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  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
  • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
• • 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
  • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
  • B01J21/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
  • B01J21/063—Titanium; Oxides or hydroxides thereof
• • 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
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• • 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
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/20—Vanadium, niobium or tantalum
• • 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
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/24—Chromium, molybdenum or tungsten
  • B01J23/28—Molybdenum
• • 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
  • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/24—Chromium, molybdenum or tungsten
  • B01J23/30—Tungsten
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/66—Silver or gold
  • B01J23/68—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/683—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum or tungsten
  • B01J23/686—Silver or gold with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium with chromium, molybdenum or tungsten with molybdenum
• • 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
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/02—Impregnation, coating or precipitation
  • B01J37/0236—Drying, e.g. preparing a suspension, adding a soluble salt and drying
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
  • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
  • C07C51/215—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of saturated hydrocarbyl groups
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
  • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
  • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
• • 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
  • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
  • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/56—Platinum group metals
  • B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
  • B01J23/652—Chromium, molybdenum or tungsten
• • 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
• • 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
  • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
  • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
  • B01J37/0027—Powdering
  • B01J37/0045—Drying a slurry, e.g. spray drying

Definitions

• the present invention relates to a catalyst composition for the selective oxidation of ethane to acetic acid and/or for the selective oxidation of ethylene to acetic acid, and to a process for the production of acetic acid utilizing the aforesaid catalyst composition.
• Catalyst compositions comprising molybdenum, vanadium and niobium in combination with oxygen for use in processes for the production of acetic acid by the oxidation of ethane and/or ethylene are known in the art from, for example, U.S. Pat. No. 4,250,346, EP-A-1043064, WO 99/20592 and DE 196 30 832.
• U.S. Pat. No. 4,250,346 discloses the oxidative dehydrogenation of ethane to ethylene and acetic acid in a gas phase reaction, at a temperature of less than about 550° C. using as a catalyst a composition comprising the elements molybdenum, X and Y in the ratio Mo a X b Y c wherein X is Cr, Mn, Nb, Ta, Ti, V and/or W, and preferably Mn, Nb, V and/or W; Y is Bi, Ce, Co, Cu, Fe, K, Mg, Ni, P, Pb, Sb, Si, Sn, Tl and/or U, and preferably Sb, Ce and/or U, a is 1, b is 0.05 to 1.0 and c is 0 to 2, and preferably 0.05 to 1.0, with the proviso that the total value of c for Co, Ni and/or Fe is less than 0.5.
• EP-A-1043064 discloses a catalyst composition for the oxidation of ethane to ethylene and/or acetic acid and/or for the oxidation of ethylene to acetic acid which comprises in combination with oxygen the elements molybdenum, vanadium, niobium and gold in the absence of palladium according to the empirical formula: Mo a W b Au c V d Nb e Y f (I) wherein Y is one or more elements selected from the group consisting of: Cr, Mn, Ta, Ti, B, Al, Ga, In, Pt, Zn, Cd, Bi, Ce, Co, Rh, Ir, Cu, Ag, Fe, Ru, Os, K, Rb, Cs, Mg, Ca, Sr, Ba, Zr, Hf, Ni, P, Pb, Sb, Si, Sn, Tl, U, Re, Te and La; a, b, c, d, e and f represent the gram atom ratios of the elements such that
• the present invention provides a catalyst composition for the oxidation of ethane and/or ethylene to acetic acid, which composition comprises in combination with oxygen the elements molybdenum, vanadium, niobium and titanium according to the empirical formula: Mo a W b Ti c V d Nb e Y f (I) wherein Y is one or more elements selected from the group consisting of: Cr, Mn, Ta, B, Al, Ga, In, Pt, Zn, Cd, Bi, Ce, Co, Rh, Ir, Cu, Ag, Fe, Ru, Os, K, Rb, Cs, Mg, Ca, Sr, Ba, Zr, Hf, Ni, P, Pb, Sb, Si, Sn, Tl, U, Re, Te, La, Au and Pd; a, b, c, d, e and f represent the gram atom ratios of the elements such that:
• Catalyst compositions embraced within the formula (I) include:— Mo a W b Ti c V d Nb e Y f Mo a. Ti c V d Nb e Y f Mo a W b. Ti c V d Nb e Mo a. Ti c V d Nb e
• Y when present, is selected from the group consisting of Bi, Ca, Ce, Cu, K, P, Sb, La and Te.
• the catalyst compositions according to the present invention comprise a titanium component.
• the catalyst compositions according to the present invention are substantially devoid of noble metals, such as Pd and/or Au.
• a second aspect of the present invention relates to a process for the preparation of the catalyst compositions according to the first aspect of the present invention, comprising the steps of:
• the mixture comprising molybdenum, vanadium, niobium, titanium, optionally tungsten and optionally Y may be formed by mixing compounds and/or complexes of each of the metals in a suitable solvent.
• the solvent is preferably water, and most preferably the mixture is a solution in water having a pH in the range from 1 to 12, preferably from 2 to 8, at a temperature of from 20° to 100° C.
• the molybdenum is introduced in to the mixture in the form of ammonium salts such as ammonium heptamolybdate, or organic acids of molybdenum, such as acetates and oxalates.
• ammonium salts such as ammonium heptamolybdate
• organic acids of molybdenum such as acetates and oxalates.
• Other compounds of molybdenum which may be used include, for example, molybdenum oxides, molybdic acid and/or molybdenum chlorides.
• the vanadium is introduced in to the mixture in the form of ammonium salts, such as ammonium metavanadate or ammonium decavanadate, or organic acids of vanadium, such as acetates and oxalates.
• ammonium salts such as ammonium metavanadate or ammonium decavanadate
• organic acids of vanadium such as acetates and oxalates.
• Other compounds of vanadium which may be used include, for example, as vanadium oxides and sulphates.
• the niobium is introduced in to the mixture in the form of ammonium salts, such as ammonium niobium oxalate.
• ammonium salts such as ammonium niobium oxalate.
• Other compounds of niobium, such as niobium chlorides, may also be used, preferably complexed with an oxalate, a carboxylic acid or similar coordinating compound to improve solubility.
• the titanium component of the catalyst composition is introduced to the mixture in the form of a soluble or reactive precursor, such as a halide or alkoxide. More preferably, the titanium component of the catalyst composition is introduced to the mixture as a titanium alkoxide, most preferably as titanium isopropoxide.
• the mixture of compounds containing the elements is prepared by dissolving sufficient quantities of soluble compounds and dispersing any insoluble compounds so as to provide a desired gram-atom ratio of the elements in the catalyst composition.
• the solvent is removed from the mixture by drying, preferably by spray-drying, to form a dried solid material.
• This dried solid material is then calcined to form the catalyst composition. Calcination is preferably performed by heating to a temperature of from 200 to 550° C., suitably in air or oxygen, for a period of from 1 minute to 24 hours.
• the catalyst composition of the present invention may be used unsupported or supported.
• Suitable supports include silica, alumina, titania, titanosilicates, zirconia, silicon carbide and mixtures of two or more thereof, preferably silica.
• Titanium may be present in a supported catalyst composition both as a component of the catalyst composition on the support, and as a component of the support itself, such as a titania support or as part of a support comprising titanium, for example as part of a mixed support comprising both titania and silica supports, or as part of a titanosilicate support.
• the catalyst composition When used on a support, the catalyst composition typically comprises at least about 10% and/or up to about 80% by weight of the total weight of the catalyst composition and the support (with the remainder being the support material). Preferably the catalyst composition comprises at least 40 wt % of the total weight of the catalyst composition and the support and/or up to 60 wt % of the total weight of the catalyst composition and the support.
• the supported catalyst composition When used on a support, the supported catalyst composition may be prepared according to the process of the second aspect of the present invention by addition of the a support material or a suitable precursor thereof, such as a sol, for example, a silica sol, to the mixture comprising molybdenum, vanadium, niobium, titanium, optionally tungsten and optionally Y.
• a support material or a suitable precursor thereof such as a sol, for example, a silica sol
• the support material or suitable precursor thereof may be added at any suitable stage, such as, for example, during drying, such as after a partial drying, of the mixture.
• the support material or suitable precursor thereof is introduced to the mixture prior to drying the mixture in step (b), most preferably by introducing the support material or suitable precursor thereof during formation of the mixture in step (a), such that said support material or suitable precursor thereof forms a component of said mixture formed in step (a).
• a process for the selective production of acetic acid from a gaseous mixture comprising ethane and/or ethylene which process comprises contacting the gaseous mixture with a molecular oxygen-containing gas at elevated temperature in the presence of a catalyst composition as hereinbefore described.
• the feed gas comprises ethane and/or ethylene, preferably ethane.
• Ethane and/or ethylene may each be used in substantially pure form or admixed with one or more of nitrogen, methane, carbon dioxide and water in the form of steam, which may be present in major amounts, for example greater than 5 volume percent or one or more of hydrogen, carbon monoxide, C 3 /C 4 alkenes and alkenes, which may be present in minor amounts, for example less than 5 volume percent.
• the molecular oxygen-containing gas may be air or a gas richer or poorer in molecular oxygen than air, for example oxygen.
• a suitable gas may be, for example, oxygen diluted with a suitable diluent, for example nitrogen.
• the elevated temperature may suitably be in the range from 200 to 500° C., preferably from 200 to 400° C.
• the pressure may suitably be atmospheric or superatmospheric, for example in the range from 1 to 50 bar, preferably from 1 to 30 bar.
• the process of the third aspect may be a fixed bed or a fluidised bed process.
• a high selectivity to acetic acid may be achieved in combination with a low, if any, selectivity to ethylene.
• the selectivity to acetic acid is at least 50 mol %, preferably at least 55 mol %, and most preferably at least 60 mol %.
• the selectivity to ethylene is less than 30 mol %, preferably less than 20 mol %, and most preferably less than 10 mol %.
• the selectivity to acetic acid is at least 60 mol % and the selectivity to ethylene is less than 10 mol %.
• Catalyst A Mo 1.00 V 0.529 Nb 0.124 Au 0.0012 Ti 0.331 O x
• Solution A 214 g of ammonium heptamolybdate was dissolved in 250 g of water at 45° C. with stirring.
• Solution B 75 g of ammonium metavanadate was added to 725 g of water in a 2-liter beaker and heated to 80° C. The ammonium metavanadate did not completely dissolve.
• Solution C 74 g of ammonium niobium oxalate was added to 275 g of water in a 6-liter stainless steel beaker and heated to 45° C. A sol formed within 30 minutes.
• Solution C was added to solution B and allowed to digest at 80° C. for 30 minutes.
• Solution A was then added to the mixture of solution C and solution B, and then stirred for 15 minutes at medium heat to give a slurry.
• 0.425 g AuCl 3 were then added to the slurry to give a slurry containing Mo, V, Nb and Au.
• 638 grams of silica sol (Nalco 41D01) were then added to the stirred slurry.
• 111 grams of titanium isopropoxide were dripped into the slurry at 50° C. Percent solids was adjusted to ⁇ 36%.
• the slurry was homogenized at 10,000 rpm for approximately 2 minutes. Spray drying was carried out in a mini-Niro spray-drier immediately after the solution was homogenized to form a spray-dried supported catalyst composition.
• the spray drying conditions used were as follows: an inlet temperature of 290° C. inlet and an outlet temperature of 138° C.
• the spray-dried supported catalyst composition was then calcined in air for 3 hours at 375° C. in a static muffle furnace.
• the resultant spray-dried supported catalyst composition (Catalyst A) had a nominal composition Mo 60.5 V 32 Nb 7.5 Au 0.07 Ti 20 O x on silica, and at a nominal metal loading of 44% of the total catalyst weight.
• the supported catalyst composition had a surface area of 32 m 2 /g and a density of 1.15 g/cm 3 .
• Catalyst B Mo. 1.00 V 0.529 Nb 0.124 Ti 0.331 O x
• Catalyst B had a similar nominal composition as Catalyst A but without the addition of gold.
• Catalyst B was prepared as described for Catalyst A, but without the addition of AuCl 3 .
• the spray-dried supported catalyst composition B had a nominal composition Mo 60.5 V 32 Nb 7.5 Ti 20 O x on silica, and at a nominal metal loading of 44% of the total catalyst weight.
• the supported catalyst composition B had a density of 1.16 g/cm 3 (and was expected to have a surface area of approximately 30 m 2 /g (not measured)).
• Comparative Catalyst 1 had a similar nominal composition to Catalysts A and B but without the addition of gold or titanium. Comparative catalyst 1 was prepared as described for Catalyst A, but without the addition of AuCl 3 or titanium isopropoxide.
• the resultant spray-dried supported catalyst composition had a nominal composition Mo 60.5 V 32 Nb 7.5 O x on silica, and at a nominal metal loading of 50% of the total catalyst weight.
• the supported catalyst composition had a surface area of 28 m 2 /g and a density of 1.2 g/cm 3 .
• Comparative Catalyst 2 had a similar nominal composition to Catalyst A but without the addition of titanium. Comparative catalyst 2 was prepared as described for Catalyst A, but without the addition of titanium isopropoxide.
• the resultant spray-dried supported catalyst composition had a nominal composition Mo 60.5 V 32 Nb 7.5 Au 0.07 O x on silica, and at a nominal metal loading of 50% of the total catalyst weight.
• the supported catalyst composition had a surface area of 36 m 2 /g and a density of 1.21 g/cm 3 .
• Comparative Catalyst 3 had a similar nominal composition to Comparative Catalyst 2 except that a palladium component was added. Comparative catalyst 3 was prepared as described for Catalyst A except that 0.0124 g of palladium (IV) chloride was added directly after the gold (III) chloride and without the addition of titanium isopropoxide.
• the resultant spray-dried supported catalyst composition had a nominal composition Mo 60.5 V 32 Nb 7.5 Au 0.07 Pd 0.007 O x on silica, and at a nominal metal loading of 50% of the total catalyst weight.
• the supported catalyst composition had a surface area of 24 m 2 /g and a density of 1.23 g/cm 3 .
• the catalyst to be tested was sieved to obtain a specific particle size distribution (psd) of 70% 230/325 mesh (50/50), 25% pans (fines) and 5% greater than 170 mesh.
• 10 grams of catalyst and an inert diluent with the same particle size distribution (St Gobain SA 539 alpha alumina, 43 g, density 1.27 g/ml) were added into a 40 cc fluidised bed reactor.
• the reaction was typically performed at a temperature between 310° C. and 320° C. and at a reaction pressure of 16 barg.
• Ethane, ethylene (to mimic a recycle of ethylene), nitrogen and oxygen mixture was fed to the reactor using Brooks Mass Flow Controllers.
• Catalyst A was tested under the conditions in Table A below: TABLE A Run Conditions (Feed mol %) Pres- Total sure Max T Flow GHSV Barg ° C. ml/min h-1 C 2 H 6 C 2 H 4 H 2 O O 2 N 2 16 311-316 428 3240 60.2 5.2 5.0 6.5 23.3 During the test there was an initial period during which the acetic acid space-time yield (STY) and oxygen conversion increased whilst the ethylene STY decreased. After this period Catalyst A settled down to produce acetic acid and low levels of ethylene. The averaged selectivity data between 100-180 hours on stream is presented in Table 1 below.
• Catalyst B was tested under the conditions in Table B below: TABLE B Run Conditions (Feed mol %) Pres- Total sure Max T Flow GHSV Barg ° C. ml/min h-1 C 2 H 6 C 2 H 4 H 2 O O 2 N 2 16 310-320 428 3200 60.2 5.0 5.0 6.5 23.3
• Catalyst B showed a similar profile to Catalyst A, in that during the test there was an initial period during which acetic acid space-time yield (STY) and oxygen conversion increased whilst the ethylene STY decreased after which Catalyst B settled down to produce acetic acid with only low levels of ethylene.
• STY acetic acid space-time yield
• the averaged selectivity data between 100-180 hours on stream is presented in Table 1 below. Comparative Catalysts

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