear binary carbanil of a transition metal. Examples of metal carbanils useful in the present invention include, but are not limited to, mixed mononuclear or polynuclear complexes of carbanyl-fasphine, carbopyl-fasphinate, carbonyl-silyphine, carbonyl-acetylene, carbonyl-cyclapentadienyl, carbonyl-hydride or carbopyla- halide of a transition metal. The binder and oxide adsorbent system and / or the substituted oxide catalyst can be used as a soup system and linked with a metal complex which acts as the second catalyst. In one embodiment, the second catalyst can be a homogeneous catalyst. Several homogeneous catalysts are known in the art and presented in Prshall "Homogeneous Catalysis" (Homogeneous Cat lysis) 1980. Examples of homogeneous catchers that can be anchored on the binder system and oxide adsorbents and / or substituted oxide catalyst include, without limited to them, a hydrogenation catalyst, an oxidation catalyst, a hydrostatic catalyst, a reduction catalyst, an isomerization catalyst, a polymerization catalyst, a carbopylation catalyst, a reforming catalyst, a metathesis catalyst of alefin, a Fischer-Tropsch catalyst, a gasification catalyst or a mixture thereof. In another embodiment, the invention relates to a method for the production of an adsorbent system and / or catalyst substituted with pending ligand, which comprises: i) the mixture of the components, comprising: (a) a binder sutituida. or it is constituted by a peptide ligand comprising a colloidal metal oxide or a colloidal metalloid oxide; b) a particle of oxide adsorbent and / or oxide catalyst unsubstituted or substituted by pendant ligand, and c) an acid, at least one of the camponeptes (a) and (b) has substitution with pending ligand, and ) removing a sufficient amount of water from the mixture to crosslink the components (a) and (b) to form a system of adsorbent and / or catalyst and binder substituted with pending ligand. The method further comprises (iii) the binding of the metal complex on the system resulting from step (ii) to form the anchored catalyst system. The unsubstituted binder and the particles of oxide adsorbent and / or oxide catalyst not included in the present invention can be converted into the substituted analogues with pending ligand using well known techniques and presented in Eisen et al., "Catalytic Activity of Ssme Immobilized Dirhadium Complexes with One Bridging Thiolate and One Bridging Chlaro Ligand "(Catalytic activity of some immobilized complexes of dirrodis with a thiolate bridge and a chlorine ligand bridge), J, Mol. Catal, Volume 43 (2), pages 199-212, 1987; Cer ak et al., "Hydrogenation Catalytic Activity of Substituted Cuclspentadiepy 1 Titapium Complexes Anchored on Polysiloxanes Prepared by a Sal-Gel Procedure" (Catalytic activity of hidragenacióp substituted cyclopeptadispoly titanium complexes sn polysiloxanes prepared by a Sol-Gel procedure) , J. Organomet. Che. Volume 509 (1), pages 77-84, 1996; Doi et al. "Metal Ciuster Catalysis: Preparation and Catalytic Praperties of Aniopic Trirutheniu Clusters Anchored to Functional ized Silica" (Catalysis of Metal Group: Preparation and Catalytic Properties of Trirutenium Anionic Groups Anchored on Functionalized Silica), Inarg. Chim. Minutes, Volume 105 (1), pages 69-73, 1985; Doi et al., "Metal Ciuster Catalysis: Preparation and Catalytic Prsperties of a Tetraruthenium Ciuster Anchored to Silica via Phosphipe Ligands" (Catállisi de Grupo de Metal; Preparation and Catalytic Properties of a Group of Tetrarrutenis Anchored to Silica through Phosphine Ligands ), J. Mol. Catal., Volume 19 (3), pages 359-63, 1983, which are incorporated herein by reference. The reaction between i) binder and / or 2) an unsubstituted oxide / oxide catalyst / adsorbent particle and a hydrosyl-reactive compound produces the oxide adsorbing particle and / or substituted oxide and agglomeration catalyst. In one embodiment, the unsubstituted binder reacts with a compound that reacts with hydroxy to produce a binder substituted with pending ligand. In another embodiment, the oxide adsorber particle and / or the unsubstituted oxide catalyst reacts with a hydroxy reactive compound to produce a particle of oxide adsorbent and / or oxide catalyst substituted with pending ligand. In another embodiment, the unsubstituted binder and a particle of oxide adsorbent and / or unsubstituted oxide catalyst react with a hydroxyl-reactive compound to produce a binder substituted by a pendant ligand and a particle of oxide adsorbent and / or catalyst. oxide substituted with pending ligand. The ligand-substituted binder and a particle of oxide adsorbent and / or ligand-substituted oxide catalyst can have free hydroxy groups that have not been substituted with the pending ligand. Once the binder substituted for the oxide adsorbent particle and / or the substituted oxide catalyst have been separated, they are combined using the techniques described above for the preparation of the binder system and oxide adsorbent and / or oxide catalyst. The hydroxyl-reactive compound is any compound capable of reacting with free hydroxy groups the unsubstituted binder and the oxide adsorbent particle and / or unsubstituted oxide catalyst. The hydroxyl-reactive compound also has a complexing group and may have a fixing end as described above. In a modality, the hydroxyl reactive compound can be an alkylation agent, an alcohol, a carboxylic acid, an organic ester, an organic anhydride, an organic tosylate, a trialkyloxopia cation, a silane, a silyl halide, a siloxy compound , an organic acid halide, an organic orthoformate or a mixture thereof. In a preferred embodiment, the hydraxyl-reactive compound is an alkylating agent. In an even more preferred odalide, the alkylating agent is an aliphatic or araliphatic halide. In one embodiment, the aliphatic or araliphatic group may have from 1 to 20 carbon atoms, preferably from 1 to 10 carbon atoms, and still more preferably from 1 to 5 carbon atoms. The aliphatic and araliphatic groups may be branched and branched groups and substituted or unsubstituted. In another embodiment, a silylating agent may be employed. Silylating agents useful in the present invention include, without limitation, alkyl and aryl silylhalides. Alternatively, the silylating agent may be a silane, a polysiloxape, a hydrocarbon-if mixed, a hydrocarbon-siloxane, or a mixture thereof. Once the substituted system of aglomerapte and adsorber of oxide and / or oxide catalyst has been prepared, a complex metal can be extracted, for example by the formation of complexes, coordination, chelation, binding to the resulting system. Techniques for incorporating or joining the metal complex ep the support are presented in Gates, "Catalytic Materials". Chapter 12, pages 301-320, in "Materials Chemistry% An E ergipg Discipline" (Chemistry of materials: a discipline and ergent), edited by Interrante, L.V.; Casper et al., In "Advances in Chemistry", Series 245, American Chemical Saciety, Washington, D.C. 1995, which are incorporated here by reference. Examples of techniques employed to incorporate the metal complex ep the soup include, without being limited to these techniques, vapor deposition, incipient moisture, aqueous impregnation or aqueous impregnation. In another embodiment, the invention relates to a method for the production of an adsorbent and / or catalyst and binder system, comprising: i) mixing the components comprising: a) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, b) a particle of oxide adsorbent and / or oxide catalyst, and c) an acid, ii) remap a sufficient amount of water from the mixture to crosslink the "a" and "b" compacts to form a adsorbent and / or catalyst and binder system, iii) the reaction of the adsorbent system and / or catalyst and binder resulting from step (ii) with a compound that reacts with hydroxy to form an oxide and / or catalyst adsorbent system of rust and binder substituted with pending ligand. The treatment of the binder system and oxide adsorbent and / or unsubstituted oxide catalyst with the hydroxyl reactive compound leads to a system of agsmerant and oxide adsorbent and / or oxide catalyst substituted with pending ligand. In one embodiment, the unsubstituted binder reacts with a reactive hydroxy compound to produce a binder substituted with pending ligand. In another embodiment, the oxide adsorbent particle or unsubstituted oxide catalyst reacts with a hydroxyl-reactive compound to produce an oxide adsorbent particle / oxide catalyst substituted with pending ligand. In another embodiment, the unsubstituted binder and an oxide adsorbed particle / unsubstituted oxide catalyst reacts with a compound that reacts with hydroxyl to produce a binder substituted with a pyridic ligand and an oxide adsorbent particle and / or a hydroxide catalyst. oxide replaced with peppertiente ligand. Once the binder and oxide adsorbent and / or substituted oxide catalyst system is prepared, a coupling or metal can be incorporated or bonded onto the support using the techniques described above to produce an anchored catalyst system. In another aspect, the invention relates to an adsorbed system and / or anchored catalyst and binder, comprising: (a) a binder, and (b) a particle of oxide adsorbent and / or oxide catalyst, and (c) ) a metal complex, where at least one of components (a) and (b) is substituted with ligand, where component (a) is crosslinked with component (b), and where if metal complex (c) it is attached directly on the component (a) and / a (b). In another aspect, the invention relates to a method for the production of an adsorbent and / or anchored catalyst system, which comprises: (i) the mixture of components, comprising: (a) a binder comprising a colloidal metal oxide or colloidal metalloid oxide; (b) an oxide adsorbed particle and / or an acid catalyst, and c) an acid, ii) a sufficient quantity of water from the mixture to retyntilate the components "a" and "b" to form a system of adresarbepte and / or catalyst and binder substituted with pendant ligand, and iii) join a metal substrate directly over the system resulting from step (ii) to form the anchored catalyst system. In this direct bonding mode, the metal complex is bonded directly onto (i) in binder and / or (2) the oxide adsorbent particle and / or the oxide catalyst. The hydroxy groups in the binder and the particle can behave as a complexing group as described above and can directly bind metal complexes. EXPERIMENTS The following examples are presented to offer people with certain knowledge in the subject a complete presentation and a full description of how the compounds claimed here are elaborated and evaluated., and have the purpose of being exemplars of the invention and of limiting the scope of what inventors consider as their invention. Efforts were made to ensure accuracy in numbers (eg quantities, temperature, etc.) but some errors and deviations may exist. Unless otherwise indicated, the parts are parts by weight, and the percentage is% by weight, the temperature is indicated in ° C at either room temperature and the pressure is atmospheric pressure or near atmospheric pressure. . EXAMPLE 1 Enhanced aluminum oxide was prepared by the process of this invention employing the following steps: i) gamma-aluminum oxide particles were produced by calcining A1 (0H) 3 at a temperature comprised between 550 and 560 ° C for produce calcined A1203 from the gamma pharma. Ii) 20 liters of this aluminum oxide ep were immersed in a tank containing 0.5% by weight of acetic acid in distilled water. The total volume of the solution was 93.7 liters. The alumina was allowed to settle on the acid solution for approximately 15 minutes to allow saturation of the solution. The acid solution was drained and the remaining alumina was rinsed in a 30 liter tank of distilled water. The distilled water was drained and the remaining alumina was dried at a temperature of 121 ° C for 90 minutes. The performance of the enhanced aluminum oxide particles of this invention was tested. Two cramatagráficas columns, each 25 cm long and with an internal diameter of 1 cm, equipped with a solvent reserve were used for this experiment. Each column was packed with 20 ce of the enhanced aluminum oxide particles produced above.

Each column was rinsed with 100 ml of water using nitrogen cylinder pressure to maintain a flow rate of about 20 ml per minute. A test solution of approximately 200 ppb of lead was prepared using lead acetate trihydrate. A total of 200 ml (10 bed volumes) of test solution passed through each column emploands the same flow velocity. The influent, the total effluence of the 10-bed volumes, and the effluent sample collected during the tenth bed volume were analyzed for the presence of lead, and the results were summarized in Table 1.

TABLE 1 TEST NUMBER TESTED CURRENT LEAD TOTAL * (μg / liter) i Influent 211 Total effluent < 5 Effluent end (102 bed volume) < 5 2 Influent 229 Total effluent < 5 Effluent end (102 bed volume) < 5 * The lower limit of detection of lead was 5 μgm / liter. This particle was also tested using the TCLP method (EPA method # 6010), and the particle of the invention passed the TCLP test for lead. Example 2 A comparison was made between the alumina enhanced with acid of this invention and alumina pa treated with acid to remove lead. Both aluminum oxide particles were calcined at a temperature of 550 ° C before the experiment. Enhanced gamma-aluminum oxide particles of the present invention were made in accordance with the procedures of example i. Two identical five-gallon containers were filled with alumina oxide for lead removal. A vessel was filled with 16 liters of the treated fuel of this invention. The other container was filled with 16 liters of untreated alumina. Two tanks were prepared each containing 100 gallons of distilled water with lead acetate trihydrate. The tanks were mixed extensively for 30 minutes. After 30 liters of mixing, the concentrations of lead in the water were determined. The water containing lead from each tank was passed through the alumina containers. A total of 80 gallons of water with lead acetate trihydrate (19 bed volumes) was passed through each of the containers at a flow rate of 62 gallons per minute. A sample of effluent water was taken from the 192 bed volume and said sample was analyzed to determine the total content of lead. The percentage reductions were then calculated. The results of the tests appear in Table 2 below.

TABLE PARTICLE CONCENTRATION CONCENTRATION REDUCTION Calcinated to INITIAL OF PORCENCUAL EFFLUENT 550 ° C before LEAD AFTER PLOHO treatment (mg / 1) CONTACT WITH (%) with acid PARTICLE (mg / 1) oxide of alu-C- * 0.58 minium not treated with acid oxide of 1.44 0.39 73 aluminum treated with acid of the present invention Example 3 A comparison was made between the treated alumina of this invention and untreated alumina to remove phosphate. Chi-rho alumino oxide particles were processed by calcining A1 (0H) 3 at a particle temperature of 480-520 ° C. The enhanced Chi-rho aluminum oxide particles of the present invention were treated with acid in accordance with the procedure of step (ii) ep Example i. The performance of the particles was measured using the same procedures as those of the pls i axis, except that one column of cormatagraphy was filled with 20 c of the treated alumina and the other column was filled with 20 cc of untreated alumina and the test solution was 9.3 mg / 1 of KH2P04, and the results appear in Table 3.

TABLE PARTICLE CONCENTRATION CONCENTRATION REDUCTION Calcinated to INITIAL OF P0RCENCUAL EFFLUENT 480 ° C before PHOSPHATE AFTER PHOSPHATE treatment (mg / 1) CONTACT (%) with acid PARTICLE (mg / 1) oxide of alu9.3 0.16 98.3 minium not treated with acid oxide of 9.3 0. 4 99.6 aluminum treated with acid of the present invention This particle of the present invention of the experiment was also tested using the TCLP method (EPA method # 1311), and the particle of the present invention passed the TCLP test for phosphate. Example 4 The ability of the particle of this invention to remove selenium was tested. Gamma-enhanced aluminum oxide particles (100% A1203) were made by the procedure of Example 1. Five columns were prepared using glass columns of 0.875"internal diameter by 12" long, each column with a volume of About 95% of the particles of A1203 formerly acid-precipitated particles of this invention of various particle sizes, within a range of 500 μm to 4,000 μm. Each bed was rinsed with approximately 5 volumes of water bed D.I. by pumping downstream at a trapsversal flow rate of 5-6 gpm / square foot (ie, approximately 95 ml / min). A test solution was prepared with a calculated calculator of selepium of 1.5 mg / L. A total of about 10 bed volumes (i.e., approximately i L per column) was pumped through each column using the same flow rate. During the test, the test solution was continuously stirred at low speed. During the bed volume, an effluent sample was taken from each column and the sample was analyzed to determine the presence of selenium. Likewise, a single sample of influent was collected and analyzed to determine the presence of selenium. The results appear in Table 4 below.

TABLE 4 I.D. sample Total selenium (a) (particle size μm) mg / L Influent 1.45 606 EFF (4,000 μm) 0.101 404 EFF (1,000 μm) 0.073 303 EFF (2,000 μm) 0.477 202 EFF (500 μm) 0.003 (b) 101 EFF (3,300 μm) 0.101 (a) = the detection limit of selenium was 0.002 mg / 1 (b) = estimated value, less than the calibration limit Example 5 n: a combination particle of this invention was made and tested to determine its ability to remove triclaroethylene (TCE). 70 g of acid-enhanced gamma-aluminum oxide particles made by the procedure of example 1 were mixed with 20 g of colloidal alumina, 5 g of Mn02, and 5 g of CuO until the mixture was homogeneous. The mixture of particles was then mixed with a 5% acetic acid solution until the mixture reached a suitable consistency for agglomeration. The mixture was extruded and cut into a particle size of approximately 1,000 μm and heated to 150 ° C for 15 minutes to crosslink the colloidal alumina. The particle in accordance with the above was tested to determine its ability to remove TCE from the water. Particles of the invention were challenged with various concentrations of TCE in water as indicated in Table 1. Two specifically elaborated columns (40 cm X 20 mm) equipped with thick glass frits were packed and dried with volumes of 10 L (measured with a graduated cylinder of 10 mL) of particles. The columns were challenged with 5 aliquots of 10 L (5 bed volumes) of the TCE solution. The fifth bed volume of each column was collected in a 50 mL Erlen eyer flask, capped, and immediately analyzed by purging and tra-GC / MS technique using a GC / MS ion trap Finnigan MAT Magnum with a concentrated liquid sample Tekmar (LSC 200). The results aparacep in Table 5.

TABLE 5 Concentration of triclaroethylene Sarbato Influent (ppm) Effluent (ppb) TCE in water 1.0 < fifty Example 6 10 The TCE adsorption and TCLP extraction procedures were carried out as follows. A sample of 20.0114 grams (a volume of approximately 24.50 mL) of the combination particle A120 / Cu0 / Mn02 of Example 5 (named 0307595TCE1) after treatment with TCE was wet packed in a 50 mL burette (with removable cap ) covered with glass wool. The sample was loaded with 5 volumes of water bed. The adsorbent material was then transferred quantitatively into the Zero Headspace Extractor (ZHE) where 200 L of Water, was sealed appropriately and stirred for 18 hours. The filtered solution was collected in 2 bottles of 100 L stored in the refrigerate at a temperature of 4 ° C until analysis by GC / MS. The Fipnigan MAT Magpum ions TC / MS trap equipped with a sample concentrator -or liquid Tekmar (LSC 2000) is used? for the analysis »The calibration curve procedure was as follows. A 50 ppm freshly prepared TCE mother solution was obtained by dissolving 34.2 μl of spectrophotometric grade TCE (Aldrich) in 20 ml dem ethanol grade 5 HPLC (Fisher) followed by one liter dilution. Dilution of this solution (1,000 μl: ΔI) resulted in Lina TCE stock solution of 50 ppb. All dilutions were achieved by the use of deionized water. A calibration curve was constructed by purging TCE solutions of i © 1.0, 0.50, 0.20, 0.10, and 0.050 ppb.

TABLE or TCE adsorbent sample found, TbP ppb detection limit, ppb 0.07595TCE1 Nd (a) 0.0050 (a) = Not detected. The fact that TCE ep sample is less than 500 ppb (EPA TCLC limit) characterizes it as Lin residue not hazard in terms of TCE. © Example 7 a 100 ml portion of phosphorous standard was diluted (Hydrogenase potassium and water) at 1000 ppm (Lab Chem, Inc.) to 2 liters. Aliquots (200 ml) of the resulting stock solution containing 50 ppm of phosphorous standard were poured over 24 hours with duplication of approximately 2 μl of (dry) volumes (both volume and mass were measured) of each alumina sample, and centrifugal. Acid-enhanced gamma-alumina oxide particles from Pblk (Cu) and Polk (CT) samples and chiral-enhanced altimine oxide particles with Pbhk (AU) and Pahk (At) acid were made using the procedures of Example 1, except that the "type" of initial alumina is different as shown in Table 7, and that the calcination temperatures were different for the four samples as shown in Table 7 below. These materials were challenged to determine the ability of alumina to remove phosphate (P04) given the variables in initial materials and treatment. Aliquots (0.4 ml) of the supernatant were diluted to 20 ml. To each of these solutions was added, with stirring, 2 drops of fenalftalein (Fisher), followed by 1 ml of reagent I of ammonium malibdata and then 2 drops of reagent I of stannous chloride (LabChem Inc.). The determination of aqueous phosphate was achieved by color determination, photometrically at 690 pm (path length, 0.5 cm) in a quartz cell and read in a Shi adzu UV-2101PC, UV / VIS scanning spectrophotometer. All dilutions will be achieved by pre-desalinated water. The results appear below.

TABLE 7 ID # Material Temperature Treatment of initial calcination washed after (time) of thermal treatment Pbhk (AU) Beamite 400 ° C acetic acid (60 min) at 0.5%, 15 min Pohk (AT) Bea ita 475 ° C acetic acid (60 min) at 0.5%, 15 min Pblk (CU) alumina 500'C oxidized acetic acid (60 min) at 0.5%, 15 min (bayerite) Palk (CT) alumina 550 ° C oxidized acetic acid (60 min) at 0.5%, 15 ip (bayerite) ID # Pore area Diameter of average diameter M2 / gram pore med: pore io (area) (Vol) μm: μm: Pbhk (AU) 102 0. 088 Pohk (AT) 14 90 0.0078 Pblk (CU) 7 93 0.0146 Palk (CT) 6.3 69 0.075 ID # For average Capacity (4V / a) P04 μm g / Kg in bulk Pbhk (AU) 0.11 13.56 Pohk (AT) 0.079 14.47 Pblk (CU) 0.2591 11.56 Palk (CT) 0.12 10.93 EXAMPLE 8 Acid-enhanced gamma-alumina oxide particles were prepared from samples Pbhk (AU), Pohk (At), Pblk (CU), and Palk (CU) by the procedures of Example 7. These materials were challenged to determine the capacity of alumina to remove lead (Pb ++) given the varibles in initial materials and treatment. A 500 ml portion of 400 ppm lead (0.6392 g Pb (N03) 2 dissolved in 10 ml of concentrated nitric acid and diluted to 1 liter with deionized water) was diluted to 2 liters with deionized water. Aliquots (450 ml) of the resulting stock solution containing 50 ppm Pb, they were overturned for 24 hours with approximately (dry) volumes (both volume and mass were measured) of each alumina sample, said aliquots were centrifuged, and stored before the GFAA analysis. The instrument used was a Shimadzu AA-6501F atomic absorption spectrophotometer. The results are presented below.

TABLE 8 ID # Capacity Pb ++, g / GRANEL Pbhk (AU) 1.9 Pohk (AT) 1.7 Pblk (CU) 3.0 Pslk (CT) 1.3 Example 9 Acid-enhanced gamma-alumina oxide particles were made from Pbhk (AU), Pohk (AT), Pblk (CU), and Pslk (CT) samples by exemplary procedures. These materials were challenged to determine the capacity of the samples. alumina to remove arcenic (As03-) given the variables in initial materials and treatment. A portion of 200 ml of 1000 ppm of standard (Fisher SA449-500) of arcenica (arcenic trioxide in 10% nitric acid) diluted to 4 liters with deanised water was used. Aliquots (450 ml) of the resulting stock solution containing 50 ppm of As were tipped for 24 hours with duplicate volumes of approximately 2 ml (dry) (both volume and mass were measured) of each sample of alumina, said Serum aliquots centrifuged and stored before analysis of 6FAA. The instrument used was a Shimadzu AA-6501F atomic adsorption spectrophotometer. The results appear below.

TABLE 9 ID # Capacity of As as As03- g / Kg, BULK Pbhk (AU) 11.9 Pohk (AT) 10.6 Pblk (CU) 8.9 Polk (CT) 8.1 EXAMPLE 10 In a large-scale pond, a 2,300-gallon tank was filled with approximately 2,000 gallons of tap water and 147.8 g of Pb (0Ac) 2"3H20 were added, the pH was adjusted to 6.7 and samples were taken from the tank and it was found that they were 8,750 ppb in Pb ++. It filled I? container with 19.6 kg of Polk (CT) in accordance with that described in Example 7. The lead water from the tank was pumped through the vessel at a rate of 1.5 gallons per minute to remove the lead. Samples of the effluent were collected after each 250 gallons and the concentration of plumb bed was determined and plotted as shown in Figure i. The tank was again filled with approximately 2,000 gallons of tap water and 147.8 g of Pb (0Ac) 2 »3H20 were added to provide a solution of 9,160 ppb" The pH was adjusted to 7.00 and the lead solution was bounded to through the same container at a flow rate of 1.5 gallons per minute. Samples of the effluent were collected after every 250 gallons and the lead concentration was determined which was plotted as illustrated in figure 1. It was found that the lead concentration of the samples for "the samples obtained at 2,000 - 3,500 was lower to the limit of detection of 0.2 ppb In this test it was determined that the removal capacity of plk ds Polk (CT) was or g / kg Example 11 Several systems of adsorbent particles and / or catalytic and binder are presented in Table 10 in example 12 below and said systems were elaborated according to the generalized procedures of this invention as presented below as well as by means of several systems that do not form part of the invention The binder and the adsorbent and / or catalytic particles were combined in a mixing vessel, the amount of each of the elements varied according to the desired bead size. The components remained constant as indicated in Table 10 below. This "dry" combination was premixed to ensure a homogeneous mixture of all components. After achieving this, a solution containing 5% acetic acid in distilled water was added to the mixture. The amount of the acid compared to the other components varied according to extrusion parameters and other processing variables, but for the procedures the range was typically between 35 and 45% by weight of the total mixture. This solution was added to the dry materials and mixed until the material had a consistency of type "Homogeneous" clay "The mixing was carried out using a Hobart" A-300"mixer The material was then ready for extrusion The mixed product containing the acetic acid solution was fed through an extruder, such as, for example, a DGL-1 dome granulator manufactured by LCI Corporation of Charlotte, N.C., United States of America. The extruded elements were fed through a QJ-230 device also manufactured by LCI Corporation, which transformed the extruded products of "rod" type into small spheres. The extrusion and spherical forming bottles provided a finished product suitable for s? Use for Lina specific application. However, sphere formation is optional and does not alter the performance of the product. After the elaboration of the spheres, the product was transferred to LI? 12: Ds oven dried where it was dried for 1 (one) hour at a temperature of 250 ° C. The product was then ready for use in an application. Example 12 The particles formed with the constituents listed below in Table 10 were tested for their ability to remove TCE. The adsorbent and / or catalyst and binder system of Table 10 were challenged with various concentrations of TCE as indicated in Table 10. Two specific columns (40 cm X 20 cm) equipped with thick glass frits were packed dry with 10 ml volumes (measured with a 10 ml graduated cylinder) of particles. The columns were challenged with 5 aliquots of 10 ml (5 volumes dg bed) of the solution of tricolaraetileno (TCE). The fifth bed volume of each column was collected in a 50 ml Erlenmeyer flask, capped, and immediately analyzed by GC / MS purge technique and traps using a Finnigan MAT / Magnutrn GC / MS trap equipped with a nitrogen concentrator. liquid sample Tekmar (LSC 2000). The particles in Table 10 were prepared in accordance with that described in Example 11. The percentage compositions of each component as well as the nature of the binder are shown in Table 10. Prior to mixing with the other components, the oxide particle ? z: of aluminum was first calcined at 50 ßC or 5 * 0 as indicated in Table 10, then treated with acid by contacting substantially with 0.5% acetic acid at room temperature for 15 minutes as usual. Candidate application submitted on the same date entitled "Acid Contacted Ephaphed Adsorbent Partial and Method to Mal-ing and Using Therefor" (Adsorbent particle enhanced by contact with acid and method to make and use said particle), bed is presented in the Previous applications the application listed above, and then dried at a temperature of 121 ° C for 90 minutes. The removal of TCE from the aqueous solution was investigated using various systems of adsorbent v / o catalyst and aglamerant of the present invention and the restiltados appear in Table 10. In the entry no. 8, a reduction of 99% of TCE was observed when the particle consisted of 40% of CuO, 40% of Mp02, and 20% of colloidal alumina as the binder. When aglamerant was used, however, the Cu0 / Mn02 particle removed only 0-1% of TCE (entries 9A and 9B). These results indicate the need for the binder material to reach the adsorbent and / or catalytic properties of the particle or to provide adsorbent and / or catalytic properties to the particle. Other particles demonstrated the ability to remove TCE. For example, entry no. 1 removed more than 95% of TCE. The entry no. 7 removed 99% of TCE. The particle that corresponds to the entry no. 7 had two particles of adsorbent and / or catalyst, one of which was carbon. Carbon was also used in combination with various metal oxide components (entries 24A and 24B), to remove TCE (> 90%). Even when the entrance na. 3 removed 96% of TCE, the PVP binder maintains the particle together both the bed binder of the present invention. Particles with PVC binder disintegrate over time, which reduces the utility of the particle. In the case of entries 5A, 5B and 6, the removal of TCE was very high (98%); however, the activated peat also disintegrates much more rapidly than the particles of the present invention. The pollutants adsorbed by the peat can also be lixidiar in the environment. Without wishing to be bound by any theory, two plausible mechanisms can explain the catalytic degradation of TCE using the particles of the present invention. The first mechanism involves a reduction oxide chemistry between TCE and the metal oxide component of the particle. TCE is electrophilic and can stabilize a negative charge if it is reduced. The transfer of electrons from LI? make up metal oxide to TCE can be the first step towards the degradation of TCE. A second mechanism includes 1 -. Lewis acid-base ds interaction between TCE and the metal oxide component, the one that increases the speed of attack nucí eofíl co of TCE by the water. Due to isolated pair ssctranes in the chlora groups of TCE, a metal oxide component can initially coordinate with the clear group. Initial coordination may also be the first step towards the catalytic degradation of TCE.

TABLE 10 Input Binder Temperature% by weight (% by weight) of Becada / A1203 crosslinking (temperatLira ep ° C (minimum calcination time) ° C), treated with acid 1 V-900 (20) 150 (15) 70 ( 550) 2 PVP (3.2) 150 (30) 91.6 (550- 3 RRP (3.2) 150 (30) 91.3 (550) 4 NA 5 NA 6 NA 7 V-900 (20) 250 (60) 40 (500) 8 V-900 (20) 250 (60) 9 250 (60) 10 V-900 (20) 250 (60-60 (5 © 0) 11 V-900 (20) 250 (60) 70 (500) 12 V- 900 (20) 250 -60) 13 250 (60) 100 .550) 14 V-900 (20) 250 (60) 67 (550) PVP (3) 15 V-900 (20) 250 (60) 71.6 (550 ) PVP (3) 16 V-900 (17) 250 (60) 13.6 ¡550) 17 V-900 (13.6) 250 (60) 17 (550) 18 V-900 (13.6) 250 (60) 17 (550) 19 V-900 (20) 250 (60) 17 (550) 20 V-900 (20) 250 (60) 17 (550) 21 V-900 (20) 250 (60) 17 (550) 22 V-900 ( 20) 550 (60) 70 (550) 23 NA "7 (550) 24 V-900 (19.9) 250 (0) 5. ^ (550) Sun P2 (20) 250 (60) 70 (550) Input CuO Mn02 0tro (s; (% by weight) (% by weight) component (s) (% by weight) 1 5 2 2.5 2.5 methylcellulase (0.5) 3 2.5 2.5 metí 1celulosa (0.5) zeolite (100) treated peat can acid (100) peat treated with acid (100) 7 carbon WPH (40) 8 40 0 9 50 50 10 10 10 11 5 5 12 10 1 zeolite (6.0) 13 14 5 5 15 --- .. w 2.5 methylcellulose (0.4) 16 1.7 1.7 tin (66) -17 1.7 1.7 zinc (66) 18 1.7 1.7 19 1.7 1.7 tin (66) 20 1.7 1.7 zinc (59.6) 21 5 5 5 5 # carbon WPH (100) 24 5.98 5.98 carbon WPH (9.95) cellulose vi cel (0.5) 25 Entrance Concentration Concentration With influent influx of effluent influencing TCE from TCE ep from TCE Experiment A 5th voltimen Bed Experiment B. { "/ of network? c.) Experiment A i 1 1.00 ppppmm <50 ppb (&5; 5%) 2 50.0 ppm 29.4 ppm (59) 50 ppm 3 5.0 ppb 0.20 ppb (96) 4 rejected * 5 50.0 ppm 1.0 ppm (98) 5.0 ppm 6 5 5..00 ppppbb 0.07 ppb (98) 7 5.0 ppb 0.06 ppb (99) 8 5.0 ppb 0.07 ppb (99) 9 50.0 ppb 50.4 ppb (0) 50.0 ppm 50 ppm 39.5 ppm (21) 5O.0 ppb 1 111 5 500..00 ppppmm 39.3 ppm (21) 50.0 ppb 12 50.0 ppm 37.2 ppm (26) 50.0 ppb 13 50.0 ppm 31.2 ppm (58) 50.0 ppb 14 rejectedM 15 rejected ** 16 rejected .zads ** 17 rejected ** 18 50.0 ppm 42.8 ppm (14) 5 .0 ppb 19 50.0 ppm 36.3 ppm (27) 5 .0 ppb 50.0 ppm 27.8 ppm (44) 50.0 ppb or --- I 50.0 ppm 24.8 ppm (5) 5 .0 ppb t ^? 50.0 ppm 42.7 ppm (15) 50.0 ppb ----? • rejected * 24 50.0 ppm < 5.0 ppm (> 90) 50.0 ppb 50.0 ppm 5.8 ppm (38) 5 .0 ppb Entrance TCE effluent concentration in the 5th bed volume (% reduction) Experimenta B 0. 5 ppm (90) 4 5 0.1 ppb (98) 6 7 8 9 49.6 ppm (1) 13 1 39.9 ppm (20) 11 45.8 ppm (8) 12 41.0 ppb (18 13 34.0 ppb (32) 14 15 1 17 18 44.4 ppb (11) 19 41.9 ppb (16) 20 27.0 ppb (46) 21 17.5 ppb (65) 20.3 ppb (59) 23 24 3.9 ppb (92) 25 11.3 ppb (77) * the sample did not allow the flow of the water ** the particles disintegrated when used PVP = GAF PVP K-60 pol ivipil pyrrolidone V-900 = LaRoche V-900 altimine gel (colloidal alumina) Sol P2 = Csndea Disperal Sol P2 ( colloidal alumina) Zeolite = Zea l and t Internation 1 CBV 100 CuO = Fisher C472 Mn02 = Kerr-McGee K'M (r) Manqanese Dioxide Electrolytic 92% Mn02 X-ray powder diffraction studies indicate that it is a mixture of manganese, tin = Fisher T.128 zinc = Fisher Z16 methylcellulose = Fisher M352 carbon WPH = powdered activated carbon WPH of calgon # of particle heated to 550 ° C in the air to convert Mn02 to Mn304 NA = not applicable Example 13 Various adsorbent and / or catalyst and binder systems of Table 11 were prepared in accordance with the procedures of Example 11 and Example 12 (preparation of aluminum oxide). The samples were tested to determine if they reacted with hydrogen sulfide at room temperature. The hydrogen sulphide was generated by the treatment of sulfur ds sodium with sulfuric acid and empty transferred in an IR cell that had been charged with 1.00 g of adsorbent system and / or catalyst and binders to be treated. The IR cell used was 9 cm long and 4 cm in diameter (a volume of approximately 120 mL). The cell was filled to approximately 170 torr of H2S and was absent? visually and the IR spectra were recorded. The parenteral composition of each component as well as the nature of the binder appear in Table 11. The aluminum oxide particle was first calcined at a temperature of 550 * C, and then treated with acid using 0.5% acetic acid and dried at a temperature of 121 * 0 druante 90 minutes using the same procedure as that described in example 12. The crosslinking temperature for each particle was 250 ° C during 1 hour. The removal of hydrogen sulphide using the adsorbent and / or catalyst and binder systems of the present invention was investigated, and the results are summarized ep Tabia 11. The removal of hydrogen sulphide by the adsorbent and / or catalyst systems and binder was monitreated by infrared spectroscopy. Based on these results, the systems of adsorbent and / or catalyst and binder of colloidal aluminum binder, acid-treated aluminum oxide, and copper oxide praparcianaron the best results in the removal of hydrogen sulfide.

TABLE 11 Agglomeration Entry 1203 (% ZnO (% CuO {% (% By weight) by weight) ep weighs by weight) 1 V-900 (40) 5 10 V-900 (50) 40 10 3 V-900 (0) 30 10 13: 4 V-900 (20) 60 10 10 5 V-900 (20) 60 20 6 V-900 (25) 70 7 V-900 (38) 60 5 8 V-900 (30) 50 20 9 V-900 ( 30) 20 50 10 V-900 (30) 69 Intrada Duration of H2S Comments 0 experiment reacted of H2S removal 16 hours S Virtually all adsorbed according to the one determined by IR 24 hours Yes Virtually all adsorbed as determined by IR 42 hours Si Descission observed © after 4 hours Virtually all adsorbed according to io determined pair IR 24 hours Yes Virtually all > ! =. adsorbed as determined by IR hours Yes Descolation cleared after 2 hours Virtually all adsorbed as determined by IR 2 hours s Decoloring observed after 2 hours Virtual all 10 adsorbed as determined by IR hours Decay observed after 3 hours Virtually all 15 adsorbed as determined by IR 8 1.5 hours Si Decoloring observed after 1.5 hours Virtually all 20 adsorbed according to the determined IR pair 16.5 hours if very slight very slow change slowly after 2 hours 10 4 hours yes Decoloring observed after 2 Hours Virtually all adsorbed as determined by IR A1203 = calcined at 550 ° C and then treated with V-900 acid = LaRoach V-900 alumina gel (colloidal alumina) EXAMPLE 14 Percentages of TCE adsorption and TCLP extraction were performed in the following manner. A sample of 20.0114 grams (bed volume of approximately 24.50 mL) of the colloidal alumina and combination particle A1203 / Cu0 / Mn02 of Table 11, entry 1, after treatment with TCE were packed ep wet condition in a burette of 50 mL (with removable cap) covered with glass wool. The sample was loaded with 5 volumes of water bed. The adsorbent material was then quantitatively transferred to the Zero Headspace Exhactor (ZHE) apparatus where 200 mL of water was added, it was sealed and treated for 18 hours. The filtered solution was collected in two bottles of 100 mL, stored in the refrigerator at a temperature of 4 ° C until analysis by GC / MS. The Finnigan MAT Magnum TC / MS trap equipped with a Tekmar liquid sample concentrator (LSC 2000) was used for analysis.

The calibration curve procedure was as follows. A fresh 50 ppm TCE stock solution was obtained by dissolving 34.2 μl of spectrophotometric grade TCE (Aldrich) in 20 L of HPLC grade methanol (Fisher) followed by dilution to 1 liter. Dilution of this solution (1000 μl: ÍL) resulted in a stock solution of 50 ppb of TCE. All dilutions were obtained using deionized water. A calibration curve was constructed by purging TCE solutions of 1.0, 0.50, 0.20, 0.10, and 0.050 ppb. The results appear below in Table 12.

TABLE 12 Sample of TCE adsorbent found, Limit of ppb detection of TCE, ppb Table 11, entry 1 Nd (a) 0.0050 (a) = not detected. The fact that TCE in the pipeline is less than 500 ppb (line of EPA TCLP) characterizes it as a non-hazardous waste in terms of TCE.

Example 15 Adsorbent and / or catalyst and catalyst supports were prepared as described in Example 11 using Bayerite alumina (calcined at 550 * C for 1 hour, and then treated with 0.5% acetic acid for 15 minutes), 25% colloidal alumina weight, employs HN03 at 7%, cure time of 1 hour, with extrusion and curing at temperatures of 300 °, 350 °, 400 °, 450 °, 500 °, 550 °, 600 °, and 650 °. Table 13 provides the cure temperature and the properties of these materials determined by BET surface area measurements, mercury pararosi etry as well as thermal gravimetric analysis. Example 16 Various adsorbent and / or catalyst and catalyst supports were formed in accordance with that described in Example 11 using Bayerite alumina (calcined at 550 * C for 1 hour, then treated with 0.5% acetic acid for 15 minutes), 25% colloidal alumina, using 7% acetic acid, cure time 1 hour, with extrusion and curing at a temperature of 300 °, 350 °, 400 °, 450 °, 500 * and 600 *. Table 14 provides the cure temperature and properties of these materials as determined by area, BET surface measurements, mercury psrasimetry, and thermal gravametric analysis. Figure 2 provides the surface area of alumina-alumina compounds prepared in accordance with that described in Experiment 15 and in Experiments 16 ep as a function of the curing temperature. Figure 2 also provides the surface area of the particle after curing for 7 hours and 14 hours. In addition, Figure 2 provides the surface area of alimine-alumina compyes prepared in accordance with that described in Experiments 15 and 16, after curing for 2 hours and 4 hours at a temperature of 350 ° C. The data appearing in Tables 13 and 14 and in Figure 2 indicate how surface area, surface morphology and acid properties (Lewis versus Bronsted sites) can be controlled by this invention. The surface area, pore area, bulk density, skeletal density, porosity, and acid properties obtained depend on the cure time and the cure temperature.

TABLE 13 Characterization of Alumina-Al-Lime Compound Initial material: Bayerite (calcined at 550 * C for 1 hour, then treated with 0.5% acetic acid for 15 minutes)% agglomerates: 25% by weight Temperature of cure: variable Curing: i hour Type of acid (concentration): HM03 (7%) Temperature Area Volume Medium area of pore superfluous cure for diameter (* C) BET m2 / g BET cc / g M2 / pore grass (o1) ) μm: 300 244.2 0.1743 105.8 0.4074 350 249.9 0.1786 400 258.0 0.1858 149.1 0.2380 450 243. 0.1780 194.1 0.0467 500 215.7 0.1587 197.9 0.0163 0 550 192.0 0.1414 600 171.4 0.1263 219.2 0.0251 650 158.1 0.1165 Median Pore Temperature Density Density 5 healing average skeletal bulk diameter (ßC) of pore (4V / A) g / mL g / mL (Area) μm: μm 300 0.0040 0.0127 1.35! .45 350 © 400 0.0043 0.0110 1.28 2.70 450 0.0039 0.0092 1.270 2.95 500 0.0048 O.OIOI 1.201 3.05 550 600 0.0040 0.0092 1.19 2.980 5 650 Temperature Porosity TGA% of TGA% of cure (%) loss loss (° C) in weight in weight 5 25-250 250-700 300 45.08 4.2 8.4 350 2.9 6.6 400 52"62 3.2 4.1 450 5 .93 2.3 2.4 10 500 60.50 3.5 1.2 550 3.8 0.6 600 59.95 2.2 0.4 650 3.2 0.2 i TABLE 14 Characterization of aluminate-Alumina Campsites Initial material: Bayerite (calcined at 550 ° C for 1 hour, then treated with 0.5% acetic acid for 15 min.)% binder: 25% by weight Curing temperature: variable Curing time: i hour Type of acid (concentration): HOAc (7%) Temperature area Average volume of surface pore curing for diameter < ° C) BET m2 / q BET cc / q M2 / pore grass (Va 1) μm: 300 274.1 0.1919 48.8 1. 0 350 303.2 0.2132 40 © 316.2 0.2241 97.4 1.53 450 298.4 0.2160 170.2 0.946 50 © 259.9 0.1909 213.2 0.72 i © 60 © 202.2 0.1419 203.8 0.30 Median Pore Temperature Density Curing density average skeletal bulk diameter (° C) pore (4V / A) g / mL q / mL 15 (Area) μm: μm 30 © 0.0039 0.0257 1.31 2.21 35 © 4 ©© 0. ©© 36 0.0160 1.27 2.50 450 ©. ©© 37 0.0113 1.15 2.66 © 500 0.0038 0.01 © 4 1.11 2.87 6 © 0 0.0044 0.0109 1.15 Temperature Porosity TGA% of TGA% of cure (%) loss of loss > 5 (° C) by weight in weight 14 -250 250-700 300 41.00 2.8 8.5 350 1.3 6.2 400 49.27 r ~) j 4.7 500 61.33 2.0 1.0 600 64.07 2.0 0.0 Example 17 A catalyst of 5/570/20% by weight of Cu0 / Mn02 / A1203-ag was prepared from colloidal A1203 according to that described in Example 11. The catalyst (0.933 g) was charged to a flow reactor "U-tube" was fixed on a gas cylinder with a synthetic mixture of 60 ppm C0, gt? ~ * 15 and 0.6% pentans in air. The CO / pentans / air mixture was passed over this catalyst with a flow rate of 80 mL / min Figure 3 provides a plot of the concentration of C0 and temperature versus time. that there is an induction period, after 2 © which the catalyst oxidizes C0 at room temperature. Experiment 18 A catalyst of 5/5/70/20% by weight of Cu0 / Ga203 / A1203-algomerant of colloidal A1203 was prepared in accordance with that described in Example 11. The catalyst 1007 g) charged in a "U tube" flow regulator fixed on a gas cylinder with a synthetic mixture of 81 ppm NO, 910 ppm CO in nitrogen. The mixture of NO / CO / Nitrogen was passed through this catalyst at a flow rate of 80 mL / min, Figure 4 presents a curve determined on these conditions. Experiment 19 Wastewater was collected through a 5-gallon aluminum oxide vessel that was calcined at 55 ° C for 2.5 hours and then washed with acid with a 0.5% solution of acetic acid. The water flow rate was about 1 ppm. The pH was 8.5. After 24 hours at the equivalent of approximately 1,440 gallons of contaminated water, the effluent was tested for the presence of uranium and the results appear 5 in Table 15.

TABLE 15 U308 TDS S04- Ma concentration of 50.5 15720 7609 .04 65.44 © influent (mg / L) concentration of 0.08 effluent (mg / L) EXAMPLE 20 A particle was prepared with the following composition in a manner similar to Example 13 for the purpose of testing its efficiency as regards the removal of chlorinated hydrocarbons from a water source: 60% of A12Q3 (alumina enhanced with acid), 5% CuO, 10% M0LECULITE (mr), 20% ds alumina binder (colloidal alumina) and 10% carbon. A partial water profile contained the following contaminants at 1 pH of 6.7; 1, 1-dichloroethene 7,100 ppb Acetone 40,000 Methylene chloride 90,000 i, 1-dichloroethanes 1,100 1, 1, 1-triclarstane 27,000 Trichlorethen 830 Toluene 1100 Tetrachlorastepo 1400 33 gallons of binder and catalyst system were placed in a cylinder of 55 gallons The spring water was pumped through the medium at a rate of 4 gpm. The effluent was analyzed to determine the presence of organic substances after the pumping of 40,320 and 70,000 gallons of spring water. The results appear in Table 16.

TABLE 16 Pollutant Effluent concentration% reduction at 4300 gallons (ppb) 1,1,1- 1280 95 triclaraethane triclaroethylene ND 100 5 tetrachloroethene 6 99.6 Pollutant Effluent concentration% reduction to 70,000 gallons (b) 1,1,1-3819 86 © trichloroethane triclarhene 10 99 tetrachloroethene 43 97 These results demonstrate that the levels of clarified hydrocarbons in the spring water were significantly reduced when the spring water was brought into contact with the binder and catalyst system. Example 21 Using the binder and catalyst system identical to that of Example 20, the removal of tetrachloroethenate from spring water was investigated. A 55-gallon cylinder was filled with 36 gallants from the binder and catalyst system. The contaminated water ftte combated from 3 wells through the medium at a combined flow rate of about 4 gpm. The pH of the subsoil water was 6.5. About 90,000 gallons of contaminated water were pumped through the binder and catalyst system. The results of the experiment appear in Table 17.

TABLE 17 Contaminant Concentration Concentration% of influent effluent reduction a. 43,100 © galanes (ppb) cis-1, 2-16 © 130 19 dicladateps 2-bu.tanana 48 ND 10 © tricioro dye 130 5 te raclsroetena 7900 Contaminant Effluent concentration% reduction to 72,679 gallons (ppb) cis-1, 2- 310 -93.7 © diclaraetena 2-butanone ND 100 trichloroethene ND 100 tetrae1orastsna 120 98.5 The increase in the concentration of cis-1,2-diclaraetene is the result of the degradation of tetrachlorosene and an indication of such degradation. Cis-i, 2-diclaraetepa is an intermediate product of the degradation of tetracloraetena, which is a hazardous waste material. In this application, several publications were referenced. The presentations of these publications in their totals are incorporated herein by reference in this application with the object of more fully describing the state of the art to which this invention pertains. It will be apparent to those skilled in the art that various modifications and variations may be made with respect to the present invention without departing from the scope or spirit of said invention. Other embodiments of the invention will be apparent to those skilled in the art from consideration of the specification and practice of the invention presented herein. The specification and the plos axes are considered only by way of illustration, and the true scope and spirit of the present invention is indicated in the following claims.

Claims (5)

1. A process for producing an adsorbent particle enhanced with acid comprising contacting a particle comprising a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous, which is produced by calcining at a temperature of particle from 300 ° C to 700 ° C, with an acid diluted for a sufficient time to increase the adsorbent properties of the particle, wherein the aluminum oxide treated with the resulting acid is subsequently not calcined, wherein the contact with acid is more than a surface wash, but less than an etching, where the acid concentration is less than or equal to 0.01 N.
2. 2. The method of claim 1, wherein the particle temperature is from 400 ° C to 700 ° C.
3. 3. The method of claim 1, wherein the acid comprises an aliphatic or arylcarboxylic acid.
4. 4. The process of claim 1, wherein the acid comprises acetic, nitric, sulfuric, hydrochloride, boric, formic or phosphoric acid, or mixtures thereof. 5. The process of claim 1, wherein the acid comprises acetic acid. 6. The process of claim 1, wherein the contact is by immersion or by submersion or of the particle in acid. 7. - The process of claim 6, wherein the contact is for at least 15 minutes. 8. The process of the 1, which also includes the step of rinsing the particles to remove excess acid. 9. The process of claim 1, further comprising the step of drying the particle. 10. The process of claim 1, wherein the strength of the diluted acid is equivalent to an aqueous acetic acid solution at less than or equal to 0.005 N. 11. The process of claim 1, wherein the strength of the acid diluted is equivalent to an aqueous acetic acid solution less than or equal to 0.001 N. 12. The process of claim 1, wherein the strength of the diluted acid is equivalent to an aqueous acetic acid solution of from 0.005 to 0.01. N. 13. The process of claim 1, wherein the strength of the diluted acid is equivalent to an aqueous acetic acid solution of from 0.001 to 0.01 N. 14. The process of claim 1, wherein the force of the dilute acid is equivalent to an aqueous acetic acid solution of from 0.005 to 0.01 N 15. The process of claim 1, wherein the calcined aluminum oxide is in the gamma, chi-ro or eta form. 16. - The process of claim 1, wherein the aluminum oxide before or after the acid treatment is not sintered. 17. The process of claim 1, wherein the particle consists essentially of aluminum oxide. 18. The process of claim 1, wherein the particle consists of aluminum oxide. 19. The process of claim 1, wherein the resulting acid-treated aluminum oxide is essentially microporous. 20. The process of claim 1, wherein the aluminum oxide is not a catalyst adsorbent or support. 21. The method of claim 1, wherein the particle, before being contacted with the acid, further comprises a second type of adsorbent and / or catalytic particle and further comprises a binder comprising a metal oxide, colloidal or a colloidal metalloid oxide. 22. The method of claim 21, wherein the binder is crosslinked to at least one of the particle types or to itself. 23. The method of claim 1, further comprising: (1) mixing the resultant particle of claim 1 with at least one other type of adsorbent and / or catalyst particle, a binder comprising oxide colloidal metal or colloidal metalloid oxide, and an acid; and (2) heating the mixture to a sufficient temperature for a sufficient time to cross-link the binder to at least one type of particle or likewise. 24.- The method of claim 23, where the heating step is from 25 ° C to 400 ° C. 25. The method of claim 23, wherein the heating step is from 70 ° C to 150 ° C. 26. A process for producing an adsorbent particle enhanced with acid, comprising contacting a particle comprising a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous, which is produced by calcination at a temperature of particle from 300 ° C to 700 ° C, with an acid diluted for a sufficient time to increase the adsorbent properties of particle 1, wherein the aluminum oxide treated with the resulting acid is subsequently not calcined, wherein the Touch with acid is more. that a wash Rup-rf -. ial but less than an engraving, where the concentration of acid is 0.1 N to 0.25 N. - 27 .- A process to produce an adsorbent particle enhanced with acid consisting essentially of putting in contact a particle comprising a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous, which is produced by calcining at a particle temperature of from 300 ° C to 700 ° C, with a dilute acid for a sufficient time to increase the adsorbent properties of the particle, where contact with acid is more than a surface wash, but less than a particle etch, where the acid concentration is less than or equal to 0.01 N. 28.- A process for producing an adsorptive particle enhanced with acid consisting essentially of contacting a particle comprising a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous that e produces by calcining at a particle temperature of from 300 ° C to 700 ° C, with a dilute acid for a sufficient time to increase the adsorbent properties of the particle, where contact with acid is more than a surface wash , but less than an engraving of the particle, where the concentration of the acid is from 0.1 N to 0.25 N. 29. The method of claim 27, wherein the particle temperature is from 400 ° C to 700 ° C. 30. A process for producing an adsorbent particle enhanced with acid comprising contacting a particle comprising a porous, non-ceramic oxide adsorbent particle with a dilute acid for a sufficient time to increase the adsorbing properties of the particle, where contact with acid is more than a surface wash but less than an etching of the particle, where the oxide adsorbent particle is not aluminum oxide, and where the acid adsorbent particle treated with the resulting acid it is not subsequently calcined, where the acid concentration is less than or equal to 0.01 N. 31. The process of claim 30, wherein the resulting acid-treated oxide is microporous. 32. The process of claim 30, wherein the strength of the diluted acid is equivalent to an aqueous acetic acid solution at less than or equal to 0.005 N. The process of claim 30, wherein the force of the dilute acid is equivalent to a solution of aqueous acetic acid unless or equal to 0.001 N. The process of claim 30, wherein the strength of the dilute acid is equivalent to an aqueous acetic acid solution of from 0.0005. at 0.01 N. 35.- The process of claim 30, wherein the strength of the diluted acid is equivalent to an aqueous acetic acid solution of from 0.001 to 0.01 N. 36.- The process of claim 30, wherein the strength of the dilute acid is equivalent to an aqueous acetic acid solution of from 0.005 to 0.01 N. 37.- The process of claim 30, wherein the oxide before or after the acid treatment is not sintered. 38.- The process of claim 30, wherein the oxide adsorbing particle is silicon dioxide, manganese oxide, copper oxide, vanadium pentoxide, zirconium oxide, iron oxide or titanium dioxide. 39.- The process of claim 30, wherein the adsorbent particle is zeolite. The method of claim 30, wherein the particle before being contacted with the acid further comprises a second type of adsorbent and / or catalytic particle, and further comprises a binder comprising a colloidal metal oxide or a metalloid oxide colloidal 41. The method of claim 40, wherein the binder is crosslinked to at least one of the particle types or to itself. The method of claim 30, further comprising, (1) mixing the resultant particle of claim 1, with at least one other type of adsorbent and / or catalytic particle, a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, and an acid; and (2) heating the mixture to a sufficient temperature for a sufficient time to crosslink the binder to at least one type of particle or to itself. 43. - A process for producing an acid-enhanced adsorbent particle comprising contacting a particle comprising a porous, non-ceramic oxide adsorbent particle with a dilute acid for a sufficient time to increase the adsorbent properties of the particle, wherein contact with acid is more than a surface wash but less than an etching of the particle, wherein the oxide adsorbing particle is not aluminum oxide, and wherein the oxide adsorbent particle treated with the resulting acid is subsequently not calcined, where the acid concentration is from 0.1 N to 0.25 N. 44.- The particle made by the process of claim 1. 45.- The particle made by the process of re-vindication 5. 46.- The particle made by the process of claim 26. 47.- The particle made by the process of claim 30. 48.- The particle made by the process of claim 38. 49.- The particle made by the process of claim 43. 50.- The particle of claim 44 or 46, wherein said particle passes the TCLP EPA tests for a particular contaminant. 51. The particle of claim 50, wherein the contaminant is lead. 52.- A process for reducing or eliminating the amount of contaminants in a liquid or gas stream comprising contacting the particle of claim 44 or 46 with the liquid or gas stream for a sufficient time to reduce the amount of or eliminate contamination of the liquid or gas stream. 53.- The process of claim 52, wherein the current is liquid. 54.- The process of claim 52, wherein the current is gas. 55.- The process of claim 52, wherein the contaminant is lead, phosphate, selenium or zinc. 56.- The process of claim 52, wherein the contaminant comprises an anion, an oxoanion, a cation, or a poly-oxoanion. 57.- A composition comprising the particle of aluminum oxide made by the process of the filing, n-dication 1 or 26. 58.- The composition of claim 57, which also comprises a second particle oxide adsorbent. . 59. The composition of claim 58, further comprising a cross-linked colloidal aluminum oxide binder. 60.- The composition of claim 57, further comprising silicon dioxide, manganese oxide, copper oxide, vanadium pentoxide, zirconium oxide, iron oxide or titanium dioxide. 61.- The composition of claim 57, further comprising a zeolite. 62. The composition of claim 57, further comprising copper oxide and manganese oxide, wherein said copper oxide and said manganese oxide have not been enhanced with acid. 63.- The composition of claim 62, wherein the composition comprises 50 to 90 parts by weight of the aluminum oxide enhanced with acid, 1 to 49 parts by weight of said copper oxide, and 1 to 49 parts by weight of said Manganese oxide. 64.- The composition of claim 63, wherein said copper oxide is CuO and said manganese oxide is MnC. 65.- The composition of -l ----_ eei-xindication 62, wherein said composition passes the TCLP EPA tests for trichlorethylene. 66.- The composition of claim 57, further comprising a noble metal. 67.- The composition of claim 57, which 1 8 it also comprises a catalyst particle. 68.- The composition of claim 57, further comprising an adsorbent particle. 69.- A process for reducing or eliminating the amount of an organic contaminant in a liquid or gas stream, comprising contacting the composition of the reviction 62 with the liquid or gas stream for a sufficient time to reduce the amount of or to eliminate the organic pollutant from the liquid or gaseous stream. 70.- The process of claim 69, wherein the organic pollutant is a chlorinated organic compound. 71.- The process of claim 69, where the organic pollutant is trichlorethylene. 72.- The process of claim 69, wherein said reduction or elimination is by a catalytic degradation process. 73.- A composition comprising (1) a particle made by the process comprising contacting a particle comprising a particle of aluminum oxide, calcined, porous, crystalline, non-ceramic, non-amorphous, which is produced by calcining to a particle temperature from 300 ° C to 700 ° C, with a dilute acid for a sufficient time to increase the adsorbent properties of the aluminum oxide particle and (2) copper oxide and (3) manganese oxide, where said copper oxide and said manganese oxide have not been enhanced with acid, wherein the concentration of the acid is less than or equal to 0.01 N. The composition of claim 73, wherein the particle temperature is 400 ° C to 700 ° C. 75.- A composition comprising (1) a particle made by the process comprising contacting a particle comprising a particle of calcined, porous, crystalline, non-ceramic, non-amorphous aluminum oxide fa, which is produced by a calcination at a particle temperature of from 300 ° C to 700 ° C, with a dilute acid, for a sufficient time to increase the adsorbent properties of the aluminum oxide particle and (2) copper oxide and (3) manganese oxide , wherein the copper oxide 15 and the manganese oxide have not been enhanced with acid, wherein the acid concentration is from 0.1 N to 0.25 N. 76.- An adsorbent and / or catalyst binder composition comprising the particle processed by the process of claim 1 or 26, and further comprising a second type of adsorbent and / or catalyst particle and a binder comprising colloidal metal oxide or metalloid oxide e colloidal. 77. The composition of claim 76, wherein the binder is crosslinked to at least one of the types of particles or to itself. 78. An adsorbent and / or catalytic binder composition comprising the particle made by the process of claim 30 or 43, further comprising a second type of catalyst particle and / or adsorbent and a binder comprising colloidal metal oxide or oxide colloidal metalloid. 79. The composition of claim 78, wherein the binder is crosslinked to at least one of the particle types or to itself. 80.- A method for encapsulating a contaminant within an adsorbent particle comprising heating the particle of claim 44 or 46 that has been adsorbed to a contaminant at a temperature sufficient to close the pores of the particle to be encapsulated in tway. -wine the contaminant inside the particle. 81. A method for regenerating the system of claim 44 or 46 that has been adsorbed to a contaminant, comprising thermally oxidizing said system or contacting said system with (1) a reagent wash comprising aqueous ammonia, a phosphine , a detergent or a mixture thereof; (2) an acid or base to cause a pH oscillation; (3) or a Lewis acid or base. 82. A method for regenerating the system of claim 47 or 49, which has adsorbed a contaminant, comprising thermally oxidizing said system or contacting said system with (1) a reactive wash comprising ammonia, aqueous, a phosphine, a detergent or a mixture thereof; (2) an acid or base to cause a pH oscillation; (3) or a Lewis acid or base. 83. A method for encapsulating a contaminant within an adsorbent particle that comprises heating the particle of claim 47 or 49 that has adsorbed a contaminant at a temperature sufficient to close the pores of the particle to thereby encapsulate the contaminant. inside the particle. 84.- The method of re-excitation 83, where the temperature is 450 ° C to 2,000 ° C. 85.- A method for producing an adsorbent and / or catalytic binder system that comprises (i) mixing components that comprise (a) ) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, (b) an oxide adsorbent and / or a catalyst particle, and (c) an acid, (ii) removing a sufficient amount of water from the mixture for crosslinking the binder with itself and / or with a component b to form an adsorbent and / or catalytic binder system, with the proviso that the binder is not a colloidal aluminum oxide or a colloidal silicon dioxide. 86.- The method of claim 85, wherein the removal is by heating or by using a drying agent. 87. The method of claim 85, wherein the removal is by heating. 88. The method of claim 85, wherein the binder comprises a colloidal metal oxide, wherein the metal is iron. 89.- The method of claim 85, wherein the binder is from 1% to 99.9% by weight of the mixture 90.- The method of claim 85, wherein the binder is from 10% to 35% by weight of mix. 91. The method of claim 85, wherein component b comprises at least two different types of adsorbent and / or catalytic oxide particles. 92. The method of claim 85, wherein component b comprises at least three different types of adsorbent and / or catalytic oxide particles. The method of claim 85, wherein the component b comprises a metal oxide particle 94. The method of claim 85, wherein the component b comprises a porous, non-ceramic metal oxide particle. The method of claim 85, wherein component b comprises a particle of an oxide of aluminum, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, magnesium, calcium, strontium, barium, boron, indium gallium, thallium, germanium, tin, lead, arsenic, antimony, or bismuth or a zeoiite or a mixture thereof. 96.- The method of claim 85, wherein component b comprises a mixture of at least two metal oxide particles having the same metal with stoichiometry and varying oxidation states. The method of claim 85, wherein component b comprises aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc oxide, zirconium or zeolite particles. The method of claim 85, wherein the component b further comprises a second type of adsorbent and / or catalytic particle of aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, dioxide of manganese, iron oxide, zinc oxide, zeolite, peat, activated carbon, zinc or tin particles. 99. The method of redy-i-nd ac i? N 85, wherein component b comprises a porous, crystalline, non-ceramic, non-amorphous particle of calcined aluminum oxide that is produced by calcining the precursor to an oxide of Calcined aluminum at a particle temperature of from 300 to 700 ° C. The method of claim 99, wherein the calcined aluminum oxide particle is in the gamma, chi-ro or eta form. 101. The method of claim 100, wherein the calcined aluminum oxide particle was pretreated with an acid activation treatment. 102. The method of claim 85, wherein the acid comprises an aliphatic or aryl carboxylic acid. 103. The method of claim 85, wherein the acid comprises acetic acid, benzoic acid, butyric acid, citric acid, fatty acids, lactic acid, maleic acid, malonic acid, oxalic acid, salicylic acid, stearic acid, succinic acid , tartaric acid, propionic acid, valeric acid, hexanoic acid, heptanoic acid, caprylic acid, pelargonic acid, capric acid, undecanoic acid, lauric acid, tridecanoic acid, myristic acid, pentadecanoic acid, palmitic acid, heptadecanoic acid, nonadecanoic acid , arachidic acid, heneicosanic acid, behenic acid, triosanoic acid, lignoceric acid, penta-cosanoic acid, ceric acid, heptasanoic acid, ontanic acid, noxia-co-sa-aO-i-CP acid, melic acid, acid phthalic, glutaric acid, adipic acid, azelaic acid, sebasic acid, cinnamic acid, acrylic acid, crotonic acid, linoleic acid or a zcla of them. 104. The method of claim 85, wherein the acid comprises nitric acid, sulfuric acid, hydrochloric acid, boric acid, acetic acid, formic acid, phosphoric acid or mixtures thereof. 105. The method of claim 85, wherein the acid is acetic acid or nitric acid. 5. The method of claim 85, wherein the concentration of the acid is from 0.15 N to 8.5 N. 107. The method of claim 85, wherein the removal is from 25 ° C to 400 ° C. 108. The method of claim 87, wherein the heating is from 70 ° C to 150 ° C. The method of claim 85, wherein during or after step (i), the mixture of step (i) is not heated above the crosslinking temperature of the colloidal metal oxide or the colloidal metalloid oxide. .- The method of claim 85, wherein after step (i), the mixture of step (i) is not heated to or above the calcination temperature of the colloidal metal oxide or the oxide colloidal metalloid. 111.- The method of claim 85, wherein ~ 3-? During or after step (i), the mixture of step (i) is not heated to or above the calcination temperature of the particle. 112. The method of claim 85, wherein during or after step (i), the mixture of step (i) 25 is not heated above 400 ° C. 113. - The adsorbent binder / catalyst system made by the process of claim 85. 114. An adsorbent and / or catalytic binder system comprising a binder that has been crosslinked with at least one type of adsorbent oxide particle and / or catalytic, wherein the binder is not a colloidal aluminum oxide or a colloidal silicon dioxide. 115. The system of claim 114, wherein the binder comprises a colloidal metal oxide or a colloidal metalloid oxide. 116.- The system of claim 114, wherein the binder comprises a colloidal iron oxide. 117. The system of claim 115, wherein the binder is from 1% to 99.9% by weight of the mixture. 118.- The system of claim 115, wherein the binder is from 10% to 35% by weight of the mixture. 119.- The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises at least two different types of adsorbent and / or catalyst oxide particles. 120.- The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises at least three different types of adsorbent and / or catalyst oxide particles. 121. The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises a metal oxide particle. 122. The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises a non-ceramic, porous metal oxide particle. 123.- The system of claim 115, wherein the oxide particle adsorbent and / or catalyst comprises particles of an oxide of aluminum, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, magnesium, calcium, strontium , barium, boron, gallium, indium, thallium, germanium, tin, lead, arsenic, antimony or bismuth, or a zeolite or a mixture thereof. 124. The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises a mixture of at least two metal oxide particles having the same metal with stoichiometry and varying oxidation states. The system of claim 115, wherein the adsorbent oxide and / or catalyst particle comprises aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, of zinc, zirconium oxide or zeolite particle. 126.- The system of claim 115, wherein the adsorbing and / or catalyzing oxide particle further comprises a second type of adsorbent particles and / or catalysts of aluminum oxide, titanium dioxide, copper oxide, pentoxide vanadium, silicon dioxide, manganese dioxide, iron oxide, zinc oxide, zeolite, activated carbon, zinc peat or tin particles. 127.- The system of claim 115, wherein the adsorbent and / or catalyst oxide particle comprises a porous, porous, non-ceramic, non-amorphous crystalline aluminum particle, which is produced by calcining the precursor to an aluminum oxide. calcined at a particle temperature of from 300 ° C to 700 ° C. 128.- The system of claim 127, wherein the particle temperature is from 400 ° C to 700 ° C. 129. The system of claim 127, wherein the particle of calcined aluminum oxide is in the gamma, chi-ro or eta form. 130.- The system of claim 129, wherein the calcined aluminum oxide particle is pretreated with an acid activation treatment. 131. The system of claim 115, wherein the particle comprises aluminum oxide, silicon dioxide and activated carbon. 132.- The system of claim 115, wherein the particle comprises aluminum oxide, silicon dioxide and activated carbon. 1 133. - The system of claim 115, wherein the adsorbent and / or catalyst oxide particle has not been treated by acid enhancement. 134. The system of claim 115, wherein the system is not a catalytic support. 135. A binder and adsorbent and / or catalytic system comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic oxide particle, wherein the binder is a colloidal alumina and the particle comprises an oxide of aluminum, copper oxide and manganese oxide. 136.- An adsorbent and / or catalyst and binder system comprising a binder that has been crosslinked with at least one type of adsorbent oxide and / or catalyst, wherein the binder is colloidal alumina and the particle comprises oxide of aluminum and carbon. 137. An adsorbent and / or catalytic binder system comprising a binder that has been crosslinked with at least one particle type of adsorbent and / or ca-talitic oxide, wherein the binder is -.- a-lúrain-a colloidal and the particle comprises copper oxide and manganese dioxide. 138.- An adsorbent and / or catalytic binder system comprising a binder that has been crosslinked with at least one type of adsorbent and / or ca-talitic oxide particle, wherein the binder is colloidal alumina and the particle comprises oxide of aluminum, copper oxide, manganese dioxide and carbon. 139.- An adsorbent and / or catalytic binder system comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic oxide particle, wherein the binder is colloidal silica and the particle comprises aluminum oxide , copper oxide and manganese dioxide. 140.- An adsorbent and / or catalytic and binder system comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic oxide particle, wherein the binder is colloidal alumina and the particle comprises oxide of aluminum, gallium oxide and copper oxide. 141. The system of claim 140, wherein the colloidal alumina is from 1 to 97% by weight, the aluminum oxide is from 1 to 97% by weight, the gallium oxide is from 1 to 97% by weight and the copper oxide is from 1 to 97% by weight. 142.- The system of claim 140, in which the alumina col e a. it is from 5 to 40% by weight, the aluminum oxide is from 40 to 97% by weight, the gallium oxide is from 1 to 10% by weight and the copper oxide is from 1 to 10% by weight. 143. An adsorbent and / or catalyst and binder system comprising a binder that has been cross-linked with at least one type of adsorbent and / or catalytic oxide particle wherein the binder is colloidal alumina and the particle comprises aluminum, and a mixed oxide comprising manganese dioxide, aluminum oxide and copper oxide. 144. The system of claim 143, wherein the colloidal alumina is from 1 to 98% by weight, the aluminum oxide is from 1 to 98% by weight and the mixed oxide is from 1 to 98% by weight. 145. The system of claim 143, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 10 to 40% by weight and the mixed oxide is from 20 to 70% by weight. 146.- An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked. at least one type of adsorbent and / or catalytic oxide particle, wherein the binder is colloidal alumina and the particle comprises aluminum oxide and copper oxide. 147.- The system of claim 146, wherein the colloidal alumina is from 1 to 98% by weight, the alumi-ni oxide is from 1 to 98% by weight and the copper oxide is from 1 to 98% by weight. weight. 148.- The system of claim 146, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight and the copper oxide is from 1 to 20% by weight. 149. An adsorbent binder system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent oxide particle and / or catalyst, wherein the binder is colloidal alumina and the particle comprises aluminum oxide, copper oxide and zirconium oxide. 150.- The system of claim 149, wherein the colloidal alumina is from 1 to 97% by weight, the aluminum oxide is from 1 to 97% by weight and the copper oxide is from 1 to 97% by weight, and the zirconium oxide is from 1 to 97% by weight. 151. The system of claim 149, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70 by weight and the copper oxide is from 10 to 20% by weight and Zirconium oxide is from 1 to 20% in. weight. 152.- An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic oxide particle wherein the binder is colloidal alumina and the particle comprises aluminum oxide and nitrate silver. 153. The system of claim 152, wherein the colloidal alumina is from 1 to 98% by weight, the aluminum oxide is from 1 to 98% by weight and the silver nitrate is from 1 to 98% by weight. 154. The system of claim 152, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight and the silver nitrate is from 1 to 20% by weight . 155. An adsorbent and / or catalyst binder system comprising a binder that has been cross-linked with at least one type of adsorbent and / or catalyst oxide particle, wherein the binder is colloidal alumina and the particle comprises aluminum, magnesium oxide, manganese dioxide and copper oxide. 156.- The system of claim 155, wherein the colloidal alumina is from 1 to 96% by weight, the aluminum oxide is from 1 to 96% by weight, the magnesium oxide is from 1 to 96% by weight the manganese dioxide is from 1 to 96% by weight and the copper oxide is from 1 to 96% by weight. 157. The system of claim 155, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, the magnesium oxide is from 1 to 30% by weight, the manganese dioxide is from 1 to 20% by weight and the copper oxide is from 1 to 20% by weight. 158. An adsorbent binder system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent and / or catalyst particle oxide, wherein the binder is colloidal alumina and the particle comprises aluminum oxide, copper oxide and a mixture of oxides comprising copper oxide, manganese dioxide and lithium hydroxide. 159.- The system of claim 158, wherein the colloidal alumina is from 1 to 97% by weight, the alumino-oxide is from 1 to 97% by weight, the copper oxide is from 1 to 97% in weight and the mixed oxide is from 1 to 97% by weight. 160.- The system of claim 158, wherein the colloidal alumina is from 10 to 40% by weight, the aluminum oxide is from 30 to 70% by weight, the copper oxide is from 1- to 20%. % by weight and the mixed oxide is from 1 to 20% by weight. 161. An adsorbent binder system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent oxide particle and / or. -catalyst, where the binder is colloidal alumina and the particle comprises an aluminum oxide and copper oxide. 162.- An adsorbent binder system and / or catalyst that "comprises a binder that has been crosslinked with at least one type of adsorbent oxide and / or catalyst, wherein the binder is colloidal alumina and the particle comprises oxide of aluminum and silver oxide 163. An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one particle type of adsorbent oxide and / or catalyst, wherein the binder system and The catalyst comprises colloidal alumina, aluminum oxide and one or more of the oxide particles of V205, W02, WO-, Ti02, Re.O7, As203, AS2O5, OSO4, Sb-Oj or mixtures thereof. An adsorbent and / or catalytic binder system comprising a binder that has been cross-linked with at least one type of adsorbent oxide and / or catalyst particles, wherein the catalyst and binder system comprises colloidal alumina, aluminum oxide and one or more of the oxide particles of V205, Zr? 2, Ti02, MgO, Th02, lanthanide oxides or mixtures thereof. 165.- An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalyst oxide particle, wherein the catalyst and binder system comprises colloidal alumina, aluminum oxide and one or more of the oxide particles CuO, ZnO, Ag20, AgO, CdO, SnO :, PbO, V205, Zr02, MgO, Th02, lanthanide oxides or mixtures thereof. 166.- An adsorbent and / or catalyst binder system comprising a binder that has been re-labeled with at least one type of adsorbent and / or catalyst oxide particle, wherein the catalyst system and binder comprises colloidal alumina, aluminum oxide, and one or more of the oxide particles of MnO2, Fe2, 03, Fe30, Ru203, OSO-i, CoO, Co203, Ru0, NiO or mixtures thereof. 167. An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalyst oxide particle, wherein the catalyst and binder system co-incinerates colloidal alumina, aluminum oxide, and one or more of the oxide particles of Fe203, Fe-.04, CoO, Co? -0.-. or mixtures thereof. 168.- An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic oxide particle, wherein the catalyst and binder system comprises colloidal alumina, aluminum oxide, and one or more of the zeolite, MgO, ThO: particles or mixtures thereof. 169.- An adsorbent and / or catalyst binder system comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalyst oxide particle, wherein the catalyst and binder system comprises colloidal alumina, aluminum, and one or more of the oxide particles of MgO, ThO; or mixtures thereof. 170. An adsorbent binder system and / or a catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalyst oxide particle, wherein the binder is colloidal alumina, and the particle comprises aluminum oxide, mixed oxides of manganese, copper oxide and carbon. 171. - The system of claim 170, further comprising lithium hydroxide. 172. An adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent and / or catalytic particle, wherein the particle comprises A1203, Ti02, CuO, Cu.O, SiO, Mn02, Mn203, Mn304 / ZnO, W02, W03, Re207, As203, As205, MgO, Th02, Ag20, AgO, CdO, Sn02, PbO, FeO, Fe203, Fe30, Ru203, RuO, Os04, Sb203, CoO, Co203, NiO or zeolite. 173. The system of claim 172 wherein the particle further comprises a second type of adsorbent particles and / or catalysts of an aluminum oxide, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, tungsten, rhenium , arsenic, magnesium, thorium, silver, cadmium, tin, lead, antimony, ruthenium, osmium, cobalt or nickel or zeolite, activated carbon, including coal and coconut carbon, peat, zinc or tin. 174. An adsorbent and / or catalytic binder system comprising a binder that has been cross-linked with at least one type of oxide particle adsorbent and / or catalyst, wherein the binder is colloidal alumina and the particle comprises oxide of aluminum, zinc oxide and copper oxide. 175. An adsorbent and / or catalyst binder system comprising a binder that has been cross-linked with at least one type of adsorbent and / or catalytic oxide particle, wherein the binder is colloidal alumina and the particle comprises aluminum and copper oxide. 176.- A method for reducing or eliminating the amount of a contaminant from a liquid or gas stream comprising contacting the system of claim 114 with the contaminant in the stream for a sufficient time to reduce or eliminate the amount of contaminant of the current. 177.- A method for reducing or eliminating the amount of a contaminant from a liquid stream or gas comprising contacting the system of claim 115 with the contaminant in the stream for a sufficient time to reduce or eliminate the amount of contaminant from the current. 178.- The method of claim 177, wherein the current is a liquid. 179. The method of claim 177, wherein the stream comprises water. - 180.- The pn - tnr-n p > Claim 177, wherein the stream is a gas. 181. The method of claim 177, wherein the stream comprises air or natural gas. 182. The method of claim 177, wherein the contaminant of the liquid stream or gas is reduced or eliminated by a catalytic reaction. 183. The method of claim 177, wherein the contaminant of the liquid stream or gas is reduced or eliminated by an adsorption reaction. 184. The method of claim 177, wherein the contaminant is acetone, ammonia, benzene, carbon monoxide, chlorine, hydrogen sulfide, trichlorethylene 1,4-dioxane, ethanol, ethylene, formaldehyde, hydrogen cyanide, sulfur hydrogen, methanol, methyl ethyl ketone, methylene chloride, nitrogen oxide, propylene, styrene, sulfur dioxide, toluene, vinyl chloride, arsenic, cadmium, chloro 1,2-dibromochloropropane, iron, lead, phosphate, radon, selenium or uranium . 185. The method of claim 177, wherein the contaminant is hydrogen sulfide. 186. The method of claim 177, wherein the contaminant comprises an anion, an oxoanion, a cation or a poly-oxoanion. 187. A method for catalyzing the decomposition of an organic compound comprising contacting the organic compound with the system of claim 114 for a time sufficient to catalyze the degradation of the organic compound. 188.- The method of claim 187, wherein the catalytic reaction is carried out at room temperature. 189. - The method of claim 187, wherein the organic compound is a chlorinated hydrocarbon. 190. The method of claim 187, wherein the organic compound is trichlorethylene. 191. A method for reducing or eliminating a contaminant from a gas stream by catalysis comprising contacting the system of claim 115 with a gaseous stream containing a contaminant comprising a nitrogen oxide, a sulfur oxide, a carbon monoxide, hydrogen sulfide or mixtures thereof for a sufficient time to reduce or eliminate the polluting amount. 192.- The method of claim 191, wherein the catalytic reaction is carried out at room temperature. - 193. A method for adsorbing an ion from a liquid or gaseous stream comprising contacting an adsorbent binder system and / or catalyst comprising a binder that has been crosslinked with at least one type of adsorbent oxide particle and / or catalytic converter with a flow of liquid or gas containing the ion. 194. The method of claim 193 wherein the ion comprises an anion, a cation, an oxo-anion, a poly-oxoanion or a mixture thereof. 195. A method for regenerating an adsorbent agglutinating system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent oxide particle and / or catalyst that has adsorbed a contaminant, which comprises thermally oxidizing said system or contacting said system with (1) a reagent wash comprising aqueous ammonia, a phosphine, a detergent or a mixture thereof; (2) an acid or base to cause a pH oscillation; (3) or a Lewis acid or base. 196. A method for producing an adsorbent binder system and / or catalyst comprising: (i) mixing components comprising: (a) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, (b) a first catalyst particle and / or adsorbent that does not crosslink with the binder, and (c) an acid, (ii) remove a sufficient amount of water from the mixture to crosslink the component itself, whereby the component b is trapped or held within of the crosslinked binder, to form an adsorbent binder system and / or catalyst. 197.- The method of claim 196, wherein the removal is by heating or by using a drying agent. 198.- The method of claim 197, wherein the removal is by heating. 199. - The method of claim 197, further comprising a second adsorbent and / or catalyst particle that is crosslinked with the binder, thereby crosslinking the binder and the second particle and thereby trapping and holding the first particle within the binder. crosslinked binder and the second particle. 200. The method of claim 197, wherein component b comprises an activated carbon particle. 201. The method of claim 197, wherein component b does not contain an oxide particle. 202. The method of claim 197, wherein the binder comprises colloidal alumina, colloidal silica or a mixture thereof. 203. The method of claim 97, wherein the binder is a colloidal alumina. 204. A composition for binding adsorbent and / or catalytic particles in order to produce an agglomerated particle comprising (a) a colloidal metal oxide or a colloidal metalloid oxide and (b) an acid, wherein the agglutinant is not an oxide of colloidal aluminum or silicon-colloidal dioxide. 205. The composition of claim 204, wherein the acid is acetic acid or nitric acid. 206.- The composition of claim 204, wherein the acid is nitric acid. 207. - A case for adsorbent and / or catalytic binder particles in order to produce agglomerated particles comprising (a) a colloidal metal oxide or a colloidal metalloid oxide and (b) an acid, wherein the binder is not colloidal aluminum oxide or colloidal silicon dioxide. 208.- The adsorbent and / or binder system made by the method of claim 197. 209.- The adsorbent and / or binder system made by the method of claim 199. 210.- A method for encapsulating a contaminant within a adsorbent particle comprising heating an adsorbent binder system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent and / or catalyst oxide particle, which has ad-sorbed a contaminant at a temperature sufficient to close the pores of the system to encapsulate the contaminant within the system in that way. 211. The method of claim 210, wherein the temperature is from 450 ° C to 2,000 ° C. 212. A method for modifying the physical content of an adsorbent binder system and / or catalyst comprising a binder that has been cross-linked with at least one type of adsorbent oxide particles and / or catalyst, wherein the binder comprises a colloidal metal oxide or a colloidal metalloid oxide comprising heating the system for a sufficient time to thereby modify the physical property. 213. The method of claim 212, wherein the heating is carried out to increase the surface area of the system. 214. The method of claim 213, wherein the physical property comprises a surface area, a pore area, a volume density, a skeletal density or porosity. 215. An adsorbent binder system and / or catalyst comprising: (a) a binder substituted or unsubstituted with a pendant ligand, and (b) a oxide catalyst particle and / or oxide adsorbent, substituted or unsubstituted, with a pending ligand, wherein at least one of the components (a) and (b) is a substituted pending ligand, and wherein the component (a) is crosslinked with the component (b). 216.- The system of claim 215, wherein the binder comprises a colloidal metal oxide or a colloidal metalloid oxide. 217.- The system of claim 216, wherein the binder comprises colloidal alumina, colloidal silica, colloidal metal oxide, wherein the metal is iron, or a mixture thereof. 218.- The system of claim 216, wherein the binder comprises colloidal alumina, colloidal silica, or a mixture thereof. 219. The system of claim 216, wherein the binder is colloidal alumina. 220.- The system of claim 216, wherein the oxide catalyst particle and / or oxide adsorbent is a substituted pending ligand. 221. The system of claim 216, wherein the binder is a substituted pending ligand. 222.- The system of claim 216, wherein the oxide adsorbing particle and / or oxide catalyst and the binder are both pending ligands substituted. 223. The system of claim 216, wherein the substitution of pending ligand on the binder and the catalyst particle and / or oxide adsorbent independently comprises at least one portion of slope liqing having a group end formed into a complex. 224. The system of claim 223, wherein the pending ligand portion further comprises a fixation end. 225. The system of claim 224, wherein the binding end comprises an aliphatic group, an aromatic group, a silyl group, a siloxy group or a combination thereof or an oligomer or polymer thereof . 226.- The system of claim 225, wherein the fixing end comprises an aliphatic or aromatic group ranging from 1 to 20 carbon atoms, branched or unbranched, substituted or unsubstituted. 227.- The system of claim 223, wherein the complex forming group comprises a group with a single pair of electrons. 228.- The system of claim 223, wherein the complex forming group comprises a hydroxyl group, an ether, a thiol, a thioether, an amine, a mono or disubstituted amine, a phosphine, a mono- or di-substituted phosphine, or a mixture thereof. 229.- The system of claim 223, wherein the complex forming group comprises an unsaturated organic moiety. 230.- The system of claim 229, wherein the unsaturated organic portion is cyclic, acyclic or aromatic. 231. The system of claim 230, wherein the unsaturated acyclic organic portion comprises an olefin, an allyl, a diene, a triene or a mixture thereof. 232. The system of claim 230, wherein the cyclic unsaturated organic moiety comprises a cyclopentadiene, cycloheptatriene, cyclooctadiene, cyclooctetraene or a mixture thereof. 233. The system of claim 230, wherein the aromatic unsaturated organic portion comprises benzene, naphthalene, anthracene, or mixtures thereof. 234. A method for using the system of claim 216, as a catalyst support system comprising agglutinating the system of claim 216 with a second catalyst particle. 235. The method of claim 234, wherein the second catalyst particle is a homogeneous catalyst. 236.- An adsorbent and / or catalyst anchored binder system comprising: (a) a substituted or unsubstituted binder, with a pending ligand, and (b) an oxide catalyst and / or an oxide adsorbent substituted or unsubstituted with a pending ligand, and (c) a metal complex, wherein at least one of components (a) and (b) is a substituted pending ligand, wherein component (a) is crosslinked with component (b), and wherein the complex metallic (c) is attached to component (a) and / or (b). 237. The system of claim 236, wherein the binder comprises a colloidal metal oxide or a colloidal metalloid oxide. 238. The system of claim 237, wherein the binder comprises colloidal alumina, colloidal silica, a colloidal metal oxide, wherein the metal is iron, or a mixture thereof. 239. The system of claim 237, wherein the binder comprises colloidal alumina, colloidal silica, or a mixture thereof. 240.- The system of claim 237, wherein the binder is colloidal alumina. 241. The system of claim 237, wherein the oxide adsorbing particle and / or oxide catalyst is a substituted pending ligand. 242.- The system of claim 237, wherein the binder is a substituted pending ligand. 243. The system of claim 237, wherein the oxide adsorbing particle and / or oxide catalyst and the binder are both substituted pending ligands. 244. The system of claim 237, wherein the substitution of pending ligand on the binder and the oxide and / or catalyst adsorbing particle independently comprises at least a portion of a pending ligand having a complex forming group end. 245. The system of claim 244, wherein the pending ligand portion further comprises an ether end. 246.- The system of claim 244, wherein the ether terminus comprises an aliphatic group, an aromatic group, a silyl group, a siloxy group or a combination thereof or an oligomer or polymer thereof. 247.- The system of claim 246, wherein the ether end comprises an aliphatic or aromatic group ranging from 1 to 20 carbon atoms, branched or unbranched, substituted or unsubstituted. 248.- The system of claim 244, wherein the complex forming group comprises a group with a single pair of electrons. 249.- The system of claim 244, wherein the complex forming group comprises a hydroxyl group, an ether, a thiol, a thioether, an amine, a mono- or disubstituted amine, a phosphine, a mono- or di-substituted phosphine or a mixture of them. 250.- The system of claim 244, wherein the complex forming group comprises an unsaturated organic portion. 251. The system of claim 250, wherein the unsaturated organic portion is cyclic, acyclic or aromatic. 252. The system of claim 251, wherein the unsaturated acyclic organic portion comprises an olefin, an allyl, a diene, a triene or mixture thereof. 253. The system of claim 251, wherein the unsaturated cyclic organic portion comprises a cyclo-pentadiene, cycloheptatriene, cyclooctadiene, cyclooctetraene or a mixture thereof. 254. The system of claim 251, wherein the unsaturated aromatic organic portion comprises benzene, naphthalene, anthracene or mixtures thereof. 255.- The system of claim 236, wherein the metal complex comprises a metal salt, a metal carbonyl complex, a metal phosphine complex, a metal amine complex, a metal olefin complex, a metal acetylene complex, a metal-polyane complex, a metal hydride complex, a metal halide complex or a mixture thereof. 256.- The system of claim 255, wherein the metal salt comprises a halide, a carbonate, an oxalate, a bicarbonate or a carboxylate such as the counter ion of lithium, sodium, potassium, - rubidi-o ---- -. -ce, sio, francium, magnesium, calcium, strontium, barium, radon, transition metals, lanthanide metals or metals actinides as the metal portion. 257.- The system of claim 255, wherein the metal carbonyl comprises a binary carbon mono-nu-nuclear or poly-nuclear of a transition metal. The system of claim 257, wherein the metal carbonyl comprises a mono-nuclear or poly-nuclear mixed carbonyl phosphine, a carbonyl phosphite, a carbonyl olefin, a carbonyl-acetylene, carbonyl-cyclopentadienyl complexes, carbonyl hydride, or a carbonyl halide of a transition metal. 259.- The system of claim 255, wherein the metal complex comprises a hydrogenation catalyst, an oxidation catalyst, a hydroformylation catalyst, a reduction catalyst, an isomerization catalyst, a polymerization catalyst, a carbonylation catalyst , a reforming catalyst, an olefin metathesis catalyst, a Fischer-Tropsch catalyst, a gasification catalyst, or a mixture thereof. 260.- A method for producing an adsorbent system and / or catalyst substituted with a pending ligand comprising: (i) mez-ßl-ßrr - components comprising: (a) a binder not substituted or substituted with a pending ligand that comprises a colloidal metal oxide or a colloidal metalloid oxide; (b) an oxide adsorbent particle and / or oxide catalyst unsubstituted or substituted with a pending ligand, and (c) an acid, wherein at least one of components (a) and (b) is a pending ligand substituted, (ii) removing a sufficient amount of water from the mixture to crosslink components (a) and (b) to form an adsorbent system and / or catalyst and binder substituted with pendant ligand. 261. The method of claim 260, further comprising (iii) ligating a metal complex on the system resulting from step (ii) to form the fixed catalyst system. 262. The method of claim 261, wherein the bond step (iii) comprises vapor deposition, incipient humidity, or non-aqueous impregnation. 263. The method of claim 261, further comprising before step (i), reacting an unsubstituted binder with a hydroxyl-reactive compound to produce a binder substituted with a pending ligand. 264. The method of claim 261, further comprising before step (i), reacting an oxide adsorbent particle and / or unsubstituted oxide catalyst, with a hydroxyl-reactive compound to produce an adsorbent particle. of oxide and / or oxide catalyst substituted with a pending ligand. 265. The method of claim 261, further comprising before step (i), reacting an unsubstituted binder an oxide adsorbent particle and / or unsubstituted oxide catalyst with a hydroxyl reactive compound to produce a binder substituted with pendant ligand and an oxide adsorbent particle and / or substituted oxide catalyst. 266.- The adsorbent binder system and / or fixed catalyst made by the process of claim 261. 267.- The method of claim 260, wherein the removal is by heating or by using a dried agent. 268. The method of claim 260, where the removal is by heating. 269.- The method of claim 260, wherein the binder comprises colloidal alumina, colloidal silica, a colloidal metal oxide wherein the metal is iron or a mixture thereof. 270. The method of claim 260, wherein the binder is colloidal alumina. 271. The method of claim 260, wherein the binder is from 1% to 99.9% by weight of the mixture. 272. The method of claim 260, wherein the binder is colloidal alumina and from 10% to 35% by weight of the mixture. 273. The method of claim 260, wherein component b comprises at least two different types of oxide and / or catalyst adsorbing particles. 274. The method according to claim 260, wherein the component b comprises at least three different types of oxide and / or catalyst adsorbing particles. 275. The method of claim 260, wherein component b comprises a metal oxide particle. 276. The method of claim 260, wherein component b comprises a porous metal non-ceramic oxide particle. 277.- The method of claim 260, wherein component b comprises a particle of an aluminum oxide, titanium, copper, vanadium, silica, manganese, iron, zinc, zirconium, magnesium, calcium, strontium, barium, boron, gallium, indium, thallium, germanium, tin, lead, arsenic, antimony or bismuth or zeolite or a mixture thereof. The method of claim 260, wherein component b comprises a mixture of at least two metal oxide particles having the same metal with varying stoichiometry and oxidation state. 279. The method of claim 260, wherein component b comprises aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc oxide, zirconium oxide or zeolite particles. 280.- The method of claim 279, wherein component b further comprises a second type of adsorbent particle and / or catalyst of aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc oxide , zeolite, activated carbon, peat, zinc or tin particles. 281. The method of claim 260, wherein component b comprises a particle of porous, porous, crystalline, non-ceramic, non-amorphous aluminum oxide that was produced by calcining the precursor to calcined aluminum oxide at a particle temperature. from 300 ° C to 700 ° C-. 282. The method of claim 281, wherein the calcined aluminum oxide particle is in the form of claim 281, wherein calcined aluminum was pretreated with an acid activation treatment. - 284. - The method of claim 260, wherein the acid comprises an aliphatic or aryl carboxylic acid. 285. The method of claim 260, wherein the acid comprises nitric acid, sulfuric acid, hydrochloric acid, boric acid, acetic acid, formic acid, phosphoric acid or mixtures thereof. 286. The method of claim 260, wherein the acid is acetic acid or nitric acid. 287. The method of claim 260, wherein the concentration of the acid is from 0.15 N to 8.
5. 5 N. 288. The method of claim 260, wherein the crosslinking temperature is from 25 ° C to 400 ° C. 289. The method of claim 260, wherein the crosslinking temperature is 70 ° C to 150 ° C and the aglu-finant is a colloidal alumina or a colloidal silica. 290. A method for producing an adsorbent system and / or catalyst and binder comprising: (i) mixing components comprising: (a) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, (b) a oxide and / or catalyst adsorbent particle, and (c) an acid, (ii) removing a sufficient quantity of water from the mixture to crosslink the binder with itself and / or the component b to form an adsorbent and / or catalyst and binder, and (iii) ) reacting the oxide adsorbent particle and / or oxide catalyst and the binder system of the stage (ii), with a compound reactive to the hydroxyl to form an oxide adsorbent system and / or oxide catalyst and substituted oligonucleotide with a pending ligand. 291. The method of claim 290, further comprising (iv) after step (iii) ligating a metal complex on the system resulting from step (iii) to form a fixed catalyst system. 292. The method of claim 291, wherein the binder is a substituted pending ligand. 293. The method of claim 290, wherein the oxide adsorbent and / or the catalyst particle is a substituted pendant ligand. 294. The method of claim 291, wherein the oxide adsorbent and / or oxide catalyst particle and the binder are both substituted pending ligands. 295. The method of claim 291, wherein the bonding of step (iv) comprises vapor deposition, incipient moisture, aqueous impregnation or non-aqueous impregnation. 296. The adsorbent system and / or catalyst and binder substituted with a pending ligand made by the process of reiv-indi-cation 290. 297. The method of claim 290, wherein the removal is by heating or using a drying agent. 298. The method of claim 290, wherein the removal is by heating. 299. - The method of claim 290, wherein the binder comprises colloidal alumina, colloidal silica, a colloidal metal oxide, wherein the metal is iron, or a mixture thereof. 300. The method of claim 290, wherein the binder is colloidal alumina. 301. The method of claim 290, wherein the binder is from 1% to 99.9% by weight of the mixture. 302. The method of claim 290, wherein 0 the binder is colloidal alumina and is from 10% to 35% by weight of the mixture. 303. The method of claim 290, wherein the component b comprises at least two different particle types of oxide adsorbents and / or catalysts. The method of claim 290, wherein the component b comprises at least three different types of oxide adsorbent particles and / or catalysts. 305. The method of claim 290, wherein component b comprises a metal oxide particle. SX- 306.- The method of claim 290, wherein the component b comprises a non-ceramic porous metal oxide particle. 307.- The method of claim 290, wherein the component b comprises a particle of an oxide of aluminum-5-n, titanium, copper, vanadium, silicon, manganese, iron, zinc, zirconium, magnesium, calcium, strontium, barium, boron, gallium, indium, thallium, germanium, tin, lead arsenic, antimony or bismuth or a zeolite or a mixture thereof. 308. The method of claim 290, wherein the component b comprises a mixture of at least two metal oxide particles having the same metal with stoichiometry and varying oxidation states. 309.- The method of claim 290, wherein component b comprises aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, manganese dioxide, iron oxide, zinc oxide, zirconium oxide or zeolite particles. 310. The method of claim 309, wherein the component b further comprises a second type of particles adsorbent and / or catalyst of aluminum oxide, titanium dioxide, copper oxide, vanadium pentoxide, silicon dioxide, Manganese dioxide, iron oxide, zinc oxide, zeolite, activated carbon, peat, zinc or tin particles. 311. The method of claim 290, wherein component b comprises a particle of porous, porous, crystalline, non-ceramic, non-amorphous aluminum oxide, which was produced by calcining the precursor to calcined aluminum oxide at a temperature of particle from 300 ° C to 700 ° C. 312. The method of claim 311, wherein the calcined aluminum oxide particle is in the gamma, chir-ro, or eta form. 313. The method of claim 312, wherein the calcined aluminum oxide particle is pretreated with an acid activation treatment. 314. The method of claim 290, wherein the acid comprises an aliphatic or aryl carboxylic acid. 315. The method of claim 290, wherein the acid comprises nitric acid, sulfuric acid, hydrochloric acid, boric acid, acetic acid, formic acid, phosphoric acid or mixtures thereof. 316. The method of claim 290, wherein the acid is acetic acid or nitric acid. 317. The method of claim 290, wherein the concentration of the acid is 0.15N to 8.5N. 318. The method of claim 290, wherein the crosslinking temperature is from 25 ° C to 400 ° C. 319.- The method of claim 290, wherein the crosslinking temperature is from 70 ° C to 150 ° C; and the aglu-finante is a colloidal alumina or a colloidal silica. 320.- The anchored adsorbent system and / or catalyst and binder made by the process of claim 291. 321. An anchored adsorbent system and / or catalyst and binder, comprising: (a) a binder, and (b) a oxide adsorbent particle and / or oxide catalyst, and (c) a metal complex, wherein component (a) is crosslinked with component (b), and wherein the metal complex (c) is directly attached to the component ( a) and / or (b). 322.- A method for producing an adsorbent and / or catalyst and binder system comprising: (i) mixing components comprising: (a) a binder comprising a colloidal metal oxide or a colloidal metalloid oxide, (b) an adsorbent particle of oxide and / or catalyst, and (c) an acid, (ii) removing a sufficient amount of water from the mixture to crosslink the binder with itself and / or with component (b) to form an adsorbent and / or catalyst system and binder, and (iii) ligating a metal complex directly onto the system resulting from step (ii) to form a fixed catalyst system. 323. The particle made by the method of claim 322.