PREPARATION OF HIGH ACTIVITY SILICA-SUPPORTED HYDROTREATING CATALYSTS AND CATALYSTS THUS PREPARED

Abstract: Process for preparing silica-supported catalysts contain­ ing 10-25 %w molybdenum and from 1-5 %w nickel and/or cobalt as hydrogenation metals, wherein a dried silica support is impregnated with an aqueous solution or an aqueous mixture obtained by contacting a hydrogenation metal compound with a nitrogen-containing organic ligand such as ethylene-diamine tetraacetic acid, diethylene triamine or nitrilotriacetic acid, in the presence of water.

Description: PREPARAIION OF HIGH ACTIVITY SILICA-SUPPORTED HYDROTREATING CATALYSTS AND CATALYSTS THUS PREPARED The present invention relates to improvements in the preparation of silica supported hydrotreating catalyst via aqueous methods. Silica-supported hydrotreating catalysts, when prepared by conventional aqueous pore-filling impregnation with catalytically active metals, tend to have very poor activity compared to corresponding alumina-based catalysts. This is thought to be because the metal ecocides (MoO3, NiO, CoO) interact very weakly with the support, and thus are very poorly dispersed on the support. Potentially, silica-based hydrotreating catalysts should perform well in treating residual oil feedstocks. Silica-based catalysts should be less prone to coke formation than alumina-based catalysts because of the lower acidity of silica. Since coke deposition is a major catalyst deactivator in such applications, an active and stable silica-based catalyst could have an enormous impact on hydrotreating such feedstocks. Processes for hydrogenating olefins and aromatics in the presence of catalysts comprising molybdenum and nickel in a particular atomic ratio supported on silica are known from U.S. patent specifications 3,167,496 and 3,167,497. These catalysts are prepared by oonventional aqueous impregnation, preferably with the precursor of the molybdenum catalytic agent prior to impregnation with the precursor of the nickel catalytic agent. The molybdenum compound content ranges between 12 and 35 %w (as MOO3) based on total weight of the catalyst. The nickel compcund is preferably present in an amount to provide an atomic ratio of molybdenum to nickel between about 2-3. In U.S. patent specification 3,420,771 a process is disclosed for hydrorefining an asphaltenic hydrocarbonaceous charge stock containing either sulphurous or nitrogeneous compounds in contact with a catalyst prepared by impregnating hydrated silica which has not been calcined (containing 5-15 %w water) with fran 4-30 %w of aqueous molybdenum compounds prior to calcining. Preferably the catalyst also contains fiun about 1-6 96w nickel. Nickel nitrate hexahydrate and phosphomolybdic acid are suggested as the source of catalytically active metals. These prior art methods of preparing silica-supported catalysts all suffer fran the disadvantage of poor catalytic metals distribution on the support. It has now been found that silica-based hydrotreating catalysts which overooce this disadvantage by having an improved dispersion of metals on the support thereby greatly increing catalyst activity, can be prepared via an aqueous method when use is made of certain large nitrogen-containing organic compounds. The present invention thus relates to a process for preparing silica-supported catalysts containing 10-25 %w molybdenum and from 1-5 w nickel and/or cobalt as hydrogenation metals, which ccnprises impregnating a dried silica support with an aqueous solution or an aqueous mixture attained by contacting a hydrogenation metal compound with a nitrogen-containing organic ligand in the presence of water. Without wishing to be bound to any particular theory, it would appear that the catalysts acoording to the present invention are prepared by methods which are believed to have in cannon that they shut off the formation of threx-dimensional oxide lattices that sulphide to large crystallites. The approach presented herein involves the coordination of large, nitregen-containing organic ligais to an O fragment, thereby preventing them fran packing into the Nt03 lattice. Examples of suitable nitrgen-contaning organic ligands comprise ethylenediamine tetraacetic acid (EDTA), diethylene triamine (DT), nitrilotriacetic acid (NIA), derivatives thereof and related compounds. When EDTA is used as large nitrogen-containing organic ligand the process according to the present invention is suitably carried out by: (a) preparing a slurry of about equal quantities of MbO3 and EDEMA in water to provide fran 10 to 25 %w of Mo on said support; (b) adding fran at least said equal quantity up to about a double quantity of (NH4)2C03 to the slurry and mixing same; (c) adding about half as much hydrazine to the mixture as the quantity of (NH4)2OD3 added; (d) heating the mixture fran step (c) to a temperature sufficient to form (NH4)2[Mo2O4(EDTA)] in a treasonable time; (e) impregnating a dried silica support with the solution fran step (d) at elevated temperature; (f) drying the Mo-impregnated silica at elevated temperature; ; (g) impregnating a dried silica support with a desired quantity of aqueous nickel and/or coaalt salt solution either before or after step (e); and (h) drying the Ni and/or CD impregnated silica at elevated temperature. Methods for preparing molybdenum compounds used to prepare the improved catalysts according to the invention have been reported by R.C. Pecsock and D.T. Sawyer in J. Am. Chew. Soc., 79, 5496 (1956) and by D.T. Sawyer and J.M. McKinnie in J. Am. Chem. Soc., 82 4191 (1960). However, a much more tractable synthesis was devised for the method of the invention as follows: EMI3.1 The compound was prepared in situ in > 95% yield and impregnated directly on the carrier. In addition to MoO3, suitable compounds include the molybdates, e.g., MbO4=, MO2O7= and Mo7O24-6. An interesting feature of the preparative system described hereinabove is the observation of severe deactivation of the catalyst if heated above 200 C in either N2 or O2 before sulphiding. At 400 C irore than half of the activity has disappeared. The deactivation observed may well correspond to thermal (N2) or oxidative (02) ligand degradation followed by sintering of the resultant metal oxide fragments. The X-ray diffraction patterns of the sulphided form of the active and deactivated catalyst were consistent with this explanation, with crystalline MoS2 being present in the deactivated catalyst, but not in the active version. When Dr is used as large nitrogen-containing organic ligand the process according to the present invention is suitably carried out by: (a) preparing a slurry of an amount of MoO3 and diethylene triamine in water to provide from 10 to 25 %w Mb on said su; (b) heating and mixing the slurry in sufficient water to dissolve the (c) impregnating a dried silica support with the solution from step (b) at elevated temperature; (d) drying the Mo-impregnated silica at elevated temperature; (e) impregnating a dried silica support with a desired quantity of aqueous nickel and/or coaalt salt solution, either before or after step (c); and (f) drying the Ni4o or Co-Mo impregnated silica at elevated tire. A suitable method for preparing the molybdenum compound used in this particular embodiment of the process according to the invention has been reported by W.F. Marzluff, Inorg. Chem., 3, 395 (1964). The compound may be prepared in situ by the reaction shown below and impregnated directly on the carrier. EMI4.1 In addition to MoO3, suitable MbOX compounds include the molybdates, e.g., MoO4=, MoO7= and MoO24-6. X-ray diffraction patterns and Rarrwi spectra of a sulphided catalyst prepared in accordance with the invention were consistent with the dispersion/activity explanation presented hereinabove. When NTA is used as large, nitrogen-containing organic ligand the process according to the present invention is suitably carried out by: (a) dissolving an appropriate amount of nitrilotriacetic acid in ammonium hydroxide; (b) adding to the mixture fran step (a) an amount of MoOx to x provide from 10 to 25 bw Mo on said support; (c) heating the mixture in step (b) until the reaction is substantially complete; (d) cooling the mixture fran step (c) and adding an amount of nickel and/or cobalt salt to provide from 1-5 %w Ni and/or Co on said support; (e) impregnating a dried silica support with the aqueous mixture from step (d); (f) drying the Ni-Mo and/or Co-Mo impregnated silica at elevated temperature. A suitable method for preparing the molybdenum compound used in this particular embodiment of the process according to the invention is as follows: EMI5.1 Dispersion control was achieved by a general method whereby a capping ligand was used on MbO3 to control sterically the crystallinity of Mc03. Further limitations on Mo particle size was attempted by chelation of nickel on the edges of sate of the NTA.MoO3-3 units, thereby interrupting the MoOx lattice. The above compound was prepared in situ and impregnated directly on the carrier. In addition to MoO3, suitable MoOx compounds include the molybdates, e.g., MoO4=, Mo2O7= and Mo7O24-6. Suitable hydrotreating catalysts in accordance with the invention generally contain fran 10-25 %w molybdenum and from 1-5 %w nickel and/or cobalt on a dried silica support. Preferably, the catalysts will contain from 10-20% molybdenum and from 2-4 %w nickel and/or cobalt. Of the latter metals, nickel is the most preferred. The Ni and/or Co compounds included in the catalysts according to the invention may be incorporated either before or after the Mo compound is impregnated therein when use is made of EDTA or form as the organic nitrogen compound. Prior art methods for incorporating these metals are well knawn and are not critical to the performance of the catalysts of the invention. A suitable method for incorporating nickel is given in Example 1. The activity testing of the catalysts according to the present invention was done in microreactor systems. These units are of conventional, fixed-bed, downflow design. Each unit consists of a 127 itrn O.D. reactor with a preheat section, a phase separator and a large product tank. Unit pressure is controlled by a motor valve on the outlet gas line and inlet H2 rate is maintained by pressure drap across a length of capillary tubing. LAPP pumps are used for charging liquid feed. Emergency circuitry automatically shunts down the unit in the event of fire, high reactor temperature, high or low unit pressure or loss of instrument air. A standard catalytically-cracked heavy gas oil was used as the microreactor test feed (feed properties: 88.99% C; 9.68% 1.28% S and 482 ppnwN). The test conditions used were as follows: 58.7 bar, 340-370 C, 1.0-2.0 LHSV, 2-4 H2/oil mol ratio. Catalysts were crushed, screened to 0.3-1 irin and dried at 482 C for testing. To facilitate control of the reactor temperature the catalysts were diluted 1-1 by volume with a high-density alumina or silicon carbide ground to 0.3-1 mm. Prior to processing hydrocarbon feed, the catalysts were presulphided at atmospheric pressure with 5% H2S in N . The temperature program for the presulphiding was 2 hours at 204 C, 1 hour at 315 C and 2 hours at 371 OC. Depending upon the metals content, the catalysts will contain from 10-20 Ww sulphur. In a typical Ni/Mb or Co/Mb hydrotreating catalyst preparation method catalytically active metals are deposited on a support by a dry (pore volume) impregnation technique. In this method, the support is impregnated with a quantity of metal-salt solution that is just sufficient to be absorbed in the pore volume of the support. The impregnating solution is generally prepared in two parts initially. One part contains the molybdenum salt and most of the water that can be used. After most of the molybdenum salt has dissolved (with heating and stirring), H202 (30%) is added (about 0.4 ml/g of Mb) to aid solubilization. The other part of the solution contains the Ni and/or Co salt(s) and sufficient phosphoric acid (85%) to aid the solubility and stability of the solution and to include about 3 w P in the catalyst. when both solutions are clear and oool, the Mb solution is added slowly (with vigorous stirring) to the Ni-P or Co-P solution. The carbined solution is then diluted to the proper volume and added slowly, usually in one or more steps, to the support. The impregnated catalyst is dried at 121 OC for about 2 hours and then calcined in air at 482 OC for about 2 hours. A substantial increase in the hydrodnitrification (HDN) activity, relative to existing commercial catalysts, is required to commercialize a new hydrotreating catalyst. In an effort to develop such an improved catalyst, a standard 72 hour HDN activity test was used to evaluate the various catalysts. In this test the hydrogenation (H2), HDW and hydrodesuiphurization (HDS) activities of a standard catalytically-cracked heavy gas oil were evaluated at 344 OC and 57.8 bar H2 partial pressure. Activities were compared based on observed rate constants for HDN and on plug flow kinetics for HDS. Suitable conditions for the hy*roconversion processes using improved catalysts according to the invention are as follows: a temperature of 350-420 OC; a total pressure of 75-200 bar; a partial hydrogen pressure of 60-200 bar; a space velocity of 0.4-1.5 kg oil/l catalyst/hour; and a hydrogen feed rate of 250-2500 Nl/kg oil feed. The hydrodenitrification of heavy oil feeds according to the present process is preferably carried out under the following conditions: a temperature of 360-410 OC; a total pressure of 100-150 bar; a partial hydegen pressure of 80-150 bar; a space velocity of 0.4-1.0 kg oil/l catalyst/hour; and a hydrogen feed rate of 500-1500 Nl/kg oil feed. The hydrogen applied can be pure hydrogen or a hydrogen-containing gas, preferably one comprising more than 70% hydrogen. The hydrogen-containing gas may also contain up to about 10% of hydrogen sulphide. The invention will now be illustrated by the following Examples: TWO catalysts, A (aluma-based) and B (silica-based) were prepared for caparison by a conventional aqueous impregnation method and were not prepared in accordance with the present invention. Catalyst A was a standard commercial hydrotreating catalyst (available from Shell Chemical Company) which was prepared by using a dry (pore volume) metals aqueous impregnation technique to impart metals onto a gamna alumina support. this catalyst was prepared by the typical aqueous impregnation method described herein above. The carposition of this alumina-based catalyst is given in Table 1. The various hydrotrating activities of this catalyst were taken as 1.0 for coparissn. Catalyst B was prepared by impregnating a dried Grade 57 silica (from Davison Chemical, a division of W.R. Grace Co.) with the same metals solution and dry (pore volume) technique used for Catalyst A. The composition of this silica-based catalyst is also given in Table 1. A silica-based catalyst, C, was prepared according to the present invention by slurrying 14.4 g PbO3 and 14.6 g EDTA in 50 ml HO. 20 g (NH4) 2m3 were then added slowly. Upon completion of this addition, 10 g N2H4 were added and the mixture was heated at reflux (ca. 90 C) for 2 hours. The solution volume was then reduced to 38 ml and the mixture was impregnated bot (ca. 90 C) on 38 g of Davison 57 silica (0.35-0.85 mm) which had been dried at 400 C for 2 hours. This material was then dried for 18 hours at 120 OC, impregnated with 7.2 g [Ni(H20)6](ND3)2 in 35 ml H20, and dried at 120 C for 12 hours. The composition of Catalyst C is also given in Table 1. A silica-based catalyst, D, was prepared according to the present invention by slurrying 14.4 g MbO3 in 25 ml 1120. To this was added 11 ml diethylene triamine (DT). The volume of this mixture was increased to 50 ml with water and the mixture was heated until all material had dissolved. The solution volume was adjusted to 56 ml with water and the hot solution was used to impregnate 40 g of 2 irrn dia. silica spheres (available commercially from Shell International Chemical Company, Ghent, Belgium) which had been dried at 400 C for 2 hours. This material was then dried at 120 C for 12 hours. 8.5 g of Ni(H2O)4(OAc)2 (CAc = acetate) was then dissolved in concentrated NH4 and diluted to 30 ml with same. dried catalyst precursor was then impregnated with this solution and dried at 120 0C for 12 hours. The composition of Catalyst D is also given in Table 1. A silica-based catalyst, E, was prepared, according to the present invention, by dissolving 19.1 g nitrilotriacetic acid (Nm) in 30 ml 24% ammonium }rcxide. To this was added 14.4 g MoO3 and the mixture was brought to boiling. After cooling to 50 -70 OC, 8.7 g nickel nitrate was added and the mixture was diluted to 50 ml with water. 35 g of 200 C dried silica spheres were then impregnated with this mixture and dried overnight at 120 CC. The composition of Catalyst E is also given in Table 1. TABLE 1 Catalyst/ Composition Surface Area (Support) (% w) m2/g Mo Ni ¯¯¯¯¯¯¯¯¯¯ A (Al2O3) 13.2 2.7 160 B (SiO2) 15.4 4.6 14Q C (SiO2) 10.6 5.0 136 D (SiO2) 13.8 2.6 E (SiO2) 15 3 EXAMPLE 2 The catalysts A-E were heated to about 200 C, presulphided and compared to determine their relative hydrotreating activities (H2 2 hydogenation; HDN = hydrodnitrification and HDS = hydrodesulphurization) over the standard catalytically-cracked heavy gas oil having the feed properties described hereinabcve. For the tests 10.4 ml of 0.3-1 mm catalyst particles were placed in a microreactor and used to contact the feed at 344 OC, 58.7 bar, H2/oil ratio = 4/1 and LHSV = 2.0. Results of the tests are shown in Table 2. TABLE 2 Catalyst/ Relative activity (Support) H2 HON HDS A 1.00 + .03 1.00 # .10 1.00 # .10 B 0.48 0.20 0.27 C 0.92 0.93 0.78 D 0.75 0.77 0.46 E 0.95 1.12 0.88 The relative activity of the commercial alumina-based catalyst A, was taken as 1.00 by definition. As can be seen from Table 2, the activity of the silica-based catalyst B, prepared in the same manner as that normally used for a commercial alumina-based hydrotreating catalyst gave very poor results for all three (H2, HDN, HDS) hydrotreating activities. However, the HDN activity of the silica-based catalyst C, prepared according to the invention is within experimental error of the activity of a top quality commmercial alumina-based hydrotreating catalyst, A, and nearly five times as active as a conventionally prepared silica-based catalyst. Also catalyst D is nearly four times as active as a conventionally prepared silica-based catalyst. Catalyst E demonstrated an HDN activity even exceeding that of a top quality commercial alumma-based hydrotreating catalyst A and was nearly six times as active as a cn'antionally prepared silica-based catalyst. This catalyst E was also within experImental error of the H2 activity and was only slightly below the HDS activity of the alumina-based catalyst A.

Claims: CLAIMS 1. Process for preparing silica-supported catalysts containing 10-25 tW molybdenum and from 1-5 %w nickel and/or cobalt as hydrogenation metals which comprises impregnating a dried silica support with an aqueous solution or an aqueous mixture obtained by contacting a hydrogenation metal compound with a nitrogen-containing organic ligand in the presence of water. 2. Process according to claim 1, wherein the dried silica support is impregnated at elevated temperature with the solution from step (d) which has been obtained by: (a) preparing a slurry of aboot equal quantities of MoO3 and EDTA in water to provide from 10 to 25 %w of Mo on said support; (b) adding from at least said equal quantity up to about a double quantity of (NH4)2CO3 to the slurry and mixing same; (c) adding about half as much hydrazine to the mixture as the quantity of nYH4)2CO3 added; (d) heating the mixture from step (c) to a temperature sufficient to form (NH4)2[MO2O4(EDTA)] ion a reasonable time; followed by drying the No-iipregnated silica at elevated temperature; whilst the dried silica support is impregnated with a desired quantity of aqueous nickel and/or cobalt salt solution either before or after the impregnation with the solution from step (d), and drying the Ni- and/or Co-ixtpregnated silica at elevated tempera- ture. 3. Process according to claim 1, wherein the dried silica support is impregnated at elevated temperature with the solution fran step (b) which has been obtained by: (a) preparing a slurry of an amount of MkO3 and d iethylene triamine in water to provide from 10 to 25 %w Mb on said support; (b) heating and mixing the slurry in sufficient water to dissolve the followed by drying the Mb-impregnated silica at elevated temperature; whilst the dried silica support is impregnated with a desired quantity of aqueous nickel and/or cobalt salt solution either before or after the impregnation with the solution from step (b), and drying the Ni-Mo or Cb-Mo impregnated silica at elevated temperature. 4. Process according to claim 1, wherein the dried silica support is impregnated at elevated temperature with the aqueous mixture from step (d) 'which has been obtained by: (a) dissolving an appropriate artaint of nitrilotriacetic'acid in amnrmium hydroxide; (b) adding to the mixture from step (a) an amount of MoOx to provide from 10 to 25 w Mo on said support; (c) heating the mixture in step (b) until the reaction is substantially complete; (d) cooling the mixture fran step (c) and adding an amount of nickel and/or cobalt salt to provide from about 1-5 %w Ni and/or Co on said support; and drying the Ni-Mo- and/or Co-Mo-impregnated silica at elevated temperature. 5. Process according to one or more of the preceding claims, wherein the catalyst is heated to about 200 C and sulphided before being used in a hydrotreating process. 6. Process according to one or more of the preceding claims, wherein the impregnation mixtures contain sufficient catalytically active metals to provide from 10-20 %w molybdenum and about 2-4 %w nickel on said support. 7. Process according to claim 3, wherein the molybdenum impregnation mixture is heated at about reflux temperature of said mixtuie. 8. Process according to one or more of the preceding claims, wherein the MoOx is MoO3, and the volume of the solution/mixture obtained is adjusted to about the pore volume of the silica support before impregnating same. 9. Process according to claim 5, wherein the impregnated silica is dried at about 200 OC and sulphided before being used in a hydrotreating process. 10. Process according to any one of the preceding claims, wherein use is made of silica spheres as support. 11. Process according to any one of the preceding claims, substar.-lally as described herein with particular reference to the EXamples. 12. A hydrotreating catalyst comprising fran 10-25 %w molybdenum and from 1-5 %w nickel and/or cobalt as hydrogenation metals supported on silica whenever prepared according to a process as claimed in one or more of the preceding claims. 13. A hydrotreating catalyst ccoprising from 10-20 %w molybdenum and from 2-4 %w nickel as hydrogenation metals supported on silica, which catalyst has been prepared by the process according to claim 8. 14. A sulphided hydrotreating catalyst comprising from 10-20 Fw molybdenum and fran 2-4 8w nickel as hydrogenation metals and from about 10-20 bw sulphur, which catalyst has been prepared by the process according to claim 5.

Inventors: THOMPSON, MARK STEWART
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1985
Main classification: B01J23
IPC codes: C10G45, B01J31, B01J23, B01J37