PROMOTED POROUS CATALYST

Abstract: A novel precious metal doped porous metal catalyst is disclosed. The precious metal is present in from 0.01 to 1.5 weight percent and distributed throughout the particles of porous metal to provide a surface to bulk ratio distribution of not greater than 60. The present invention is further directed to a process of forming said doped catalyst and to improved processes of catalytic hydrogenation of organic compounds.

Description: PROMOTED POROUS CATALYST BACKGROUND OF THE INVENTION The present invention is directed to a new catalyst product and to a process of reducing organic compounds using said product More specifically, the present invention is directed to porous base metal catalyst product having at least one piecious transition metal dopant distributed on the surface aiea of the catalyst such that the suitace to bulk latio of dopant has a distinctly low value, as fully desciibed herein below The piesent doped catalyst pioduct has been found to exhibit high catalytic activity and extended catalytic life compared to previously achieved values Hydrogenation catalysts based on highly porous nickel materials are well known Such materials are part of a family of metal alloy deπved products sold by W R Grace & Co -Conn under the trademark "Raney®" These porous materials, when microscopically viewed, take on a sponge-like appearance having tortuous pore channels throughout the nickel metal particle Thus, such materials are geneπcally viewed as porous or spongy metal alloy products. The metal alloy is generally composed of a major amount of a base metal selected from nickel, cobalt or copper with minor amounts of aluminum and other metals such as iron, chromium or molybdenum, as deemed appropriate foi a particular application The porous base metal catalyst product is normally referred to in terms of the metal which is the majoi component of the spongy metal product These high surface area products have been found to have sites for hydrogen activation and. thus, exhibit catalytic activity when used in hydrogen reduction reactions. It is known that the activity of spongy base metal catalysts can be enhanced ("promoted") by the incorporation of small amounts of certain transition metals For example, French Patent 913.997 proposed incorporating chromium in up to 3.5 percent based on the content of nickel present in a Raney nickel cataly st Promotion of catalysts w as initially accomplished using ti ansition metal elements which are readily available commodity metals, such as iron, molybdenum or chromium These metals could be used in large amounts without causing a detrimental economic limitation to their commercial usefulness In genei al, porous base metal catalysts, such as porous nickel catalysts aie formed by first producing a base metal-aluminum (piefeired) or base metal-silicon alloy using conventional metallurgical techniques The foi med alloy is gi ound into a fine powder and classified by passing it thiough a sieve to provide a material having a desired particle size which is normally less than 500 microns and, preferably less than 75 microns Largei particles are l ecycled for further grinding The alloy powdei is then treated with a base to leach out a substantial amount of the aluminum metal or silica present The base may be selected from eithei an inorganic (preferred) oi organic compound For example, in conventional processes an aqueous solution having from about 5 to 50 weight percent concentration of an alkali metal hydroxide (e.g., sodium hydroxide) is employed as the leaching agent. The treatment of the alloy is usually carried out at elevated temperatures of from about 40°C to 1 10°C The alloy powder can be directly added to the alkali solution oi it can be foi med into an aqueous suspension which is then contacted with the alkali solution The aluminum contained in the alloy dissolves to form an alkali metal aluminate (e.g., sodium aluminate) with vigorous evolution of hydrogen. When silicon is in the alloy, the base forms the corresponding alkali metal silicate The powder and alkali are normally allowed to remain in contact with each other tor several hours at elevated temperatuie (e.g., 40°- 1 10°C) until the aluminum ι oι silicon) content is reduced to the desired level The crude porous catalyst is separated from the reaction liquor and then conventionally washed with watei until the wash water has a slightly alkaline pH value of about 8 The poie volume, pore size and surface area of the leached alloy will depend upon the amount of aluminum (or silicon) in the initial alloy and the degree of leaching The nature of the poiosity of the resultant base metal catalyst is one of tortuous pores thi oughout the volume of the catalyst particle The resultant product normally has a pore volume (BET) of from about 0 05 to about 0 3 cc/g; an average pore diameter ranging from about 50 to 500 Angstroms; and a surface area (BET) of at least 10 m7g, preferably ranging from about 20 to about 150 m 2 /g The iesultant porous base metal pi oduct has been used as a hydi ogenation catalyst to cause reduction of organic compounds, such as, tor example, nitioorgamcs. to then corresponding amine compound In older to tuithei enhance the catalytic properties of such porous pioducts, the addition of piomoter metals, such as Group VIII transition metals (e.g., iron or chromium), has been previously accomplished by (0 adding the promoter metal to the base metal and aluminum (oi silicon) when metallurgically producing the initial alloy, (n ) adding a salt of the promoter metal to the alkali leaching solution; or (in) contacting the leached or leached and washed porous base metal catalyst with a salt solution of the promotei metal The process of adding promoter metal to the base metal during alloy foimation, as disclosed in U S. Patent 3,781.227, has certain limitations. Firstly, it can be envisioned that some of the promoter metal is "encapsulated" in the solid body or skeleton of the base metal and not on the surface area of the resultant catalyst. In this form, the promoter metal does not cause a direct enhancement of the hydrogenation catalyst sites which are located on the surface aiea of the highly porous material Furthei , a portion of the promoter metal may be removed during any one or all of the steps requned to form the porous alloy Thus, large amounts of a promoter metal are normally added duπng alloy formation to compensate for any loss during processing and through encapsulation Because of the possible loss of promoter metal during processing and the inefficiency of encapsulated promoter metal, the alloy- addition method is not consideied appiopnate when the metal is a costly transition metal, such as platinum, palladium, osmium, ruthenium or the like Alternately, promoter metals have been added to the alkali leaching solution (see Great Britain Patent 1.1 19.512 and U.S. Patent 3,326.725) in attempts to enhance resultant poious nickel's catalytic activity The leaching solution is normally an alkaline aqueous oi aqueous-alcoholic solution In geneial, the promotei metal is intioduced as an acid salt, such as a hahde salt. In most instances, the leach solution does not maintain the piomoter metal in solution but, instead, causes it to plate out on the outer shell of the porous base metal particle. Thus, the resultant porous particle has the promoter metal located on only a small fraction of the particle ' s surface area Spongy nickel oi othei base metal catalysts which have been previously formed and washed by conventional processes have been subjected to dopant metals just prior to use, in attempts to promote its catalytic activity. The dopant metal is normally introduced as an aqueous or aqueous/alcoholic solution of an acid salt, such as PtCl 4 . PdCl 2 , H 2 PtCl or the like. In JACS l± 1515 ( 1949) and JACS 72 1 190 ( 1950) Levering et al disclosed the addition of an organic tertiary amine to the acid salt dopant solution These authors taught that one should use the doped spongy metal product immediately aftei the addition of dopant (without furthei washing), in order to achieve enhanced catalytic performance. Such products exhibited only slight increase in catalyst activity and substantially no improvement in their active catalyst life. It is highly desired to provide a promoted porous base metal catalyst (e.g., Raney® nickel) which exhibits high catalytic activity after storage (maintains good initial activity) and extended catalyst life duπng use (exhibits slow or delayed deactivation) Further, it is desued to provide a promoted base metal catalyst which has a precious transition metal as its promoter metal and said precious transition metal is substantially uniformly distributed as a coating on the surface aiea of the porous metal catalyst Thus, the precious transition metal is substantially uniformly disti ibuted across the particle diameter of said catalyst Still furthei it is desned to pi ovide a piecious ti ansition metal promoted porous base metal catalyst wheiein said promoter metal is piesent in up to about 1 5 percent by weight and the pi omotei metal ' s surface to bulk ratio (as defined heiein below) is less than 60 SUMMARY OF THE INVENTION The present invention provides a novel ti ansition metal promoted porous base metal catalyst The ti ansition metal is pi esent in ti oni 0 01 to about 1 5 peicent by weight and is disti ibuted thi oughout the sui face aiea of said porous catalyst so as to have a sui face to bulk distribution of not greater than 60 The present invention furthei provides a novel method of forming said precious transition metal promoted porous base metal catalyst Finally. the present invention provides an improved process for hydrogenation of organic compounds utilizing said catalyst DETAILED DESCRIPTION The following defined terms are used in this specification and appended claims "Base metal" refers to metals of iron, nickel, cobalt, copper and mixtuies thereof which are used to form porous oi spongy metal catalyst products These metals may be combined (e g , alloyed) with minor amounts of other metals (e g , chiomium, titanium, molybdenum, zinc, ziiconium aluminum) as an alloy oi co-deposited coating When more than one base metal is present in the spongy metal catalyst, all of said base metals shall be included in determining the S/B ratio, as defined below The preferred base metals are nickel and cobalt and most preferably comprises nickel alone or with minor amounts of other metals "Precious metal " refers herein to transition metals of palladium, platinum, ruthenium, rhodium, rhenium, osmium, iridium and mixtures thereof. "Dopant metal" refers to a transition metal which is distinct from the metals forming a porous base metal catalyst and is present in low concentrations in the base metal catalyst to enhance its catalytic properties (e.g., dopant precious metals, as defined below, and may also include chromium, molybdenum, titanium, zinc. iron, zironium or mixtures thereof). "Dopant precious metal" and "promoter precious metal " each refers herein to precious transition metals of Pd, Pt. Ru. Re, Rh, Ir and Os present in small quantities on the surface area of a porous, paniculate base metal for the purpose of enhancing the catalytic properties of said porous, particulate base metal. The preferred dopant transition metals are those of platinum and palladium with palladium being most preferred. "Surface volume" refers to the outer volume or shell of a catalyst particle of the present invention which is roughly the outer 50 Angstroms of the particle ' s radius (i.e., extending from the outer surface of the particle inward toward the center of the particle by about 50 Angstroms). "Surface dopant concentration" refers to the atomic ratio of dopant metal to base metal within the surface volume of a catalyst particle. "Bulk dopant concentration" refers to the atomic ratio of dopant metal to base metal for the entire catalyst particle. "Surface to Bulk Ratio" or "S/B" in respect to a porous base metal catalyst product, refers to ratio of surface dopant concentration to bulk dopant concentration. The present invention is directed to a novel hydrogenation catalyst product based on a porous base metal catalyst which has up to about 1 .5 weight percent of a precious transition metal selected from palladium. platinum, rhodium, ruthenium, rhenium, indium or osmium or mixtures thereof coated on the surface area of said catalyst and having said precious tiansition metal of sufficiently low concentration in the particle ' s surface volume to provide a surface to bulk ratio. S/B. of less than 60. The present catalyst is particularly useful in reducing nitroaromatics to their respective amine derivatives. The present catalyst is based on porous, paniculate base metal catalyst product, preferably a nickel metal (e.g.. Raney® nickel) product. The present invention shall be described by using a porous, paniculate base etal product wherein the base metal is composed of nickel It is to be understood that othei porous, paniculate base metal products (Co, Cu, Fe) can be substituted and used to form the present improved catalyst and the process of hydiogenation using the same. The porous base metal (e.g., nickel) catalyst product is formed by conventional techniques. For example, a nickel/aluminum alloy is initially formed by a pyrometallurgical process to provide an alloy having from about 30 to 60 (preferably from about 42 to 56) weight percent nickel and from about 70 to 40 (preferably from about 58 to 44) weight percent aluminum. Small amounts of other base metals may, optionally, be present. The alloy is crushed and ground into particles having an average particle size of less than 500 micron diameter, preferably less than 75 micron diameter. The powder product is activated by leaching the aluminum from the alloy with an alkali solution, such as an aqueous solution of sodium hydroxide (preferred) or potassium hydroxide. The alkali is used at concentrations of greater than about 15 weight percent, preferably from 15 to 35 and most preferably from 20 to 35 weight percent. The leaching can be carried out at ambient temperature but preferably is conducted at elevated temperatures which can be as high as the boiling point of the leaching solution. Temperatures of from about 40° to 1 10°C (preferably 60° to 100°C) are suitable to cause substantial rate of leaching and remov al of the aluminum metal fi om the alloy When the piesent catalyst is contemplated toi use in fixed bed leactors. the porous, paniculate base metal pioduct may have an average particie size diameter (or laigest dimension) of from about 0 1 to 0.8 cm The alloy is leached with an alkali solution described above having an alkali concentration of from about 5 to 35 weight percent, preferably from about 5 to 20 weight percent The leaching is normally carried out at elevated temperatures of fiom about 30° to about 90°C. preferably from about 30° to 50°C The lesultant poious participate catalyst pi oduct is composed of base metal, such as nickel and, optionally, minoi amounts (up to about 15 wt percent preferably up to about 12 wt percent) of othei transition metals as well as residual aluminum It is to be understood that the term "base metal" and the like used to described and define the spongy metal catalyst herein and in the appended claims shall mean (unless specifically stated otherwise) a metal product composed of a major amount (at least about 85 wt percent) of a single base metal oi a mixture of base metals (normally one base metal is in majority) which has a minor amount (up to about 15 wt percent, preferably up to about 12 wt. percent) of other metal(s) such as chromium, titanium, molybdenum, zinc, zirconium or mixtures thereof as well as with residual aluminum. The product has a high degiee of tortuous pores throughout each of the particles to provide a high surface aiea poious paniculate catalyst pi oduct This pioduct is washed with water to remove the aluminate by-pioduct Total removal of the aluminate is not required. The washing is conducted with water having a temperature of from ambient to about 60°C, preferably between 30 and 45°C It is preferred that the washing be conducted under an inert (e.g., N 2 oi Ar) atmosphere oi one having a dilute concentration (2-8%, preferably 3-5%) of hydrogen The resultant particulate product normally has a poie volume (Nitrogen-BET) of from about 0 05 to about 0 3 cc/g. an avei age pore dia etei ianging from about 50 to 500 Angstroms, a surface aiea (BET) of at least 10 m7g and prefei ably l anging from about 20 to about 150 m7g and an average particle diametei of less than 500 microns preferably of less than 75 microns oi , when contemplated tor use in fixed bed reactoi s of fiom about 0 1 to 0 8 cm In the instant inv ention washing is continued until the effluent wash water has an alkaline pH of fiom at least 8 to about 12 w ith from 9 to 12 being pi efeπed and fiom 10 to 1 1 5 being most pi etei red The alkalinity of the aqueous sluπy containing the porous base metal catalyst mav be substantially the same as the alkalinity of the dopant precious metal solution to be used to from a doped catalyst, as described heiein below The poious base metal catalyst is tieated w ith an alkaline solution of a basic salt of the dopant piecious metal to pi ov ide the catah st oi the piesent invention The salts found useful in pioviding the unique catalyst are alkaline salts represented by the general formula (A) X MY } wherein A iepresents a cation or ligand selected from ammonia, ammonium, or an alkali metal such as sodium, potassium or the like or mixtures thereof, M represents a precious transition metal, as defined below, Y represents an anion selected from hahde, hydioxide, oxide, cai bonate bicarbonate, nitrate sulfate oi a C |-C 4 cai boxylate, and x and y represent integei s of from 1 to about 6 to pi ovide a neutral (charge balanced) salt product A is prefei ably selected fi om ammonia or ammonium and most pieferably selected fiom ammonia oi if A is an alkali metal it is preferably selected from sodium The salt should be soluble in water oi alcohol or mixtures thereof and cause the solution to exhibit an alkaline pH of from 8 to 12, pietei ably from 9 to 1 1 5 and most preferably from 9 5 to 1 1 5 Examples of such salts aie (NHAPtCAnH.O (NHAPd(NOA-nH 2 0. (NH-,) Pt(NO, ) ..H 2 O [Pt(NHA][PtCl 4 ], (NHARuCk, NH 4 ReO 4 . (NHARe0 4 KReO 4 NaReO 4 , [Rh(NHACl]Cl 2 , (NH 3 ) 4 PtCl 2 , K 2 Osθ4.nH 2 O, and the like The symbol "n" can be an integer of 0 to 4 The precious tiansition metal (M) of the basic salt is selected from Pd, Pt. Ru. Rh. Re. Ii and Os and mixtuies thereof with Pd and Pt being preferred and Pd being most pieterred It has been found that the piesently described precious tiansition metals provide high catalytic activity and extended catalytic lite when plated in very low amounts on the surface area of a porous base metal particulate material according to the present invention The porous, particulate base metal catalyst is doped with the precious transition metal according to the present invention by contacting an alkaline sluπy of the porous base metal material with an alkaline solution of a piecious metal salt Alternately, one can add the solid salt dnectly to the affected slurry wheieupon it dissolves to form the combined alkaline solution and sluπy The salt should be used in an amount such that the weight concentration of dopant transition metal in the resultant doped catalyst is from 0 01 to 1.5%, preferably from 0.05 to 1 % and most preferably from 0 1 to 0 5% by weight based on the weight of the porous base metal catalyst The exact amount of salt used will depend on the degiee of doping desired in the finished catalyst Normally, the alkaline salt should be added to water or watei -alcohol to provide a solution of salt wherein the salt concentration is from about 5 to 40 (pieferably 10-30) weight percent The poious base metal catalyst may, in addition to the piecious transition metal dopant, be doped with a non-precious metal dopant selected from iron, chromium, molybdenum, titanium, zinc, vanadium, znconium or mixtures thereof. They may reside as a coating on the surface in the form of a dopant metal in its zero valence state oi in an oxidized state These dopant metals may be present in up to 3 weight percent (preferably fiom 0.2 to 3 weight percent, most preferably from 0 5 to 2 weight percent) of dopant metal based on the weight of the porous base metal catalyst They are added by conventional processes using dopant metal salt solutions The doped base 0/67903 ' ' ' " PCT/US00/12O86 metal catalyst must also be doped with a dopant precious metal, as descπbed herein The alkaline precious metal salt solution is contacted with an aqueous slui ry of the powder porous base metal catalyst, previously formed as desci ibed above, toi a sufficient time to allow substantially complete plating out of the precious tiansition metal onto the surface area of the base metal catalyst The exact length of time will depend on the particle size, and specific porosity of base metal used, the pH of the solution and the concentration and particular precious transition metal present Normally, the porous base metal catalyst and the alkaline precious transition metal salt are maintained in contact in the slurry foi an extended period of time such as fiom about 10 to 60 minutes or longei with from about 15 to 45 minutes being preferred The temperature at which this is conducted is not cntical and can be, tor example from room temperature to about 80°C such as from 30-45°C. The spent solution is then separated from the doped catalyst. The doped catalyst must then be washed until the wash solution is free of precious transition metal. The wash solution should be an aqueous solution (preferred) or an aqueous-alcoholic (C| -C^ alkanol) solution Dui ing the washing a majority of by-product salts (e.g , NHjCl, NaCl) are removed The washing should continue until the solution containing the doped catalyst has a pH of at least 0.25, preferably at least 0.5 and most preferably at least 1 (e.g., 1 .5), unit lower than the alkaline pH at which the porous base metal catalyst and the alkaline precious transition metal dopant salt aie contacted The pH can be reduced by washing the doped catalyst with watei oi water-alcohol solutions (preferred) and/or by the addition of an acidic agent oi a butfei agent to cause the resultant slurry to have the desired pH It is pieterred that the aqueous suspension of doped catalyst resulting fiom the washιng(s) have a resultant pH of from about 8 to 9 5, preferably 8 to 9 It is preferred that the pH of the doping slurry be high (e.g., 9 5- 12) and that the aqueous slurry of doped catalyst is at least 1 unit lowei after washing When the base metal catalyst and precious transition metal dopant aie contacted in an alkaline sluπy having a pH of 8 to 9.5. the product should be washed with at least 25 parts (e.g., from 25 to 100 parts) of watei for each part by weight of doped catalyst solid The wash water may be of neutial pH or slightly alkaline by the addition of a base such as NH 4 OH, NaOH or the like. The washing can be optionally followed by an alcohol (C|-C 3 alkanol) or water-alcohol wash. The resultant doped base metal catalyst is normally stoied as an aqueous slurry until use. In addition to washing, or in lieu thereof, the doped catalyst can be removed from the spent dopant solution and soaked in watei 01 an aqueous alcoholic (C|-C 3 alkanol ) bath for at least 12 houi s. preferably at least one day prior to use. This aging has been found to aid in achieving a highly desired catalyst of low S/B ratio. It has been found that the doped catalyst product formed in the manner described above can be stored for an extended period of time of from one day to six months or greater pnoi to use without losing its catalyst activity. In addition, the doped catalyst product foi med in the manner descπbed above exhibits extended catalytic active life during use when compared to conventional catalyst products of the same material. It is believed, though not meant to be a limitation on the subject invention, that solutions of the present precious transition metal salts are capable of penetrating into the pores of the base metal catalyst wherein precious metal electrochemical ly plates out when reduced by the base metal itself and/or by a traction of the surface hydrogen of the base metal material In addition, it has been found that beyond the removal of undeposited species, the final washing and/or soaking of the precious transition metal doped porous base metal catalyst also aids in providing a more homogeneous or even distribution of precious transition metal throughout the surface area of the product. The immediate use after addition of the dopant salt does not allow the full migi ation of the dopant to the interior of the particles, w hile the present more time-extended process completes this migration to a final, more stable configuration Removal of undeposited species by washing also makes tor a chemically enhanced product which is more compatible with a vaπety of hydrogenation processes and has been shown in some processes to lead to superior activity. As stated previously, the doped catalyst of the piesent invention is a highly porous particulate product in which the pores are of a tortuous nature throughout each of the particles to provide a high surface aiea doped catalyst product. The surface area as used herein and in the appended claims is all areas assessable to nitrogen and measured by the Nitrogen-BET method. The term "surface" as used herein and in the appended claims shall be surfaces of the tortuous pores throughout said particles and of the particles, per se. The presently produced precious transition metal doped poi ous base metal catalyst has been found to have a more homogeneous or even distribution of precious transition metal throughout the surface area of each particle of the porous base metal catalyst. This can be described in terms of the atomic ratio of the precious transition metal to base metal as a function of the cross-section of the catalyst particles. This distribution can be readily measured by x-ray photoelectron spectroscopy ("XPS") or electron spectroscopy for chemical analysis ("ESCA") Anothei technique to determine the atomic ratio of the metals is transmission electron microscopy ("TEM"). ESCA analytical method simultaneously measures the outer surface volume or skin to a depth of about 50 A of a large number of particles. Thus, an atomic ratio of dopant metal to basic metal in the surface v olume of the particles can be measured and when compared to the bulk chemical analysis one can determine the amount of dopant enhancement at the surface versus the overall amount of dopant It has been found that with respect to the present doped catalysts, the amount of dopant enhancement in the surface volume is low and thus the amount of dopant metal residing in the internal v olume (between about 50 A to the center of a particle) is proportionately higher than that of kno n doped porous catalysts Pπoi known doped catalysts are products where the dopant metal is very highly concentrated in the outer surface volume and, conversely, the dopant metal is in a very low concentration in its internal volume. The ratio of surface concentration to bulk concentration of the dopant precious metal (referred to herein aftei and in the appended claims as 'S/B ratio") can be ieadily determined by ESCA analysis and bulk analy sis of a product The S/B ratio of the precious transition metal doped base metal catalyst of the piesent invention is less than about 60. with S/B ratios of about 10 to 50. preferably 10 to 40 being attainable. All ratios within this range of 10 to 60 being encompassed herein by this statement. In contrast, porous base- metal catalysts conventionally doped with equivalent amounts of precious metal have S/B ratios which are a multiple factoi highei Thus, it one were to plot a concentration of precious transition metal across the particle diameter, one would obtain a curve less steeply peaked at the edges (outer 50A) for the piesentiy doped catalyst product than for conventionally formed catalyst product having the same degree of dopant precious metal. The subject doped catalyst, especially the preferred doped nickel catalyst, has been found to exhibit improved catalytic activity of from about 1.2- 1.8x greater than the conventional doped catalyst and over conventional doped base metal derived alloy catalysts as shown by comparative examples herein below The doped catalyst product of the present invention can be described as a porous, base-metal catalyst material. It is composed of a major amount (up to about 85 wt%) of a base metal, e.g. Ni, Co. Cu. or Fe. and minor amounts of up to about 15 wt. percent, preferably up to about 12 wt percent of othei metals (than the major base metal ) selected from aluminum, chromium, iron, copper, molybdenum, tin, znconium. zinc, titanium, v anadium or mixtures thereof. The porous base metal catalyst has a precious metal dopant selected from Pt. Pd, Ru. Rh. Re, Ir. Os or mixtures thereof in up to about 1 .5 wt. percent (e.g.. 0.01 to 1 .5), preferably from 0.05 to 1 . such as 0. 1 to 0 9 and most preferably from 0. 1 to 0.5 wt. percent (and all ranges included within said range of 0.05 to 1 .5 wt percent) The dopant piecious transition metal is coated on a portion of the surface area of said poious base metal and is distributed within the particles with respect to their diameter so that its S/B ratio is less than 60. such as from about 5 to about 60, pref erably less than 50, more preferably less than 40 and most preferably less than 35. The lower the S/B ratio the more preferred is the resultant catalyst. The product of the present invention is formed by the process of contacting a solution of an alkaline salt of the precious transition metal which may be described by the formula A,MY, wherein each of the symbols A, M, Y, x and y are defined above, with an alkaline slurry of a porous base metal catalyst. The slurry, at a pH of from 8 to 12. preferably from about 9 to 1 1.5, is contacted with an alkaline salt solution, as descπbed above, for a period of time to allow substantially all of the precious transition metal of the salt to become coated on and adhered to portions of the surface area of said porous base metal catalyst. The product of said contact is then washed until the wash solution is essentially tree of dopant metal and has a pH which is at least 0.25 unit lower than the pH of the doping slurry. Alternately or in addition to the pH adjustment (preferable) the washing is conducted with at least 25 wt. parts of water for each wt. part of solid product. The doped base metal catalyst of the present invention is aged in an aqueous or aqueous-alcoholic solution tor at least 12 hours preferably one day prior to use The washed product is maintained in an aqueous or aqueous-alcoholic bath until use. The doped catalyst product of the subject invention is useful as a hydrogenation catalyst. The present product has been found to have high catalytic activity and provide extended catalytic life when compared to conventional porous base metal catalysts which have the same dopant. The present doped catalyst products have S/B ratios which aie substantially lower (more uniform doping) than conventional products. The piesent invention further provides for improved catalytic hydrogenation reduction processes conducted in the presence of the above- described doped catalyst. Said processes include all hydrogenation reactions which are carried out with porous base metal catalysts, such as Raney® nickel catalysts. Examples of such reactions are descπbed in Skeleton Catalysts in Organic Chemistry by B. M. Bogoslawski and S.S. Kaskowa and in Use of Nickel Skeleton Catalysts in Organic Chemistiy VEB Deutsches Verlag dei Wissenschaften. Berlin 1960 Pg. 40- 124, the teachings of which are incorporated herein in their entirety by reference. Accordingly, for example, the metal catalysts prepared according to the invention can be employed for the hydrogenation of unsaturated hydrocarbons with an ethylenic and/or triple bond, or of diene systems, of aromatic compounds, such as, foi example, benzene, naphthalene, diphenyl and their derivatives, or of anthraquinone and phenanthrene, of heterocyclic compounds with nitrogen, oxygen or sulfur atoms in the ring system, of carbonyl groups, of carboxyl groups or their esters, of carbon-nitrogen compounds, such as, for example, nitriles. acid amides, oximes and ketimines, of unsaturated compounds containing halogen, sulfur, nitroso and nitro groups, of azo and azoxy compounds, of hydrazines, Schiff's bases, lmines and amines, of carbon-oxygen compounds, such as, for example, alcohols, ethers, ethylene oxides and organic peroxides and ozonides, of carbon-carbon compounds and of nitrogen-nitrogen compounds. The doped catalysts prepared according to the invention are preferably used for the hydrogenation of nitroso and nitro derivatives of aromatic compounds, unsaturated hydrocarbons, and nitriles. Foi example, nitrobenzene and nitrotoluene as well as dinitrobenzene and dinitrotoluene can be leadily reduced to their corresponding primary amine deriv ative by contacting the nitro aromatic compound with hydrogen in the presence of the doped catalyst of the present invention The reactions can be carried out at ambient temperature and pressure or at elevated temperatures of up to about 175°C, preferably between about 60°C and 150°C The reactions can be earned out at pressures of up to about 1000 psig with preferred pressures being from about 100 to about 500 psig. It has been unexpectedly found that the present doped catalyst provides very high degree of enhanced reactivity when used under elevated temperature and pressure conditions Thus, conditions of temperature of from about 130 to 175°C and pressures of from 300 to 500 psig are preferred. The use of the doped catalyst of the present invention is exemplified herein by illustration of hydrogenation reduction of para- nitrotoluene. The hydrogenation may be earned out in a continuous sump phase hydrogenation apparatus, which consists of a number of reactors of customary construction connected in series, with the aid of which a hydrogen cycle is produced. Other conventional batch and continuous apparatus may be used. The catalyst of the present invention can be suspended in an aqueous-alcoholic mixture (e.g., a C Cι alkanol). Alternately, the catalyst may be of a fixed bed type (larger particle size of from about 0.1 to 0.8 cm) used in a packed bed reactor with either a liquid or vapor phase reaction mixture conventionally used. The doped catalyst of the present invention can be suspended in the hydrogenation apparatus in an ethanol/water mixture, tor example with a mixture composed of 95% by weight of ethanol and 5% by weight of water, as the solvent. A solution of para-nitrotoluene in the ethanol/water mixture is formed and to it the catalyst is added. The treatment is then carried out at elevated pressure, for example 60 to 500 psig of hydrogen pressure, and at temperatures of 75°C- 140°C. The following examples are given for illustrative purposes only and are not meant to be a limitation on the invention as defined by the claims appended hereto. All parts and percentages are by weight unless otherwise indicated. Further, any range of numbers recited in the specification or claims, such as that representing a particular set of properties, conditions, physical states or percentages is intended to literally incorporate expressly herein any number falling within such range, including any subset of numbers within any range so recited. Example I Preparation of Base Metal Catalyst A previously formed nickel-aluminum alloy composed of about 42 weight percent nickel/58 weight percent aluminum was ground into a powder having particle size of about 30-40 microns average diameter. The powdered alloy was intermittently added in small portions to a 30 weight percent sodium hydroxide solution which was preheated to 80°C prior to introduction of alloy. The weight ratio of NaOH (solid) to Al of the alloy was about 2.7: 1. The addition was carried out at a rate of about 1000 g alloy powder per hour. After completion of the addition of alloy powder, the resultant slurry was maintained at 80°C with agitation for about 4 hours. The resultant spongy nickel catalyst was separated from the slurry liquid by decantation followed by washing of the solid catalyst until the spent wash solution had a pH of about 9. The washing of the solid catalyst was carried out by cyclic addition of water at 45°C followed by stirring, settling of solids and decanting of the wash water. The resultant spongy nickel metal catalyst was stored as a 50 wt. percent aqueous slurry. Example II Precious Metal Doped Nickel Catalyst A series of nickel catalysts were prepared in the same mannei as described in Example I above except that the pH of the final wash water was varied Separate slurries were formed with pH of from 8 to 12 and each catalyst was then doped with a precious metal, as descπbed below Standardized aqueous solutions of Pd salts and of Pt salts weie formed These solutions had a pH of about 9 to 10 A series of doped catalyst were formed by introducing with agitation a portion of a standardized precious metal salt solution having a precious metal content of from 0 1 to 1 0 weight percent precious metal based on the spongy nickel catalyst (solid content) of the treated slurry The treated slurry was maintained under agitation for about 30 minutes The agitation was then stopped and the solids allowed to settle A portion of the liquid was decanted and analyzed for precious metal content The analysis showed no precious dopant metal present in the spent liquid The slurry was washed by cyclical water/decantation to a final pH of about 9 and with at least 25 parts by weight of water foi each part of catalyst product The lesultant precious metal doped spongy nickel catalysts weie stored undei watei for at least one day prior to being tested and used Table I below provides the data and descπption with respect to each of the series of samples produced. This description includes • precious metal dopant salt (PM) • dosage of dopant in the doped catalyst (% piecious metal based on nickel of spongy catalyst) • pH of dopant solution • pH of catalyst slurry befoie doping treatment • pH of catalyst sluπy after (post) doping treatment • bulk analysis (ICP) of doped catalyst • Sui face Analysis (XPS) of doped catalyst • Surface to Bulk (S/B) Ratio Bulk chemical analysis was analyzed by Inductive Coupled Plasma- Atomic Emission Spectroscopy ("ICP"). Each sample was washed with water and then completely dissolved in a mixture of HCl/NHO^ acid (3- 1 ) solution. The sum of the peicent assays determined was normalized to 100% The weight percentages tor piecious metal, nickel, and lesidual aluminum aie reported in Table I as well as the atomic i atio of precious metal to nickel The average precious metal dopant concentration at the doped catalyst particles' outer shells (surface volume) was determined by X-ray Photoelectron Spectroscopy (XPS). For each measurement, a small sample of about 0.5 g water-wet catalyst was removed from its slurry and dried in a U- shaped tube under flowing helium gas at a temperature of 130°C. The dried sample is then sealed in the tube and transported to the XPS lnstiument. The sample was introduced via an antechamber to the XPS instrument. XPS measurements were earned out on a PHI 5600 ESCA system (φ Physical Electronic). The catalyst was handled under an Argon atmosphere within an environmentally controlled glove box Moisture content was no higher than 0.40 ppm and oxygen content was generally 0.00 ppm within the glove box environment. Spectra were obtained using an aluminum x-ray source operating at 14.8 kV/25 mA energy and the detector positioned at 45° relative to the mateπal being analyzed. Instrument calibration was performed using a Cu reference standard after 10 minutes sputtering in Argon. Because the 2 p3 / 2 and 3 p3 2 photoelectron peak energies of Cu are widely separated in energy, measurement of these peak binding energies provided a quick and simple means of checking the accuracy of the binding energy scale The material was loaded as a thin layer onto double-sided tape mounted to a 1 inch diameter stainless steel stub. The stub was placed in an enclosed transfer vessel and mounted onto the intro chamber of the XPS instrument. The sample was transferred in vacua ( 10 " ' torr) into the main analysis chamber and further vacuum of 10 " ' to 10 " ' torr was achieved. A 5 minute surface scan to identify all detectable elements from 1 - 1 lOOeV was performed. Based on the findings from the survey, a 60 minute detailed scan on selected elements was performed with an energy resolution of 0. 125 eV. For convenience, the spectral data were imported into an external curve-fitting software package (MULTIPAK v2.2a). Other conventional methods can be used. All the curve-fitting and atomic concentration functions were performed using this software. Sensitivity factors for each element were automatically configured within the software and used in the atomic concentration calculations. The Surface/Bulk ("S/B") ratio was calculated as follows (e.g., with Pd and Ni as dopant and base metal, respectively): S/B ratio = surface Pd/Ni bulk Pd/Ni which is [(XPS Pd atom concentration/(XPS Ni atom concentration)] [(ICP bulk %Pd/atomic wt Pd)/(ICP bulk %Ni/atomic wt. Ni)] Example III A sample was made in the same manner as described above in Example II for Samples 2D-2F except that the base metal catalyst was nickel based having about 2 wt.% Fe and 2 wt.% Cr in the spongy catalyst. The dopant catalyst was analyzed in the same manner as described above and the results are reported as Sample 3 in Table I below. Example IV A series of catalytic hydrogenation reactions to convert 4-nιtrotoluene to 4-methyl aniline were carried out using Pd doped nickel based catalyst, as follows: 10 parts of a selected catalyst was transferred into a reaction flask, washed twice with 12000 parts of 95% ethanol/5% water (Pharmco Products) Then 12000 parts of 95% ethanol containing 500 parts of 4-nιtrotoluene (Aldπch) was introduced into the leaction flask The reaction flask was evacuated and filled with hydrogen gas. Stirring of the solution at 1200 rpm was commenced when the tempeiature leached 75°C and the pressure was at 60 psig. Each reaction was conducted in duplicate. The hydrogenation reaction was monitored using a multi-point absorption reactor system which measured the gas uptake at constant reaction pressure. This was accomplished by measunng the pressure drop in a pre- calibrated ballast reservon The system was capable of recording the parameters of reaction time, pressure, temperature and pressure in ballast reservoir. These parameters were recorded at the rate of 12 points/minute duπng the first 10 minutes of reaction and then at increments of each 1 percent pressure drop in the ballast reservoir The data obtained were plotted versus time and the reaction rates were calculated from the slope in the linear portion of the hydrogen uptake. At the completion of each reaction, ahquots of reaction solution were taken and analyzed by gas chromatography-mass spectrometry. The only two materials identified were the starting 4- nitrotoluene and the 4-methylanιhne product. The results are given in Table II below Table II Catalyst Activity 4-nitrotoluene conversion at 75°C/60 psig *source of Pd was (NH APdCAHoO Example V A series of hydrogenation reactions of 4-nitrotoluene was conducted using different combinations of temperature and pressure conditions (a matrix of Temp/Pressure combinations using 200 and 400 psig and 125°C and 140°C). The catalyst used was palladium doped nickel based catalyst (2G) described in Example II above. Each of the hydrogenation reactions were conducted using a Bench Top EZE Seal Reactor (Autoclave Engineers) which is divided into a feed section, a high pressure section and a low pressure section. The reactor was also equipped with the pressure drop sensing monitor described in Example IV above. The reactor feed section is equipped with lines for hydrogen, nitrogen and vacuum. The high pressure section of the reactor has a forward pressure regulator, a varying volume ballast reservoir and a pressure transducer. The low pressure section is in-line with the reactor and its pressure was monitored by a pressure transducer. During each reaction, the gas consumption in the reactor section caused a continuous pressure drop in the calibrated ballast reservoirs. The pressure of the ballast, the autoclave pressure, the tachometer reading, the hydrogen consumption and the reaction temperatuie weie continuously momtoied and l ecorded as described in Example IV In each reaction, 65 parts of wet catalyst (2G) was transferred into the reactor beakei , washed with 12000 parts 95% ethanol/5% water (Pharmco Products) and then the reactor was sealed, and connected to EZE reactoi . The system was evacuated and filled with hydrogen followed by the addition of 28000 parts of an ethanol solution which contains 3500 parts of 4-nιtιotoluene via a gas-tight syringe The ieactor was pressurized with hydiogen to the indicated piessure (eithei 200 oi 400 psig) and then heated to the indicated temperatuie (eithei 125°C oι 140°C) When the tempei ature/pressure parameters weie reached, stirring ( 1300 rpm) and data acquisition was simultaneously initiated After gas absorption ceased the reactor was cooled and the liquid phase extracted under pressure Each set of leaction conditions was used in duplicate runs. Table III below provides the initial catalyst activity in terms of conversion of 4-nitrotoluene (mmol H 2 /mιn) tor each of the four conditions of the temperature/pressure matrix Table III Initial Catalyst Activity (Sample 2G) The above results show that increases in eithei temperature or pressure alone do not enhance the catalytic activity of the present catalyst ( similar results aie achieved with acid salt doped catalyst) Howevei . the subject catalyst shows synergistic high catalyst activity under increased combined temperature/pressure conditions. ExampleVI A series of catalyst were tested for their response to recycling reactions (each used in five consecutive (5) batch reactions). The series included catalyst 2G and, foi comparative purposes Catalysts formed according to Examples I (Sample I) and Comparative Example II (Sample 5F) (see below). The reactions were each carried out using the procedure and reactor equipment described in Example VHI under temperature/pressure combined conditions of 140°C and 400 psig At the end of the fifth cycle, the substrate (4- nitrotoluene) to catalyst contact ratio reached a total of 250. The results are shown in Table IV below The precious transition metal doped catalyst of the present invention exhibited superior activity over the cycles tested when compared to undoped catalyst (Sample 1 ) and to conventional acid salt doped catalyst (Sample 5F). Table IV Catalyst Activity in Batch Recycle The above shows that undoped base metal catalyst had lower catalytic activity in each of the five cycles than doped catalyst. However, of the doped catalysts, the present doped catalyst exhibited higher initial and overall activity than conventional acid salt doped catalyst Comparative Example I For comparative purposes, a sample of base metal catalyst was prepared in the same manner as in Example II above except that the dopant salt solution was formed with a solution of palladium salt (NH 3 ) 4 Pd(OH) 2 - H 2 O, having a pH of 13.7. The resultant doped catalyst is labeled 1 - Comparative. This high pH dopant solution was used to prepare a doped catalyst formed with the same nickel base catalyst of samples 2D (having a pre-dopant pH of 1 1 ) and the same concentration (0.25 wt. percent) of ' Pd metal dopant of those samples. The results are shown in Table I-C below and compared with those of samples 2D. Table I-C Comparative Example ft For comparative purposes, a series of palladium metal doped nickel base metal catalysts were formed using the same procedure described in Example II above except that acidic precious metal salt solutions were used to provide the dopant metal. The samples were analyzed in the same manner as described in Example II using ICP and XPS techniques. The results are given in Table II-C. The resultant doped catalyst products had very high S/B ratio showing that a much greater fraction of the doped metal resided in the surface volume of the catalyst particles. Table II-C The data in Tables I-C and II-C shows a sti ong dependencv of the S/B latio on the type of salt used and the thus pH of the dopant solution which pi ovides the dopant pi ecious metal The high S/B i atio attained when an acidic dopant salt or a very alkaline dopant salt (Sample 1 -Comparative) is used indicated that one does not achieve the same type of dopant distribution as when using dopant salts having a pH in the range of fiom about 8- 12 Comparative Example III Foi compai ative pin poses a senes of Pd acid salt foi med catalysts Samples 5G to J weie tested in the same mannei as above and compared to Samples 2H, 21, 2F, and 2K in Table III C below Each compaied pair of samples contained 0 25 wt % Pd dopant and were formed using spongy nickel metal catalyst sluines having the same pie-doping pH condition Table III-C The present basic salt formed doped catalyst pi ovided a higher activity in each compai ison Comparative Example IV Foi compai ative purposes, duplicate hvdrogenation reactions of 4- nitrotoluene were conducted in the same manner as described in Example V at reaction conditions of 140°C and 400 psig except that the palladium doped nickel based catalyst used was Sample 2G pπoi to washing and aging The catalytic activity was only 7 4 mmol H7mιn compared to the 9 6 mmol Ho/min value obtained under the same conditions with the catalyst of the present invention

Claims: IN THE CLAIMS: 1. A product comprising a porous particulate metal material comprising a base metal having from about 0.01 to about 1.5 weight percent of a precious transition metal coated on the surface of said base metal and distributed throughout said particulate material to have a S/B ratio of less than 60. 2. The product of Claim 1 wherein the precious transition metal is selected from Ru. Rh. Re, Pd, Pt, Os, Ir or mixtures thereof and said base metal is selected from Ni, Co. Cu, Fe or mixtures thereof. 3. The product of Claim 2 wherein the precious transition metal is selected from Pt or Pd or mixtures thereof and the base metal is selected from nickel, cobalt or mixtures thereof. 4. The product of Claim 1 wherein the porous particulate metal material comprises at least 85 weight percent of a base metal selected from Ni, Co, Cu or Fe or mixtures thereof and further comprises up to 15 weight percent of aluminum, molybdenum, chromium, iron, copper, tin, zirconium, zinc, titanium, vanadium or mixtures thereof. 5. The product of Claim 1 wherein the porous paniculate metal material further has up to about 3 weight percent of a metal selected from the group consisting of molybdenum, chromium, zirconium, zinc, titanium, vanadium, iron or mixtures thereof on the surface of said base metal material. 6 The pioduct of Claim 2 wheiein the pi omotei piecious metal is piesent in fiom 0 05 to I weight percent and the S/B latio is from about 10 to 50 7 The product of Claim 3 wherein the promoter precious metal is present in from 0 05 to 1 weight percent and the S/B ratio is from about 10 to 50 8 The pioduct of Claim 4 wherein the promoter piecious metal is present in from 0.05 to 1 weight percent and the S/B ratio is from about 10 to 50 9 The product of Claim 5 wherein the piomotei precious metal is present in from 0 05 to 1 weight percent and the S/B ratio is from about 10 to 50 10 The product of Claim 2 wherein the porous particulate base metal material has an average particle diametei of less than 500 microns and a surface area of at least 10 m7g 1 I The pi oduct of Claim 3 wheiein the poi ous particulate base metal mateiial has an average particle diameter of less than 500 microns and a surface area of at least 10 m7g. 12. The product of Claim 10 wherein the porous particulate base metal material has an average particle diameter of less than 75 microns and a surface area of at least 10 m7g 13 The product of Claim 1 1 wherein the poious particulate base metal matei ial has an average particle diametei of less than 75 mici ons and a suiface aiea of at least 10 m7g 14 The product of Claim 1 wherein the porous particulate base metal material has a particle diameter range of from 0.1 to 0.8 cm and a surface area of at least 10 m7g. 15 The pioduct of Claim 2 wheiein the poious particulate base metal matei ial has a particle diametei l ange of fiom 0 1 to 0 8 cm and a suiface aiea of at least 10 m7g 16 The product of Claim 2 wherein the S/B ratio is from about 10 to about 40 17 The product of Claim 3 wherein the S/B ratio is from about 10 to about 40 18 The product of Claim 1 wherein the porous particulate base metal material has a surface area of from 20 to 150 m7gm, the promoter precious metal is selected from Pt or Pd or mixtures thereof, the amount of promoter precious metal in the product is from 0 05 to 1 weight percent, and the S/B ratio is from about 10 to 40 19 The product of Claim 2 wherein the porous particulate base metal material has a surface area of from 20 to 150 m7gm; the promoter precious metal is selected from Pt or Pd or mixtures thereof; the amount of promoter precious metal in the product is from 0 05 to 1 weight percent; and the S/B ratio is from about 10 to 40 20 The product ol Claim 4 wherein the porous particulate base metal matei ial has a surface area of from 20 to 150 m7gm. the promotei piecious metal is selected from Pt or Pd or mixtures theieof, the amount of promoter metal in the product is fiom 0.05 to 1 weight percent; and the S/B i atio is from about 10 to 40 21 The product of Claim 5 wherein the porous particulate base metal matei ial has a suiface aiea of fi om 20 to 150 m7gm, the piomoter piecious metal is selected from Pt oi Pd oi mixtui es theieof; the amount of promoter piecious metal in the pi oduct is fiom 0 05 to 1 weight percent, and the S/B ratio is from about 10 to 40 22 A hydrogenation catalyst formed by contacting an aqueous alkaline slurry of porous particulate material comprising a base metal with an alkaline solution of an alkaline promoter piecious metal salt iepresented by the formula A X MY, wherein A represents a cation oi ligand selected from ammonia, ammonium, alkali metal or mixtures theieof, M represents a precious transition metal atom selected from Pt, Pd, Re. Ru, Rh, Ir or Os or mixtures thereof, Y is an anion selected from hahde, nitrate, hydroxide, caibonate, bicarbonate, sulfate, or a C|-C 4 carboxylate, and x and y each independently represent an integer of from 1 to 6. causing said porous metal mateπal and an effective amount of salt to remain in contact at a pH of from about 8 to 12 for a sufficient time to have from 0 01 to about 1 5 wt. percent, based on the catalyst, of said promoter precious metal M deposit on a portion of the surface of said porous metal material; and washing said tieated porous metal mateπal with an aqueous solution to lower the pH at least 0.25 unit below the contact pH oi with 25 parts of solution per part of solid treated porous metal material or both 23 A hydrogenation reduction catalyst fonned by contacting an aqueous alkaline slurry of porous particulate material comprising a base metal with an alkaline solution of an alkaline promoter precious metal salt represented by the formula A MY wherein A represents a cation or ligand selected from ammonia, ammonium, alkali metal or mixtures thereof, M represents a precious transition metal atom selected from Pt. Pd. Re. Ru, Rh. Ir or Os or mixtures thereof, Y is an anion selected from hahde. nitrate, hydroxide, carbonate, bicarbonate, sulfate, or a C|-C 4 carboxylate. and x and y each independently represent an integer of from 1 to 6: causing said porous metal material and an effective amount of salt to remain in contact at a pH of from about 8 to 12 foi a sufficient time to have from 0.01 to about 1.5 weight percent, based on the catalyst, of said promoter precious metal M deposit on a portion of the surface of said porous metal material; and retaining the product of said promoter precious metal containing porous metal material in a water or water/alcohol slurry for at least about 12 hours. 24. The catalyst of Claim 22 wherein the base metal is selected from Ni, Co. Cu, Fe, or mixtures thereof 25. The catalyst of Claim 23 wherein the base metal is selected from Ni, Co. Cu, Fe. or mixtures thereof. 26. The catalyst of Claim 22 wherein said M is selected from palladium or platinum or mixtures thereof and said base metal is nickel 27. The catalyst of Claim 23 wherein said M is selected from palladium or platinum or mixtures thereof and said base metal is nickel. 28. The catalyst of Claim 22 wherein said aqueous slurry of base metal particulate material has a pH of from 8 to 12 and said salt solution has a pH of from 8 to 12 and wherein the formed catalyst has from 0.05 to I wt. percent of promoter precious metal deposited on a portion of the surface of the material. 29. The catalyst of Claim 23 wherein said aqueous slurry of base metal particulate material has a pH of from 8 to 12 and said salt solution has a pH of from 8 to 12 and wherein the formed catalyst has from 0.05 to 1 wt. percent of promoter precious metal deposited on a portion of the surface of the base metal material. 30. The catalyst of Claim 28 wherein the base metal particulate material and salt are contacted at a pH of from 10 to 1 1 .5. 3 1 . The catalyst of Claim 29 wherein the base metal particulate material and salt are contacted at a pH of from 10 to 1 1 .5. 32. The catalyst of Claim 22 wherein the catalyst product has a S/B ratio of from about 10 to 50. 33. The catalyst of Claim 23 wherein the catalyst product has a S/B ratio of from about 10 to 50. 34. The catalyst of Claim 28 wherein the S/B ratio is from about 10 to about 40. 35. The catalyst of Claim 29 wherein the S/B ratio is from about 10 to about 40. 36 The catalyst of Claim 28 wheiein the product is formed from a porous base metal material having a surface area of from 20 to 150 m7gm; the promoter precious metal is selected from Pt or Pd or mixtures thereof; the amount of promoter precious metal in the product is from 0.05 to 1 weight percent, and the S/B ratio is from about 10 to about 40. 37 The catalyst of Claim 29 wheiein the product is formed from a porous base metal matei ial having a surface area of from 20 to 1 0 m7gm: the promoter precious metal is selected from Pt or Pd or mixtures thereof; the amount of promoter precious metal in the product is from 0.05 to i weight percent; and the S/B ratio is from about 10 to about 40. 38. A catalytic hydrogenation process comprising contacting an organic compound having at least one group capable of undergoing reaction with hydrogen in the presence of a catalyst selected from the products of Claim 1 , 2, 3, 4, 5. 6, 7, 8, 9, 10, 1 1 , 12, 13, 14. 15, 16 or 17. 39. The process of Claim 38 wherein said group is selected from ethylenic unsaturation, acetylenic unsaturation. oxygen or sulfur atoms of ring systems, carboxyl, carbonyl, nitriles, amides, oximes. ketimines. nitroso, nitro. azo, azoxy, imines, alcohols, ethers or oxides group 40. The process of Claim 38 wherein the organic compound is selected from nitroaromatic or dinitroaromatic compounds or mixtures thereof. 41 . A process of forming a hydrogenation catalyst comprising: contacting an aqueous alkaline slurry of porous metal particulate material comprising a base metal with an alkaline solution of an alkaline promoter precious metal salt represented by the formula A λ MY wherein A represents a cation or ligand selected from ammonia, ammonium, alkali metal or mixtures thereof. M represents a promoter precious metal atom selected from Pt, Pd, Re, Ru, Rh, Ii or Os or mixtures thereof, Y is an anion selected from hahde, nitrate, hydroxide, carbonate, bicarbonate, sulfate, or a C 1 -C4 carboxylate, and x and y each independently represent an integer of from 1 to 6; causing said porous base metal material and an effective amount of salt to remain in contact at a pH of from about 8 to 12 foi a sufficient time to have from 0.01 to about 1.5 wt. percent, based on the catalyst, of said promoter precious metal M deposit on a portion of the surface of said porous base metal material; and washing said treated porous base metal material with an aqueous solution to lower the pH at least 0.25 unit below the contact pH or with 25 parts of solution per part of solid treated porous base metal material or both. 42. A process of forming a hydrogenation catalyst comprising; contacting an aqueous alkaline slurry of porous base metal particulate material comprising a base metal with an alkaline solution of an alkaline promoter precious metal salt represented by the formula A MY } wherein A represents a cation or ligand selected from ammonia, ammonium, alkali metal or mixtures thereof, M represents a promoter precious metal atom selected from Pt, Pd, Re, Ru, Rh. Ir or Os or mixtures thereof, Y is an anion selected from hahde, nitrate, hydroxide, carbonate, bicarbonate, sulfate. oi a C|-C 4 carboxylate, and x and y each independently represent an integer of from 1 to 6; causing said porous base metal material and an effective amount of salt to remain in contact at a pH of from about 8 to 12 for a sufficient time to have from 0.01 to about 1.5 weight percent, based on the catalyst, of said promoter precious metal M deposit on a portion of the surface of said porous base metal material; and retaining the product of said precious transition metal containing porous base metal material in a water or water/alcohol slurry for at least about 12 hours.

Inventors: SCHMIDT STEPHEN RAYMOND, SCHMIDT, STEPHEN, RAYMOND
Applicants: GRACE W R & CO, W.R. GRACE & CO.-CONN.
Application year: 2000
Main classification: B01J25
IPC codes: B01J25, C07B61, C07C209, C07C211