GB2323094A - A hydroconversion catalyst - Google Patents

Abstract

A hydroconversion catalyst composition includes a catalytically active matrix having a surface area of between about 50 m<SP>2</SP>/g to about 290 m<SP>2</SP>/g, a silicious molecular sieve support medium distributed through the matrix and having a surface area of between about 250 m<SP>2</SP>/g to about 1200 m<SP>2</SP>/g and a catalytically active phase supported on the support medium and including a first metal selected from group IIIA of the periodic table of elements eg. Ga or B, a second metal selected from group VIB of the periodic table of element eg. Cr or Mo. The matrix preferably further includes aluminum, gallium, cobalt, molybdenum, and phosphorus.

Description

HYDROPROCESSING SCHEME FOR PRODUCTION OF PREMIUM ISOMERIZED LIGHT GASOLINE BACKGROUND OF THE INVENTION The present invention relates to a process for hydroconversion of light and heavy feedstock, especially heavy naphtha feedstock1 to a catalyst for use in hydroconversion processes with a feedstock having sulfur and nitrogen contaminants and to a process for providing such a catalyst Light naphtha feedstock can be treated by hydroconversion to produce premium isomerized light gasoline blending components. Numerous catalysts including the various zeolite catalysts are useful in such processes.

Heavy naphtha feedstock would also be a useful source of blending components. However, conventional zeolite catalysts are rapidly deactivated by sulfur, nitrogen, coke, and other contaminants which may be present in heavy naphtha feedstock.

U.S. Patent No. 4,734,539 to Lawlor et al. discloses such a catalyst which is useful in some applications.

However, the catalyst of Lawlor et al. is susceptible to sulfur deactivation and has a one dimensional pore system which leads to rapid deactivation by coke as well.

U.S. Patent No. 4,962,269 to LaPierre et al. also discloses a process for isomerization using zeolite catalyst. However, LaPierre et al. use Y or ZSM-20 zeolite, which is a specialty product (and therefore increases the cost of the process). LaPierre et al.'s process also leads to an undesirable increase in aromatics.

It is the primary object of the invention, therefore, to provide a process for hydroconversion of a heavy naphtha feedstock having a high content of sulfur and nitrogen contaminants so as to provide useful gasoline blending products.

It is a further object of the invention to provide a catalyst for hydroconversion processes which is not significantly deactivated by sulfur, nitrogen and coke.

It is a still further object of the invention to provide such a hydroconversion catalyst which provides significant levels of isomerization without increasing the output of aromatic.

It is another object of the invention to provide a process for preparing a catalyst in accordance with the invention.

Other objects and advantages will appear hereinbelow.

SUMMARY OF THE INVENTION In accordance with the invention, the foregoing objects and advantages are readily attained.

In accordance with the invention, a catalyst system is disclosed which comprises a catalytically active matrix; a support medium distributed through the matrix and comprising a silicious molecular sieve material; and a catalytically active phase supported on the support medium and comprising a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements.

Preferably, the catalyst systems comprises a catalytically active matrix comprising a first metal selected from group IIIA of the periodic table of elements, a second metal selected from group IIIA, a third metal selected from group VII, a fourth metal selected from group VIB, and a fifth metal selected from group VA; a support medium distributed through the matrix and comprising a silicious molecular sieve material; and a catalytically active phase supported on the support media and comprising a group IIIA metal and a group VIB metal.

In further accordance with the invention a process is disclosed for upgrading sulfur rich heavy naphtha feedstock which process comprises the steps of providing a heavy naphtha feedstock having an initial sulfur content and an initial octane number; and contacting said feedstock with a hydroconversion catalyst system under a hydrogen atmosphere at hydroisomerization temperature and pressure so as to provide a final product having a final sulfur content which is less than the initial sulfur content of the feedstock, and having a final octane number which is substantially equal to or greater than said initial octane number of the feedstock, and wherein the final product has an increased isomerized component and substantially no increase in aromatic content with respect to said feedstock.

A two stage process wherein the feedstock is first hydrodesulfurized and then upgraded is also disclosed.

A process is also disclosed in accordance with the invention for providing the catalyst systems of the invention, which process comprises the steps of providing a support medium comprising a silicious molecular sieve material having a surface area of between about 250 m2/g to about 1200 m2/g and supporting a catalytically active phase comprising a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements; providing a matrix material having a surface area of between about 50 m2/g to about 290 m2/g; mixing said support medium with said matrix to form a substantially homogeneous paste having a ratio by weight of said support medium to said matrix of at least about 0.1; forming said paste into catalyst elements; and calcining said catalyst elements whereby at least a portion of said first metal of said catalytically active phase migrates from said support medium to said matrix whereby said matrix is catalytically active.

DETAILED DESCRIPTION The invention relates to a catalyst system, particularly a hydroconversion catalyst for use in hydroisomerization of naphtha feedstocks including heavy naphtha, cracked naphtha, straight run naphtha and the like so as to isomerize the feedstock and provide gasoline or gasoline additives having improved RON/MON values. In accordance with the invention, the catalyst also reduces sulfur and nitrogen levels in the feedstock without rapid deactivation of the catalyst, and prevents increases in undesirable aromatics production.

The catalyst of the invention includes a catalyst system comprising a matrix, a support medium within or distributed through the matrix, a catalytically active phase supported on or incorporated within the matrix so as to render the matrix catalytically active, and a catalytically active phase supported on the support medium.

The matrix preferably includes aluminum, preferably in the form of a mesoporous or gamma alumina matrix, and supports a catalytically active phase which includes a group IIIA metal, preferably gallium.

In accordance with the most preferred embodiment of the invention, the matrix further includes or supports additional metals which round out the active phase of the matrix. These metals include a group VIII metal, preferably nickel or cobalt, most preferably cobalt; a group VIB metal, preferably chromium or molybdenum, most preferably molybdenum, and a group VA metal, preferably phosphorus. of the foregoing metals, the total ratio in the final catalyst by weight of cobalt to molybdenum is preferably between about 0.5 to 5, and the total ratio by weight of phosphorus to molybdenum is preferably at least about 0.4. This combination of metals provides the catalyst system with significantly improved and unexpected characteristics as demonstrated by the Examples discussed below.

The gallium, cobalt or nickel, molybdenum and phosphorus of the matrix active phase serve to render the matrix catalytically active so as to increase the activity of the catalyst system towards the desired dehydrogenation and hydrodesulfurization reactions.

The matrix preferably has a surface area of between about 50 m2/g to about 290 m2/g. The matrix is "mesoporous" in that the pore diameter of the matrix is preferably in the range of about 20 A to about 500 . The matrix also preferably has a particle size distribution wherein at least 95% of the particles are smaller than 200 microns, at least 85% smaller that 90 microns, at least 60% smaller than 45 microns, and at least 40% smaller than 25 microns.

The physical characteristics of the matrix as set forth above serve to allow sufficient access of potentially heavy feedstock molecules to the support medium and catalytically active metals distributed through or supported on the matrix.

The support medium is preferably a hydrothermally stable porous crystalline silicious molecular sieve material such as zeolite catalyst or other metallosilicate, especially aluminosilicate. The support medium is preferably an MFI type zeolite such as ZSM-5 or ZSM-12 zeolite, and, according to the invention, excellent results are provided by using a mixture of ZSM-5 and ZSM-12 as will be set forth and demonstrated below. The support medium preferably has a surface area of between about 250 m2/g to about 1200 m2/g. The support medium is also preferably characterized by XRD techniques as showing lines between 22 and 25 of 26, in particular those lines located at (23, 06), (23, 226) and (23, 856) for A and those located at (20, 90), (22, 90) and (23, 17) for B, as main lines. The support medium preferably has an Si/Al atomic ratio of at least about 10, preferably between about 10 to about 200.

The catalytically active phase which is supported on the support medium preferably includes a plurality, preferably two, catalytically active metals. One metal is a group IIIA metal, preferably gallium or boron and most preferably gallium, and the other is a group VIB metal, preferably chromium. Gallium and chromium are each present as oxides in the final catalyst in an amount of between about 0.01% to about 5.0% by weight of the catalyst.

Further, the total ratio by weight in the catalyst of gallium to chromium is preferably between about 1 to about 10. The final catalyst further exhibits a ratio of Si to M, where M is defined as the group IIIA metal other than aluminum plus the group VIB metal, of between about 10 to about 50.

The final catalyst preferably has a chemical surface composition characterized by the following atomic ratios: Si/Al = 0.01 - 1.0; Si/Ga = 10 - 250; Si/Cr = 1 - 50; and Si/(Ga+Al+Cr+Mo+Co+P) = 0.001 - 5.0. The catalyst preferably has a particle diameter of between about 0.5 mm to about 3 mm, a surface area of between about 140 m2/g to about 250 m2/g, a pore volume of between about 0.3 cc/g to about 0.9 cc/g; and a pore diameter of between about 60 A to about 140 A.

The catalyst according to the invention exhibits improved isomerization without increasing aromatics as shown in the Examples to follow, and also possesses resistance to deactivation by sulfur, nitrogen and coke contaminants.

Catalyst according to the invention may be prepared, according to the invention, as follows.

The zeolite support medium is provided initially supporting the desired catalytically active phase, preferably gallium and chromium. The gallium and chromium elements may be deposited on or supported by the zeolite by any means known in the art such as impregnation, exchange, direct syntheses, and the like. In this regard, the zeolite with metals may suitably be directly synthesized in accordance with the method disclosed in co-pending and commonly assigned U.S. Patent Application No. 08/055,089- filed May 3, 1993.

If the metals are to be impregnated onto the zeolite support, it is preferable to impregnate the chromium first, followed by the gallium, so that a good distribution of the chromium can be ensured.

Impregnation is preferably carried out with a salt of the metal in an aqueous medium. Preferable salts include Cr(N03)2.9H20 and Ga(NO3) 2 - 9H2O, although others are suitable.

Dissolving the salt in the aqueous medium allows an effective exchange or impregnation of the metal into the molecular sieve.

Each impregnation is preferably followed by a drying step. The drying steps may be carried out at a temperature of between about 800C to about 1500C, preferably about 1200C, under a flow of air containing water vapor equivalent to about 0.5 kg H2O/hour-kg of catalyst for a period of between about 1 hour to about 6 hours.

The zeolite support in accordance with the invention is provided with an amount of gallium and chromium to provide the final catalyst composition with between about 0.01% wt to about 5.0t wt of each metal in oxide form. The zeolite support also preferably has a resulting Si/M atomic ratio, where M is the total active phase metal, of between about 0.01 to about 5.0.

After incorporation of the metals, which may be in oxide forum, the support with metal is mixed with the alumina gel matrix material to form a substantially homogeneous paste. The paste may at this point be extruded or otherwise formed into any desired form such as, for example, cylindrical, trilobe and/or quadrilobe shapes, granules, particles or any other form in which it is desirable to provide the catalyst system of the present invention, which shapes and/or forms are collectively referred to herein as catalyst elements.

The catalyst elements are then impregnated with aqueous solutions(s) containing a mixture of the salts of the desired group VIII, VIB and VA metals. Preferred salt solutions include MovO(NH4)6 4H20 (ammonium heptamolybate); Co(NO3)2-6H2O (cobalt nitrate); H3PO4 (phosphoric acid) and the like. The impregnated catalyst elements are then dried as described above so as to leave the desired metals deposited or impregnated onto the matrix. Of course, the desired metals may be incorporated or deposited in numerous other ways which are known to those skilled in the art.

Further, the metals may also be incorporated onto the matrix prior to mixing with the support medium if desired.

Once the desired metals are in place on both the matrix and support medium, the catalyst elements are then calcined in accordance with the invention so as to provide the final catalyst product.

During the calcining procedure, a portion of the gallium originally supported on the zeolite support migrates to the alumina gel (matrix) portion of the catalyst to provide the above-mentioned surface ratios with respect to gallium. Thus, the matrix of the final catalyst comprises an alumina matrix supporting gallium in addition to the cobalt, molybdenum and phosphorus which, as set forth above, are critical in providing the desired operation of the catalyst system in accordance with the invention.

In accordance with the invention, calcining is carried out at a temperature of about 6000C for a period of about 6 hours under a flow of air containing water vapor equivalent to about 0.5 kg H2O/hour-kg of catalyst. Preferably, calcining is carried out in two stages. The first calcining stage is carried out between about 1200C to about 3500C for about 1-6 hours, and the second stage is carried out between about 3500C to about 7000C for about 1-6 hours.

The process as set forth above provides the catalyst of the invention which yields excellent isomerization of naphtha feedstock without increased aromatic production and which catalyst is resistant to deactivation from sulfur, nitrogen and coke. In accordance with the process, gallium is transferred from the support medium to the matrix where it is functional to help provide the improved characteristics of the catalyst. In accordance with the most preferred embodiment of the invention, the transferred gallium along with the cobalt, molybdenum and phosphorus of the matrix serve to provide enhanced reduction of and resistance to sulfur and nitrogen contaminants in the feedstock, and provide excellent activity of the catalyst toward the desired isomerization reaction without increasing aromatics production so as to yield upgraded products having increased octane number.

In use, the catalyst is preferably contacted with the feedstock under process conditions effective to provide the desired reaction, typically including a pressure of between about 1 bar to about 50 bars, a temperature of between about 2500C to about 4500C, a space velocity of between about 0.1 to about 3 h-', a recycle gas ratio of between about 30 to about 1000 standard e/e of feed and a recycle liquid ratio of between about 1 to about 10 e/e of feed. A minimum hydrogen partial pressure at the inlet of the reaction stage is adjusted to between about 0.5 bar to about 40 bars depending upon the total pressure, generally representing about 50% hydrogen purity in the recycle stream.

The catalyst according to the invention is preferably installed in a reactor in a number of reaction stages which may be in fixed bed and/or combined bed arrangement. The process may include one or more reaction stages, swing reaction stages, liquid and gas recycle and the like, all as is known in the art. The catalyst is preferably provided in a particle diameter of about 0.5 mm to about 3.0 mm in a dense load.

A plurality of parallel reactors may also suitably be used, along with a control or sensor device to take a reactor off stream when it is ready for regeneration.

The preferred feedstock has a sulfur content of between about 1 to about 8500 ppm, although feedstocks having a sulfur content up to about 50,000 ppm may be satisfactorily treated in accordance with the invention.

A hydrodesulfurization step may be useful when large concentrations of sulfur are present in the feedstock.

Conventional hydrodesulfurization techniques may be used to reduce sulfur content by factors greater than 60%. However, such sulfur reduction is frequently accompanied by loss of octane number. In accordance with the invention, such a desulfurized intermediate produce may be contacted with the catalyst system of the present invention so as to provide a final product having a further reduced sulfur content, a large fraction of isomerized product, increased octane number (which is generally increased at least to and potentially exceeding the original octane number of the feed), and no substantial increase in aromatics production.

Hydrodesulfurization is generally preferred for feedstocks having sulfur content exceeding 20,000 ppm, preferably exceeding 1,000 ppm, and up to about 50,000 ppm.

The feed to be contacted with the catalyst system of the invention preferably has a sulfur content of between about 1 ppm to about 20,000 ppm, although such feedstock generally contains a minimum of at least 50 ppm of sulfur.

The feedstock may also have a nitrogen content of up to about 200 ppm, preferably no greater than about 25 ppm. In accordance with the invention, the catalyst system is substantially unaffected by these amounts of nitrogen and may be useful in reducing nitrogen in the feedstock during hydroconvers ion processes.

The final product after contact with the catalyst system according to the invention is characterized by an upgraded product having improved characteristics. The final product exhibits an increase in isomerized component of about 5-20%. Sulfur is reduced in varying amounts depending upon whether a hydrodesulfurization step is used. If a hydrodesulfurization step is used, sulfur may be reduced by greater than 60%, typically between about 60% to about 70%.

If the feedstock is fed directly to the hydroconversion catalyst of the present invention, sulfur reduction is typically at least about 20% to about 40% and may be as great as about 30% to about 70%. The final product also exhibits a substantially unchanged aromatic content, and an octane number greater than about 85 RON (83 MON). The actual increase in octane number, of course, depends upon the feedstock. A heavy straight run naphtha may typically be increased by about 30 to about 40 RON, while a heavy cracked naphtha cut may be increased by about 2 to about 10 RON.

The final product resulting from contact with the hydroconversion catalyst according to the invention also exhibits improved distillation temperature or T90 values, as will be demonstrated in the examples to follow.

Example 1 This example illustrates the preparation of two catalysts according to the invention. The chemical compositions of the two catalysts are set forth below in Table 1. The catalysts were prepared as follows.

H-ZSM5 zeolite was provided as the support medium and impregnated with aqueous solutions of Cr(NO3)3-H2O and Ga(NO3)3-9H2O. The impregnated zeolite was combined with a gamma alumina matrix to form a substantially homogeneous paste, which was extruded and dried. The extruded catalyst elements were then impregnated with aqueous solutions of MrO23(NH4)6-4H2O, Co(NO3)2 6H2O (Catalyst #1), Ni(No3)2 (Catalyst #2), and H3PO4. The impregnated solid was then dried and calcined so as to provide the catalysts described in Table 1.

TABLE 1 chemical composition of the catalyst CoMoP/Al2O3+GACR/H-ZSM-5 NiMoP/Al2O3+GaCr/H-ZSM-5 Al (%) 18.0 16.9 Si (%) 24.0 16.4 Mo (t) 4.87 4.9 Co (z) 3.10 0 P (8) 1.30 0.9 Cr (ppm) 809 612 Ga (ppm) 3773 1210 Ni (%) 0 4.1 Mechan. 5.7 4.7 Resist.

kg/p Area 204 213 (m2/9) The surface composition of catalyst S1 was determined by XPS technique as follows: TABLE 2 Elements Co (2pew?) 0.83 Mo (3d) 1.025 p 0.54 Al (2p) 17.43 Si (2P) 22.68 Ga (2p3/2) 0.16 Cr (2p3/2) 0.16 0(1s) 58.26 ExamPle 2 This example illustrates the importance of both the active metal supported on the zeolite support medium and also on the matrix. Three catalysts were prepared as shown in Table 3: TABLE 3 Catalyst Composition CATALYST COMPOSITION A CoMoPjAl2o3 + GaCr/H-ZSM-5 B CoMoP/Al203 + H-zSM-5 C A1203 + GaCr/H-ZSM-5 Catalyst A is the most preferred catalyst according to the invention, and has active phases on both the matrix and zeolite support. Catalyst B does not have active metal on the zeolite. Catalyst C has active metal on the zeolite, but does not include the CoMoP metals on the matrix which only has a portion of Ga transferred during calcination as described above.

Catalysts A, B and C were used in hydroisomerization of n-octane at a temperature of 3500C, pressure of 400 psi, H2/n-C8 ratio of 7.33 v/v and a LHSV of 3.75 h-l. Table 4 contains the results obtained.

TABLE 4 CATALYST CATALYST CATALYST A B C Total Conversion(%) 54.46 70.68 52.22 Gas Yield(%) 14.87 36.35 19.43 Liquid Yield (C5+) (%) 39.60 34.32 33.04 Gas Product Selectivity($) 27.30 51.43 37.21 Liquid Product Selectivity(%) 72.70 48.57 63.29 Saturated Linear Products(%) 5.79 9.35 5.18 Isomers C,+(%) 49.72 32.36 38.64 Unsaturated Liquid Products(%) 0.70 1.04 0.46 Cyclic Products (%) 10.55 5.43 9.10 Aromatics(%) 5.94 0.39 9.41 As shown, Catalyst A provides the highest selectivity toward isomers and the lowest gas formation. Catalyst B exhibits a relatively high gas product selectivity, but is lowest in the desired isomer formation. Catalyst C, formulated in accordance with the broader aspect of the invention, provides less total conversion and less selectivity toward C5+ liquid products, but good isomerization.

Thus, in accordance with the invention, Catalyst A having active phases containing Ga + Cr as well as Co, Mo and P provides the best results.

Catalyst C, also formulated in accordance with the invention so as to have gallium transferred to the matrix, also provides desirable results.

Example 3 Catalyst A of Example 2 was further used in hydroisomerization of heavy virgin naphtha under hydroconversion conditions similar to Example 2 but at different pressures of 150 and 400 psig so as to demonstrate the effect of pressure on the hydroisomerization process of the present invention. Table 5 contains the results.

TABLE 5 FEED PRODUCTS Pressure (psig) 150 400 API 58.9 58.0 61.0 Sulfur (ppm) 94 49 25 Nitrogen (ppm) < 1 < 1 Br number < 1 < 1 < 1 RVP (psi) 2.81 5.60 7.0 RON 57.9 69.6 80.0 MON 57.0 69.6 80.0 Paraffins(%V) 56 49 52 Olefins($V) 0 1 0 Naphtenes(%V) 32 33 31 Aromatic (%V) 12 17 16 Simulated Distillation F (T90) 0/10 133/169 81/160 77/138 30/50 214/248 210/244 196/239 70/90 284/324 282/324 270/297 As shown, the process improves as pressure increases from 150 to 400 psig. Specifically, sulfur reduction, RCN, API gravity and T90 are all improved. Note also that aromatic and olefin content remain substantially unchanged as desired, and that the Reid vapor pressure remains below 9 psi.

Example 4 This example illustrates a two stage process using a commercial hydrodesulfurization catalyst and process followed by hydroconversion using Catalyst A of Example 2 according to the invention. Hydrodesulfurization was carried out at 3400C and 400 psig, and a ratio of H2/HC of 500 Nv/v and LHSV of 1.0 h, Hydroisomerization of the intermediate product was then carried out at 3300C, 700 psig, H2/HC ratio of 500 Nv/v and LHSV of 0.75 h4. The results are contained in Table 6.

TABLE 6 Hydro- Hydro desulfurization isomerization Heavy Cracked Intermediate Final Product Naphtha API 46.3 52.3 56.5 Sulfur 8910 31 < 20 (Ppm) RON 77 44 81 T90(tF) 410 385 334 Br No. 78 < 1 < 1 Yield(%wt.) 95 90 As shown, hydrodesulfurization reduces sulfur, but octane number (RON) as well. The catalyst of the present invention restores the lost octane number to a level higher than the feed, further reduces sulfur content, increases API gravity, and reduces T90, all as desired in accordance witn the present invention.

Example 5 This example illustrates a two stage process similar to Example 4 but using a heavy FCC naphtha feedstock and Catalyst A of Example 2.

Hydrodesulfurization was carried out at 3400C, 400 psig, H2/HC ratio of 500 Nv/v and LLISV of l.Oh-'.

Hydroisomerization was then carried out at 330"C, 700 psig, H2/HC ratio of 500 Nv/v and LHSV of 0.75-t. The results of this example are set forth below in Table 7.

TABLE 7 Hydro- Hydro desulfurization isomerization Heavy FCC Naphta Intermediate Final Product API 33.2 Sulfur 3820 30 28 (ppm) RON 92.8 88.1 91 T90(OF) 459 385 455 Br No. 11 cS, (%wt.) As shown, sulfur content is further reduced by Catalyst A, and RON is restored almost to the original value.

ExamPle 6 This example demonstrates that an atmospheric straightrun naphtha with low sulfur content (60 ppm) can be treated with the catalyst of the present invention to provide transformation to more suitable isomerized hydrocarbon products with high RON and MON values, and low RVP (Reid Vapor Pressure) and aromatic content, by contacting the feedstock with the catalyst under the following conditions: Reaction temperature = 2800C - 3200C Total Pressure = 200 psig H2/HC feedstock molar ratio = 3 L.H.S.V. = 1-2 h' The feedstock is pre-heated by means of conventional heat-exchanger with product stream before contact with the catalyst of the present invention. Table 8 sets forth 'the volumetric boiling point distribution (T90) obtained after reaching the steady state of reaction. Benefits obtained by use of the catalyst of the present invention can be summarized as follows: low RVP; good HDS activity (sulfur removal); high content of light and medium isomerized product with high octane number (RON and MON); and the original content of aromatics which remain unchanged through the reaction.

TABLE 8 - Feedstock and product properties Feedstock Product Dist (% vol.) IBP - 10 36 - 86 95 - 98 30 - 50 101 - 117 103 - 109 70 - 90 135 - 157 114 - 119 FBP 195 125 API gravity 55 65 Octane RON 55 85 Aromatics (t vol.) 17 17 Sulfur 60 ppm 5 ppm Example 7 This example demonstrates that light cuts of FCC (650C - 1700C) with moderate content of sulfur (600 ppm) can also be used directly as regular feedstock to the catalyst of the present invention to produce light isomerized gasoline with high RON and MON, with no aromatic production, good sulfur removal and a better resulting RVP.

The example was run by contacting the feedstock with the catalyst under the following conditions: Reaction temperature = 320"C - 350"C Total Pressure = 400 psig H2/HC feedstock ratio = 5 L.H.S.V. = 0.75 h The feedstock was pre-heated by means of conventional heat-exchanger with product stream before contact with the catalyst of the present invention. Volumetric boiling point distribution obtained after reaching the steady state of reaction is presented and compared in Table 9.

TABLE 9 - Feedstock and product properties Feedstock Product Dist (% vol.) IBP - 10 72 - 84 65 - 73 30 - 50 92 - 117 83 - 95 70 - 90 139 - 150 107 - 122 FBP 162 148 API gravity 55 57 Octane RON 92.6 95.2 Sulfur 600 ppm 74 ppm The product was a light isomerized gasoline having a high RON number, improved RVP and less sulfur with no aromatic production.

Example 8 This example demonstrates that the catalyst of the invention must include an MFI type zeolite (or metallosilicate) rather than other types of zeolite because of its selectivity toward light isomerized products from either straight-run or heavy cracked naphtha, with or without high sulfur content. In this example, and also in Examples 9-11 to follow, cobalt, molybdenum and phosphorus metals were not added to the matrix so as to more clearly demonstrate the influence of a change in zeolite.

Preparation of GaCr/HY(non-MFI! catalyst: The catalyst is prepared by an identical procedure used to prepare the MFI based catalyst. 100 g of commercial HY zeolite are impregnated with aqueous solutions of Cr(NO,),9H,O and Ga(NO,),.9H20, until a total amount of about 0.01% to 5% by weight metals are present and the Ga/Cr atomic ratio is in the range of 1 to 10. The impregnated support medium was combined with a matrix (alumina) so as to form homogeneous paste which was extruded and then calcined.

This catalyst was then compared with the MFI based catalyst prepared according to the invention, formed with same metals and amounts and prepared by identical procedure on a commercial H-ZSM-5 zeolite. The results are set forth below in Table 10.

TABLE 10 - Activity and selectivity of the catalysts GaCr/Hy + alumina GaCr/ZSM-5 + alumina Liquid yield (%) 46.81 59.88 BTX (t) < 1 < 1 Isomers C5+ (t) 3.73 34.72 I/C ratio < 1 1.04 Gas yield (%) 53.19 40.12 Cl - C4 (t) 77.28 94.55 C3 = (%) 22.72 5.45 Table 10 clearly shows the improved activity, selectivity and stability of GaCr/ZSM-5 catalyst to produce light isomerized gasoline from similar feedstock at the same operational conditions used to run Example 6, rather than the undesirable cracking and dehydrogenating activity exhibited by GaCr/HY catalyst under the same conditions and with the same feedstock.

Example 9 This example demonstrates that the support medium of the catalyst must include both gallium and chromium to produce the best catalytic isomerization of naphtha feedstock (cracked or not) Three catalysts are prepared, one with only gallium (Ga/ZSM-5), one with only chromium (Cr/ZSM-5), and the third with both gallium and chromium in accordance with the invention (GaCr/ZSM-5). Each catalyst was prepared so as to contain the same total amount of gallium, chromium, and gallium plus chromium, respectively.

Preparation of Ga/ZSM-5 catalyst: This catalyst is prepared by an identical procedure used to prepare the GaCr/ZSM-5 based catalyst of the present invention. 100 g of the same commercial HZSM-5 zeolite used to prepare the GaCr based catalyst are impregnated with an aqueous solution of Ga(NO3)3-9H2O, as the only active metal present. The impregnated support medium was combined with the alumina matrix so as to form a homogeneous paste which was extruded and then calcined.

Preparation of a Cr/ZSM-5 catalyst: This catalyst is prepared by an identical procedure used to prepare the GaCr/ZSM-5 based catalyst of the present invention. 100 g of the same commercial HZSM-5 zeolite used to prepare the GaCr based catalyst are impregnated with an aqueous solution of Cr(NO3)3 9HzO, as the only active metal present. The impregnated support medium was combined with the alumina matrix so as to form a homogeneous paste which was extruded and calcined.

These catalysts were compared with the GaCr/ZSM-5 based catalyst, formed with same metals and amounts and prepared by identical procedure on the same commercial H-ZSM-5 zeolite. The results are set forth below in Table 11.

TABLE 11 - Activity and selectivity of the catalysts Ga/ZSM-5 + Cr/ZSM-5 + GaCR/ZSM-5 + alumina alumina alumina Liquid yield (t) 10.16 56.55 59.88 BTX (%) > 89 < 1 < 1 Isomers C5 + (%) 2.13 10.62 34.72 I/C ratio 1.02 1.03 1.04 Gas yield (t) 89.84 43.45 40.12 Table 11 clearly shows the improved activity, selectivity and stability of the GaCr/ZSM-5 catalyst according to the invention to produce light isomerized gasoline from similar feedstock at the same operational conditions used to run Example 6. Undesirable sidereactions, such as aromatization in the case of Ga/ZSM-5 catalyst, and cracking and dehydrogenating activity in the case of Cr/ZSM-5 catalyst, are favored if Ga and Cr are not both present in the final catalyst.

Example 10 The catalyst of the present invention was analyzed to show that the final catalyst1 after activation (or calcination), has a gallium enrichment on the surface of the catalyst which is believed to result from a shift of gallium from the support medium to the matrix to provide a Ga203/A1203 matrix having catalytic activity.

PreParation of GaCr/ZSM-5 catalyst: 100 g of commercial ZSM-5 zeolite are impregnated with aqueous solutions of Cr(NO3)3.9H20 and Ga(NO3)3.9H20 until a total amount of about 0.01% to 5% by weight of such metals are present and the Ga/Cr atomic ratio is in the range of 1 to 10. The impregnated support medium was combined with alumina matrix so as to form a homogeneous paste, which was extruded and then calcined.

The catalyst surface with and without activation is characterized by using XPS (X-ray Photoelectron Spectroscopy) technique. The relative abundance of elements was tested using an Al a anode as a source of X-ray emissions. The results obtained are found in Table 12.

TABLE 12 - XPS surface characterization of the catalyst with and without calcination GaCr/ZSM-5 + A1203 Dried fresh catalyst Activated Si/Al surface ratio = 0.1475 0.1711 Si/Ga surface ratio = 8.5968 7.4750 Si/Cr surface ratio = 42.98 37.37 Ga/Si+Al+Cr surface ratio = 0.015 0.020 Area superficial BET = 300 +/- 10 m2/g Fresh catalyst simply dried exhibits less gallium at the surface of the catalyst (high Si/Ga ratio) than the activated one (low Si/Ga ratio). The activated catalyst also showed less aluminum and more chromium at the surface.

Thus, the activation step provides a gallium enrichment on the surface of the catalyst resulting from the shift of the gallium to the matrix so as to enhance the catalytic activity of the matrix.

Example 11 This example demonstrates that the shift of gallium to the matrix to form Ga203/A1203 makes the matrix a catalytically active phase that provides more activity to the final catalytic system.

To run this test, a sample of Ga203/A1203 mixture is prepared by conventional procedure and placed in the reactor under the same reaction conditions used in Example 6.

Another test is run under the same conditions of Example 6, using unextruded (no alumina content) GaCr/ZSM-5 as catalyst.

The results obtained were compared with Example 6.

Table 13 clearly shows that the catalyst GaCr/ZSM-5 + A1203 of the invention exhibits more activity for this reaction than the sum of activities observed with the simple mixture of GaCr/ZSM-5 catalyst and Ga203/A1203, with less gas yield and significantly more isomer production. The mixture also exhibited more aromatics and coke formation.

Furthermore, this comparison also demonstrates that the claimed catalyst is a more stable and selective catalyst for this process.

TABLE 13 - Activity and selectivity of the catalysts Quality product distribution (Run time = 6 hours) Ga203/Alp3 GaCr/ZSM-5 GaCr/ZSM-S + A12OZ Total conversion(%) 3.58 43.88 52.18 Gas yield (C-C,)(%) 14.01 25.63 19.43 Liquid yield(C5+)(%) 85.99 74.37 80.57 Isomers (cm+)(%) 0.01 28.76 30.80 Cyclic products (%) > 0.01 1.48 2.11 Saturated linear products (%) 98.57 10.64 8.15 Unsaturated liquid products (%) > 0.05 1.53 4.85 Aromatic products (%) > 0.01 0.78 1.88 Coke (%) 1.34 2.89 4.56 These results clearly confirm the regenerability, stability and reproducibility of the catalyst prepared according to the present invention.

This invention may be embodied in other forms or carried out in other ways without departing from the spirit or essential characteristics thereof. The present embodiment is therefore to be considered as in all respects illustrative and not restrictive, the scope of the invention being indicated by the appended claims, and all changes which come within the meaning and range of equivalency are intended to be embraced therein.

Claims (45)

Claims

1. A hydroconversion catalyst system, comprising: a catalytically active matrix; a support medium distributed through the matrix and comprising a silicious molecular sieve material; and a catalytically active phase supported on the support medium and comprising a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements.

2. A catalyst system according to claim 1, wherein said matrix has a surface area of between about 50 m2/g to about 290 m2/g, and wherein said support medium has a surface area of between about 250 m2/g to about 1200 m2/g.

3. A catalyst system according to claim 1, wherein said matrix comprises a first metal and a second metal selected from group IIIA of the periodic-table of elements.

4. A catalyst system according to claim 3, wherein said first metal is aluminum and said second metal is gallium.

5 A catalyst system according to claim 3, wherein said matrix further comprises a third metal selected from group VIII, a fourth metal selected from group VIB, and a fifth metal selected from group VA of the periodic table of elements.

6. A catalyst system according to claim 5, wherein said first metal is aluminum, said second metal is gallium, said third metal is selected from the group consisting of cobalt, nickel and mixtures thereof, said fourth metal is selected from the group consisting of molybdenum, chromium and mixtures thereof, and said fifth metal is phosphorus.

7. A catalyst system according to claim 6, wherein said third metal is cobalt and said fourth metal is molybdenum.

8. A catalyst system according to claim 6, wherein said aluminum is present as alumina.

9 A catalyst system according to claim 8, wherein said alumina is gamma alumina.

10. A catalyst system according to claim 1, wherein said matrix has a particle size distribution as follows: at least less than 95% 200y 85% SOIL 60t 45y 40% 25y whereby said support medium and said catalytically active phase are accessible to heavy molecules of feedstock to be treated with said catalyst.

11. A catalyst system according to claim 1, wherein said support medium is an aluminosilicate having an atomic ratio of silicon to aluminum of at least about 10.

12. A catalyst system according to claim 11, wherein said first metal of said catalytically active phase is selected from the group consisting of gallium, boron and mixtures thereof, and said second metal of said catalytically active phase is selected from the group consisting of chromium, molybdenum, and mixtures thereof.

13. A catalyst system according to claim 12, wherein said first metal of said catalytically active phase is gallium and said second metal of said catalytically active phase is chromium.

14. A catalyst system according to claim 7 wherein said support medium is an aluminosilicate having an atomic ratio of silicon to aluminum of at least about 10.

15. A catalyst system according to claim 14 wherein said first metal of said catalytically active phase is selected from the group consisting of gallium, boron and mixtures thereof, and said second metal of said catalytically active phase is selected from the group consisting of chromium, molybdenum, and mixtures thereof.

16. A catalyst system according to claim 15, wherein said first metal of said catalytically active phase is gallium and said second metal of said catalytically active phase is chromium.

17. A catalyst system according to claim 16, wherein said catalyst has a total ratio by weight of gallium to chromium of between about 1 to about 10.

18. A catalyst system according to claim 16 wherein said catalyst system has a chemical surface composition characterized by atomic ratio as follows: Si/Al = 0.01 - 1.0 Si/Ga = 10 - 250 Si/Cr = 1 - 50 Si/(Ga+Al+Cr+Mo+Co+P) = 0.001 - 5.0

19. A catalyst system according to claim 18, wherein said catalyst system has a particle diameter of between about 0.5 mm to about 3 mm, a surface area of between about 140 m2/g to about 250 m2/g, a pore volume of between about 0.3 cc/g to about 0.9 cc/g, and a pore diameter of between about 60 to about 140 .

20. A catalyst system according to claim 1, wherein said support medium is an MFI zeolite.

21. A catalyst system according to claim 1, wherein said support medium is selected from the group consisting of ZSM-5 zeolite, ZSM-12 zeolite, and mixtures thereof.

22. A catalyst system according to claim 21, wherein said support medium comprises a mixture of ZSM-5 zeolite and ZSM-12 zeolite.

23. A catalyst system according to claim 1, wherein said support medium has an MFI structure characterized by XRD technique as showing lines between 22 and 25 of 2e as main lines.

24. A hydroconversion catalyst system comprising: a catalytically active matrix comprising a first metal selected from group IIIA of the periodic table of elements, a second metal selected from group IIIA, a third metal selected from group VII, a fourth metal selected from group VIB, and a fifth metal selected from group VA; a support medium distributed through the matrix and comprising a silicious molecular sieve material; and a catalytically active phase supported on the support media and comprising a group IIIA metal and a group VIB metal.

25. A catalyst system according to claim 24, wherein said first metal is aluminum, said second metal is gallium, said third metal is selected from the group consisting of cobalt, nickel and mixtures thereof, said fourth metal is selected from the group consisting of molybdenum, chromium and mixtures thereof, and said fifth metal is phosphorus.

26. A catalyst system according to claim 25, wherein said aluminum is in the form of an alumina matrix, and said second, third, fourth and fifth metals are supported by said alumina matrix.

27. A catalyst system according to claim 24, wherein said group IIIA metal of said catalytically active phase is gallium, and said group VIB metal of said catalytically active phase is chromium.

28. A process for preparing a hydroconversion catalyst system, comprising the steps of: providing a support medium comprising a silicious molecular sieve material having a surface area of between about 250 m2/g to about 1200 m2/g and supporting a catalytically active phase comprising a first metal selected from group IIIA of the periodic table of elements and a second metal selected from group VIB of the periodic table of elements; providing a matrix material having a surface area of between about 50 m2/g to about 290 m2/g; mixing said support medium with said matrix to form a substantially homogeneous paste having a ratio by weight of said support medium to said matrix of at least about 0.1;, forming said paste into catalyst elements; and calcining said catalyst elements whereby at least a portion of said first metal of said catalytically active phase migrates from said support medium to said matrix whereby said matrix is catalytically active.

29. A process according to claim 28, wherein said matrix comprises a first metal selected from group IIIA of the periodic table of elements.

30. A process according to claim 29, wherein said matrix further comprises a second metal selected from group VIII, a third metal selected from group VIB and a fourth metal selected from group VA of the periodic table of elements.

31. A process according to claim 30, wherein said first metal is aluminum in the form of alumina, and said matrix is provided by impregnating said alumina with said second, third and fourth metals.

32. A process according to claim 31, wherein said alumina is sequentially impregnated with said second, third and fourth metals.

33. A process according to claim 30, wherein said first metal is aluminum, said second metal is selected from the group consisting of cobalt, nickel, and mixtures thereof, said third metal is selected from the group consisting of molybdenum, chromium and mixtures thereof, and said fourth metal is phosphorus.

34. A process according to claim 33, wherein said second metal is cobalt and said third metal is molybdenum.

35. A process according to claim 34 wherein said support medium is an aluminosilicate, said first metal of said catalytically active phase is gallium, and said second metal of said catalytically active phase is chromium, and wherein said calcining step provides a catalyst having a chemical surface composition characterized by atomic ratio as follows: Si/Al = 0.01 - 2.0 Si/Ga = 10 - 250 Si/Cr = 1 - 50 Si/(Ga+Al+Cr+Mo+Co+P) = 0.001 - 5.0

36. A process according to claim 28, wherein said calcining step provides a catalyst having a surface area of between about 140 m2/g to about 250 m2/g, a pore volume of between about 0.3 cc/g to about 0.9 cc/g and a pore diameter of between about 60 A to about 140 .

37, A process according to claim 28, wherein said calcining step includes calcining said catalyst elements at a temperature of about 6000C for a period of about 6 hours.

38- A process according to claim 28, wherein said calcining step includes a first stage carried out at a temperature of between about 1200C to about 3500C for a period of between about 1 to 6 hours and a second stage carried out at a temperature of between about 3500C to about 7000C for a period of between about 1 to 6 hours.

39 A process according to claim 38, wherein said calcining step is carried out under a flow of air containing water vapor equivalent to about 0.5 kg H20/hour-kg of catalyst.

40. A process according to claim 28, wherein said step of providing said support medium includes providing an aluminosilicate having a ratio by weight of silicon to aluminum of at least about 10, and impregnating said aluminosilicate with said first metal of said catalytically active phase and said second metal of said catalytically active phase.

41. A process according to claim 40, wherein said impregnating step includes impregnating said aluminosilicate with said second metal of said catalytically active phase, drying said aluminosilicate at a temperature of -between about 800C to about 1500C, subsequently impregnating said aluminosilicate with said first metal of said catalytically active phase, and again drying said aluminosilicate at a temperature of between about 800C to about 15O0C.

42. A process according to claim 41, wherein said drying steps are carried out at a temperature of about 1200C.

43. A process according to claim 41, wherein said drying steps are carried out under a flow of air containing water vapor equivalent to about 0.5 kg H2O/hour-kg of catalyst.

44. A hydroconversion catalyst system substantially as described hereinbefore.

45. A process for preparing a hydroconversion catalyst system substantially as described hereinbefore.