the finally calcined catalysts of this invention are designed to fall within the following composition ranges : ______________________________________catalyst composition , wt . % component broad range preferred range______________________________________coo and / or nio 1 - 15 2 - 8moo . sub . 3 and / or wo . sub . 3 5 - 35 8 - 25f 0 . 5 - 10 1 - 7sio . sub . 2 1 - 10 2 - 5al . sub . 2l o . sub . 3 balancewt . ratio ,( coo + nio )/( moo . sub . 3 + wo . sub . 3 ) 0 . 1 - 1 . 0 0 . 12 - 0 . 5______________________________________ in the succeeding description , it will be understood that the proportions of the various raw materials utilized will be selected to provide finished catalysts falling within the above composition ranges . also , in order to avoid repetition of the cumbersome &# 34 ; coo and / or nio &# 34 ; and &# 34 ; moo 3 and / or wo 3 &# 34 ; terminology , the description will be confined to the preferred nickel - molybdenum type catalysts , but it will be understood that corresponding cobalt components can be substituted in whole or in part for any of the described nickel components , and corresponding tungsten components in whole or in part for any of the described molybdenum components . in the preferred method for manufacturing catalysts of this invention , an alumina hydrogel is first shaped , as by conventional extrusion techniques , into particles of the desired size and shape , e . g . extrudates having a diameter between about 1 / 32 &# 34 ; and 1 / 4 &# 34 ;, preferably about 1 / 20 &# 34 ;- 1 / 8 &# 34 ;. the extrudates are then dried and calcined at e . g . 800 °- 1400 ° f . to convert the extrudates into porous gamma alumina having a surface area of about 150 - 350 m 2 / g and a pore volume of about 0 . 3 - 1 . 2 ml / g , as determined by mercury porosimeter measurements at 50 , 000 psi . the calcined extrudates are then impregnated with an aqueous solution of a suitable molybdenum compound which upon calcination yields moo 3 , the preferred compound being ammonium heptamolybdate . in this impregnation , as well as all impregnation steps described herein , the &# 34 ; pore saturation &# 34 ; technique is preferably utilized , in which the volume of impregnation solution utilized is only sufficient to substantially saturate , i . e . fill , the pores of the support particles . this is preferably accomplished by spraying the solution at a controlled rate onto the agitated particles , or a stream of such particles moving for example on a conveyor belt . the volume of solution employed is at least about 90 % of the pore volume of the particles to be impregnated , but not substantially in excess of 100 % of such pore volume . there should be substantially no drainable excess of liquid . by operating in this manner , maximum uniformity of distribution of active components is obtained , as well as maximum control over proportions of active components absorbed or adsorbed by the support particles . when using older impregnation techniques involving soaking the particles in an excess of solution , differential ionic adsorption rates and destabilization of the solution with resultant formation of precipitates frequently lead to maldistribution of active components on the support , and control over the amounts of active components adsorbed is more difficult . these considerations are particularly important when the impregnating solution contains ions of more than one active component , as e . g . those containing nickel fluosilicate to be subsequently described herein . it will be appreciated also that in the pore saturation technique it is important that highly soluble compounds of the active components be utilized in order to provide , in a pore - saturating volume of the solution , sufficient dissolved precursors of active component ( s ) to provide the predetermined desired amount of such active component ( s ) in the finished catalyst , thereby avoiding the necessity for multiple impregnations and calcinations . the preferred ni , f and mo compounds employed herein are all highly soluble , as distinguished for example from nif 2 which is only slightly soluble in water and which would hence not be suitable for single - step impregnation by the pore saturation technique . following impregnation with the desired molybdenum component , the wet particles are dried and calcined in conventional fashion in air at temperatures ranging between about 700 ° and 1400 ° f . this calcination is believed to result in substantial chemical combination of the molybdenum with the alumina gel to form aluminum molybdate , ( alo ) 2 mo0 4 . xh 2 o . the calcined particles are then impregnated with sufficient of a concentrated aqueous solution of nickel fluosilicate to saturate the pore volume of the particles and provide the predetermined desired amounts of ni and f in the finished catalyst . in the case of essentially non - volatile active components such as ni and mo , it is a simple matter to predetermine the concentration of soluble precursors thereof needed in a pore - saturating volume of solution to provide the desired active metal content in the finished catalyst . however , in all known impregnation methods for adding fluorine to alumina - based catalysts , some volatilization and loss of fluorine during drying and calcination occurs . the amount of such loss depends upon several variables such as the initial f concentration , calcination temperatures , hydrolytic reactions occurring while steam is present , and the presence of absence in the catalyst of other acidic components which can chemically complete with hf for the reactive alumina base . a certain amount of experimentation is therefore required in any given method for the manufacture of f - containing catalysts by impregnation , in order to achieve a desired target f content in the finished catalyst . this problem is considerably alleviated when using nickel fluosilicate as a fluorine source , because the weight - ratio of f / ni in nisif 6 . 6h 2 o is about 1 . 95 / 1 , which is normally higher than will be desired in the finished catalyst . hence , in many case , even though some 20 - 40 % of the f is lost by volatilization , the residual f / ni ratio after calcination will be satisfactory . however , in cases where adjustment of the f / ni ratio in the final catalyst is desired , such may readily be achieved by adding to the nickel fluosilicate impregnation solution additional ni in the form of a soluble salt such as the nitrate or acetate , or additional f in the form of hf , nh 4 f or the like . in all cases however , the major portion of the ni and f components in the final catalyst , and usually all of at least one of said components , is derived from the nickel fluosilicate . following impregnation with the nickel fluosilicate solution , the catalyst is again dried and calcined as above described to complete the preferred method of manufacture . the finished catalyst should have a surface area between about 100 - 300 m 2 / g and a porosity of about 0 . 2 - 1 . 0 ml / g . according to a non - preferred modification of the foregoing procedure , the molybdenum component , e . g . ammonium heptamolybdate or moo 3 , can be mulled with the alumina hydrogel , and the mixture then extruded , calcined and impregnated with the nickel fluosilicate solution . this procedure has the advantage of eliminating one impregnation - calcination sequence , but generally yields catalysts of somewhat lesser activity and mechanical strength . in still another modification the calcined alumina extrudates can be impregnated with a single solution containing all three active components , i . e . ammonium heptamolybdate and nickel fluosilicate . however , in this case it is necessary to add an acid to the solution , preferably phosphoric acid , in order to stabilize the solution against precipitation . in general sufficient acid should be added to reduce the ph of the solution to about 0 . 5 - 3 . 0 . after calcination the catalysts produced by this method are substantially as active as those prepared by the preferred method , at equivalent f , ni and mo contents . due to the presence of phosphate however , there is a greater tendency to lose fluorine during calcination and during use of the catalyst in denitrogenation . surface areas are also somewhat lower . the least preferred catalyst preparation method embraced herein consists in first impregnating the calcined alumina extrudates with the nickel fluosilicate solution , calcining , then impregnating with the molybdate solution and again calcining . this method generally results in catalysts of relatively low activity and low fluorine content . they are however definitely more active than corresponding non - fluorided catalysts . the catalysts of this invention can be used to advantage for the hydrodenitrogenation of substantially any mineral oil feedstock , including light and heavy gas oils , cycle oils , naphthas , kerosene , turbine fuels , diesel fuels , reduced crude oils , residual oils , shale oils and other syncrudes , etc . the denitrogenation conditions are conventional , falling within the following ranges : ______________________________________denitrogenation conditions broad range preferred range______________________________________temp ., ° f . 450 - 900 550 - 800h . sub . 2 pressure , psi 200 - 3000 500 - 2000lhsv 0 . 2 - 10 1 - 5h . sub . 2 / oil , scf / b 200 - 8000 500 - 4000______________________________________ prior to contact with the feedstock , the catalyst should be presulfided with h 2 s or an h 2 s - yielding compound under conventional conditions including temperatures ranging between about 100 °- 900 ° f . in this and the succeeding examples , the support employed was a 1200 °- 1250 ° f . calcined gamma alumina extrudate having a surface area of 254 m 2 / g and a pore volume of about 0 . 64 ml / g . the extrudates had a &# 34 ; trilobal &# 34 ; or three - leaf clover type of cross - section as illustrated in fig5 - a of u . s . pat . no . 3 , 857 , 780 , the &# 34 ; diameter &# 34 ; across two lobes of the cross - section being about 0 . 045 in . a first impregnation solution was prepared by dissolving 160 gms of ammonium heptamolybdate in 250 ml of water . additional water and concentrated nh 4 oh was added to give 375 ml of solution having a ph of 9 . 0 . this solution was rapidly added to 500 gms of the alumina extrudates which were then shaken thoroughly to effect pore saturation . the wet extrudates were dried and calcined by heating to 600 ° c . over a three - hour period and holding at 600 ° c . for 15 minutes . after cooling , the extrudates were then pore - saturated in the same manner as above with 350 ml of an aqueous solution containing 111 . 3 gms of dissolved nisif 6 . 6h 2 o . after aging for about one hour the extrudates were dried and calcined by heating to 500 ° c . over a two - hour period and holding at 500 ° c . for one hour . the properties of the finished catalyst are tabulated in table 1 below . a single - impregnation solution was prepared by first partially dissolving 165 gms of ammonium heptamolybdate in 200 ml of distilled water and then adding 56 gms of 85 % orthophosphoric acid to obtain a clear water - white solution . next , 111 . 3 gms of nisif 6 . 6h 2 o was dissolved in 150 ml of distilled water and heated to 60 ° c . the two solutions were then mixed to obtain about 450 ml of slightly hazy solution having a ph of about 1 . 7 - 2 . 0 . this solution was then employed to pore saturate 500 gms of the alumina extrudates as above described , with vigorous agitation . a small amount of excess liquid was drained from the extrudates . after aging for 45 minutes , the extrudates were then dried and calcined by heating to 500 ° c . over a period of 2 hours and holding at 500 ° c . for 1 hour . properties of the finished catalyst are given below in table 1 . this catalyst was prepared in the same manner and using the same constituents as used for catalyst a , except that the alumina extrudates were first impregnated with the nisif 6 . 6h 2 o solution , calcined at 500 ° c ., then impregnated with the ammonium heptamolybdate solution , and recalcined at 500 ° c . properties of the respective catalysts were as follows : table 1______________________________________ catalyst a b c______________________________________moo . sub . 3 , wt .% 20 . 1 17 . 7 19 . 2nio , wt .% 4 . 29 3 . 47 4 . 00f , wt .% 5 . 2 3 . 3 3 . 19sio . sub . 2 , wt .% 3 . 6 2 . 6 3 . 06p , wt .% -- 2 . 34 -- surface area , m . sup . 2 / g 184 162 195pore vol ., ml / g 0 . 42 0 . 41 0 . 45______________________________________ each of the foregoing catalysts was tested for denitrogenation activity , along with a commercial fluorine - free comparison catalyst prepared from the same alumina support material and containing 18 wt . % moo 3 , about 3 wt . % nio and 3 wt . % p ( added as phosphoric acid with the molybdenum component ). the nickel was added by impregnation with ni ( no 3 ) 2 solution . the test feed was a light diesel fuel boiling between about 400 ° and 650 ° f ., containing 0 . 65 wt . % sulfur and 0 . 038 wt . % total nitrogen . the tests were carried out at 700 ° f . and 700 psig , with a h 2 recycle rate of 3000 scf / b of feed . each catalyst was tested at 5 . 0 lhsv and 2 . 5 lhsv , and the product nitrogen values were plotted against reciprocal space velocity so that relative activities based on the first order kinetics could be determined at equal conversion levels . at 97 . 5 % conversion of total nitrogen ( 10 ppm product nitrogen ), the relative activities of the catalysts were as follows : table 2______________________________________ catalyst comparison a b c______________________________________relative activity 100 179 156 120______________________________________ it is thus apparent that nickel fluosilicate provides effective fluorine - promotion of the catalysts . although some f and ni were lost from catalyst b due to a slight excess of unabsorbed impregnating solution and to fluorine volatilization , it is apparent in view of its high activity that appropriate adjustment of its f and ni contents would give an activity comparable to that of catalyst a . the following claims and their obvious equivalents are believed to define the true scope of the invention .