Process For Recovering Precious Metals From Molecular Sieve Bodies

Abstract

Precious metals such as those of the platinum group can be effectively recovered from crystalline aluminosilicate supports, for example from spent catalysts, without appreciable degradation of the crystal structure by ion-exchange using a base metal ion containing medium and subsequent sequestration of the precious metal in elemental form on a nonionic cross linked borane reducing resin.

Claims

1. A process for recovering precious metal from a crystalline aluminosilicate-based molecular sieve support containing the same ionic form, the process comprising contacting said molecular sieve under ion-exchange conditions with an aqueous solution of at least one metal cation substantially unreactive with a nonionic borane reducing resin, said resin comprising a solid cross-linked copolymer containing a plurality of amine- or phosphine-borane adducts, to produce an aqueous solution containing precious metal cations, recovering the crystalline molecular sieve and contacting said solution with said nonionic borane reducing resin at a temperature of from about 20° C. to about 35° C. and at a pH of greater than 1 but less than about 8 to reduce and sequester the precious metal cations as elemental values within said resin, and recovering the precious metal from said resin.

2. The process according to claim 1, wherein the amine- or phosphine-borane adduct is of the formula ##STR00006## wherein R1 and R2 are severally (a) hydrogen, (b) (C.sub.1-C.sub.8) optionally substituted alkyl groups, (c) (C.sub.6-C.sub.8) optional LY substituted aryl groups, (d) (C.sub.7-C.sub.12) optionally substituted araalkyl groups, and “Z” is phosphorus or nitrogen.

3. The process according to claim 2, wherein the sieve support comprises an aluminosilicate zeolite.

4. The process according to claim 3, wherein recovering the precious metal from said resin comprises recovering a platinum group metal have an atomic number greater than 44.

5. The process according to claim 1, wherein the temperature is between 20° C. and 30° C.

6. The process according to claim 1, wherein the pH is between 2 and 4.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0011] The process of the present invention takes advantage of the unique selectivity for reducing precious metal ions which is possessed by a particular class of nonionic borane reducing resins. These compositions are known in the art to be useful as reducing agents for certain metal ions, aldehydes, ketones, alkenes and the like.

[0012] Particularly preferred for use in this invention are the resins characterized and the method for their preparation described in U.S. Pat. No. 4,223,173 issued Sep. 16, 1980 to L. Manziek, the disclosure of which is incorporated by reference herein in its entirety. In general, these nonionic cross-linked reins have the general formula

##STR00001##

wherein “Q” represents a group having the formula

—(CH.sub.2).sub.m-T-(CH.sub.2).sub.n—

and wherein “m” and “n” are severally integers from 0 to 3, and “T” represents the groups

##STR00002##

wherein R.sup.1 and R.sup.2 are severally (a) hydrogen, (b) (C.sub.1-C.sub.8) optionally substituted alkyl groups, (c) (C.sub.6-C.sub.8) optionally substituted aryl groups, (d) (C.sub.7-C.sub.12) optionally substituted araalkyl groups; and “Z” is phosphorus or nitrogen.

[0013] The preferred nonionic borane resins of this invention are those wherein “T” in the general formula above is the group

##STR00003##

wherein “Z” is nitrogen, and R.sup.1 and R.sup.2 are severally hydrogen, unsubstituted alkyl groups having from 1 to 4 carbon atoms, or unsubstituted aryl groups, particularly phenyl.

[0014] In general, the borane reducing resins are prepared by protonating a cross-linked resin having functional groups

##STR00004##

as defined hereinabove, using a strong mineral acid such as hydrochloric, phosphoric or sulfuric. Preferably, hydrochloric acid is used in at least a stoichiometric quantity with respect to the weak base moieties of the resin, i.e.,

##STR00005##

of the starting resin. The protonated reaction product is then reacted with a borohydride salt such as sodium-, lithium- or potassium borohydride dissolved in an appropriate organic solvent such as methanol or ethanol. The temperature conditions of the two reactions are not narrowly critical, but are preferably and advantageously at or near ambient room temperature. Details of the preparations are set forth in the aforesaid U.S. Pat. No. 4,223,173.

[0015] The precious metal-containing crystalline aluminosilicate molecular sieves suitably treated in accordance with the present invention include the well-known zeolitic molecular sieves and the PO-4 containing aluminosilicates, i.e., the so called SAPO class of molecular sieves, both types exhibiting significant ion-exchange capabilities. The zeolitic molecular sieves comprise a group of several hundred known naturally occurring and synthetically produced species which range in Si/Al.sub.2 molar ratios from 2.0 up to several hundred. At the lower end of this scale are the widely used zeolite A, zeolite X and zeolite Y of the synthetic species, and clinoptilolite, chabazite and erionite of the naturally occurring minerals. At the high end are the synthetic zeolites prepared using organic templating agents. These include ZSM-5, ZSM-20, ZSM-34, ZSM-38 and zeolite beta as well as the silicon-substituted or alumina-extracted forms of lower Si/Al zeolites such as LZ—IO (steam and acid extracted zeolite Y), LZ-210 (Si-substituted zeolite Y) and LZ-211 (Si-substituted mordenite). Typical of zeolitic molecular sieves suitably treated by the process of this invention are those reviewed by E. M. Flanigen in Pure and Applied Chemistry, Vol. 52, pp. 2191-2211 (1980). Another comprehensive review of natural and synthetic zeolites appears in “Zeolite Molecular Sieves”, D. W. Breck, published by Wiley-Interscience, New York 1974.

[0016] The SAPO molecular sieves comprise the class of silicoaluminophosphate compositions described in U.S. Pat. No. 4,440,871 and the numerous subclasses thereof in which the crystal structure of the compositions contain one or more other tetrahedra 11 y and/or octahedrally coordinated metal oxide units of metals such as iron, magnesium, cobalt, zinc, chromium, gallium, germanium, manganese and titanium. These compositions are well known in the art and have been discussed in detail in many patent and literature references. The use of precious metal-loaded SAPO or SAPO-based molecular sieve catalysts in hydrocarbon conversion reactions such as reforming and dehydrocyclization are disclosed in U.S. P. 4,741,820 and U.S. P. 4,499,315. As adsorbent bodies of the type produced by the precious metal recovery process of this invention, these molecular sieves are found to be useful, for example, in the purification of organic feeds tocks as disclosed in U.S. Pat. No. 4,899,016.

[0017] In the precious metal recovery procedure, the metal-loaded molecular sieve is first contacted with an aqueous solution containing metal cations, or complexes of said cations, substantially unreactive with a nonionic borne resin as determined by the following procedure: A small sample of the resin, ordinarily about 0.1 gram, is placed in a vial to which a concentrated solution preferably aqueous, of the metal ion or complex in question is added. The vial is then sealed and permitted to stand for an extended period of time, typically about 3 weeks, to ensure adequate contact between the solution and the resin.

[0018] A substantial reaction is determined by any appropriate analytical means which can include visual observation, i.e., to detect a change in color of the resin, gravimetric analysis to detect an increase in weight of the resin, or contact, of the resin with a solution of a metal ion or complex, such as AuCl.sub.4.sup.−, known to be reactive with the resin and determining the capability of the resin to further react with such a reagent.

[0019] Metal ions known to be substantially unreactive toward the borane resin used herein are Na+, Li.sup.+, K.sup.+. Mg.sup.+2, Ca.sup.+2, Cr.sup.+3, Cr.sup.+6, UO.sub.2.sup.+, Mn.sup.+2, Fe.sup.+3, Co.sup.+2, Ni.sup.+2, Cu.sup.+2, Zn.sup.+2, Cd.sup.+2, Sr.sup.+2, Pb.sup.+2, TI.sup.+, and Pb.sup.+4, It is particularly preferred that the solution initially contacting the precious metal-loaded molecular sieve contain at least Na.sup.+ or K.sup.+ cations because of the favorable ion-exchange properties these ions exhibit with respect to molecular sieves in general.

[0020] The concentration of these non-reactive cations in the contacting solution and the proportions of molecular sieve and solution are not critical, but at least stiochiometric quantities of the base metal ions are advantageously present.

[0021] Very low concentrations contribute to the effectiveness of removal of the precious metal cations from the starting molecular sieve. Depending upon the precise chemical composition of the starting molecular sieve, the base metal cations can be derived in whole or in part from the molecular sieve itself.

[0022] The solution of base metal cations can also contain non-metallic cations, particularly H.sup.+ or NH.sub.4.sup.+, which facilitate the extraction of precious metal values from the molecular sieve, but such non-metal cations should not be present in sufficient concentrations to cause significant destruction of the crystal structure of the molecular sieve, i.e., ion-exchange conditions should be maintained.

[0023] It will be understood by those skilled in the art that the stability of the crystal structure of the various molecular sieves toward the treatment with ion-exchange solutions varies greatly among the various species.

[0024] Optimum reaction conditions can readily and routinely be determined, however, by even those relatively unskilled in the zeolite art.

[0025] It will be further understood that as used herein the term “ion-exchange conditions” concerns not only the exchange of zeolitic cations but also the exchange of precious metal cations present in the molecular sieve internal cavities in the form of non-zeolitic molecular complexes, salts, and the like.

[0026] As used herein, the term “precious metal” refers to silver and gold and to the platinum group metals having an atomic number of greater than 44 and which are selectively reduced by the borane resin employed in the present process, namely Rh, Pd, Os, Ir and Pt.

[0027] The contact of the ion-exchange solution with the starting molecular sieve composite is maintained for a period of time sufficient to produce a solution containing the desired precious metal values in ionic form. Thereafter this solution, before or after isolation from the molecular sieve, is contacted with the nonionic borane reducing resin whereby the precious metal ions are reduced to elemental metal and sequestered by the resin.

[0028] Ordinarily, the molecular sieve is removed from the solution prior to contact by the borane resin, thereby avoiding the necessity for separating the two solid phases before recovery of the precious metal from the resin is carried out.

[0029] Moreover, while the resin is hydrolytically stable at very low pH conditions, i.e., pH=1 or even lower, the molecular sieve can be unstable at such conditions and must, therefore, be isolated from the system when necessary to preserve its structural integrity.

[0030] On the other hand, the borane resin is found to be much more effective in precious metal ion reduction at pH conditions in the range of 6 to 8, particularly pH=7, than at lower pH conditions. Under these conditions it is not absolutely essential to isolate the molecular sieve from the system, but the resin particles must be separated from the molecular sieve crystals before recovery of the elemental precious metal from the resin is carried out.

[0031] The hydrolytic stability, and hence the reducing capacity, of the resin is also significantly affected by the temperature of the solution being treated. Ambient room temperatures of from about 20° C. to 30° C. are much preferred in the precious metal reduction stage. A temperature of about 23° C. to 25° C. is especially preferred.

[0032] Isolation of the sequestered precious metal from the borane resin can readily be accomplished by calcination at elevated temperatures sufficient to thermally destroy the resin. Calcination temperatures of 500° C. to 800° C. are suitably employed. In the reduction of the precious metal ions, the BH.sub.3 adduct of the resin is converted to boric acid and removed from the resin by solution in the treated solution. BH.sub.3 moieties remaining on the resin can result in the production of borate glass during calcination, an occurrence which is advantageously avoided by removing any remaining BH.sub.3 functionality via reduction with and aldehyde or a ketone, for example.

[0033] The invention is illustrated with reference the following example.

Example 1

[0034] (a) An acrylic-based amine-borane reducing resin is prepared in accordance with the teachings of U.S. Pat. No. 4,311,812, the disclosure of which is incorporated by reference herein in its entirety. A 50 gram sample of an acrylic based macroreticular weak base resin having a weak base capacity of 5.4 meg. of weak base per gram of dry resin is stirred for 5 hours with an aqueous hydrochloric acid solution containing 360 meg. of HCL. The resin is washed with deionized water to a neutral pH, then with two 300 ml portions of acetone and then vacuum dried at 50° C. for 8 hours. A 52.8 gram portion of the dried resin is added to a 500 ml round bottom flask equipped with a sealed mechanical stirrer, pressure compensating dropping funnel and mineral oil bubbler. A solution of 10 grams sodium borohydride in 250 ml. of dry N, N-dimethylformamide is added rapidly with continuous stirring at room temperature until no further hydrogen is evolved. The N, N-dimethylformamide is removed by filtration and the remaining resin is backwashed with deionized water until the wash water is chloride free. The resin is vacuum dried at 30° C.

[0035] (b) A spent palladium-loaded catalytic mass used in the hydrocracking of a mineral oil feedstock is treated initially under ion-exchange conditions to extract the palladium values by contact at 25° C. with an aqueous solution containing sodium and magnesium cations and having a pH of about 7. The catalyst was initially prepared by ion-exchanging a sodium zeolite Y having a Si/Al.sub.2 molar ratio of 4.8 to reduce the Na.sub.2O content to about 1 weight percent. The zeolite was then back-exchanged with magnesium cat ions to the extent that its MgO content was about 3 weight percent. This product was slurried with water containing 20 weight percent alumina gel and sufficient palladium tetramminochloride to introduce 0.5 weight percent palladium into the final product. The wet filter cake from the filtered slurry was dried and calcined at 930° F. over a five hour period. The crystallinity of the zeolite catalyst support, originally at about 90 percent as a consequence of the hydrothermal abuse incurred during use in the hydrocracking process, is only slightly further reduced to about 85 percent as a consequence of the ion-exchange palladium removal step. Thereafter the zeolite is recovered by filtration and the palladium-containing medium passed through a fixed bed of the borane resin particles of part (a) hereof at a temperature of 25 degrees celsius and a pH of 7.0. The pure palladium metal reduced and sequestered on the borane resin is recovered by destructive calcination of the resin at 750 degrees centigrade.

[0036] The Overall Processes for Recovery of Precious Metal from Spent Molecular Sieve Catalyst.

[0037] This invention describes the recovery of either palladium or platinum from spent Molecular Sieve Catalyst (MSC) which is carried out hydrometallurgically. The spent MSC is first stripped of all Coke deposits through burn-off in a reactor at a temperature of 800 to 900 degrees Celsius. The pellets are then ground to a mesh size of 10 to 50 microns whereupon the powdered material is fed into an acid solution, at a temperature of 80 to 100 degrees Celsius. After initial dissolution of the precious metal the solution is brought into contact with Amborane® resin pellets in such a proportion that 1 kg of resin will absorb approximately 0.75 kg of precious metal. Thus 100 kg of MSC containing 0.5% PD or PT metal will be brought into contact with 0.67 kg of Amborane® resin.

[0038] After a contact time of 15 minutes the mixture of MSC and Resin is removed from the reactor. The larger particle Resin is separated from the mixture by simple screen separation, is washed and then air dried. After drying is complete, the Resin is incinerated in an oven at 750 degrees centigrade. After the incineration is complete the Platinum or Palladium metal is then removed from the furnace as a granular powder.

[0039] The MSC plus acid solution is then filtered to remove the undissolved Molecular Sieve carrier, now free of precious metal. After washing and drying of the residual Molecular sieve, this de-aluminated Molecular Sieve is available for further use as a fresh catalyst material.