SA99526033B1 - Catalyst for the production of a gas phase of acetic acid from ethane, processes for its preparation and methods for its use - Google Patents

Abstract

Abstract: A mixed metal oxide catalytic system composed of molybdenum, vanadium, lanthanum and palladium provides higher yields than acetic acid in the low-temperature single-stage oxidation of ethane with molecular oxygen-containing gas. oxygen without or with reduced production of by-products eg ethylene and carbon monoxide (CO).

Description

a catalyst for the production of a gaseous state of acetic acid from ethane; Processes for its preparation and methods for its use Full Description This application is a partial application of Application No. 7.2.8567 48 filed in the Kingdom of Saudi Arabia on a) ETA corresponding to 17/17/1433AD. Invention background:

° The present invention relates to a catalyst; The method of its preparation and catalytic processes for its use, and more specifically to the hydrogenation separation - selective oxidation 2 at low temperature of ethane (or a mixture of ethane and ethylene to acetic acid acid 2060). The invention is concerned with catalytic processes Single-stage using a new catalyst characterizes an increased conversion of ethane and production of acetic acid in

00 Roof is a special treatment as the flowing product stream contains distinct amounts of by-products, for example ethylene and carbon monoxide (CO). Numerous leaflets are indicated in this application. Those references describe the state of the field in which this invention relates; They are incorporated here by attribution. As a result of environmental legal restrictions; Carbon monoxide, CO, is a by-product *0 that is not required from an industrial point of view. Moreover, the separation of ethylene from ethane has a significant impact on the economic aspects of ethane oxidative dehydrogenation separation processes; Whereas, the required product is an oxygenated hydrocarbon ¢, for example, acetic acid. A. Traditionally, acetic acid is produced by methanol carboxylation using expensive rhodium catalysts. rhodium in homogeneous liquid-state reactions; which require complex methods for extracting the catalysts and separating the products; More recently, very expensive raw materials for the conversion of ethylene into acetic acid were recorded by the production of acetaldehyde as a by-product Ye. yay v a process for the more selective production of 0 76846 EP discusses acetic acid publication 0 by the oxidation of 0 ethane by oxygen in contact with -: a physical mixture of two catalysts consisting of to ethane Ethane oxydehydrogenation to separate hydrogenation [ oxidation catalyst a) catalyst and ethylene ethylene ° | ethylene hydration/oxidation for the hydration of [oxidation catalyst b) a catalyst for ethane 8 only for the catalytic oxydehydrogenation of metals one or more metals Jud 7 can Cus; Mox Vy 2 by the formula A R + Cd «Zn Mg » Be: Na Lie W Ti ¢ Sr.

Ca 1 + Nb from ethylene agent For ethylene hydration/oxidation The catalyst is chosen for hydration / oxidation 0 Palladium oxide Molecular Sieve Catalyst Molar shaker catalyst or agents - tungsten -phosphorus oxides tungsten oxides ¢ palladium European Patent Bulletin. tin molybdenum catalyst containing tin-molybdenum employs the catalytic system prepared by means of a physical mixture of two types of catalysts No. 1742. yo molybdenum It has been reported that the use of catalyst systems containing molybdenum in oxydchydrogenation temperature for oxidative hydrogenation separation of vanadium and vanadium by Thorstenson et al. 0 0 C to ethylene 6 by means of any ethane reduced to ethane JB-111; Gazette Catalysts; gad? 8 pages. EM.

Thorsteinson et al., This study discusses another transition molybdenum-0 (VavA)-0 mixed oxide catalysts; The catalytic 56 together with vanadium metal oxide and vanadium molybdenum catalysts are . Ce tal length O 6 00 Mn “Cr” Ti, for example, is active at temperatures as low as 8000 C for oxidative hydrogenation separation. A portion of the acetic acid produced as a by-product 0 of ethane to ethylene oxydehydrogenation Several US patents have been granted (No. At a low temperature of ethane to ethylene oxydehydrogenation 1£4Y

¢ 0 ve is concerned with the use of catalysts of formula Mon V, Nb; Ax in which A is “Ce as 1 Pi Tl O NA equals VY +1 equals AT ; E equals 50087 0 X and equals 1 - © . US Patent No. 071 directs the use of a calcined catalyst of the formula Mo, Vy Nb, Sb Xe Ls to form acetic acid as a by-product US Patent No. 73766 4 Merri Concerning Oxide Catalysts Containing V “NO Mo and a Fourth Metal Selected from MncIn 28 0 6 Co or Not for 0 Oxidation / ammoxidation treatment / 8 of unsaturated aliphatic aldehydes to corresponding saturated aliphatic carboxylic acides European patent publication no. tungsten vanadium 0 vanadium rhenium 0 and at least one of the alkali metals for the production of ethylene and acetic acid by oxidation of ethane by gas 5 containing molecular oxygen replacing tungsten in whole or in part Using molybdenum implemented in European patent publication No. 100a, an increase in the selectivity of acetic acid is produced in light of the selectivity of ethylene.

0 European Patent Bulletin No. 0 SYAOEA is concerned with a process for the production of acetic acid by Gb ethane oxidation in contact with a solid catalyst containing the empirical formula, and VR Mo where 14 is one or More than one optional element selected from Cu Co 6x “We Nb” and many others; Except for molybdenum, 1 molybdenum is equal to Yo a which is equal to 0-1,..

V, Tip Ox Jin European Patent Publication No. 27461 is concerned with the use of the Yo-factor as a catalytic formation. Acetic acid aes to 6 oxidation for the oxidation of ethane includes additional components from a large list of potential components.

° Moreover; MoVND-containing catalysts enhanced by phosphorous and boron have recently been reported to produce relatively higher yields of acetic acid compared to unsupported catalysts by producing by-products e.g. carbon monoxide (CO); Carbon Dioxide 8 and Ethylene © . and look; US Application Serial No. Vo A remu filed on September 11th Lahk 1 by Karim et al. 0 entitled “Catalysts for the oxidation of ethane to Aes ¢ acetic acid for their preparation and processes for their use.” More Novelty; it reported a catalyst containing niobium “palladium ¢ molybdenum” and vanadium for use in saw sage 0 ethane oxidation See; American serial application number L 33 filed in YE December 19897 by Karim et al. 'Catalysts for the production of acetic acid from the oxidation of ethane 0 Processes for their preparation and methods for their use.' From a commercial point of view, niobium is an expensive raw material that can be None of these publications discuss or suggest the advantages of the catalysts discussed in the present invention, which are commercially cheaper and include higher efficiency for the selective yield of acetic acid during the oxidation process. 8 Single-stage ethane moieties with reduced or zero CO and ethylene production and higher acetic acid yield and/or selectivity. A) General description of the invention: One of the objectives of the present invention is to overcome specific defects, Ti. The objective, Sa, of the present invention is to provide improved methods for conducting fluid-state catalytic chemical reactions. Yo The other goal of the current Sad is to provide improved catalytic systems for the production of acetic acid from ethane.

. Another objective of the present invention is to provide an improved method for producing acetic acid with high selectivity and yield for the required product; eg acetic acid acid 2666 and a reduced yield of by-products eg carbon monoxide .CO The further objective of the present invention is to provide methods for the preparation and use of improved catalysts for the production of acetic acid. The foregoing and other objectives and features of the present invention will be identified in or highlighted by the present description. Detailed description of the invention: The present invention is generally concerned with fluid-state catalytic reactions and catalysts 0 to carry out these reactions 0 and more specifically » the present invention is concerned with methods whereby ethane 6 is oxidized by molecular oxygen to acetic acid in a gas-state reaction with relatively high rates of conversion » selectivity and productivity; preferably at temperatures equal to Seon mer and pressures equal to eT and this is achieved by the use as a catalyst of calcined composition Ui, 6 of formula 0, Mo, Vy Pd; Lag where 8 equals co -1 slab why did mari to mi 0 1 equals ARR 1 5 ri w * is a number determined by the valence requirements of the other elements in the composition (ial In preference between approximately Yo numerical values of gba “gram-degree ratios represent relative proportions of iron” Lac Ve Mo 20 in succession; in the catalyst 0 the elements are believed to unite in compatibility of YO with oxygen in the form of various oxides.

One of the objects of the present invention relates to improved Mo-V-Pd-La-O catalytic systems useful in fluid-state catalytic chemical reactions e.g. oe direct conversion of ethane to acetic acid by oxidation of Mastering ethane oxidation - With the use of the new catalyst, high yields and/or high selectivity© to acetic acid are achieved by low rates of by-products such as carbon monoxide (CO) and/or ethylene. For one preferred embodiment, no measurable amounts of byproducts of carbon monoxide and/or ethylene (ply) were produced. The catalyst, Ta, of the present invention can be used with or without a support. The catalyst includes alumina, ¢ silica 8 + titania, zirconia, zeolites 85, silicon carbide, molybdenum carbide, molecular sieves, and micro-scale porous materials. micro and/or other nanoscale; and mixtures derived therefrom. When the catalyst is used above 0 um, the supported (stabilized) catalyst preferentially includes approximately N° by weight of the catalytic composition and 159-960 by weight of the support material. The other object of the present invention relates to methods of preparing the agents The improved catalyst of the invention Jal comprising the formula Mo 1.5 V 0.1.00 Pd 0000000105 La 0.0000001-0.2 The choice of the formed primary compounds 71 compounds used in addition to the 0 specific methods used in the preparation of a catalyst can have an effect Distinguished on the effectiveness of the catalyst.With preference, the catalyst is prepared from a solution of soluble compounds (salts, complexes or other compounds) from any of the metals, and with preference, the solution is an aqueous system that includes a pH (acidity or alkalinity) equal to Ye L, and at a temperature of approximately 7 78 001 C. In general, the mixture of the elements containing the elements is prepared by dissolving sufficient quantities of soluble compounds and dispersing the insoluble compounds so that the to provide

A

Atomic ratios - grams of elements in the catalytic composition. Hence, the catalytic composition is prepared. By separating the water and/or other solvent from the mixture of the compounds in the solution system by heating to a temperature close to calcined dry catalyst calcined bits in air or oxygen for a time period of approximately one hour to several hours You Requirement. lal Production Composition 0 In solution in the form of molybdenum salts and with preference; Molybdenum is brought in, for example, ammonium paramolybdate ammonium salts from molybdenum organic acid salts or organic acid salts «ammonium paramolybdate s oxalates; Oxalates, acetates, for example, molybdenum acetate, are some of the other molybdenum compounds that are soluble. glycolates and glycolates « 0200618168 0 Partially soluble in water, which can be used to include molybdenum chlorides and chlorides « molybdic acid ¢ molybdenum oxides. in the form of ammonium salts on ammonium metavanadium eg ammonium metavanadium | Ammonium 5 from vanadium, for example, organic salts or organic salts “ammonium decavanadate” can also be used. tartrates; Tartrate, oxalates, oxalates, ¢ acetates, acetates, vanadium compounds that are partially soluble in water, for example vanadium oxides and vanadium sulfates. In order to achieve complete solubility; It is possible to add a specific amount of acid, and preferably ¢, the lanthym is introduced into the slurry. oxalic or tartaric tartrates 0 e.g. lanthanum catalyst 1 in the form of lanthanum salt slurry etc.. » nitrate; Nitrate oxide in the catalytic slurry in the form of pai palladium and preferably; The palladium or a solution of palladium salts is an activated vegetable alumina or alumina pad over palladium ¢ nitrate; Nitrates, chlorides, chlorides, acetates, for example, acetates, palladium Yo, etc.

and preferably; The catalyst is prepared by the following general method. Aqueous solutions of vanadium and molybdenum 2 are prepared separately. The vanadium solution is mixed with the molybdenum solution at a special temperature, preferably between 1 and 1 pH. The third component (palladium©) is slowly added to the combined gel solution. For the supported catalysts, the required amount of the aforementioned suitable support material can be added to the aforementioned combined gel solution. After mixing and heating for approximately half to "an hour, the resulting gel is dried to initial moisture with stirring at approximately Ye Ve. After drying the resulting mixture at 11 C for 110 hours, the agent The catalyst is heated to a YO at a rate equal to oY/min and calcined at this temperature for hours to produce the required oxide composition.This diet appears to be close to the ideal value providing a catalyst with the required structure and properties.Objective The other of the present invention relates to methods using an improved catalyst.vo Catalyst-optimized systems can be used in a variety of fluid-state catalytic chemical reactions to convert at least one fluid-state reactant to at least one fluid-state product. The reaction oxidizes lower alkanes primary to the corresponding acids. a according to another embodiment; The fluid phase reactants include alpha-beta unsaturated aliphatic aldehydes and oxygen-containing gas 5 (Se) air; oxygen “etc..) and the fluid-state products include af - alpha-beta unsaturated carboxylic acids. According to »the catalyst according to the present invention is not limited to the hydrogenation separation of Yo - J ethane oxidation of acetic acid and can be applied for the oxidation of alpha - alpha-beta Gn aliphatic aldehydes unsaturated aldehydes in the vapor phase with molar oxygen to yield alpha-beta carboxylic acids

0 composed of an alkene of an alkene 1 or an unsaturated corresponding alkane and carboxylic acids. to the corresponding acids, carbon atoms, and the products, ethane, according to a proposed embodiment; The fluid-state reactants include ethane, acetic acid, and the fluid-state include acetic acid, which contains gas. The raw material used as a source of ethane can be represented by a gaseous stream, ° . ethylene and ethylene ethane by volume at least of ethane or a mixture of ethane fo on alkane can contain very small amounts of alkane gas also the gaseous stream by volume of Jo is less than ¢ carbon tom and alkenes 5 consisting of 4-7 carbon atoms each. Also, the gaseous stream can contain predominant quantities; more than 15 of; and water in the form of carbon dioxide ¢ nitrogen by volume; of nitrogen 0 : steam. Generally, the reaction mixture used to carry out the process is represented by one mole of ishan; one mole of molar oxygen either in the form of pure oxygen or in the form of air; (You) and zero pounds 7 moles of water in A flowing stream image. The water vapor or the effluent stream is used as a reaction diluent and a reaction heat modifier and also acts as an accelerator to separate the agglomeration of the reaction product in the vapor state. Other gases may be used as oxidation reaction diluents, carbon dioxide, nitrogen, or heat modifiers, for example helium; nitrogen. carbon dioxide. The gaseous components of the reaction mixture may include ethane; Oxygen and diluted; And those components are preferably mixed homogeneously before being introduced into the reaction range 0 separately a; after you mix; Before being introduced into the range 0, the components may be preheated. The reaction must have a temperature of approximately 10-402 °C. The concentration of oxygen in the gaseous-feed mixture may vary widely; or higher than the feed mixture by applying the correct measures to avoid 2960-11 from the explosion problems. Air is a preferred source of oxygen for nutrition. the amount of oxygen Ye or less; Who. The stoichiometric present in can represent a stoichiometric quantity. Hydrocarbons in food

1 _ bar; And preferably from 9071, the reaction contains a pressure of Bl in general, so it is - 001 bar; a temperature of approximately 196 days; with a preference of YT) sec; 001-101 is approximately catalyst and the contact time between the reaction mixture and the catalyst ranges from 6 hourly velocity sec; and the instantaneous spatial velocity (Nem) with a preference of 1 hour; and preferably 0000001 . which is approximately 8,000,088 hours 1; In preference to © 7 h 00-701 is greater than the contact time is determined as the ratio between the apparent volume of the catalyst layer

Jeli and the volume of the gaseous reaction mixture fed into the catalyst bed through specified conditions in a unit time. The spatial velocity is estimated by determining the total gas equivalent of the reactor outlet in liters Ve (catalyst Jalal) of the total flow involved over a period of one hour Divided by liters of i ge this volume at room temperature converts to the volume at zero temperature 0 in the reactor . 1 bar at a pressure equal to and diluted gas The reaction pressure can be supplied initially by feeding the gaseous reactant and ; after the start of the reaction; It is maintained by the use of 31 appropriate vo backpressure settings. placed above the reactor outlet stream and preferably the reaction temperature is provided by placing the catalyst layer within a walled tubular converter which is placed in an oven heated to the required reaction temperature. A The improved catalysts according to the present invention provide Unexpectedly high yield values of acetic acid using a single-stage conversion from ethane to acetic acid. This can be achieved by using a single lin structure according to the present invention in a single reaction domain. Preferably the yield (7) for acetic acid is greater than 719; With greater preference, it is greater than 1,770, with greater preference, it is greater than 255, and with greater preference, it is greater than 771. 7h

YY

to an amazing ethane acid; The single-stage conversion of sm ethane provides reduced rates of by-products, for example, acetic acid monoxide and ethylene 08. In favor of ¢, the selectivity (7) for carbon monoxide is CO for carbon; and with greater preference less than 1 ; and with a greater preference of 1,5 and with a greater preference of less than 0 IY less than and with a preference of ; the yield (7) for eilin is 1 0 ; and greater preference is close to zero foo is less than © 1 ; And with a greater preference less than / 1.9 and with a greater preference less than » IX they are less than ethylene

J with greater preference less than 20559 ; The greater preference is close to zero, in general, the process is carried out in one stage, where all oxygen and reactants are supplied as a single feed, with the recycling of the unreacted primary reactants. any way ; The medium of hydrocarbon BE enables the multi-stage to add oxygen to the reactor with 0 and avoids 6 acid Aa This can improve the yield of 0 acid also to use the actually harmful conditions. And the following examples are considered Illustrated for some of the products and methods for their preparation are located within . Of course, it will not be considered specific in any way to the present invention. 0 The intent of the present invention. Embodiments of the present invention 1 are done to show the examples specified in Table No. p.: catalyst ss) The catalyst evaluations are carried out in a tubular reactor with a fixed bed of acetylase composition. BTRS jr Standard processing conditions using a sterile reactor ye stainless steel is of volume of air at degree AS ethane of volume ethane To for gaseous feed be and instantaneous spatial velocity near psig 001 equal to 7360 m; And at a pressure equal to Jews)» YC calcined catalyst hour 'using? A gram of calcined catalyst is 1101 min

The reaction products are analyzed directly by gas chromatography. oxygen is analyzed; Nitrogen and carbon monoxide (CO) using a column of 9 m V x mm consisting of 11 molar vibrations 0 carbon dioxide is analyzed. Ethane and ethylene using a column of 9 m Y x mm filled with sole sold ° via the trade name PORAPACK N 0 Acetic acid and water are analyzed using a column of 0.9 m 36 mm © Lime Via material sold under the brand name HAYASEP Q © HAYASEP . For each Nl, the values of transformation and selectivity depend on the stoichiometry of the reaction. Jia No. 1 Ve Km Na Moi 2 Pd 5 R Mo Ammonium metavanadate is added (Aldrich Chemicals; Test -H +) in an amount equal to 1 gram to 5 ml of distilled water and heated to TA 0 °C with stirring. 1 gram of oxalic acid is added to the previous solution. The color of the solution changes from yellowish green to dark green. Dark brown as the pH is between ?-e” 0 in pA (Solution A). 1 ammonium paramolybdate tetrahydrated 5 el (Aldrich Chemicals ACS Aldrich Chemicals 74 °C?) in an amount equal to 1 gram is added to 17.7 ml of water and heated to 5 °C to obtain a colorless solution with a pH of 11 °C equal to 58 (Solution B) 0 Solution B is slowly mixed with 0 Solution A In order to obtain a dark blue-green solution with a pH of 5.77 at 14C DH 0 Y.0 15 - 2 grams of palladium is slowly added to the mixture Gelatinization followed by the required amount of 0 lanthanium nitrate This dark color consistency is stirred vigorously to achieve a homogeneous gelatinization mixture which is then slowly dried to initial moisture during 170-768 min at 18-56°C with continuous YO stirring . The resulting solid material is placed in a tray and further dried in the oven at a temperature equal to 1070 C for 11 hours. The dried material is cooled to room temperature and placed

Ve m 1 min Y at a rate of 5 Yo. The temperature is raised from 5 degrees Celsius in the room to Oo for a period of time; Hours. To and later keep in the catalyst in order to check the reproducibility of catalysts A Example No. is prepared

X Example, Qom

Mo | V Yuen Pd 2.88504 1-8 108-05 ° A gram of ammonium metavanade TA except for the use of Method 1 Italics Example No. . (%) Test - Aldrich Chemicals ammonium metavanadate??

Y, for example, Qom

Mo | V 0.628 Pd 2885-04 L210E05 oxalic acid except for the use of; A gram of oxalic acid 1 Example No. Blo the Ve £ ad , Example Mo 1 V Yon Pd 2.3804 L31.0E05 oxalic acid A gram of oxalic acid VY Except for the use of Method 1 Italics of Example No. 0 at (Example Mo 1 V 773 Pd 288-04 L21.0E-05 Ve except for the use of no gram of methavanadate | ammonium 1 Method Italics of Example No. 7448 = test + Aldrich Chemicals ammonium metavanadate 1 Example No

Mo | V Penn Pd 2676-04 L21.0E-05 g of quaternary ammonium paramolybdate 058 except using Example 1 Example No. ila Method 0 ACS Chemicals Jin ja) ammonium paramolybdate tetrahydrated hydrate ‎ ‎ -89-?).‎ \Y,0¢— Aldrich Chemicals A.C.S

Vv ad , Example Mo A R 5 Pd and 458-04 L21.0E-05 palladium except using 308-03 grams of palladium 1 The method is the same as Example No. 70 yo

A Example No

Mo | V 0.628 Pd 2.888-04 1065 In order to check the reproducibility of the catalyst. 1 Method Example No. Yo to Ye The surface area 1 of the catalysts described in the examples varies from . square/gm. Described by Specified in Table ? AES Catalyst Evaluation Data for

Y table number catalyst evaluation data (7 01 7/mm1) 0; pressure © 051; ethane/air I (UE conditions) tee | acid | CO | 60 | example number | ethane | oxygen leaching acetic acid er | [a [a rar |v eT [ran ee nee uh Te oo [re [oar] ert Tre |e [ ea ae

Tre. [er fee [on] eT Tree . Salt Aga catalysts according to the present invention have demonstrated an ideal reductive-oxidative behavior that results in an effective

Ci al Based on the data 0 high molecular oxidation and high selectivity towards oxidation products 0 of the invention a catalyst, the following general characteristics can be deduced for the present catalysts. Reflecting a high rate of oxidation - Separation of ethane High transformation of ethane -1 alkane Alkane dehydrogenation Hydrogenation

Vi to acetic acid ethylene from the oxidation of ethylene Sle modifier - Y .acetic acid The previous description of the present invention is intended for clarification and not for limitation. Various changes and modifications in the embodiments described can be made by experts in the field. And she can. To be carried out without deviating from the essence or intent of the present invention 05

Claims (1)

No protective elements 1-1 catalytic agent for oxidation (aga) oxidation of ethane to acetic acid containing a catalyst composition comprising the following elements 7 (molybdenum) Mo “(Vanadium) 1 (Paladium) Pd “(Lanthanium) La” in the form of oxides ; - 01088; in the following ratios: +- Mo, Vy, Pd, Lag Oy ° 6 a, where 7 8 equals 1 - ©¢ A equals a= ae) 9 © equals RENO — 0,.6 a equals a_n, and 1 where x is a specific number by sal requirements for other elements in configuration 1” catalyst 1 ?- catalyst according to claim number 1; where J ranges from 4998-05 v to 5.0E-03 1 *- catalyst 1 according to claim No. 6 Cus that catalyst 1 for said catalyst 7 is a support-stabilized catalyst. catalyst according to Claim No. 3, as the aforementioned support is chosen from the Y group consisting of alumina ¢ silica titania ¢ zirconia ¢ silicon carbide ¢ molybdenum carbide carbide « zeolites; - zeolites and molar quakes; and other fine porous materials on the micro/nano scale and ° mixtures derived therefrom. Jalal - #1 catalyst according to claim No. 7; Whereas, the catalyst – the aforementioned prop includes fone by weight catalyst installation and 796-80 by weight Adley ov VA; Including the steps 1 according to claim No. catalyst process to form the catalyst 1-1 —: the following lanthanum and palladium 0 vanadium » molybdenum a) formation of a molybdenum-containing mixture x solution; palladium ¢ b drying said mixture to form a dry solid; and 8 said catalyst said dried solid to form the catalyst calcined c = process under claim 6; Whereas, the aforementioned mixture represents a water system included = v 1 .01-1 "at a pH of 11 °C, including protection No. 76, as the aforementioned mixture represents a system paid lay process =A N=) of the pH pH degree eX process according to Claim No. 6, as the aforementioned mixture is formed by merging 4-1 of a first solution with a second solution, as the first solution and the second adapter each contain element ¥ at least one molybdenum vanadium selected from the group consisting of molybdenum oY .palladium and palladium lanthanum lanthanum “ vanadium ¢ since calcining 0 mentioned includes heating (NHR) of the protective element practical 0 -1 of approximately 496-790 in said solid calcined to a calcining temperature of -" 16-1 hr. air or oxygen 2 for a time period ranging from approximately to ethane acid for ethane 1 for Selective oxidation 0 of catalyst catalyst 7) 1 - + takes place by a process comprising the following steps acetic acid palladium and palladium vanadium ; Vanadium molybdenum An amalgamation of the elements of molybdenum { 1 in the following proportions B ¢ Mo, Nu Pd. Lag Ox ° where 1 ¢ © — \ equals a 7 0 74 _ oy) equals b A ya 6 +, — equals len © 9 to form a mixture; And Ym ree) Nawi 80. b) Every year 40 the aforementioned mixture to form the catalyst Wn catalyst where the catalyst “VY of claim No. a catalyst catalyst -10-1 stabilizer including support. catalyst is a catalyst Sadly Acetic aes J) ethane selectivity oxidation for oxidation catalyst catalyst - 1 Yoo « molybdenum containing a catalyst composition composed mainly of acetic molybdenum with ¥ in the form of lanthanum oxides ¢ palladium « vanadium vanadium 1 - + ; For the following oxides - Mo, Vb Pd. Lay Oy ° where oy ¢ 0 —) equals 8 7 equals m - yria © A ' © equals l © q ER oY B RENNES equals 11 0 is a specific number of By the valence requirements of the other elements in formation x where 11 is the catalyst. ER: 01" 4998-05 ranging from J where 07 depending on claim number catalyst -1 ¢ .5.008-03 to A 7