the catalyst according to the present invention comprises titanium oxide , molybdenum oxide and vanadium oxide supported on a metal substrate , and the respective proportions thereof used are in the range of ti / mo / v = 97 - 65 / 3 - 20 / 0 - 15 in an atomic percentage . a preferable proportion of mo is in the range of 5 to 15 in an atomic percentage . if the proportion of molybdenum used is less than 3 in an atomic percentage , resistance to peeling - off is inferior , while if it exceeds 20 , the effectiveness of resistance to peeling - off is not more improved . further , vanadium oxide is not essential to be added , but if it is added to titanium oxide and molybdenum oxide , it is possible to obtain a catalyst having a further higher activity , but if its proportion used exceeds 15 in an atomic percentage , more effectiveness is not obtained . catalyst raw materials used in the present invention are not limited , if they afford titanium oxide , molybdenum oxide or vanadium oxide at the time of calcination of a catalyst . that is , any compounds of ti , mo or v capable of forming an aqueous slurry thereof such as metatitanic acid , ammonium molybdate , ammonium metavanadate , etc . are usable . when the above catalyst compounds are calcined before slurrying or being supported on a substrate , the shrinkage of catalyst particles after supported is small and a catalyst having a small particle size of catalyst compounds is obtained . namely , since molybdenum oxide ( moo 3 ) has a high vapor pressure , it vaporizes at calcination and coats or adsorbs on the surface of tio 2 particles so that moo 3 is present between the respective tio 2 particles . thus , even when the catalyst compounds are formed into a definite shape and again calcined , tio 2 particles do not adhere to one another to crystallize or sinter , but remain in the form of small particles , and also there occurs no shrinkage at calcination due to sintering ; hence it is possible to obtain a dense and strong catalyst product . further , since catalyst compounds are present in the form of fine particles , it is possible to obtain a slurry having a high concentration and a high stability without any additives at the time of slurry preparation . the calcination temperature is preferred to be 500 ° c . or higher . in addition , since moo 3 has a good compatibility with the metal substrate and increases the contact area at the time of calcination , the adhesion of the catalyst compounds to the substrate is remarkably improved . the metal substrate used in the present invention has no particular limitation and any of stainless steel , mild steel , etc . are usable . further , any of forms such as flat sheet , reticulated form , expanded metal , etc . are usable . in the case of a metal substrate obtained by subjecting the metal surface to spray with molten aluminum , etc . to form a roughened surface , contact of the metal surface with the catalyst compounds is improved as well as the catalyst surface area increases , thereby the catalyst activity and resistance to peeling - off are both improved . the denitration catalyst according to the present invention is obtained by adding water to the above catalyst compounds to form a slurry , applying the slurry onto the above metal substrate , drying and preferably calcining the resulting material . the slurry concentration may be of such an extent that the slurry can be applied onto the substrate . the process of applying the slurry onto the substrate has no particular limitation . for example , the process may be carried out by immersing the substrate in the slurry , removing superfluous liquid by a centrifugal separator , blowing off , suction , impact or the like means and drying . thus obtained catalyst is preferably calcined usually at about 500 ° c . when catalyst compounds comprising titanium compounds and molybdenum compounds are subjected to a primary calcination at about 500 ° c ., moo 3 has a higher vapor pressure at the temperature to coat or adsorb the surface of tio 2 particles as shown in fig2 so that moo 3 6 is present among the respective tio 2 particles 4 ; and when the particles are ground , the grindability of the particles is improved to obtain fine particles . when fine particles of catalyst compounds are increased and water is added thereto to form a slurry , it is possible to lower the slurry viscosity even when the particle concentration is high . hence it is possible to immerse a substrate in a high concentration slurry and have the slurry supported on the substrate . when the high concentration slurry is supported , it is possible to form a high density catalyst layer having a high strength on the substrate . when catalyst compounds ( particles ) are supported on a metal substrate , followed by calcination , there is generally raised a problem that the catalyst particles shrink due to sintering of tio 2 particles by heat to generate cracks . whereas in the case of the present invention , since moo 3 is present among tio 2 particles , contact of tio 2 particles themselves is hindered to prevent tio 2 particles from sintering so that shrinkage due to sintering is reduced and crack generation can be prevented ; hence a strength reduction of the catalyst layer does not occur . further , when calcination is carried out after the catalyst has been supported on a metal substrate 8 , moo 3 particles 6 coating tio 2 particles 4 contacts with the metal substrate 8 to react partially therewith , as shown in fig3 ; hence adhesion of catalyst compounds onto the metal substrate is improved so that the catalyst compounds is not peeled off from the substrate . the present invention will be described in more detail by way of examples , but it should not be construed to be limited thereto . ammonium molybdate ( 3 ( nh 4 ) 2 o . 7moo 3 . 4h 2 o )( 3 . 81 kg ) and ammonium metavanadate ( nh 4 vo 3 )( 1 . 04 kg ) were added to metatitanic acid ( 50 kg ) containing 30 % by weight of titanium oxide , followed by kneading the mixture on heating by means of a kneader to obtain a pasty slurry containing 35 % by weight of water . this slurry was granulated by an extrusion granulator , followed by drying by a fluidized bed dryer , calcining at 550 ° c . for 2 hours , grinding the resulting material into powder having a size of 90 % or more of 100 mesh pass by means of a hammer mill and adding water to the powder to obtain a slurry . as to the quantity of water added at that time , a water content of 35 to 50 % by weight , preferably 40 to 48 % by weight afforded superior slurry properties . in this example , water ( 4 . 6 kg ) was added to the resulting powder ( 5 . 4 kg ) to obtain a catalyst slurry , followed by immersing in this slurry , a sus 304 expanded metal lath of 0 . 2 mm thick , rotating them by means of a centrifugal separator to remove superfluous slurry , drying the resulting material and calcining at 500 ° c . for 2 hours to obtain a catalyst . the quantity of the catalyst compounds supported was 150 kg / m 2 per unit surface area of the catalyst . this value is very small as compared with 800 to 1 , 000 g / m 2 in the case of a conventional catalyst disclosed in japanese patent application laid - open no . sho 63 - 111945 / 1988 . the surface area in this case refers to a projected area of one surface of the catalyst including the openings of the expanded metal . the object of removing the superfluous slurry by means of a centrifugal separator is to prevent the openings of the expanded metal from clogging with slurry and to obtain a porous metal plate catalyst . as to the process of the centrifugal separation can be replaced by air - flowing , vibration - impacting , etc . in addition , as seen from fig8 showing a plane view of the catalyst , in a magnification of 4 , the openings of the expanded metal lath are not filled with the catalyst , but the whole surface area of the catalyst is thinly coated with the catalyst compounds . a process for producing the above expanded metal lath is illustrated in fig1 . a stainless steel sheet ( sus 304 ) 1 of 0 . 2 mm thick is cut to have zigzag slits 3 as shown in fig1 ( a ) and ( b ), followed by expanding the sheet in the direction 5 perpendicular to that of the slits 3 so that the slits are opened to obtain an expanded metal lath 7 . the cross - section of the metal 7 is shown in fig1 ( c ) and its plane view is shown in fig1 ( d ). an expanded metal lath of 0 . 8mm thick is obtained from the stainless steel sheet of 0 . 2 mm thick . pitch p of the openings 7 was 22 mm and openings 9 occupied about 79 % of the surface area . example 1 was repeated except that the quantity of ammonium molybdate added was changed to 1 . 03 kg , 2 . 12 kg or 8 . 29 kg , to obtain a catalyst . example 1 was repeated except that no ammonium molybdate was added , to obtain a catalyst . example 1 was repeated except that a substrate obtained by subjecting , in advance , a sus expanded metal to aluminum metal - spray in an oxidation atmosphere in a rate of 50 g / m 2 , 100 g / m 2 or 250 g / m 2 , used to obtain catalysts . example 1 was repeated except that the quantity of ammonium metavanadate added was changed to 0 kg , 0 . 5 kg , 2 . 14 kg or 4 . 39 kg , to obtain a catalyst . example 1 was repeated except that the expanded metal lath was replaced by a sus flat sheet of 0 . 2 mm thick , to obtain a catalyst . example 1 was repeated except that an expanded metal lath obtained by subjecting the substrate to aluminum - spray in an amount of 50 g / m 2 was used and the quantity of the catalyst compounds supported was changed to 100 g / m 2 to 200 g / m 2 by controlling the degree of centrifugal separation , to obtain catalysts . example 1 was repeated except that there was used a substrate obtained by heat - treating an alloy sheet of 50 μm thick consisting of fe - cr - al ( fe : 75 %, cr : 20 % and al : 5 % by weight , respectively ) at 900 ° c . to form an al 2 o 3 whisker on the surface thereof , to obtain a catalyst . in order to test the denitration activities of the respective catalysts obtained in the above examples and comparative example , the percentage denitrations thereof were measured according to the conditions shown in table 1 . table 1______________________________________catalyst dimension 20 mm × 100 mm______________________________________gas compositionno 200 ppmnh . sub . 3 240 ppmco . sub . 2 12 % o . sub . 2h . sub . 2 on . sub . 2 balancegas quantity 184 l / htemperature 350 ° c . ______________________________________ in order to test the strength of catalysts , a piece of catalyst ( 100 mm × 100 mm ) was ten times dropped onto an iron plate from a height of 1 m , followed by measuring the weight reduction of the catalyst and obtaining the percentage peeling - off according to the following equation : ## equ1 ## fig4 shows a chart obtained by plotting the percentages denitration and the percentages peeling - off of catalysts obtained in examples 1 - 4 and comparative example 1 relative to the quantities of mo added . as seen from this chart , mo addition can notably reduce the percentage peeling - off of the catalyst and its quantity added is effective in 3 to 20 atomic %, preferably 5 to 15 atomic %. fig5 shows a chart obtained by plotting the percentages denitration and the percentages peeling - off of the catalysts obtained in examples 1 and 5 - 7 relative to the quantities of al metal spray . as seen from this chart al metal - spray can further reduce the percentage peeling - off and also can afford a catalyst having a superior activity and strength . fig6 shows a chart obtained by plotting the percentages denitration and the percentages peeling - off of the catalysts obtained in examples 5 , 13 and 14 relative to the quantities of the catalyst compounds supported . as seen from this chart , even when the quantity of the catalyst supported is 1 / 5 ( 150 g / m 2 ) or less that of conventional catalyst ( comparative example 2 described later ), the catalysts of the present invention have the same degree of percentage denitration and percentage peeling - off as those in the case of conventional catalyst . table 2 shows the measurement results of the percentages denitration and the percentages peeling - off of the catalysts obtained in examples 8 - 12 and 15 . as seen from this table , vanadium addition can afford a catalyst having a further higher activity and also as to the form of the substrate , the process of the present invention is applicable not only to an expanded metal lath but also to a flat sheet lath . table 2______________________________________ex . percentage denitration (%) percentage peeling - off (%) ______________________________________ 8 60 13 9 68 1210 81 1211 75 1412 72 1815 72 5______________________________________ water ( 3 . 4 kg ) and inorganic fibers of kaolin ( 1 . 5 kg ) were added to the catalyst powder ( 10 kg ) obtained in example 1 , followed by kneading the mixture by means of a kneader to obtain a catalyst paste , applying this paste under pressure onto the same expanded metal substrate as used in example 1 by means of rolls , air - drying the resulting material and calcining it at 500 ° c . for 2 hours to obtain a sheet - form catalyst . the quantity of the catalyst compounds supported was 820 g / m 2 . its percentage denitration and percentage peeling - off were measured as in the above use examples 1 and 2 to give 75 % and 15 %, respectively . as seen from the above results , the catalyst obtained according to the production process of the present invention has a percentage denitration and a percentage peeling - off to the same degree as that in the case of catalyst obtained according to conventional production process , in 1 / 5 or less the quantity of the latter catalyst compounds supported . according to the production process of the present invention , it is possible to obtain a catalyst having a high activity and a superior resistance to peeling - off in a state of a small quantity of catalyst compounds supported . further , use of an expanded metal lath as a substrate affords an effectiveness mentioned below . a catalyst using a flat sheet as a substrate and a catalyst using an expanded metal lath as a substrate were incorporated in a unit at pitch of 6 mm , respectively , and the respective percentages denitration were compared under the conditions shown in table 3 listed below . the results are shown also in table 3 . table 3______________________________________test catalyst dimension : 150 mm × 150 mmconditions : length of the unit : 500 mm filling pitch : 6 mm gas quantity : 172 nm . sup . 3 / h temperature : 350 ° c . [ nh . sub . 3 ]/[ no ] 1 . 2 molar ratio : substrate : flat sheet expanded metal lathpercentage 72 78 . 3denitration (%): ______________________________________ as seen from the results , the catalyst unit using an expanded metal lath exhibited a higher percentage denitration than that in the case of the catalyst unit using a flat sheet catalyst . the reason consists in that use of a flat sheet as a substrate causes fluctuations of gas streams between the flat sheet catalysts so that a large quantity of gas flows at a broad path between the sheets , while only a small quantity of gas flows at a narrow path , to cause channeling or deviation of gas stream , thereby reducing the percentage denitration . whereas , in the case of an expanded metal lath as a substrate , the gas not only flows through paths between the substrates , but also passes through the openings of the expanded metal lath and flows in other paths to reduce channeling . further , since the gas streams cause turbulence to reduce a boundary film formed along the surface if the catalyst . thus , use of an expanded metal lath as a substrate makes it possible to obtain a higher percentage denitration than that in the case of use of a flat sheet . further , example 15 shows that even in the case of using a thin sheet of 50 μm thick as a substrate , a catalyst having a small peeling - off and a high activity can be obtained . further , by using a metal honeycomb substrate of a thin sheet , it is possible to obtain a very compact denitration apparatus .