Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
  • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
  • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/85—Chromium, molybdenum or tungsten
  • B01J23/88—Molybdenum
  • B01J23/887—Molybdenum containing in addition other metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/8876—Arsenic, antimony or bismuth
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
  • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
  • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
  • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
  • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
  • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
  • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
  • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
  • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
  • C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Definitions

• This invention relates to a mixed metal oxide catalyst containing oxides of molybdenum, bismuth, iron, cesium and, optionally, other metals for the production of unsaturated aldehydes from olefins, such as methacrolein by gas phase catalytic oxidation of isobutylene in the presence of air or another gas containing molecular oxygen.
• Mo a W b Bi e Fe ⁇ iSb f X ⁇ O where X is potassium, rubidium and/or cesium, Y is phosphorus, sulfur, silicon, selenium, germanium and/or boron, Z is zinc and/or lead, A is magnesium, cobalt, manganese and/or tin, a is 12, b is 0.001 to 2, c is 0.01 to 3, d is 0.01 to 8, e is 0.01 to 10, f is 0.01 to 5, g is 0.01 to 2, h is 0 to 5, i is 0.01 to 5, j is 0 to 10 and k is sufficient to satisfy the valences .
• U.S. patent no. 4,511,671 discloses a catalyst for manufacturing methacrolein of the formula : Mo a W b Bi c Fe (t A ⁇ B f C g D h O x
• A is at least one of nickel and/or cobalt
• B is at least one of alkali metals, alkaline earth metals and/or thallium
• C is at least one of phosphorus, tellurium, antimony, tin, cerium, lead, niobium, manganese and/or zinc
• D is at least one of silicon, aluminum, zirconium, and/or titanium
• a is 12, b is 0 to 10, c. is 0.1 to 10, d is 0.1 to 20, e is 2 to 20, f is 0 to 10, g is 0 to 4, h is 0 to 30 and x is determined by the atomic valences.
• U.S. patent no. 4,556,731 discloses a catalyst for production of methacrolein and methacrylic acid of the formula:
• A is an alkali metal, such as potassium, rubidium, cesium or mixtures thereof, thallium, silver or mixtures thereof
• B is cobalt, nickel, zinc, cadmium, beryllium, calcium, strontium, barium, radium or mixtures thereof
• X is bismuth, tellurium or mixtures thereof and M is (1) Cr+W, Ge+ , Mn+Sb,' Cr+P, Ge+P, Cu+W, Cu+Sn, Mn+Cr, Pr+W, Ce+W, Sn+Mn, Mn+Ge or combinations thereof, (2) Cr, Sb, Ce, Pn, Ge, B, Sn, Cu or combinations thereof, or (3) Mg+P, Mg+Cu, Mg+Cr, Mg+Cr+W, Mg+W, Mg+Sn or combinations thereof, a is 0 to 5, b is 0 to 20, c is 0 to 20,
• U.S. patent no. 5,245,083 discloses a catalyst for preparing methacrolein of a mixture of composition (1) of the formula:
• a n Mo a O p where A is at least one of K, Rb and Cs, m is 2, n is 1 to 9 and p is 3n+l.
• X is at least one of Ni and Co
• Y is at least one of K, Rb, Cs and Tl
• Z is at least one of the elements belonging to Groups 2, 3, 4, 5, 6, 7, 11, 12, 13, 14, 15 and 16, specifically beryllium, magnesium, calcium, strontium, barium, titanium, zirconium, cerium, niobium, chromium, tungsten, manganese, copper, silver, zinc, cadmium, boron, aluminum, germanium, tin, lead, phosphorus, arsenic, antimony, sulfur, selenium and tellurium, a is 12, b is 0.1 to 10, c is 0 to 20, d is 0 to 20, e is 0 to 2, f is 0 to 4, and g satisfies the valence requirement and composition (2) of the formula:
• Ln h Mo a O D where Ln is at least one of the rare earth elements, h is 0.2 to 1.5, i is 1 and j satisfies the valence requirement.
• the atomic ratio of the rate earth element to molybdenum is disclosed to be in the range from 0.2 to 1.5 with an atomic ratio less than 0.2 resulting in high selectivity but poor activity and with an atomic ratio greater than 1.5 resulting in high activity but poor selectivity.
• A is nickel and/or cobalt
• B is at least one of alkali metal, alkaline earth metals and thallium
• C is at least one of phosphorus, arsenic, boron, antimony, tin, cerium, lead and niobium
• D is at least one of silicon, aluminum, zirconium and titanium
• a is 0.1 to 10.0
• b is 0.5 to 10.0
• c 0.1 to 10.0
• d 12
• e is 2.0 to 20.0
• f is 0.001 to 10.0
• g is 0 to 10.0 and h satisfies the valence requirement.
• the ratio of a/b is 0.01 to 6.0 so that bismuth is combined very stably with tungsten and compounds such as bismuth trioxide and bismuth molybdate are not formed.
• A is Co or a mixture of Co and Mg having an atomic ratio of not more than 0.7
• B is Rb, Cs or a mixture thereof
• a is 0 to 8
• b is 0 to 8
• c is 0 to 1.2
• c is 0 to 2.5
• e is 1.0 to 12
• f is 0 to 2.0
• g satisfies the valence requirement.
• the relative atomic ' ratio of iron to bismuth and cerium should be 0 ⁇ d/ (a+b+d) ⁇ 0.9.
• the relative atomic ratio of bismuth, cerium and potassium should be 0.05 ⁇ b/ (a+b+c) ⁇ 0.7.
• the relative atomic ratio of potassium to bismuth and cerium should be 0 ⁇ c/ (a+b+c) ⁇ 0.4.
• Bismuth, cerium, potassium, iron and cobalt are indispensable elements for the disclosed invention.
• Prior art discloses mixed metal oxide catalysts which contain molybdenum, bismuth, iron, cesium and other metals for the production of methacrolein. Furthermore, prior art discloses certain ranges of amounts of these metals . Some prior art discloses relative ratios of certain components to other components . The effect of the selection of certain components for a mixed metal oxide catalyst for the production of methacrolein and the relative relationship of some of these components to other components has not been investigated in complete detail.
• the present invention is for a catalyst of the general formula:
• Mo z Bi a Fe o Cs g 0 x a is in the range from 0.1 to 1.5, c is in the range from 0.2 to 5.0, g is in the range from 0.1 to 1.5 and x is determined by the valences of the other components.
• the process of making the catalyst is generally to dissolve the metal compounds of molybdenum, bismuth, iron, cesium and, optionally, other metals, such as tungsten, cobalt, nickel, antimony, magnesium, zinc, phosphorus, potassium, rubidium, thallium, manganese, barium, chromium, boron, sulfur, silicon, aluminum, titanium, cerium, tellurium, tin, vanadium, zirconium, lead, cadmium, copper and niobium, and precipitate a catalyst precursor which is calcined to form a mixed metal oxide catalyst.
• other metals such as tungsten, cobalt, nickel, antimony, magnesium, zinc, phosphorus, potassium, rubidium, thallium, manganese, barium, chromium, boron, sulfur, silicon, aluminum, titanium, cerium, tellurium, tin, vanadium, zirconium, lead, cadmium, copper and niobium
• the metal compounds may be salts (e.g., nitrates, halides, ammonium, organic acid, inorganic acid) , oxides, hydroxides, carbonates, oxyhalides, sulfates and other groups which may exchange with oxygen under high temperatures so that the metal compounds become metal oxides.
• the metal compounds are soluble in water or an acid.
• the molybdenum compound and the tungsten compound are ammonium salts, that the phosphorus compound is phosphoric acid, and that the bismuth compound, the ferric compound, the nickel compound, the cobalt compound, the magnesium compound, the zinc compound, the cesium compound, the potassium compound, the rubidium compound, the thallium compound, the manganese compound, the barium compound, the chromium compound, the boron compound, the sulfur compound, the silicon compound, the aluminum compound, the titanium compound, the cerium compound, the tellurium compound, the tin compound, the vanadium compound, the zirconium compound, the lead compound, the cadmium compound, the copper compound and the niobium compound are nitrates, oxides or acids and the antimony compound is an oxide.
• the process of using the catalyst is generally to contact propylene or isobutylene and a molecular oxygen-containing gas in the presence of the catalyst of the present invention.
• This process is a gas phase catalytic oxidation of an olefin to an aldehyde.
• the use of the catalyst of the present invention in this process increases activity and selectivity to the production of methacrolein.
• a catalyst for producing acrolein or methacrolein by oxidation of propylene or isobutylene.
• the oxidation is a catalytic reaction that converts an olefin in the presence of oxygen to an unsaturated aldehyde and water:
• Carboxylic acid is also produced in a side reaction.
• the catalyst is a mixed metal oxide of the formula:
• a is in the range from 0.1 to 1.5
• c is in the range from 0.2 to 5.0
• g is in the range from 0.1 to 1.5
• x is determined by the valences of the other components .
• g is in the range from 0.4 to 1.5
• U.S. patent no. 5,728,894 discloses three relationships ' of relative atomic ratios : iron to bismuth and cerium: 0 ⁇ d/ (a+b+d) ⁇ 0.9
• bismuth, cerium and potassium 0.05 ⁇ b/ (a+b+c) ⁇ 0.7 potassium to bismuth and cerium: 0 ⁇ c/(a+b+c) ⁇ 0.4
• the first relationship of relative atomic ratios defines the relative amount of iron to bismuth. Based on this relationship, the iron content should be less than the bismuth content, which can be seen in the examples of U.S. Patent no. 5,728,894.
• the second relationship of relative atomic ratios defines the relative amount of cerium content .
• Cerium is not a required element of the catalyst of the present invention.
• U.S. Patent no. 5,728,894 discloses cerium as an indispensable element of this prior art catalyst .
• the third relationship of relative atomic ratios defines the relative amount of alkaline metals in the catalyst to the bismuth content.
• the relative amount of alkaline metals to bismuth is greater than the upper limit disclosed in U.S. Patent no. 5,728,894 (0.4).
• cerium, potassium and cobalt are indispensable elements while in the catalyst of the present invention these elements are optional.
• the catalyst of the present invention is of the formula: Mo 12 Bi a b Fe c Cs g M m 0 x wherein M is one or more selected from cobalt, nickel, magnesium, zinc, potassium, rubidium, thallium, manganese, barium, chromium, cerium, tin, lead, cadmium and copper, m is in the range from 0 to 9 and b is 0 to 9.
• the catalyst is of the formula: Mo 12 Bi a W b Fe o Cs g M m M ' I ..0 je wherein M' is one or more of antimony, phosphorus, boron, sulfur, silicon, aluminum, titanium, tellurium, vanadium, zirconium and niobium and m' is from 0 to 9. M' and m 1 would not be taken into account in the formulae above for relative amounts of components. Most preferably, the catalyst is- of the formula:
• c:g is in the range of 3.3-4.8
• c:a is in the range of 2.4-4.8
• the process of ' making the catalyst is generally to dissolve the metal compounds dissolved in water or in an acid and precipitate a catalyst precursor which is calcined to form a mixed metal oxide catalyst.
• the metal compounds may be salts (e.g., nitrates, halides, ammonium, organic acid, inorganic acid) , oxides, hydroxides, carbonates, oxyhalides, sulfates and other groups which may exchange with oxygen under high temperatures so that the metal compounds become metal oxides.
• the metal compounds are soluble in water or an acid.
• the molybdenum compound and the tungsten compound are ammonium salts, such as ammonium paramolybdate or ammonium molybdate and ammonium paratungstate or ammonium tungstate, respectively, that the phosphorus compound is phosphoric acid, that the bismuth, iron, cobalt, nickel, cesium, magnesium, zinc, phosphorus, potassium, rubidium, thallium, manganese, barium, chromium, boron, sulfur, silicon, aluminum, titanium, cerium, tellurium, tin, vanadium, zirconium, lead, cadmium, copper and niobium compounds are nitrates, oxides or acids and that the antimony compound is an oxide, such as antimony oxide or antimony trioxide.
• ammonium salts such as ammonium paramolybdate or ammonium molybdate and ammonium paratungstate or ammonium tungstate, respectively
• the phosphorus compound is phosphoric acid
• the present invention does not depend on a particular order of addition of the components. While a particular order of addition of the various metal compound components may affect the performance of the catalyst, the present invention is directed toward the particular relative amount of certain components to other components without regard to the order in which the steps in the process of making the catalyst occur.
• An example of making the catalyst of the claimed invention is to dissolve an ammonium salt of molybdenum, such as ammonium paramolybdate or ammonium molybdate and, optionally, an ammonium salt of tungsten, such as ammonium paratungstate or ammonium tungstate, and phosphoric acid in water, dissolve a bismuth nitrate in an acid, dissolve a iron nitrate and, optionally, a cobalt nitrate, a nickel nitrate, a magnesium nitrate, and a zinc nitrate in water or in the acid with the bismuth nitrate, mix the solutions at a temperature in the range from 40°C to 100°C, preferably 60°C to 95°C, to obtain a precipitate to form a slurry and then add a cesium nitrate and, optionally, an antimony oxide to the slurry while maintaining the temperature.
• an ammonium salt of molybdenum such as ammonium paramolybdate
• the cesium nitrate and the antimony oxide may be added to the slurry as solids.
• the slurry may be aged for 2 to 24 hours, preferably 8 to 18 hours, most preferably 5 to 10 hours.
• the liquid of the slurry is removed by evaporation and the solid precipitate is dried and calcined to obtain a catalyst.
• the liquid may be removed and the solid precipitate dried at the same time by spray drying.
• the liquid may be evaporated at a temperature of 50° to 125°C.
• Drying of the catalyst precursor may be in air or an inert gas and in an oven or a spray dryer. Preferably, drying is in an oven in air at a temperature of 100-150°C for 2-5 hours
• the catalyst precursor may be calcined at a temperature of 200-600°C for 1-12 hours. Calcination may be in two stages, one at a temperature of 150- 400°C for 1-5 hours and another at a temperature of 460-600°C for 4-8 hours. For a two-stage calcination, preferably, the first is at a temperature of 290-310°C for 2 hours and second at a temperature of 460-500°C for 6 hours. Denitrification may occur in the first step.
• calcination is in one stage at a temperature of 485°C for 2 hours with a temperature ramp of up to 10°C/min from ambient temperature to 485 °C instead of an initial step or denitrification at a temperature of 300°C for two hours. Calcination may be done in a high temperature oven or kiln.
• the catalyst may be processed by sieving, forming and other means known in the art to obtain catalyst particles of a certain size. Desired particle size and particle size distribution are related to the design of the reactor (size, shape, configuration, etc.), to the pressure drop . intended for the process and to the process flow.
• the catalyst may be sieved or formed after the first stage calcination and before the second stage calcination. In a commercial process the catalyst precursor may be sieved and formed after spray drying and before calcination.
• the X-ray diffraction pattern of the mixed metal oxide compounds is descriptive of the catalyst made by the process of the present invention.
• the catalyst compositions of the Examples above have a characteristic X-ray diffraction having diffraction peaks at the diffraction angles of 2 ⁇ , measured by using Cu K ⁇ radiation, at 25.5, 26.6 and 28.0 (+/-0.1 0 ). There may be several additional diffraction peaks present in a catalyst composition of the present invention but these peaks will normally be evident .
• the catalyst of the present invention may be used as an unsupported catalyst or a supported catalyst.
• the surface area of an unsupported catalyst is from 0.1 to 150m 2 /g, preferably from 1 to 20 m 2 /g.
• the support should be an inert solid which is chemically unreactive with any of the active components of the catalyst and is preferably silica, alumina, niobia, titania, zirconia or mixtures thereof.
• the catalyst may be affixed to the support by methods known in the art, including incipient wetness, slurried reactions and spray drying.
• the catalyst is not limited by shape, size or particle distribution and may be formed as appropriate for the reaction vessel in the process. Examples are powder, granules, spheres, cylinders, saddles, etc.
• the catalyst is used in the gas phase catalytic oxidation of a feedstock gas comprising propylene or isobutylene, oxygen, water and an inert gas, such as nitrogen,,, to produce acrolein or methacrolein.
• Oxygen may be supplied in the pure form or in an oxygen containing gas, such as air or as an oxygen-diluent gas mixture.
• the diluent gas may be nitrogen, a hydrocarbon which is gaseous under the process conditions or carbon dioxide.
• the reaction temperature is preferably from 250-450°C, most preferably 370-410°C.
• the reactor may be a fixed bed or a fluidized bed reactor. Reaction pressure may be from 0 to 100 psig.
• Space velocity may be from 800 to 8000 hr "1 .
• a second solution was prepared by adding 1.3 ml of 70% nitric acid to 9.3/ ml of de-ionized water. 9.98 g of bismuth nitrate was dissolved in the nitric acid solution. To this solution was added 19.94 g of ferric nitrate, 23.92 g nickel nitrate, 12.03 g of cobalt nitrate, 2.64 g of magnesium nitrate, 3.24 g of zinc nitrate and 85.3 ml of de-ionized water.
• the second solution was added to the first solution dropwise. Precipitates were formed during the addition which created a slurry.
• the slurry was aged for 10 hours at 80°C while being stirred. After aging, the liquid was evaporated at 100 °C. The solid was dried at 120°C for 3 hours. The dried solid was calcined at 300°C for 2 hours in flowing air. The calcined solid was sieved to a mesh size of 20-30. The sieved solid was calcined at 500°C for 6 hours in flowing air.
• a catalyst of the following composition was obtained: Mo 12 Bi 1 . 0 W 0-3 Fe 2 . 4 Co 2 . 0 Ni 4>0 Sb 0 ⁇ 7 Cs 0 ⁇ 6 Mg 0-s Zn 0-s .
• Example 1 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 5.20 g, so that the composition of the catalyst was Mo 12 Bi 0.s W 03 Fe 2,4 Co 2 . 0 Ni 4 . 0 Sb 0 . 7 Cs 0 . 6 Mg 0-s Zn 05 .
• EXAMPLE 3 The procedure of Example 1 was repeated except the amount of the bismuth nitrate was 11.6 g and the amount of the ferric nitrate was 23.4 g so, that the composition of the catalyst was Mo 12 Bi 1 . 2 W 0 . 3 Fe 2 . 9 Co 2 . 0 Ni 4 . 0 Sb 0 . 7 Cs Q . s Mg 0 . 5 Zn 0 . 5 .
• Example 2 The procedure of Example 1 was repeated except the amount of ammonium paramolybdate was 45.01 g, the amount of the amount of nickel nitrate was 36.0 g, the amount of magnesium nitrate was 5.21 g, cobalt nitrate, zinc nitrate and ammonium paratungstate were not present and the ammonium molybdate solution was heated to 95°C over 45 minutes before the second solution was added and the catalyst precursor 485 °C with a 10°C/min ramp so that the composition of the catalyst was Mo 12 Bi x 2 Fe 2 . 4 Ni s _ 0 Sb 0 _ 7 Cs Q _ s Mg : 0 .
• Example 1 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 5.98 g and the amount of ferric nitrate was 11.57 g so that the composition of the catalyst was Mo 12 Bi 0 . 6 W 0 . 3 Fe 2 . 0 Co 2-0 Ni 4 . 0 Sb 0 . 7 Cs 0,6 Mg 0 . 5 Zn 0 . s .
• EXAMPLE 6 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 6.25 g and the amount of ferric nitrate was 17.4 g so that the composition of the catalyst was Mo 12 Bi 0 . s W 0 . 3 Fe 2.0 Co 2-0 Ni 4 . 0 Sb 0 . 7 Cs 0 . s Mg 0,s Zn 0 . ⁇ .
• Example 2 The procedure of Example 1 was repeated except no ammonium paratungstate was added so that the composition of the catalyst was Mo 12 Bi 1.0 Fe 2 . 4 Co 2.0 Ni 4 . 0 Sb 0.7 Cs 0.6 g 0 . s Zn 0 . s .
• Example 2 The procedure of Example 1 was repeated except no ammonium paratungstate was added and 44.7 g of ammonium molybdate was added so that the composition of the catalyst was Mo 12 . 3 Bi 1 . 0 Fe 2 . 4 Co 2 . 0 Ni 4 . 0 Sb 0 . 7 Cs 0 . ⁇ g 0 . 5 Zn 0 . B .
• Example 2 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 2.65 g so that the composition of the catalyst was Mo 12 Bi 0 . 25 W 0 . 3 Fe 2 . 4 Co 2 . 0 Ni 4.0 Sb 0 . 7 Cs 0 . s Mg 05 Zn 0 . s . COMPARATIVE EXAMPLE 2
• Example 2 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 14.39 g so that the composition of the catalyst was Mo 12 Bi 1 . s W 0 . 3 Fe 2 . 4 Co a . 0 Ni 4 . 0 Sb 0>7 Cs 0 . ⁇ Mg 0 . 5 Zn 0 . s .
• Example 2 The procedure of Example 1 was repeated except the amount of cesium nitrate was 4.68 g so that the composition of the catalyst was Mo u Bi 1.0 W 0 . 3 Fe 2 . 4 Co 2 . 0 Ni 4 . 0 Sb 0.7 Cs 1 . 2 Mg 0.5 Zn 0.s .
• Example 1 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 8.12 g, the amount of ferric nitrate was 16.91 g and the amount of cesium nitrate was 16.91 g so that the composition of the catalyst was
• Example 2 The procedure of Example 1 was repeated except the amount of bismuth nitrate was 11.24 g, the amount of ferric nitrate was 22.63 g and the amount of cesium nitrate was 1.89 g so that the composition of the catalyst was Mo 12 Bi 1 . 2 W 0 . 3 Fe 2 . 9 Co 2 . 0 Ni 4 . 0 Sb 1 . 5 Cs 0 . 5 Mg 0 . s Zn 0.5 .
• Example 2 The procedure of Example 1 was repeated except the amount of ferric nitrate was 10.31 g so that the composition of the catalyst was o 12 Bi 1 . 0 0 . 3 Fe 1 . 2 Co 2 . 0 Ni 4 . 0 Sb 0 . 7 Cs 0 . ⁇ Mg 0 . s Zn 0 . s .
• Example 2 The procedure of Example 1 was repeated except the amount of ammonium paramolybdate was 54.46 g so that the composition of the catalyst was Mo ls Bi 1 . 0 W 0.3 Fe 1.2 Co 2 . 0 Ni 4 . 0 Sb 0 . 7 Cs 0 . s Mg 0 . s Zn 0.5 .
• Example 2 The procedure of Example 1 was repeated except the amount of ammonium paramolybdate was 32.86 g so that the composition of the catalyst was Mo g Bi 1 _ 0 W 0 _ 3 Fe 2 _ 4 Co 2 _ disciplineNi 4.0 Sb 0-7 Cs 0-s Mg 0.s Zn 0-s .
• Catalyst activities are reported in Table I relative to example 6, for which 1.5 cc of catalyst at a flow rate of 38 seem gave 97.7% conversion, 89.1% selectivity to methacrolein and methacrylic acid, and a one-pass yield of 87.0%. Repeated tests of example 6 suggest that the accuracy of the activity measurement is roughly ⁇ 5%.
• the catalyst which has a ratio outside the ranges of 2-6, 3.3-5 and 0.9 to 1.1, respectively, and has selectivity as good as that of catalysts of the present invention (Comparative Example 2) has activity which is unsuitable for good catalyst performance (0.65 relative activity) .
• Those catalysts which have ratios outside the ranges of 2-6, 3.3-5 and 0.9 to 1.1, respectively, and have activity higher than that of catalysts of the present invention (Comparative Examples 1, 5 and 7 at 2.25, 1.48 and 1.62 relative activity) have selectivities which are unsuitable for good catalyst performance (-1, -4 and -2 relative selectivity) .

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