PROCESS FOR REMOVING METALS FROM ALUMINOSILICATE MATERIALS

Abstract: Disclosed is a process for removing accumulated metals, particularly vanadium and nickel, from particulate aluminosi­ licate materials and aluminosilicate materials that are obtained by the process. The process may advantageously be used to remove accumulated metals from spent alumino­ silicate contact materials used in selective vaporization processes of the type described in United States Patent 4,263,128. The process of this invention yields materials suitable for effective recycling to a selective vaporization unit or for ecologically-acceptable disposal, as well as, optionally, recovery of metals in saleable form.

Description: PROCESS FOR REMOVING METALS FROM ALUMINOSILICATE MATERIALS This invention relates to a process for removing accumulated metals, particularly vanadium and nickel, from particulate aluminosilicate materials and to the aluminosilicate materials obtained by the process. The process may advantageously be used to remove accumulated metals from spent aluminosilicate contact materials used in selective vaporization processes of the type described in United States Patent 4,263,128. The process of this invention yields materials suitable for effective recycling to a selective vaporization unit or for ecologicallyacceptable disposal, as well as, optionally, recovery of metals in saleable form. United States Patent 4,263,128 discloses a selective vaporization process which reduces the Conradson Carbon and metals content of heavy hydrocarbon feedstocks destined for catalytic cracking or oTher hydrocarbon conversion processes. Broadly, the selective vaporization system comprises a contactor, a burner/regenerator and an inventory of circulating, fluidizable, essentially inert contact material. Rapid application of heat, generated within the burner and carried by the circulating inventory of inert contact material, selectively vaporizes most of the hydrocarbon components of the feed. During this selective vaporization, non-vaporized components of the.feedstock, including metals, are deposited on the contact material. The spent contact material, bearing deposits of Conradson Carbon and metal components of the hydrocarbon feedstock, is then introduced into a burner/regenerator where combustible portions of the deposited materials are oxidized. The contact material is then recycled to the contactor. Because contaminating metal deposits are not concurrently removed in the regenerator, the quantity of metal contaminants on a particle of contact material typically increases during each of its cycles through the selective vaporization unit. The accumulated metals that are deposited on the contact material during selective vaporization can have undesirable effects upon the properties of The material. For example, excessive quantities of vanadium on the contact material can cause the material to agglomerate in the selective vaporization unit. In practice, in selective vaporization processes, the metals content of the selective vaporization contact material has been held at acceptable levels by with drawing a portion of that material on a continuous or semi-continuous basis and replacing it with fresh contact material. In order to maintain the overall efficiency of selective vaporization processes, it would be desirable to remove the metals from the contact material That is withdrawn from the selective vaporization unit and then to recycle the metalsdepleted contact material back to the selective vaporization unit. In addition, it would be desirable to recover the metals removed from the contact material in saleable form. The '128 patent discloses that the preferred contact material for selective vaporization comprises calcined kaolin clay, an aluminosilicate material. Metals which deposit and build up on the surface of such contact material during The selective vaporization step tend to combine chemically with The material during The combustion step. Separation of those metals from the contact material is difficult, often leading to degradation of The material itself during the metals-removal process. Metals extraction processes which lead to co-extraction of alumina or silica are not useful in treating aluminosilicate materials, such as calcined kaolin clay, because such processes adversely affect the integrity of the materials. For example, approximately 90% vanadium recovery could be obtained by boiling the particles in 10% caustic soda but The particles are degraded and become essentially useless as a contact material thereafter. Decreasing the severity by lowering the temperature or concentration of caustic decreases the vanadium recovery significantly but the amounts of alumina and silica extracted are sufficient to interfere with subsequent liquid ion extraction processes for recovering the metal. As another example, strong mineral acids will extract nickel and vanadium from aluminosilicate contact materials, such as microspheres of calcined kaolin clay, but alumina is co-extracted, leading to a reduction in the amount of material available for recycling, an undesirable increase in the surface area of the microspheres and decreased attrition resistance depending upon the amount of alumina extracted. The present invention is directed to a process for the effective reactivation of spent metal-containing aluminosilicate contact materials used in selective vaporization processes and the recovery of accumulated metals, particularly vanadium and nickel, from those materials. In a preferred process of the invention, the vanadium and nickel are recovered in saleable form. An advantage of the process is that usually the integrity of the treated aluminosilicate contact material is not destroyed or unduly degraded physically or chemically, so that the product may be recycled to the selective vaporization unit substantially free of contaminating metals. Alternatively, the treated contact material may be disposed of in an ecologically acceptable manner. Broadly, the process of the present invention comprises: (a) treating an aluminosilicate material contaminated with nickel and vanadium values with alkali chloride selected from lithium chloride, potassium chloride, and mixtures Thereof, in the substantial absence of moisture, at a temperature above the melting point of the chloride or chlorides, under conditions effective to convert the nickel and vanadium in the aluminosilicate material to soluble form and (b) removing soluble nickel and vanadium values from the treated aluminosilicate material. In a first embodiment of the invention, the alkali chloride is K or Li chloride, or a mixture of potassium chloride and lithium chloride. In this first embodiment, the nickel and vanadium values may be removed from the aluminosilicate material that is obtained in step (a) in a multi-stage process comprising: (1) contacting the aluminosilicate material with an aqueous liquid to obtain an aqueous extract of nickel chloride, (2) separating the aluminosilicate material from the aqueous extract of nickel chloride obtained in step (1), and (3) treating the aluminosilicate material that is obtained in step (2) to remove the vanadium values Therefrom. Preferably, step (3) is conducted by contacting the aluminosilicate material with an aqueous solution of a base, such as an alkali carbonate, to obtain an aqueous extract comprising vanadium values; or by contacting that material with an aqueous solution of hydrochloric acid, sulfuric acid, or mixtures Thereof. In a second embodiment of the invention, the alkali chloride is selected from potassium chloride, lithium chloride and mixtures thereof. In this embodiment, the nickel and vanadium values may be removed from the aluminosilicate material that is obtained in step (a) in a single stage process that comprises contacting that material with an aqueous solution of hydrochloric acid, sulfuric acid, or mixtures thereof, to extract the nickel and vanadium values from the aluminosilicate material. As mentioned above, the aluminosilicate material obtained by the process of the invention is suitable for use in a-selective vaporization process of the type described in United States Patent 4,263,128. That material, after being treated by the process of this invention, is.characterized by an alumina to silica molar ratio of about 1:2, a mullite content of about 10% by weight, an alkali metal oxide content of at least about 1% by weight, the alkali metal oxide being present as an oxidic material selected from lithium aluminosilicate, potassium aluminosilicate and admixtures thereof, depending upon which alkali metal chloride is used in the roast. Tridymite and cristobalite may also be present. These phases may be determined by x-ray diffraction. Figure 1 is a schematic outline of a first preferred embodiment of the process of This invention. Figure 2 is a schematic outline of another preferred embodiment of the process of this invention. Referring to Figures 1 and 2, there are depicted two preferred embodiments of this invention. In each embodiment, the metal - containing spent aluminosilicate contact material preferably was obtained from the charge of contact material utilized in a selective vaporization process of the type described in United States Patent 4,263,128. Preferably, the contact material had been withdrawn from the burner/regenerator of a selective vaporization unit. Excess carbon borne by the contact material should be removed by calcining. Contact materials bearing carbon in an amount of less than about 0.04% by weight may be treated without precalcining but at a higher carbon loading, the contact material should normally be precalcined. The preferred aluminosilicate contact material that may be treated by the process of the present invention comprises metal- - contaminated microspheres of calcined kaolin clay obtained from a selective vaporization process of the type described in United States Patent 4,263,128. The microspheres of calcined kaolin clay that are utilized in such processes may be made, for example, by a process of the type described in United States Patent 3,663,165 (Example 1, column 6, lines 44-57). The chemical composition of the calcined kaolin clay microspheres that are preferably used in such selective vaporization processes generally corresponds to that of a dehydrated kaolin clay. Typically, the calcined microspheres analyze about 51 to 53% by weight SiO2, 41 to 45% by weight A1203 and O to 1% by weight H20; the balance including minor amounts of indigenous impurities, notably iron, titanium and alkaline earth metals. Iron content (expressed as Fe203) and titanium content (expressed as Tiro2) are, usually, respectively, 0.4 to 2.5% by weight, and up to 2% by weight. The term "kaolin clay" as used herein embraces clays, the predominating mineral constituent of which is kaolinite, halloysite, nacrite, dickite, anauxite and mixtures Thereof. Figure 1 depicts a first preferred embodiment of the invention in which the nickel and vanadium values are removed from the aluminosilicate material separately. In the first stage of this embodiment, the aluminosilicate material is contacted with potassium chloride, lithium chloride, or mixtures thereof, and is thermally treated in the substantial absence of moisture. The thermal treatment may be conducted in air, nitrogen or another inert dry gas. The amount of moisture present in the gas should be less Than about 1%, preferably less than about 0.5%, still more preferably less than about 0.1% of the weight of the contact material being treated. During the thermal treatment, the nickel values in the aluminosilicate material are converted into water soluble form. The heat treatment is preferably conducted at a temperature ranging -from about 1450 to about 220o0F, most preferably from about 1750 to about 1950 F, for a time period from about 5 to about 60 minutes, preferably from about 10 to about 30 minutes. In the embodiment of Figure 1, after the first stage alkali chloride/thermal treatment, the resulting mixture is contacted with an aqueous liquid under conditions sufficient to extract nickel values from the aluminosilicate material. For example, the mixture may be contacted with an aqueous liquid at 50-600C for 15 minutes. The resulting solid and liquid phases are separated, preferably by filtration and washing. The resulting aqueous phase includes extracted nickel, chlorine ions and alkali metal ions. The presence of iron suppresses the solubility of vanadium, and therefore if desired, iron may be added to the aqueous liquid if The iron content of the contact material is not sufficient to prevent co-extraction of vanadium and nickel. The exact nature of the aqueous liquid used for extraction of the nickel chloride is not critical, as long. as contaminants contained therein do not interfere with dissolution of the nickel chloride, removal of vanadium and recovery of lithium, if a mixture of chlorides is used in the thermal treatment. The slightly acidic aqueous solution (e.g., a pH of about 1.5-3) that results from the aqueous liquid extraction step may be treated by a number of techniques to remove the nickel values Therefrom. Thus it may be treated (e.g. neutralized to a pH of about 8.0), suitably with potassium hydroxide, lithium hydroxide, potassium carbonate, and/or lithium carbonate, to precipitate hydrated nickel oxide. or nickel hydroxide or carbonate, which is then separated from the aqueous phase. The pH values of the solutions and slurries referred to herein are the pH values that those solutions and slurries would have at 250C. The precipitate that is separated in the process described in the preceding paragraph may then be heated to obtain nickel oxide. The aqueous phase from which the precipitate is separated contains alkali chloride and may be recycled for use in the alkali chloride/thermal treatment step described above. Nickel values may be recovered from the solution that results from the aqueous liquid extraction step by a technique other than the precipitation technique described above. For example, the nickel ions may be removed by liquid ion exchange or electrolysis. Iron and vanadium may be co-extracted along with nickel from the aluminosilicate material during the aqueous liquid extraction step described above. We have discovered that the amount of vanadium that is extracted during the aqueous liquid extraction step may be minimized by maintaining the iron content of the aqueous phase at a certain minimum level. In particular, the-extraction of vanadium may be minimized by maintaining the iron content of the aqueous phase at a level of at least about 50 ppm by weight Foe203, preferably at least about 150 ppm by weight Fe2O3. The iron content may be maintained at these levels by utilizing high iron content aluminosilicate material (e.g., metal-contaminated calcined kaolin clay containing about 1.5 to 2.5% by weight Fe2O3), by adding iron (e.g., as ferric oxide) to the aluminosilicate material before the thermal treatment step, < or, preferably, by adding iron (e.g., as ferric chloride) to the aqueous phase during the aqueous liquid extraction step. Generally, if the pH of the aqueous liquid extract solution is greater than about 2.5, then in order to have a suitable iron content in the aqueous phase, ferric chloride may be added to reduce the pH to, preferably about 1.7 to about 2.3, most preferably about 2.3. It is preferred to add the iron as ferric chloride because it causes a comparatively small increase in the ferric oxide content of the treated contact material, with most of the iron remaining in the aqueous phase during the aqueous liquid extraction step. When the alkali chloride that is used in the first embodiment of the invention is a mixture of potassium chloride and lithium chloride, the weight ratio of KCl to LiCl is most preferably from about 1:1 to about 2:1, preferably from about 1.5:1 to about - 1.7:1. In order to minimize extraction of vanadium in the aqueous liquid extraction step for removal of nickel, the weight ratio of KC1 to LiCl is best at least about 1.2:1. The total weight of the alkali metal chlorides should preferably be at least about 10%, more preferably, about 15% of the weight of the contact material to be treated. Far larger amounts of the chlorides may be used if desired. In addition, the solids to aqueous liquid weight ratio in the aqueous liquid extraction should preferably be from about 1.5:1 to about 2:1. As depicted in Figure 1, the solid aluminosilicate material resulting from the aqueous liquid extraction step is subjected to an alkali extraction treatment to remove vanadium values from that material. In that treatment, the aluminosilicate material is contacted with an aqueous solution of an alkali selected from alkali hydroxide, alkali carbonate, and mixtures thereof. Preferably, in the alkali extraction step, the aluminosilicate material is contacted with an alkali carbonate solution, such as sodium carbonate or most preferably potassium carbonate, to extract the vanadium as soluble alkali vanadate. Preferably, the contact takes place at or near the boiling point of the alkali carbonate solution. The alkali carbonate solution used typically contains at least about 1.5% by weight alkali carbonate. When lithium chloride or a mixture of lithium chloride and potassium chloride is used in the thermal treatment step, alkali acetate, a mixture of alkali carbonate and alkali acetate, or a mixture of alkali acetate and alkali hydroxide, at a temperature above the melting point of the alkali acetate, is preferably utilized as the alkali in the alkali extraction step, so that a substantial quantity of the lithium in the aluminosilicate material may be extracted therefrom. Substantial quantities of the lithium extracted from the aluminosilicate material may be recovered without adversely affecting the extraction of vanadium values from the material. After alkali extraction, the solid and liquid phases are separated, e.g., by filtration and washing. The metals-depleted aluminosilicate material may then be dried and recycled for use in a selective vaporization unit. In those embodiments of the invention in which lithium chloride is utilized in the alkali chloride/thermal treatment step described above, a substantial quantity of lithium, a relatively expensive material, becomes deposited on the aluminosilicate material. As described above, a substantial quantity of the lithium may be extracted from the aluminosilicate material by conducting the alkali extraction step in the presence of alkali acetate under a set of specified conditions. Alternatively, a substantial quantity of the lithium may be removed from the aluminosilicate material by contacting the material with alkali acetate material after the alkali extraction step. For example, the lithium could be extracted from the aluminosilicate material by a variation of the process for extracting lithium from B-spodumene described in United States Patent 2,924,507, using potassium acetate in place of sodium acetate. Specifically, in such a variation, the aluminosilicate material is contacted with molten potassium acetate at a temperature of about 3240C and at ambient pressure, to obtain a molten material containing lithium acetate. The resulting lithium acetate containing material may be dissolved into an aqueous solution into which potassium carbonate is introduced to precipitate the lithium as lithium carbonate. After recovery of the solid lithium carbonate, the remaining potassium acetate solution may be utilized or disposed of in an appropriate way. The aqueous vanadate-containing solution That is obtained from the alkali extraction step preferably is treated for recovery of vanadium. Vanadium recovery may be carried out by a. liquid ion exchange technique using a quaternary amine in the carbonate, sulfate or chloride form. In such a technique, the aqueous vanadate-containing solution is contacted with the quaternary amine to extract the vanadate ions from the aqueous phase to the organic phase (i.e., the quaternary amine phase). Quaternary amines that are useful in the liquid ion exchange step of the process are described in Australian Patent Specification 245,763. Such a material is commercially available, in the chloride form,. as Aliquat 336 Liquid Ion Exchange Reagent&commat;. In the most preferred embodiment of the invention, the quaternary amine that is utilized in the ion exchange step is Aliquat 336 Liquid Ion Exchange Reagents that has been converted to the carbonate form by treatment with alkali carbonate. Alternatively, the quaternary amine may be used in sulfate form, which is obtained by treating the quaternary amine with sulfuric acid. It is preferred to use the quaternary amine in its carbonate form, because the aqeuous phase resulting from the liquid ion exchange step may then be utilized, in whole or in part, as a feed stream to the alkali extraction step that was described above without introducing chloride ions into that step. The organic phase from the liquid ion exchange step may be stripped with an ammoniacal solution, such as an ammonia-and ammonium chloride-containing solution, for a time sufficient to precipitate substantial quantities of the vanadium as ammonium metavanadate. If ammonium ions are provided in the form of an aqueous alkaline solution other than an ammonia and ammonium chloride-containing solution, e.g., an aqueous solution comprising ammonium carbonate and ammonium sulfate, the ammonium metavanadate is precipitated by evaporation of ammonia. Typically, the organic phase is contacted with the ammonia and ammonium chloride-containing solution for a period from about 1 to about 5 minutes, at a temperature from ambient temperature to about 500C. Vanadium is recovered as solid ammonium metavanadate from the ammoniacal stripping step. The ammonium metavanadate may then be thermally decomposed to vanadium pentoxide. The organic phase from the ammonium stripping step may be reconverted to the carbonate form then recycled to the liquid ion exchange step. The aqueous raffinate resulting from the liquid ion exchange step is preferably recycled to the alkali extraction step. If the quaternary amine usea in the liquid ion exchange step was in the sulfate form, t is preferred to remove a portion of the sulfate from the aqueous raffinate before recycling it to the alkali extraction step to maintain the sulfate concentration.below about 60 g/l. This may be accomplished by precipitating the sulfate as barium sulfate by adding an appropriate amount of barium carbonate to the aqueous raffinate. An advantage of the first embodiment of the invention described hereinabove is that nickel values can be extracted from the aluminosilicate material into an aqueous phase with no significant co-extraction of vanadium and then vanadium values are extracted from the aluminosilicate material in a separate step. This sequential separation of nickel and vanadium can be less complicated and expensive than when it is required to separate vanadium and nickel values which have been co-extracted from the alumino-silicate material. Another advantage of the first embodiment of the invention is that it does not result in large amounts of liquid wastes. In particular, as described above, the liquid streams obtained in the first embodiment may be effectively. recycled, with resultant savings in material and disposal costs. In a different vanadium recovery procedure, after the nickel has been removed by extraction with water, the vanadium is removed by extraction with acid. Acid extraction may be accomplished by contacting the solid aluminosilicate material obtained from the water extraction step with an aqueous acid solution comprising sulfuric acid, hydrochloric acid or mixtures thereof. The resulting liquid phase, which contains vanadium values, may then be treated by liquid ion exchange processes to recover the vanadium therefrom, as described in United States Patent 4,126,663. The solid phase resulting from the acid extraction step may be treated as in the first embodiment described above. In a second embodiment of the-invention, shown in Figure 2, the aluminosilicate material is contacted with potassium chloride, lithium chloride, or mixtures thereof, and heated under the same conditions described above in connection with the description of the alkali chloride/thermal treatment of the first embodiment of the invention. Thereafter, the nickel and vanadium values in the aluminosilicate material are co-extracted therefrom by contacting that material with an aqueous solution of hydrochloric acid or sulfuric acid, or mixtures thereof. Preferably, the contact occurs at a solids:liquid ratio from about 1:1 to about 1:2 and at an elevated temperature (e.g., boiling) for from about 1 to about 3 hours in a closed vessel. The resulting solid and liquid phases are separated by filtration or centrifugation and then washed. The aluminosilicate solids may then be recycled. The aqueous phase, which contains extracted nickel and vanadium values, may be treated by liquid ion exchange for vanadium recovery. Alternatively, the aqueous phase may be neutralized and then treated by conventional methods for metals recovery or disposed of in any ecologically-acceptable manner. When the acid reactant used in the extraction is hydrochloric acid, it is preferably used as a solution containing from about 10 to about 36% HCl by weight, preferably from about 15 to about 20% by weight and the solids:liquid ratio should be about 1:1. The preferred reaction conditions include heating at or near The boiling point for from about 30 minutes to about 3 hours. When the acid reactant is sulfuric acid, it is preferably used as a solution having a concentration of up to about 70% by weight, preferably about a 40-70% solution, more preferably about a 45-60% solution and the solids:liquid ratio should be about 1:1. The preferred reaction conditions include heating at or near the boiling point for at least about 30 minutes, preferably from about 45 minutes to about 2 hours. EXAMPLES The following Examples demonstrate various alternative embodiments of the process of the present invention, as well as the results of optimization studies carried out for each embodiment. The Examples are set forth for the purpose of illustration only and are not to be construed as limiting the scope of the invention in any manner In each Example, the following procedure was employed. Samples of spent aluminosilicate contact material microspheres of calcined kaolin clay as described above were obtained from the burners of selective vaporization units. The mullite content of these samples had increased to about 10%. In each Example, The spent aluminosilicate contact material was mixed with an alkali chloride solution, oven-dried slowly to about 2200C and introduced into a substantially closed, electrically heated, Lindberg crucible furnace (Model F-95454). Thermal treatment was conducted in the presence of oxygen. Since the heating occurred in static air in a closed crucible, the moisture driven off during heating was not free to re-enter the crucible. In Examples of the first embodiment, the thermal reaction pnihst was stirred and extracted with water (solids/liquid weight ratio = 1:1.6) at a temperature of about 50"C to about 600c for abet 30 min to extract nickel chloride, filtered, washed and dried. In some Examples, the filter cake (solid phase) was further treated by extracting it with water and then by refluxing it with a 1.5 to 2% by weight alkali carbonate solution (solids/liquid weight ratio = 1:2) for about 30 min to extract vanadium as soluble alkali vanadate. The resulting solid and liquid phases were separated and the metals-depleted contact material, which was suitable for recycling to a selective vaporization unit, was analyzed for its metals content. Extraction of vanadate ions from the carbonate extracts was effected by shake-out tests in separatory funnels using Aliquat 336 Liquid Ion Exchange Reagent9. The filter washes from-both the alkali chloride treatment/water extraction and alkali carbonate extraction were analyzed for their metals content. Example 1 - Potassium Chloride Reaction/Potassium Carbonate Extraction The procedure set forth above was employed using a 25% KC1 solution in the alkali chloride treatment step, in a proportion of 32% by weight of KCl based upon the dry weight of KNV/J spent aluminosilicate contact material, and a 2% K2CO3 solution for the alkali carbonate extraction. The KNV/J material had a vanadium and nickel content of 1.26% V and 0.22% Ni, by weight, as well as 0.02% C, 0.044% S, 0.47% Na2O, 54% SiO2, 2.43% Fe2O3 and 42% Al203. The resulting filter washes were analyzed for content of V, Ni and Na2O. Extraction efficiencies Mere calculated from final contact material filter cake analyses; the small differences between these extractions and those based on filter analyses reflected volatilization losses. The results of these analyses are shown in Tables I and II. TABLE I KCl REACTION/K2CO3 EXTRACTION % Extracted Based on Filter Cakes Reaction Conditions V Ni V+Ni Na2O K2O in Filter Temp/Time F/Mins % % % % Cake (%) 1800/15 54 59 55 53 3.28 1800/30 55 64 56 55 4.13 1850/15 55 64 56 57 3.75 1850/30 58 68 59 57 4.49 1900/15 56 68 58 57 4.10 1900/30 54 68 56 51 5.14 1950/15 57 68 59 49 4.81 1950/30 56 73 59 45 6.22 Average V + Ni Extracted: 57 # 2%. TABLE II KCl REACTION/K2CO3 EXTRACTION: V, Ni AND Na2O EXTRACTIONS Total % Reaction Extracted. % Extracted Conditions % Extracted % Extracted in Filter Based on Apparent Temp./Time in H2O in 2% K2CO3 Washes Filter Cakes Volatilization* (%) F/Mins V Ni Na2O V Ni Na2O V Ni Na2OV Ni Na2O V Ni 1800/15 0.5 57 64 43 - 6 43 57 70 54 59 53 11 2 1800/30 0.3 61 67 41 - 6 42 61 73 55 64 55 13 3 1850/15 0.3 65 67 43 - 6 43 65 73 55 64 57 12 1850/30 0.3 65 64 42 - 11 42 65 75 58 68 57 16 3 1900/15 0.3 67 65 44 - 7 44 67 72 56 68 57 12 1 1900/30 0.3 69 57 38 - 7 39 69 64 54 68 51 15 1950/15 0.3 69 60 41 - 7 42 69 67 57 69 49 15 1950/30 0.2 70 46 30 - 7 30 70 53 56 73 45 26 3 * As % of V or Ni in feed (spent contact material). These results demonstrate that vanadium and nickel extractions were relatively independent of reaction temperature and time in the range from about 180off to about 19500F and about 15 to about 30 min, with an average nickel extraction of about 67% and an average vanadium extraction of about 56%; or a total nickel and vanadium metals extraction of 57% i 2%. About 15%, on average, of the vanadium extracted was volatilized, with no significant nickel volatilization. The use of KCl in the alkali chloride/thermal treatment step provided virtually complete segregation of vanadium and nickel between the first (water) and the second (carbonate) extractions. The extracted aluminosilicate contact material showed no weight loss after the treatments and the small weight gains observed -- 1.6% to 6% -were due to the K20 pick-up, which increased with time and temperature of the treatments. About 50% to about 70% of the Na2 0 was extracted and this was largely independent of specific reaction conditions. This advantageously prevented sodium build-up. Example 2 - Potassium Chloride + Lithium Chloride Reaction/Potassium Carbonate Extraction This Example employed mixtures of KCl and LiCl, in varying proportions relative to each other and relative to the weight of the KNV/J spent aluminosilicate contact material. Analyses were carried out as in Example l and the results are shown in Tables III and IV. These results demonstrate that vanadium and nickel extractions were relatively independent of reaction temperature and time, in the range of about 18000F to about 1950S and about 15 to about 3Q min, with an average nickel extraction of about 79% and an average vanadium extraction of about 67%; or a total nickel and vanadium metals extraction of about 69 to 70%. Fran about 16% to about 28% of the vanadium extracted was volatilized, with 16% to 18% volatilized at the preferred shorter reaction time. No nickel was volatilized. The function of KCl in the alkali chloride/thermal treatment step was to facilitate segregation between the first and second extractions. As the proportion of KCl in The KCl/LiCl mixture increased, there was no effect upon either the levels of vanadium or nickel extraction, although it decreased the Li2O loss into the contact material with some increase in K2O pick-up. The extracted contact material showed a small weight gain, due to K20 and Li2O pick-up. TABLE III KCl/LiCl REACTION/K2CO3 EXTRACTION % Extracted Reaction Based on Conditions KCl + LiCl Filter Cakes Filter Cake Temp/Time % of KNV/J V Ni V+Ni K2O Li2O F/Mins KCl LiCl (%) (%) 1800/15 24.4 20.0 65 77 67 2.50 1.87 1800/30 24.4 20.0 68 77 70 2.22 2.65 1850/15 24.4 20.0 66 77 68 2.44 4.28 1850/30 24.4 20.0 68 77 70 2.57 2.03 1900/15 24.4 20.0 65 77 67 3.65 2.76 1900/30 24.4 20.0 68 82 70 3.36 2.80 1950/15 24.4 20.0 65 73 66 3.21 1.10 1950/30 24.4 20.0 71 82 72 3.04 2.83 1850/15 32.0 20.0 67 77 68 2.79 0.92 1950/15 32.0 20.0 66 82 68 3.96 0.82 1950/30 32.0 20.0 65 82 68 4.80 1.74 Average V + Ni extracted: 69%. TABLE IV KCl/LiCl REACTION/K2CO3 EXTRACTION: V AND Ni RECOVERY Total % Reaction Extracted % Extracted Conditions % Extracted in Filter Based on Apparent Temp/Time % of KNV/J In H2O In 2%K2CO3 Washes Filter Cakes Volatilization %* F/Mins. KCl LiCl V Ni V Ni V Ni V Ni V+Ni V Ni 1800/15 24.4 20.0 0.5 81 47 - 47 81 65 77 67 18 1800/30 24.4 20.0 0.4 81 47 - 48 81 68 77 70 21 1850/15 24.4 20.0 0.5 82 47 - 47 82 66 77 68 18 1850/30 24.4 20.0 0 83 45 - 45 83 68 77 70 23 1900/15 24.4 20.0 0.5 80 43 - 43 80 65 77 67 22 1900/30 24.4 20.0 0.4 86 43 - 43 86 68 82 70 25 1950/15 24.4 20.0 0.2 80 46 - 47 80 65 73 66 18 1950/30 24.4 20.0 0.6 83 42 - 43 83 71 82 72 28 1850/15 32.0 20.0 0.5 82 49 - 49 82 67 77 68 16 1850/15 32.0 20.0 0.7 85 49 - 50 85 66 82 68 16 1950/30 32.0 20.0 0.7 83 38 - 39 83 65 82 68 26 * As % of V or Ni in feed (spent aluminosilicate contact material). The use of lithium chloride in the alkali chloride/thermal treatment step incurs lithium replacement costs, due to Li20 pick-up by the contact material. Li2O levels in the extracted contact material represent the need for make-up lithium carbonate. Recovery of up to 80% to 90% of the Li2O from the extracted material is possible by treating the material with potassium acetate or sodium acetate before returning it to the selective vaporization contactor for recycling. Table V demonstrates the results of varying the KCl/LiCl ratios at a fixed reaction temperature and time of 1900F and 30 minutes, respectively. The spent aluminosilicate contact material treated (KNV/H) contained 1.34% V, 0.36% Ni and 1.55% Fe203 by weight. It was found That with a fixed KCl addition (24.4%), LiCl addition could be reduced from 20% to 15% without affecting the vanadium or nickel extraction efficiency and with the advantage of some reduction in lithium loss. With fixed LiCl addition,. although a 20% or 25% reduction in KCl addition did not significantly affect the levels of overall vanadium or nickel extraction, vanadium and nickel were no longer segregated between the water and carbonate extracts. Only in the cases where the KCl/LiCl ratio was at least 1.2:1 was the vanadium substantially segregated into the second (carbonate) extract. At lower KCl levels, vanadium was distributed between the two extracts. TABLE V KCl/LiCl REACTION/K2CO3 EXTRACTION: VARYING KCl + LiCl ADDITIONS % Extracted Total % Extracted % Extracted Based Apparent % of KNV/H In H2O In 2% K2CO3 in Filter Washes on Filter Cakes Volatilization %* KCl LiCl V Ni V Ni V Ni V Ni V+Ni V Ni 24.4 20.0 0.6 76 52 - 53 76 62 83 66 9 7 24.4 15.0 0.5 80 56 - 56 80 62 83 66 6 3 24.4 10.0 0.3 66 41 - 41 66 51 81 58 10 15 24.4 5.0 0.2 70 39 - 39 70 45 75 51 6 5 24.4 - 0.5 63 41 - 42 63 49 64 52 7 1 10.0 20.0 12 66 45 - 57 66 73 81 75 16 15 5.0 20.0 12 36 32 - 44 36 74 56 70 30 20. 10.0 25.0 23 70 41 - 64 70 72 78 74 8 4 5.0 25.0 35 32 24 - 60 32 75 50 70 15 38 * As % of V or Ni in Feed (spent aluminosilicate contact material). Example 3 - Potassium Chloride + Lithium Chloride Reaction/Potassium Carbonate Extraction In this Example, 25 g samples of spent aluminosilicate contact material containing 1.7% V, 0.41% Ni and 1.66% Fe2O3 by weight, designated KNV/K, were blended with mixtures of a 25% KC1 solution and a 25% LiCl solution, in varying proportions relative to each other and relative to the dry weight of the contact material. The contact material and KCl/LiCl mixture was heated to 18500F for 15 minutes then extracted with water at 50-600C and then further extracted with 2% K2CO3 under reflux. While the KCl/LiCl ratios varied in this example, reaction temperature and time remained fixed at 18500F and 15 minutes, respectively. Analyses were carried out as in Example 1 and the results are shown in Table VI. Metals extractions of about 70% resulted with mixtures of 20 or 24.4% KC1 and 20% LiCl, or 24.4% KC1 and 15% LiCl, based upon the dry weight of the spent contact material. The optimal ratio for spent contact material/KC1/LiC1 .ranged from 100:20:15 to 100:24.4:20. The preferred KCl/LiCl weight ratio, in terms of metals extraction, metals separation and minimal retention of Li2 0 in the solids was determined to be 1.6:1. TABLE VI KCl/LiCl REACTION/K2CO3 EXTRACTION: VARYING KCl + LiCl ADDITIONS Total % Extracted % Extracted % Extracted in Filter Based on Apparent Li2O in % of KNV/H In H2O In 2% K2CO3 Washes Filter Cakes Volatilization %* Filter KCl LiCl V Ni V Ni V Ni V Ni V+Ni V Ni Cake (%) 24.4 15.0 0.2 66 62 - 62 66 66 83 69 4 17 1.6 24.4 12.0 0.2 79 57 - 57 79 58 80 62 1 1 1.4 20.0 15.0 0.2 83 56 - 56 83 63 83 67 7 - 1.9 20.0 12.0 4.0 46 47 0.5 51 47 54 61 57 3 10 2.0 15.0 15.0 4.0 85 60 - 64 85 62 83 66 - - 2.2 15.0 12.0 5.0 83 50 - 55 83 63 80 66 8 - 2.1 24.4 20.0 0.2 68 64 - 64 68 68 83 71 4 15 1.9 10.0 20.0 0.4 87 65 - 65 87 70 83 72 5 - 1.9 15.0 20.0 14.0 78 46 - 60 78 73 83 75 13 5 3.1 * As % of V or Ni in Feed (spent aluminosilicate contact material). Example 4 - Potassium Chloride + Lithium Chloride Reaction/Potassium Acetate Extraction In this example, a 100 g sample of KNV/K spent aluminosilicate contact material was blended with 24.4 g KC1 and 20.0 g LiCl (dry basis) then heated to 18500F for 15 minutes. Nickel was extracted from the product with water at 50-600C. After extraction, the filter cake contained 1.73% V, 0.12% Ni, 1.47% K2O and 1.32% Li2O. A A 20 g aliquot of the filter cake was mixed with a solution containing 20 g potassium acetate and 20 g water. Thereafter, the mixture was dried at 2200C and introduced into a Lindberg crucible furnace at 3050C. The temperature was slowly raised to 3240C and maintained at this level for 30 minutes. The crucible was allowed to cool and the contents were extracted by stirring with 100 ml water at 90-1000C for 30 minutes. The flurry was filtered, washed and dried. and the solids analyzed. As a result, 92% of the Li2O, and 39% of the vanadium were extracted, as indicated by analysis of the filter cake: 1.032 V, 0.12% Ni, 0.10% Li2O, 6-12% K2O. Another 20 g aliquot of the filter cake was mixed with 20 g potassium acetate, with the addition of 0.65 g KOH, the equivalent of the 2% K2 CO3 normally used in the second stage carbonate extraction, then heated as described above. As a result, 92% of the Li2 0 was extracted and 68% of The vanadium was extracted, as indicated by analysis of the filter cake: 0.57% V, 0.12% Ni, 0.11% Li2O and 5-93% K2O. Example 5 - Potassium Chloride + Lithium Chloride Reaction/Alkali Acetate + Alkali Carbonate or Alkali Hydroxide Extraction Lithium recovery was studied for spent aluminosilicate contact material treatments in which the second stage extraction was an extraction with an alkali acetate and an alkali carbonate or an alkali acetate and an alkali hydroxide. In this example, 300 g of spent aluminosilicate contact material, KNV/K, were mixed with 73.2 g KC1, 60.0 g LiCl and water in an evaporating dish to form a thin paste. The mixture was evaporated under a heat lamp with occasional stirring then dried for 1 hour at 2200C. The dry mixture was heated in 5 batches (85 g each) at 18500F for 15 minutes. The calcine (424 g) was crushed, screened (100 mesh sieve) and extracted with 300 ml water (550C) for 30 minutes. When filtered and dried the resulting 300.0 g residue analyzed: Ni V K2O Li2O Assay residue (x) 0.10 1.7 1.4 2.2 Metals extraction (%) 77.2 7.4 91.0 67.6 Various lithium recovery procedures were studied by contacting a sample of the residue from the above-described first stage extraction with a concentrated solution of alkali acetate and alkali carbonate, or alkali acetate and alkali hydroxide, in a wide form crucible. The resulting slurries were evaporated under a heat lamp, then dried at 2200C for 1 hour in an air oven. The dried product was placed in a 305"C crucible furnace and the temperature was slowly increased to the desired final temperature. After the desired residence time had passed, the sample was removed, then crushed, screened (100 mesh sieve) and extracted with 10 times its weight of 550C water for 30 minutes. The resulting slurry was filtered and the filter cake washed with additional warm water. Tables VII and VIII indicate the metals content of the filtrate and dry filter cakes. As shown in the Tables, lithium recoveries between 93 and 97% were obtained. Vanadium extraction efficiencies were fairly insensitive to process conditions and averaged about 74%. Lithium extraction according to these processes resulted in a nearly stoichiometric build-up of sodium or potassium oxide in the treated contact material. The preferred reaction conditions for the second stage extraction, in terms of lithium recovery, were heating of the water-extracted contact material at about 3240C for about 30 to about 60 minutes with about 3 moles potassium atoms per mole lithium atoms present in the material. The potassium atom requirement was supplied from potassium acetate and potassium carbonate in the mole ratio of 2:0.5. These conditions provided a total lithium recovery of 97%. Residual metal content of the thus treated contact material was: 0.1% Ni, 0.53% V, 0.28% Li2-O and 7;6% K2O. The second stage extraction procedures according to this example permitted simultaneous vanadium and lithium recovery while providing, for example, up to 72% total vanadium extraction. With the use of sodium, rather than potassium salts, a slight reduction in extraction efficiencies was observed. Ninety-three percent lithium and 71% vanadium recoveries were achieved using 2.5 mole Na per mole Li and a 1:1 acetate: carbonate mole ratio and heating the contact material at 3350C for 1 hour. Observed lithium recoveries with the use of sodium salts ranged from 91-93%, with 71-76% vanadium recovery. The use of sodium salts to recover lithium resulted in the retention of Na2O (4.5%), as well as K2O (1%), in the treated contact material. When sodium hydroxide was used in place of the corresponding carbonates, lithium extraction was reduced by 20% and vanadium extraction by 10-20%, although the lithium extraction required less water. An alternate embodiment of this process, thermally treated spent aluminosilicate contact material with lithium chloride and extracted the mixture with water. The extracted and washed solids analyzed 1.3% V, 0.13% Ni and 3.2% Li2O. The contact material was then refluxed with an equal weight of sodium acetate (anhydrous) as a 50% solution at the boiling point, with no added NaOH. It was found that only 59% of the Li2O and 40% of the vanadium had been extracted. Comparison of the results of this Example with those of Example 4 reveals that the combination of potassium acetate and potassium hydroxide provides for both effective removal of vanadium and effective recovery of lithium. TABLE VII KCl/LiCl REACTION/K SYSTEM 2ND STAGE EXTRACTION Thermal K System Treatment Final Filter % Extracted Sample Salts Temp./Time Cake Analysis (%) 2nd Stage Total* Wt. (g) Wt. (g) C/Min V Li2O K2O V Ni Li2O V Ni Li2O 20.0 5.9 K acetate 324/60 0.53 0.28 7.6 70 0 88 72 78 97 2.1 K carbonate 20.0 8.83 K acetate 324/60 0.56 0.31 7.8 68 0 86 70 78 96 20.0 5.9 K acetate** 324/60 0.56 0.66 8.0 67 0 71** 70 78 91 1.7 K hydroxide 20.0 5.9 K acetate 324/60 0.50 0.31 6.9 71 0 87 74 78 96 2.1 K carbonate 20.0 5.9 K acetate 324/60 0.52 0.32 7.8 71 0 86 73 78 96 2.1 K carbonate 20.0 2.4 K acetate 324/15 0.47 0.39 6.9 73 0 83 75 78 94 3.4 K carbonate 20.0 3.4 K acetate 324/30 0.48 0.27 7.7 73 0 88 75 78 96 4.7 K carbonate 15.0 4.32 K acetate 300/30 0.46 0.35 7.0 74 0 80 76 78 94 1.55 K carbonate * Recovered in first (water) extraction and second (acetate) extraction. ** Amount of acetate used was insufficient in view of high Li content of final filter cake. TABLE VII (cont'd) KCl/LiCl REACTION/K SYSTEM 2ND STAGE EXTRACTION Thermal K System Treatment Final Filter % Extracted Sample Salts Temp./Time Cake Analysis (%) 2nd Stage Total* Wt. (g) Wt. (g) C/Min V Li2O K2O V Ni Li2O V Ni Li2O 15.0 4.32 K acetate 300/90 0.46 0.35 7.0 74 0 80 76 78 94 1.55 K carbonate 15.0 4.32 K acetate 330/60 0.48 0.23 7.9 72 0 90 74 78 97 1.55 K carbonate 15.0 4.32 K acetate 360/30 0.52 0.48 7.7 70 0 79 72 78 93 1.55 K carbonate 15.0 4.32 K acetate 360/90 0.52 0.29 8.3 70 0 87 72 78 96 1.55 K carbonate 15.0 4.32 K acetate 324/60 0.70 0.93 7.8 59 0 58 62 78 86 1.3 K hydroxyde * Recovered in first (water) extraction and second (acetate) extraction. TABLE VIII KCl/LiCl REACTION/Na SYSTEM 2ND STAGE EXTRACTION K System Thermal Treatment Final Filter % Extracted Sample Salts Temp./Time Cake Analysis (%) 2nd Stage Total Wt. (g) Wt. (g) C/Min V Li2O Na2O K2O V Ni Li2O V Ni Li2O 15.0 3.6 Na acetate 344/60 0.56 0.64 4.8 1.1 68 0 72 71 78 91 1.2 Na carbonate 15.0 3.6 Na acetate 344/60 0.55 0.60 4.5 1.1 69 0 74 72 78 92 2.0 Na carbonate 15.0 3.6 Na acetate 335/60 0.56 053 4.4 1.0 69 0 77 71 78 93 2.0 Na carbonate 15.0 3.6 Na acetate 344/60 0.78 1.5 N/A 1.0 55 0 33 58 78 78 0.9 Na hydroxide Example 6 - Lithium Chloride Reaction/Water Extraction/Sulfuric Acid Extraction After ccataeting three batches of 100 g KNV/K spent aluminosilicate contact material (1.8% V, 0.41% Ni) each with 100 g of 25% LiCl, they were dried and heated for 15 minutes at 18500F. The agglomerates were broken to pass 100 mesh, mixed and extracted with 300 ml water at 50-600C for 1 hour with HC1 (5.4 g of 36.5%) being added to reduce the pH to li0 and ensure dissolution of any precipitated nickel hydroxide. After ftering, washing and drying the samples and again passing them through a 100 mesh sieve, the product weighed 294.4 g and contained 1.3% V, 0.13% Ni and 3.2% Li2O. After dividing the filter cake into 25 g aliquots the samples were extracted by refluxing with various amounts of 35% w/w H2 SO4 for various reaction times,and filtered and washed. The results are shown in Table IX. Overall weight loss, coextraction of alumina,and residual Li2O content in the treated aluminosilicate contact material were generally independent of the relative proportion of 35% H2SO4 used in the extraction. Co-extraction of alumina and weight loss increased, and residual Li2 0 in the treated material decreased, with increasing reaction times. Alternatively, higher concentrations of sulfuric acid such as 50-60% w/w H2 SO4 may be used in the second stage extraction. For example, when, after the first stage LiCl reaction and water extraction, a 25 g spent contact material sample was refluxed for 1 hour with boiling 50% w/w H2SO4, extraction totals were 86% V and 83% Ni, with 10% A1203 extraction and Li2O content of 0.65% in the product. Thus, lithium chloride provides superior removal of metals as compared to potassium chloride but exacts a penalty in the processing required to recover the expensive lithium. TABLE IX LiCl REACTION/WATER EXTRACTION/H2SO4 EXTRACTION Amount Reflux Final Filter Cake 35% H2SO4 Time Total % Extracted Analysis (%) Total Weight (ml) (Min) V* Ni* V+Ni* Al2O3** V Ni Li2O Loss (%) 20 60 79 84 79 4 0.38 0.07 1.8 5 20 120 80 84 80 5 0.36 0.07 1.4 6 20 180 81 84 80 7 0.35 0.07 1.1 7 30 60 79 84 79 3 0.37 0.07 2.0 4 30 120 82 84 81 6 0.34 0.07 2.0 6 30 180 82 84 81 8 0.34 0.07 1.1 7 50 60 81 84 80 4 0.36 0.07 1.9 5 50 120 82 84 80 7 0.34 0.07 1.3 7 50 180 82 86 82 10 0.33 0.06 0.98 7 * Based on final filter cake analysis. ** Based on 35% H2SO4 extract. The spent aluminosilicate contact material treated in Examples 1-6 had high iron content, containing from about 1.55 to about 2.43% ferric oxide. In Examples 7 and 8, the spent aluminosilicate contact material had much lower iron content, ranging between 0.43 and 0.6% ferric oxide. The following Examples demonstrate that the addition of iron, as ferric chloride in the water extraction or as ferric oxide to the alkali chloride-aluminosilicate material mixture before thermal treatment, ensured adequate separation of nickel and vanadium. Example 7 - Potassium Chloride Reaction/Potassium Carbonate Extraction - Low Iron Content Spent Aluminosilicate Contact Material: Ferric Chloride Addition This Example used a 25% KC1 solution in the alkali chloride/thermal treatment step, in a proportion of 32 parts of KCl by weight per 100 parts by weight of KNV/C and KNV/P spent aluminosilicate contact material and a 2% K2 CO3 solution for the alkali carbonate extraction. The KNV/C and KNV/P spent aluminosilicate contact materials contained much less iron than the KNV/H, KNV/J and KNV/K samples, as indicated by the following analysis: - % Ni - % Fe2O3 KNV/C 0.92 0.21 0.60 KNV/P 0.85 0.22 0.43 KNV/H 1.34 0.36 1.55 KNV/J 1.26 0.22 2.43 KNV/K 1.7 0.41 1.66 After reacting 25 g samples of spent aluminosilicate contact material with KC1 at 19500F for 15 minutes7 the products were extracted with 40 ml water and 0.85 g FeCl3* 6H2O (equivalent to 1% Fe203 on the sample) or 0.43 g ECl3. 6H2O (equivalent to 0.5% Fe2O3 on the sample) for 30 minutes. This was repeated without the addition of FeCl3. 6H2O. The products were then extracted with 50 ml of K2CO3 at reflux for 30 minutes, filtered and washed. The filter washes were analyzed and the results are shown in Tables X and XI. TABLE X KCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: FeCl3 ADDITION Contact % Extracted Total % Extracted % Extracted Based Analysis of Material FeCl3 . 6H2O In H2O In 2% K2CO3 In Filter Washes on Filter Cakes Filter Cake (%) Sample Added (g) V Ni V Ni V Ni V Ni V Ni Fe2O3 KNV/C 0.85 0.4 65.5 36.4 - 37 66 64 75 0.31 0.05 0.76 KNV/C 0.43 0.5 67.6 44.7 - 45 68 55 66 0.39 0.07 0.82 KNV/C 0 8.2 71.4 37.5 - 46 71 54 65 0.40 0.07 0.46 KNV/P 0.85 0.5 75.3 43.2 - 44 75 49 71 0.41 0.06 0.81 KNV/P 0.43 0.5 58.0 43.7 - 44 58 58 72 0.30 0.06 0.78 KNV/P 0 13.2 58.8 30.9 - 44 59 61 71 0.31 0.06 0.38 TABLE XI KCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: FeCl3 ADDITION KNV/C (g) KNV/C (g) KNV/C (g) KNV/P (g) KNV/P (g) KNV/P (g) 0.85 g FeCl3 0.43 g FeCl3 No FeCl3 0.85 g FeCl3 0.43 g FeCl3 No FeCl3 Balance Of Fe2O3 Added Added Added Added Added Added Fe2O3 in Sample 0.150 0.150 0.150 0.108 0.108 0.108 Fe2O3 added as 0.250 0.126 0 0.250 0.126 0 FeCl3 . 6H2O Total Fe2O3 Input 0.400 0.276 0 0.358 0.234 0 Fe2O3 in H2O Extract 0.141 0.040 0.0002 0.152 0.025 0.0004 Fe2O3 in Filter Cake 0.201 0.216 0.123 0.216 0.205 0.101 (0.76%) (-)% (-)% (0.18%) (-)% (-)% Total Fe2O3 Recovered 0.342 0.256 0.123 0.368 0.230 0.101 Apparent Loss by 0.058 0.020 0.027 - 0.004 0.007 Volatilization (39%) (13%) (18%) (0%) (4%) (6%) These results demonstrate that the addition of ferric chloride to the first-stage water extraction permitted the desired separation of vanadium and nickel with no significant loss of vanadium into The nickel-containing water extract. Addition of FeC13, even in an amount equivalent to 1% Fe2O3 based upon the weight of the sample, resulted in only a comparatively small increase in the Fe2O3 content of the extracted contact material. The amount of Fecal3 added to the water extraction stage in an amount equivalent to 0.5% Fe2O3 also provided vanadium/nickel separation. Example 8 - Potassium Chloride Reaction/Potassium Carbonate Extraction - Low Iron Content Spent Aluminosilicate Contact Material: Ferric Oxide Addition This Example used samples of the same low-iron clay content spent- aluminosilicate contact material and the procedure set forth in the preceding Example, except that no ferric chloride was added in the water extraction stage. Instead, 1% (0.25 g) or 0.5% (0.13 g) Fe2O3, based on weight of the sample used,was added to the contact material-KCl mixture before drying and heating at 19500F for 15 minutes. After filtering and washing the products, the filter washes were analyzed and the results recorded in Tables XII and XIII. TABLE XII KCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: FeCl3 ADDITION Contact % Extracted Total % Extracted % Extracted Based Analysis of Material Fe2O3 In H2O In 2% K2CO3 In Filter Washes on Filter Cakes Filter Cake (%) Sample Added (g) V Ni V Ni V Ni V Ni V Ni Fe2O3 KNV/C 0.25 0.2 79.8 39.0 - 39 80 50 75 0.43 0.05 0.94 KNV/C 0 8.2 71.4 37.5 - 46 71 54 65 0.40 0.07 0.46 KNV/P 0.25 0.1 65.6 40.8 - 41 66 60 81 0.32 0.04 1.01 KNV/P 0.13 0.9 62.2 35.5 - 36 62 57 76 0.34 0.05 0.76 KNV/P 0 13.2 58.8 30.9 - 44 59 61 71 0.31 0.06 0.38 TABLE XIII KCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: Fe2O3 ADDITION KNV/C (g) KNV/C (g) KNV/P (g) KNV/P (g) KNV/P (g) 0.25 g Fe2O3 No Fe2O3 0.25 g Fe2O3 0.13 g Fe2O3 No Fe2O3 Balance Of Fe2O3 Added Added Added Added Added Fe2O3 in Sample 0.150 0.150 0.108 0.108 0.108 Fe2O3 Added 0.250 0 0.250 0.130 0 Total Fe2O3 Input 0.400 0 0.358 0.238 0 Fe2O3 in H2O Extract 0.052 0.002 0.024 < 0.0001 0.0004 Fe2O3 in Filter Cake 0.252 0.123 0.269 0.205 0.101 (0.9%) (--%) (1.01%) (--%) (--%) Total Fe2O3 Recovered 0.304 0.123 0.293 0.205 0.101 Apparent Loss by Volatilization 0.096 0.027 0.065 0.033 0.007 (24%) (18%) (18%) (14%) (6%) These results illustrate that the addition of 1% Fe2O3 to the spent contact material-KCl reaction mixture provided virtually complete segregation of vanadium and nickel with no significant loss of vanadium into the nickel-containing water extract. Fe2O3 addition in an amount equivalent to 0.52 of the sample weight still provided good separation between nickel and vanadium. Example 9 - Potassium Chloride + Lithium Chloride Reaction/Potassium Carbonate Extraction - Low Iron Content Spent Aluminosilicate Contact Material: FeC, or FeOn Addition This Example I reacted 25 g samples of spent aluminosilicate contact material KNV/P, with 20 g of 25% KC1, and 20 g of 25% LiCl, with the addition of varying amounts of Fe203 at 1900 F for 15 minutes, and extracted the products with 40 ml of water at 50-600C for 30 minutes. The resulting product was extracted with 50 ml of 2% K2CO3 at reflux for 30 minutes and filtered and washed. This was repeated with and without The addition of FeCl3. 6H2O to the water used for extraction of nickel, in place of addition of Fe 203 to the admixture of contact material and alkali chloride prior to the thermal treatment. Results of analysis of the filter washes and filter cakes are shown in Tables XIV and XV. TABLE XIV KCl/LiCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: Fe2O3 OR FeCl3 ADDITION FeCl3.6H2O Fe2O3 Added Added to Total % Contact to KCl/LiCl H2O Extracted % Extracted Material Reaction Extraction % Extracted in Filter Based on Analysis of Sample (g) (% of (g) (Fe2O3 In H2O In 2% K2CO3 Washes Filter Cakes Filter Cakes (%) (KNV/P) KNV/P) % of KNV/P) V Ni V Ni V Ni V Ni V Ni Fe2O3 1 - - - - 18.2 65.1 17.0 - 35 65 58 86 0.34 0.03 0.33 2 - - 0.43 0.5 0.2 72.5 34.6 - 35 73 59 90 0.33 0.02 0.76 3 - - 0.21 0.25 1.7 69.6 31.5 - 33 70 59 90 0.33 0.02 0.51 4 0.13 0.5 - - 12.0 74.9 25.2 - 37 75 63 90 0.30 0.02 0.59 5 0.06 0.25 - - 10.5 73.3 23.3 - 34 73 60 90 0.32 0.02 0.45 TABLE XV KCl/LiCl REACTION/K2CO3 EXTRACTION - LOW IRON CONTENT SPENT ALUMINOSILICATE CONTACT MATERIAL: Fe2O3 ADDITION KNV/P CONTACT MATERIAL SAMPLE (g) Balance Of Fe2O3 1 2 3 4 5 Fe2O3 in Sample 0.108 0.108 0.108 0.108 0.108 Fe2O3 Added - - - 0.130 0.060 Fe2O3 Added as FeCl3 . 6H2O - 0.125 0.063 - Total Fe2O3 Input 0.108 0.233 0.171 0.238 0.168 Fe2O3 in H2O Extract 0.0001 0.013 0.0003 0.0001 0.0002 Fe2O3 in Filter Cake 0.0867 0.201 0.134 0.155 0.119 Total Fe2O3 Recovered 0.087 0.214 0.134 0.155 0.119 Apparent Loss by Volatilization 0.021 0.109 0.037 0.083 0.049 (19%) (18%) (34%) (35%) (29%) These results demonstrate that addition of ferric chloride (in an equivalent to 0.5% Fe2O3 on the sample) to the water extraction ensured vanadium and nickel separation. When 1% Foe203 was added to the KCl/LiCl reaction before heating, the KCl/LiCl ratio in the mixture was preferably 1.6:1. Example 10 - Potassium Chloride + Lithium Chloride Reaction/Hydrochloric Acid Extraction this Example contacted 25 g samples of KNV/H spent aluminosilicate contact material (1.34% V, 0.36% Ni, 1.55% Fe203) with mixtures of 25% KC1 and a 25% LiCl solutions, in a proportion such that the contact material:KCl:LiCl ratio, by weight, was 100:24.4:20, and dried the resulting mixtures at 22O0C for 1 hour and heated them for 15 minutes at 18500F. The products were then extracted by refluxing at boiling with various amounts of 1:1 HC1 (20%) for various reaction times then filtered and washed. The results are shown in Table XVI. Vanadium and nickel extractions were generally independent of the amount of 1:1 HC1 used and extraction time. Co-extraction of alumina increased at the longer reaction times of 120 and 180 minutes but remained at acceptable levels. TABLE XVI KCl/LiCl REACTION/HCl EXTRACTION Total % Extracted Amount Extracted In Based on Final Filter HCl/H2O Extraction Filter Washes (%) Filter Cake Cake Analysis (%) Extractant (ml) Time (min) V Ni Al2O3 V Ni V Ni Li2O K2O 50/50 15 75 79 3.5 75 78 0.44 0.08 1.17 1.40 50/50 60 72 83 3.6 72 78 0.45 0.08 0.72 1.31 50/50 120 67 79 5.7 67 81 0.45 0.07 0.42 1.46 50/50 180 70 78 7.9 70 78 0.42 0.08 N/A 1.42 20/20 15 69 78 1.2 69 78 0.44 0.08 0.98 1.51 20/20 120 70 81 5.1 70 81 0.41 0.07 0.56 1.48 10/10 15 69 78 1.9 69 78 0.47 0.08 1.01 1.17 10/10 60 69 78 2.3 69 78 0.46 0.08 0.73 1.32 10/10 180 65 86 6.0 65 78 0.44 0.08 0.55 1.42 Example 11 - Potassium Chloride - - - - Reactlon/Hydrochlorlc Acid Extraction This Example contacted 25 g samples of KNV/H spent aluminosilicate contact material (1.34% V, 0.36% Ni, 1.55% Fe203) with 24 g or 32 g 25% KCl,.dried the resulting mixtures at 2200C and heated them for 15 minutes at 19000F. The products were then extracted by refluxing at boiling with various amounts of 1:1 HC1 (20%) for various times and'then filtered and washed. The results are shown in Table XVII. vanadium and nickel extractions were substantially independent of the amount of 1:1 HC1 used and the extraction time. Alumina extraction increased, to levels which remained acceptable, with longer extraction times. Reactions carried out using a higher KC1:KNV/H ratio showed increased extraction of nickel and vanadium. TABLE XVII KCl REACTION/HCl EXTRACTION Total % Extracted Amount Extraction Extracted In Based on Final Filter HCl/H2O Time Filter Washes Filter Cake Cake Analysis (%) KCl% of KNV/H Extractant (ml) (min) V Ni Al2O3 V Ni V Ni K2O 24 50/50 15 57 62 4.5 55 64 0.60 0.13 2.50 24 50/50 60 48 49 4.7 58 64 0.56 0.13 2.18 24 50/50 120 61 60 7.8 60 64 0.53 0.13 2.05 24 50/50 15 56 58 5.1 57 61 0.58 0.14 2.37 24 50/50 180 60 58 8.0 60 61 0.53 0.14 2.07 24 50/50 15 54 57 5.0 58 64 0.56 0.13 2.43 24 50/50 180 62 63 9.6 60 64 0.53 0.13 2.01 32 50/50 60 58 67 - 65 75 0.47 0.09 2.71 Example 12 - Lithium Chloride Reaction/ Hydrochloric Acid Extraction This Example contacted 25 g samples of KNV/H spent aluminosilicate contact material with 20, 25 or 30 g of 25% KC1, dried the resulting mixtures at 2200C and heated them at 18500F for 15 minutes. The products were extracted by refluxing at boiling with various amounts of 1:1 HC1 (20%) for various times; then filtered and washed. The results are shown in Table XVIII. Increasing the LC1:KNV/H ratio from 20g:25g to 25g:25g increased metals extraction As the LiCl:KNV/H ratio became higher e.g., 30g:25g, metals extraction did not increase. TABLE XVIII LiCl REACTION/HCl EXTRACTION Total % Extracted Amount Extraction Extracted In Based on Final Filter HCl/H2O Time Filter Washes Filter Cake Cake Analysis (%) LiCl% of KNV/H Extractant (ml) (min) V Ni Al2O3 V Ni V Ni Li2O 20 50/50 15 69 59 7.0 72 75 0.37 0.09 1.88 20 25/25 60 68 61 - 81 83 0.26 0.06 1.40 20 10/10 180 59 60 9.0 67 81 0.44 0.07 0.86 25 20/20 60 72 76 6.2 78 83 0.30 0.06 1.26 30 20/20 60 76 74 7.9 78 83 0.30 0.06 0.99 Example 13 - Alkali Chloride Reaction/Sulfuric Acid Extraction his Example contacted samples of KNV/K spent aluminosilicate contact material with an equal weight of 25% LiCl solution, dried the resulting mixtures at 2200C and heated them at 18500F for 15 minutes. The products were extracted by stirring with water at 50-600C for 30 minutes (solids/liquid ratio 1:1.6) with addition of HC1 to reduce the pH to 1.0. The solids were filtered off, washed, dried and analyzed. 25 g samples were reacted with 20 ml of sulfuric acid of various concentrations by boiling under reflux for 1 hour. The reaction products were filtered and washed and the dried residual solids were analyzed to determine overall extraction levels of vanadium and nickel and losses of lithium into the extracted contact material. The results are shown in Table XIX. Extractions of vanadium and nickel were independent of sulfuric acid concentration in the range 45 to 70% but co-extraction of alumina increased with increasing acid concentration; lithium losses were reduced by increasing acid concentration. TABLE XIX LiCl REACTION/H2O AND/H2SO4 EXTRACTION Analysis of % Extracted Solids after H2O H2SO4 Based on Final Li2O Content Al2O3 Extraction (%) Concentration Filter Cake of Final Extracted Weight V Ni Li2O (%) V Ni Filter Cake (%) (%) Loss (%) 1.30 0.17 3.90 45 85 83 1.40 6 5 1.30 0.17 3.90 50 86 83 0.65 10 8 1.09 0.13 4.00 60 80 83 0.60 12 12 1.09 0.13 4.00 70 83 85 0.11 24 14 Example 14 - Potassium Chloride Reaction/Sulfuric Acid Extraction This Example contacted 25 g samples of KNV/M spent aluminosilicate contact material (1.79% V, 0.39% N, 2.36% Fe2O3) with 32 g of 25% KC1 solution, dried the resulting mixtures at 2200C and heated them for 15 minutes at a series of temperatures. Samples A, B and C were extracted-with water at 50-600C for 30 minutes (solids/liquid ratio 1:1.6), filtered and washed. The filter cakes were then extracted with 20 ml 50% H2SO4 under reflux for 1 hour. The residual solids were separated by filtration, washed, dried and analyzed to determine overall extraction of vanadium and nickel. In the case of samples D, E and F, only a single extraction was carried out using 20 ml 50% H2SO4, with no prior water extraction. The results are shown in Table XX. Vanadium extractions were substantially independent of reaction temperature in the range of 1850 to 19500F but . good extraction of nickel required a temperature of 1900 to 19500F. With reaction temperatures of 1900/19500F± average extractions were: V: 65%, Ni: 65%. TABLE XX KCl REACTION/H2SO4 EXTRACTION Total % Extracted Sample Reaction Temp ( F) V Ni Al2O3 Weight Loss (%) A 1850 63 50 9 3 B 1900 68 69 16 6 C 1950 63 65 9 3 D 1850 62 53 7 4 E 1900 65 61 9 4 F 1950 63 63 6 3

Claims: CLAIMS 1. A process for removing nickel and vanadium values from an aluminosilicate material contaminated therewith, the method comprising (a) treating the contaminated aluminosilicate material with alkali chloride(s) selected from lithium and potassium chlorides in the substantial absence of moisture, at a temperature above the melting point of the chloride or chlorides, under conditions effective to convert the nickel and vanadium in the aluminosilicate material to soluble form and (b) removing soluble nickel and vanadium values from the treated aluminosilicate material. 2. A process according to claim 1 wherein the alkali chloride treatment is conducted at a temperature of 785 to 12050C [about 1450 to about 22000F1 for from 5 to 60 minutes, preferably at a temperature of 955 to 10700C [about 1750 to about 19500F] for from 10 to 30 minutes. 3. A process according to claim 1 or 2 wherein nickel values are removed from the aluminosilicate material in step (b) without appreciable co-extraction of alumina or silica from that material. 4. A process according to any preceding claim wherein in step (a) the aluminosilicate material is contacted with a mixture of potassium chloride and lithium chloride in which the weight ratio of KCl to LiCl is between 1:1 and 2:1 and wherein the total weight of the chlorides is at least 10X of the weight of the aluminosilicate material. 5. A process according to any preceding claim wherein the contaminated aluminosilicate material comprises a particulate contact material that has been contacted with petroleum feedstock in a selective vaporisation process, at least a portion of the resulting decontaminated aluminosilicate material being used for contact with petroleum feedstock in a selective vaporisation process. 6. A process according to any preceding claim wherein the removal of the soluble nickel and vanadium values from the treated aluminosilicate material comprises contacting the treated aluminosilicate material with aqueous liquid to obtain an aqeous nickel chloride extract, separating the aluminosilicate material from the aqueous extract, and treating the separated aluminosilicate material to remove vanadium values. 7. A process according to claim 6 wherein the coextraction of vanadium with nickel in the aqueous nickel chloride extract is reduced by maintaining the iron content [calculated as Fe203] of the aqueous extract at at least 50 ppm, e.g. by adding appropriate iron values to the contaminated aluminosilicate starting material and/or to the aqueous liquid for nickel extraction if the contaminated aluminosilicate starting material has insufficient inherent iron content. 8. A process according to claim 6 or 7 wherein nickel values are recovered from the aqueous nickel chloride extract, e.g. by liquid ion exchange, or by electrolysis, or by precipitation e.g. of hydrous nickel oxide, nickel hydroxide or nickel carbonate. 9. A process according to any of claims 6 to 8 wherein vanadium values are removed by treating the separated aluminosilicate material with an aqueous solution of alkali [e.g. alkali hydroxide and/or carbonate and preferably alkali carbonate selected for example from potassium and sodium carbonates, most preferably aqueous solution containing from 1.5 to 2.5 wt.% potassium carbonate] to obtain an aqueous extract containing vanadium values. 10. A process according to any of claims 6 to 8 wherein vanadium values are removed from the separated aluminosilicate material by contacting the separated material with aqueous hydrochloric and/or sulfuric acid, preferably with 10 to 36% hydrochloric acid or 40 to 70X sulfuric acid, to obtain an aqueous extract containing vanadium values. 11. A process according to any of claims 1 to 5 wherein nickel and vanadium values are removed together from the treated aluminosilicate material,[e.g.] by contacting the separated material with aqueous hydrochloric and/or sulfuric acid, preferably for a period of from 30 minutes to 3 hours, to obtain an aqueous extract containing nickel and vanadium values. 12. A process according to claim 11 wherein the separated aluminosilicate material is contacted with (a) aqueous 10 to 36 wit.% hydrochloric acid at or near its boiling point for from 30 minutes to 3 hours or (b) aqueous 40 to 70 wit.% sulfuric acid at or near its boiling point for at least 30 minutes. 13. A process according to any of claims 9 to 12 wherein vanadium values are recovered from the resulting aqueous extract by liquid ion exchange, e.g. by contacting the extract with an organic phase comprising quaternary amine in the sulfate, carbonate or chloride form to transfer vanadium values, in the form of vanadate ions, from the extract into the organic phase and, when said quaternary amine is in the sulfate form, optionally treating the aqueous raffinate from the ion exchange with barium carbonate. 14. A process according to claim 13 including stripping the organic phase including the vanadate ions with aqueous ammoniacal stripping solution preferably comprising (a) ammonium carbonate and at least one other ammonium salt, e.g. ammonium sulfate, or (b) ammonium hydroxide and ammonium chloride] to obtain ammonium metavanadate. 15. A process according to any of claims 6 to 8 wherein step (a) involves the use of lithium chloride and wherein the separated aluminosilicate is treated with alkali acetate at a temperature above the m.p. of the acetate loptionally together with alkali carbonate and/or hydroxide], and then contacted with water to obtain an aqueous extract containing vanadium and lithium values. 16. An aluminosilicate particulate contact material obtained by a process according to any of claims 1 to 15, preferably having an alumina to silica molar ratio of about 1:2, a mullite content of about 10X by weight and an alkali metal oxide(s) content of at least 1X by weight, the alkali metal oxide(s) preferably being present as oxidic material selected from lithium and potassium aluminosilicates.

Inventors: PITTS, FRANK
Applicants: ENGELHARD CORPORATION
Application year: 1985
Main classification: B01J29
IPC codes: C22B3, C10G25, C22B34, C01G31, B01J29, C22B7, C01G53, B01J21