SELF-PROMOTED HYDROTREATING CATALYSTS

Abstract: Self-promoted molybdenum and tungsten sulphide hy­ drotreating catalysts are prepared by heating one or more water soluble catalyst precursors in a non-oxidizing atmo­ sphere in the presence of sulphur at a temperature of at least about 200°C. The precursors will be one or more com­ pounds of the formula (ML)(Mo y W 1-y O₄) wherein M is one or more promoter metals selected from Mn, Fe, Co, Ni, Cu, Zn and mixtures thereof, wherein O ≦ y ≦ 1 and wherein L is a nitrogen containing, neutral multidentate, chelating ligand. Ina preferred embodiment the ligand L will comprise one or more chelating alkyl di or triamines and the non-oxidizing atmosphere will comprise H₂S.

Description: This invention relates to self-promoted molybdenum and tungsten sulphide hydrotreating catalysts. More particularly, this invention relates to self-promoted molybdenum and tungsten sulphide hydrotreating catalysts produced by heating one or more water soluble molybdate and/or tungstate catalyst precursors containing the promoter metal as part of the precursor molecule in the presence of sulphur at elevated temperature for a time sufficient to form said self-promoted catalyst. The petroleum industry is increasingly turn ing to coal, tar sands, heavy crudes and resids as sources for future feedstocks. Feedstocks derived from these heavy materials contain more sulfur and nitrogen than feedstocks derived from more conventional crude oils. Such feedstocks are commonly referred to as being dirty feeds. These feeds therefore require a considerable amount of upgrading in order to obtain usable products therefrom, such upgrading or refining generally being accomplished by hydrotreating processes which are well-known in the industry. These processes require the treating with hydrogen of various hydrocarbon fractions, or whole heavy feeds, or feedstocks, in the presence of hydrotreating catalysts to effect conversion of at least a portion of the feeds, or feedstocks to lower molecular weight hydrocarbons, or to effect the removal of unwanted components, or compounds, or their conversion to innocuous or less undesirable compounds. Hydrotreating may be applied to a variety of feedstocks, e.g., solvents, light, middle, or heavy distillate feeds and residual feeds, or fuels. In hydrotreating relatively light feeds, the feeds are treated with hydrogen, often to improve such compounds in the presence of hydrogen, which processes are collectively known as hydrotreating or hydrorefining processes, it being understood that hydrorefining also includes some hydrogenation of aromatic and unsaturated aliphatic hydrocarbons. Thus, U.S. Patent No. 2,914,462 discloses the use of molybdenum sulfide for hydrodesulfurizing gas oil and U.S. 3,148,135 discloses the use of molybdenum sulfide for hydrorefining sulfur and nitrogen-containing hydrocarbon oils. U.S. 2,715,603, discloses the use of molybdenum sulfide as a catalyst for the hydrogenation of heavy oils, while U.S. 3,074,783 discloses the use of molybdenum sulfides for producing sulfur-free hydrogen and carbon dioxide, wherein the molybdenum sulfide converts carbonyl sulfide to hydrogen sulfide. Molybdenum and tungsten sulfides have other uses as catalysts, including hydrogenation, methanation, water gas shift, etc. reactions. In general, with molybdenum and other transition metal sulfide catalysts as well as with other types of catalysts, higher catalyst surface areas generally result in more active catalysts than similar catalysts with lower surface areas. Thus, those skilled in the art are constantly trying to achieve catalysts that have higher surface areas. More recently, it has been disclosed in U.S. Patent Nos. 4,243,553, and 4,243,554 that molybdenum sulfide catalysts of relatively high surface area may be ob tained by thermally decomposing selected thiomolybdate salts at temperatures ranging from 300-8000C in the presence of essentially inert, oxygen-free atmospheres. Suitable atmospheres are disclosed as consisting of argon, a vacuum, nitrogen and hydrogen. In U.S. 4,243,554 an ammonium thiomolybdate salt is decomposed at a rate in excess of 150C per minute, whereas in U.S. 4,243,553, a substituted ammonium thiomolybdate salt is thermally decomposed at a very slow heating rate of from about 0.5 to 2 C/min. The processes disclosed in these patents are claimed to produce molybdenum disulfide catalysts having superior properties for water gas shift and methanation reactions and for catalyzed hydrogenation or hydrotreating reactions. In accordance with this invention self-promoted molybdenum and tungsten sulphide hydroprocessing catalysts are obtained by heating one or more water soluble catalyst precursors of the formula (ML)(MOyWIyO4) in a non-oxidizing atmosphere in the presence of sulphur at an elevated temperature, preferably at a temperature of at least about 1500C, especially at least about 2000C for a time sufficient to form said catalyst, wherein M comprises one or more divalent promoter metals preferably selected from Mn, Fe, Co, Ni, Cu, Zn and mixtures thereof, wherein y is any value ranging from 0 to 1, and wherein L is one or more, neutral, nitrogen-containing ligand at least one of which is a chelating polydentate ligand. In a particularly preferred embodiment ligand L will have a denticity of six and will be either three bidentate or two tridentate chelating, alkyl amine ligands, M will be selected from Ni, Fe, Co and mixtures thereof and the non-oxidizing atmosphere will contain hydrogen sulphide as the source of sulphur. Hydroprocessing is meant to include any process that is carried out in the presence of hydrogen, including, but not limited to, hydrocracking, hydrodenitrogenation, hydrodesulfurization, hydrogenation of aromatic and aliphatic unsaturated hydrocarbons, methanation, water gas shift, etc. These reactions include hydrotreating and hydrorefining reactions, the difference generally being thought of as more of a difference in degree than in kind, with hydrotreating conditions being more severe than hydrorefining conditions. Some of the catalysts of this invention have hydrotreating or hydrorefining activities substantially greater than that of conventional hydrotreating catalysts such as cobalt molybdate on alumina. The catalysts of this invention may be used in bulk form or supported on a suitable inorganic refractory oxide support such as alumina. A particularly significant advantage of this invention is that the water solubility of the catalyst precursor permits the precursor to be impregnated onto a suitable support such as alumina, via conventional impregnation techniques such as incipient wetness and adsorption. As hereinbefore stated, the catalyst precursor is a water soluble metal late having the formula ML(MoyWl-yO4) wherein M is one or more divalent promoter metals preferably selected from Mn, Fe, Co, Ni, Cu, Zn and mixtures thereof. Preferably M will be selected from (a) Ni, Co, Fe and mixtures thereof and (b) mixtures of (a) with Zn, Cu, Mn EMI5.1 mixtures thereof. Still more preferably M will be selected from Fe, Ni, Co and mixtures thereof. Thus, the promoter metal may be a single metal such as Ni in which case the precursor will have the formula (NiL)(MoyWl-yO4). Alternatively the promoter metal may be a mixture of two, three, four, five or even six promoter metals. For the case of two promoter metals, such as Ni and Co, the precursor will have the formula f(NiaCOla)L] (MOyWlyO4) wherein O < a < l. In the case of three promoter metals such as Ni, Co and Zn, the precursor will have the formula of the form [(NiaCobZnc)Li (MOyWlyO4) wherein O < a, b EMI5.2 c < l and a + b + c = 1. Where there are four metals such as Fe, Ni, Co and Zn, the precursor will have the formula [(FeaNibCocZnd)L](MoyWl-yO4) wherein 0 < a, b, c EMI5.3 d < 1 and a + b + c + d = 1, and so on. The precursor may be a self promoted molybdate, tungstate or combination thereof. If it is only a molybdate it is obvious that y will have a value of 1. Alternatively, if the precursor is a tungstate y will be zero. The ligand L, will generally have a denticity of six and will be one or more neutral, nitrogen containing ligands wherein at least one of said ligands is a multidentate chelating ligand which chelates the promoter metal cation to form a chelated promoter metal cation [ML]2+. Thus, the catalytic metal oxide anion (MoyWl-yo4)2- will be ionically bound to the chelated promoter metal cation [ML]2+. By neutral is meant that the ligand itself does not have a charge. Those skilled in the art know that the term "ligand" is used to designate functional coordinating groups which have one or more pairs of electrons available for the formation of coordinate bonds. Ligands that can form more than one bond with a metal ion are called polydentate while ligands that can form only one bond with a metal ion are called monodentate. Monodentate ligands are not capable of forming chelates. Hence, if one uses one or more species of monodentate ligands in the precursor molecule, then one must also use at least one polydentate chelating ligand. Preferably L will be one or more polydentate chelating Ligands. The denticity of the ligand L will generally be six, because the promoter metal cations prefer six-fold coordination. Hence, if more than one species of ligand is employed in the precursor molecule, the denticity of the ligand species will usually add up to six. It should be understood that it is possible for ligand L to have a total denticity of less than six, but in most cases L will have a total denticity of six. Thus, L will be three bidentate ligands, two tridentate ligands, a mixture of a bidentate and a quadridentate ligand, a hexadentate ligand or a mixture of a polydentate ligand with monodentate ligands as long as the combination has a total denticity of six. As has heretofor been stated, it is preferred to use chelating bidentate and tridentate ligands. In general, the ligands useful in this invention include alkyl and aryl amines and nitrogen heterocycles. Illustrative but non-limiting examples of ligands useful in the catalyst precursors of this invention are set forth below. Monodentate ligands will include NH3 as well as alkyl and aryl amines such as ethyl amine, dimethyl amine, pyridine, etc. Useful chelating bi dentate amine ligands are illustrated by ethylenediamine, 2,2'-bipyridine, l,10-phenylene bis(dimethyl-amine), o-phenylene diamine, tetramethylethylenediamine and propane-1,3 diamine. Similarly, useful chelating tridentate amine ligands are represented by terpyridine and diethylenetriamine while triethylenetetramine is illustrative of a useful cheating quadradentate amine ligand. Useful chelating pentadentate ligands include tetraethylenepentamine while sepulchrate (an octazacryptate) is illustrative of a suitable chelating hexadentate ligand. However, as a practical matter it will be preferred to use chelating, polydentate alkyl amines for L. Illustrative, but not limiting examples of alkyl amines that are useful in the catalyst precursor of this invention include ethylenediamine, diethylenetriamine, and tetraethylenetetramine. It is particularly preferred to use bidentate and tridentate alkyl amines such as ethylenediamine and diethylenetriamine. In general, the precursor salts useful for forming the catalysts of this invention may be prepared by mixing an aqueous solution of ammonium molybdate and/or tungstate with an aqueous solution of the chelated promoter metal cation iML)2+ which, in the presence of excess metallate, ligand and/or chelated promoter metal cation, will result in the formation of the precursor salt as a precipitate which is readily recovered. The chelating promoter cation is easily formed by, for example, mixing an aqueous solution of one or more water soluble promoter metal salts with the ligand. The water soluble salt may be any water soluble salt that is that is convenient to use such as a halide > sulfate, perchlorate, acetate, nitrate, etc. Alternatively, an aqueous solution of ammonium molybdate and/or tungstate may be mixed with the ligand with the resulting solution mixed with the an aqueous solution of promoter metal salt or the salt can be added to the ligand and dissolved into the solution of molybdate and/or tungstate. The catalyst precursor preparation will be further understood by reference to the Examples, infra. The catalysts of this invention may be used in bulk or supported on a suitable support, preferably supported on a suitable inorganic refractory oxide support such as alumina. As previously stated, an advantage of the catalyst precursors useful in this invention resides in their water solubility which permits them to be supported on suitable support materials by techniques well-known inn the art, such as impregnation, incipient wetness and the like, the choice being left to the convenience of the practitioner. When using the impregnation technique, the aqueous impregnation solution will be contacted with the support for a time sufficient to deposit the precursor material onto the support either by selective adsorption or alternatively, the excess water may be evaporated during drying, leaving behind the precursor salt. Advantageously, the incipient wetness techniques may be used whereby just enough of an aqueous precursor salt solution is added to dampen and fill the pores of the support. The catalysts of this invention may be prepared by heating one or more catalyst precursor salts, bulk or supported, in the presence of sulfur in a non-oxidizing atmosphere, at a temperature of at least about 2000C for a time sufficient to form the catalyst. Preferably the sulfur required during the formation of the catalyst will be present in the form of a sulfur bearing compound and in an amount in excess of that required to form the catalyst. Thus, it is preferred that the catalyst be formed by heating the precursor in the presence of sulfur or, preferably in the presence of a sulfur bearing compound which can be one or more solids, liquid, gases or mixtures thereof. Mixtures of hydrogen and H2S have been found to be particularly preferred. Preferably the temperature will range between from about 250-6000C, more preferably from about 250-5000C and still more preferably from about 300-4000C. The non-oxidizing atmosphere may be inert or net reducing. As discussed previously molybdenum and tungsten sulfide catalysts have many uses, including hydrotreating. Hydrotreating conditions vary considerably depending on the nature of the hydrocarbon being hydrotreated, the nature of the impurities or contaminants to be reacted or removed, and, inter alia, the extent of conversion desired, if any. In general however, the following are typical conditions for hydrotreating a naphtha boiling within a range of from about 250C to about 2100C, a diesel fuel boiling within a range of from about 1700C to 3500C, a heavy gas oil boiling within a range of from about 3250C to about 4750C, a lube oil boiling within a range of from about 290-5000C, or residuum containing from about 10 percent to about 50 percent of material boiling above about 5750C. Space Hydrogen Pressure Velocity Gas Rate Feed Temp., C psig V/V/Hr SCF/B Naphtha Typical 100-370 150-800 0.5-10 100-2000 Diesel Typical 200-400 250-1500 0.5-6 500-6000 Heavy Typical 260-430 250-2500 0.3-4 1000-6000 Lubricating Typical 200-450 100-3000 0.2-5 100-10,000 oil Residuum Typical 340-450 1000-5000 0.1-2 2000-10,000 The invention will be further understood by reference to the following examples. EXAMPLES Catalyst Precursor Preparation A tris(ethylenediamine) nickel molybdate Ni (en) 3Mo04 catalyst precursor was prepared by dissolving ammonium molybdate into ethylenediamine (en) and the resulting solution cooled to OOC in an ice bath. An aqueous solution of nickel chloride was slowly added, in aliquots, to the above solution, with agitation after the addition of each aliquot. A precipitate was formed and recovered by vacuum filtration. This precipitate was Ni (en) 3MoO4 and was washed with distilled water and acetone and then dried in a vacuum oven at 500C for three hours. The resulting cake was screened, pelletized, sized to 20/40 mesh (Tyler). More specifically, 20.5 gm of (NH4)6Mo7024.4H2O (ammonium heptamolybdate) was added to 500 ml of ethylene-diamine (en) in a 250 ml-Erlenmeyer flask. This amount of en was in excess of that stoichiometrically required to form the precursor and the excess aided in precipitating same from solution. From 40 to 50cc of distilled H20 was used twice to wash off any solid or solution remaining on the sides of the flask. The resulting solution was cooled to OOC in an ice bath and kept in the bath for the duration of the preparation. In a separate flask 27 gm of NiC12 6H2O were dissolved into 300 ml of distilled H2O. This Ni2+ solution was added slowly, in aliquots, to the (NH4)2MoO4/en aqueous solution with agitation after each addition. A precipitate formed immediately. This precipitate was separated out by vacuum filtration through a Buchner funnel. The product, Ni(en)3MoO4, was washed with distilled H20, then with ethanol, and dried under vacuum for 16-24 hrs. 46.0 gm of Ni (en) 3MoO4 were recovered. This same procedure was used for the preparation of Co (en) 3MoO4, except that an appropriate amount of CoC12.6H2O was used instead of NiC12.6H2O. To form a supported catalyst, 43 grams of Co (en) 3MoO4 were dissolved into 140 cc of distilled water. Sixty grams of a reforming grade of -A1203 (Englehard Industries), which had been calcined overnight at 5000C, were impregnated with this solution via the incipient wetness technique using four successive aliquots. After each aliquot was added to the alumina support, the impregnate was dried under vacuum at about 1000C for six hours. The final impregnate was ground and pelletized using a 4% aqueous solution of polyvinyl alcohol as a binder. The bulk Ni (en) 3MoO4 was also pelletized using the same technique. Finally, another sample of Coen)3MoO4 was prepared and pelletized as above in bulk. The pelletized catalyst precursors were placed into a stainless steel reactor at 1000C at atmospheric pressure where they were purged for one hour under nitrogen. Ten percent of hydrogen sulfide in hydrogen was introduced into the reactor at a space velocity of 0.75 SCF/hr for each 10 cc of catalyst in the reactor. The temperature in the reactor was then raised to 325-360oC and kept at this temperature for one to three hours to form the catalyst after which the temperature in the reactor was lowered to 1003C, the H2S/H2 gas flow was stopped and the reactor was purged with nitrogen until room temperature was reached. Reaction Conditions At least about 20 cc of each catalyst was loaded into a stainless steel, fixed-bed reactor. The conditions in the reactor were as set forth below: Temperature 325 C Pressure 3.15 MPa Hydrogen rate 3000 SCF/bbl LHSV 2,3 and 4 V/V/Hr. The liquid product was analyzed for sulfur by X-ray fluorescence and for nitrogen by combustion analysis. The feedstock used was a light catalytic cycle oil (LCCO) that was about 20 wt.% paraffinic having properties set forth in Table 1. In all of these experiments, the results obtained from the catalysts of this invention were compared to results obtained for commercial HDS and HDN catalysts comprising cobalt molybdate on g-A1203 and nickel molybdate on g-A1203, respectively. The cobalt molybdate comprised 12.5 percent molybdenum oxide and 3.5 percent cobalt oxide supported on the gamma alumina and the nickel molybdate comprised 18 percent molybdenum oxide and 3.5 percent nickel oxide on gamma alumina. These commercial catalysts were sulfided employing the same procedure used to form the catalysts of this invention, except that the temperature was 360 C for one hour. Example 1 In this experiment, the LCCO feed was hydrotreated at an LHSV of 2 comparing two of the catalysts of this invention to the commercial cobalt molybdate on alumina HDS catalyst. The results are set forth in Table 2. Example 2 This experiment was the same as in Example 1 except that the LHSV was 3. The results are shown in Table 3. Example 3 In this experiment, the unsupported catalyst of this invention prepared from the Co(en)3MoO4 was compared to the commercial HDN catalyst, the results of which are shown in Table 4. These results show the remarkable HDN selectivity for the catalyst of this invention. The liquid hourly space velocity (LHSV) used in this invention was 4. Example 4 In this experiment, the LCCO feed was hydrotreated at LHSV ranging from 1 to 6 with a catalyst prepared by impregnating a chromia on alumina support material with a Ni (en) 3MoO4 salt. The Ni (en) 3MoO4 salt was prepared by dissolving 40.6 g of ammonium paramolybdate in a mixture of 900 ml ethylenediamine (en) and 100 ml water in a 2 liter round bottom, three-neck flask. Next, 56 g of nickel chloride was dissolved in 100 ml H20 and transerred to a dropping funnel. While vigorously stirring the molybdate solution with an air driver stirrer, the nickel chloride solution was added to the flask via the dropping funnel. A violet powder precipitated. This precipitate was filtered, washed with acetone and then vacuum dried at 500C. 94.6 gms of product was obtained (calculated yield = 94 g). 50 g of 19% Cur203 on A1203 in the form of 1/8" pellets (Alfa Products Div. Morton Thiokol, Inc.) were calcined at 5000C for 3 hrs and, after cooling, crushed to a -20 + 40 mesh powder. This powder was then placed into a 500 ml ROTOVAC flask. 45.8 g of the Ni(en)3MoO4 were dissolved in 120 ml of water and added to the flask. The flask was evacuated and rotated in a 700C water bath until the water was completely removed. The final impregnated solid weighed 104.6 gms. This impregnate was then ground, pelletized and sulfided at 360 C for one hour following the procedure for Examples 1-3. This catalyst gave a % HDS of 70.5 and % HDN of 56.6 when tested with the LCCO feed at 3250C, 3.15 MPa and 3,000 SCF of hydrogen per bbl of oil at an LHLSV of 3.0. Example 5 25 grams of MgO in 20-40 mesh size were impregnated with 87.2 cc of solution containing 30.7 grams of Ni (en) 3MoO4. The resulting impregnate was vacuum dried at 50 C overnight. The final impregnated solids weighed 61.6 grams. The final catalyst was sulfided at 4000C for one hour with a 10% H2S in hydrogen mixture, following the procedure for Examples 1-3. This catalyst gave a % HDS of 58.1 and % HDN of 31.3 when tested with the LCCO feed at 3250C, 3.15 MPa and 3,000 SCF of hydrogen per bbl of oil at an LHSV of 3.0. Table 1 LCCO Feed Gravity ( API) 18.6 Sulfur, wt. % 1.5 Nitrogen ppm 370 GC distillation Wt. % Temp., C 5 231 10 251 50 293 70 321 90 352 95 364 Table 2 Catalyst % HDN % HDS cobalt molybdate on g-A1203 25.5 87.4 Catalyst Precursor Ni(en)3MoO4 83.0 86.8 Co(en)3MoO4 supported on &gamma;-Al2O3 40.3 90.9 Table 3 Catalyst % HDN % HDS cobalt molybdate on -A1203 19.0 83.6 Catalyst Precursor Ni(en)3MoO4 69.6 80.2 Co(en)3MoO4 supported on 7-A1203 25.5 85.1 Table 4 Catalyst % HDN % HDS cobalt molybdate on &gamma;-Al2O3 12.8 81 Catalyst Precursor Co(en)3MoO4 82.4 87.6

Claims: CLAIMS: 1. A self-promoted molbdenum and tungsten sulphide catalyst formed by heating one or more catalyst precursors of the formula (ML)(MOyW1y04) in a non-oxidizing atmosphere in the presence of sulphur at an elevated temperature for a time sufficient to form said catalyst, wherein M comprises one or more divalent promoter metals, wherein y is any value ranging from 0 to 1, and wherein L is one or more, neutral, nitrogen-containing ligands at least one of which is a chelating polydentate ligand. 2. A catalyst according to claim 1 wherein M comprises one or more divalent promoter metals selected from Fe, Co, Ni, Zn, Cu, Mn and mixtures thereof. 3. A catalyst according to claim 2 wherein said promoter metal M comprises one or more divalent metals selected from (a) Fe, Co, Ni and mixtures thereof and (b) mixtures of (a) with Zn, Cu, Mn or mixtures thereof. 4. A catalyst according to claim 3 wherein M is selected from Ni, Fe, Co and mixtures thereof. 5. A catalyst according to any one of the preceding claims wherein said sulphur is in the form of one or more sulphur-bearing compounds. 6. A catalyst according to any one of the preceding claims wherein said ligand L, is selected from alkyl amines, aryl amines, nitrogen heterocycles and mixtures thereof, preferably an alkyl amine. 7. A catalyst according to any one of the preceding claims wherein said ligand L has a total denticity of six. 8. A catalyst according to any one of the preceding claims wherein ligand is selected essentially from two trident ate ligands and three bidentate ligands. 9. A catalyst according to any one of the preceding claims wherein excess sulphur is present as H2S. 10. A catalyst according to any one of the preceding claims wherein said non-oxidizing atmosphere comprises a mixture of H2 and H2S. 11. A catalyst according to any one of the preceding claims wherein said elevated temperature is at least about 200"C. 12. A catalyst according to any one of the preceding claims which is supported on an inorganic refractory oxide support. 13. A supported, self-promoted molybdenum and tungsten sulphide catalyst according to any one of claims 2 to 12 formed by (a) compositing an inorganic refractory oxide support with one or more water soluble catalyst precursor salts characterized by the formula (ML)(MoyW1 y04) wherein M comprises one or more divalent promoter metals selected from Fe, Co, Ni, Zn, Cu, Mn, and mixtures thereof, wherein y is any value ranging from 0 to 1 and wherein L is one or more neutral, nitrogen-containing ligands at least one of which is a chelating polydentate ligand and (b) heating said composite in a non-oxidizing atmosphere in the presence of sulphur at an elevated temperature for a time sufficient to form said catalyst. 14. A process for preparing the supported, self-promoted catalysts according to claim 13, said process comprising: (i) compositing a porous, inorganic refractory oxide support with a water soluble catalyst precursor salt characterized by (ML)(MoyW1-yOq) wherein M comprises one or more divalent promoter metals selected from Mn, Fe, Co, Ni, Cu, Zn, and mixtures thereof, wherein y is any value ranging from 0 to 1, and wherein L is one or more neutral, nitrogen-containing ligands at least one of which is a chelating polydentate ligand; and (ii) heating said composite formed in (i) in a non-oxidizing atmosphere in the presence of excess sulphur in the form of one or more sulphur bearing compounds and at an elevated temperature, preferably at a temperature of at least about 200"C, to form said self-promoted catalyst. 15. A process according to claim 14 wherein said support comprises alumina. 16. A process according to claim 14 wherein said support comprises chromium oxide. 17. A process according to claim 16 wherein said chromium oxide support is supported on a refractory, inorganic oxide support material.

Inventors: HO, TEH CHUNG, MCCANDLISH, LARRY EUGENE
Applicants: EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1985
Main classification: B01J27
IPC codes: B01J31, B01J23, C10G45, B01J27, B01J37