HYDROCRACKING CATALYST COMPRISING A BETA ZEOLITE (*BEA) FRAMEWORK SUBSTITUTED WITH Ti AND Zr AND METHODS FOR ITS PREPARATION AND USE

Abstract

The invention relates to methods for hydrocracking or hydrotreating hydrocarbon containing feedstocks. This is accomplished via the use of a catalyst which comprises a β zeolite of *BEA framework, where a portion of aluminum atoms in the *BEA framework have been substituted by from 0.1-5.0 wt % of each of Ti and Zr, calculated on an oxide basis.

Claims

1. A method for hydrocracking or hydrotreating a hydrocarbon containing feedstock, comprising contacting said feedstock with (i) a catalyst, said catalyst comprising an active phase metal and a β zeolite of *BEA framework, wherein a portion of aluminum atoms in said *BEA framework have been substituted by from 0.1 to 5.0 wt % of Ti atoms and from 0.1 to 5.0 wt % Zr atoms, said wt % being calculated on an oxide basis, and (ii) hydrogen, to hydrocrack or hydrotreat said feedstock.

2. The method of claim 1, wherein said catalyst further comprises from 0.1 to 5.0 wt % of Hf atoms calculated in an oxide basis.

3. The method of claim 1, wherein said catalyst wherein said β zeolite has the following characteristics: (a) a crystal lattice constant of a=1,260 to 1.270 nm, b=1.260 to 1,270 nm, and c=2.6200 to 2.6500 nm. (b) a specific surface area of 400 to 800 m.sup.2/g, and (c) a molar ratio of SiO.sub.2 to Al2O.sub.3 of 10 to 200.

4. The method of claim 1, wherein said zeolite containing catalyst support has a specific surface area of 15 to 500 m.sup.2/g; a volume of pores having a diameter of 600 A or in the range of 0.40 to 0.75 ml/g; and an amount of an active phase metal component ranging from 0.01 to 40 mass %.

5. The method of claim 1, further comprising: filling a reactor vessel which is a flow reactor with the hydrocracking catalyst; and treating a feedstock having a boiling point of 300° C., to 833° C. in the presence of hydrogen at a reactor temperature of 300° C. to 450° C., a hydrogen pressure of 4 to 30 MPa, a liquid hourly space velocity (LHSV) of 0.1 to 10 h.sup.−1, and a hydrogen/oil ratio of 500 to 2500 Nm.sup.3/m.sup.3.

6. The method of claim 5, wherein the flow reactor is a flow reactor selected from the group consisting of a stirred tank, an ebullient bed reactor, a baffled slurry tank, a fixed bed reactor, a rotating tubular reactor and a slurry-bed reactor.

7. The method of claim 5, wherein the hydrocarbon oil comprises refined oil obtained from (1) crude oil, (2) synthetic crude oil, (3) bitumen, (4) oil sand, (5) shale oil or (6) coal oil.

8. The method of claim 5, wherein the hydrocarbon oil comprises refined oil obtained from crude oil, synthetic crude oil, bitumen, oil sand, shale oil or coal oil, and said refined oil is a) vacuum gas oil (VGO), b) deasphalted oil (DAO) obtained from a solvent deasphalting process or demetallized oil, c) light coker gas oil or heavy coker gas oil obtained from a coker process, d) cycle oil obtained from a fluid catalytic cracking (FCC) process or e) gas oil obtained from a visbraking process.

9. The method of claim 1, further comprising: filling a hydrotreating apparatus which is a flow reactor with the hydrocracking catalyst; and treating a feedstock having a boiling point of 375° C. to 650° C. in the presence of hydrogen at a reactor temperature of 330° C. to 450° C., a hydrogen pressure of 7 to 15 MPa, a liquid hourly space velocity (LHSV) of 0.2 to 1.5h.sup.−1, and a hydrogen/oil ratio of 1000 to 2000 Nm.sup.3/m.sup.3 to yield a middle distillate.

10. The method of claim 1, wherein said β zeolite contains from 0.1-2.0 mass % of each of Ti and Zr, on an oxide basis.

11. The method of claim 2, wherein said zeolite contains from 0.1-2.0 mass % Hf, on an oxide basis.

12. The method of claim 1, wherein said catalyst is on an inorganic support,

13. The method of claim 12, wherein said inorganic support comprises at least one of alumina and. silica.

14. The method of claim 1, wherein said β zeolite has a molar ratio of SiO.sub.2 to Al.sub.2O.sub.3 of 10 to 100.

15. The method of claim 14, wherein said molar ratio is 30 to 70,

16. The method of claim 3, wherein said surface area is 500-700 m.sup.2/g.

17. The method of claim 12, wherein said catalyst has a specific surface area of 150-500 m.sup.2/g,

18. The method of claim 17, wherein said specific surface area is 150-450 m.sup.2/g.

19. The method of claim 1, wherein said active metal phase component comprises from 0.01-40 mass % of said catalyst calculated on an oxide basis.

20. The method of claim 19, wherein said active metal phase comprises 10-35 mass % of said catalyst, calculated on an oxide basis.

21. The method of claim 1, wherein said active metal phase metals comprises Fe, Co, Ni, Rh, Pd, Ag, In, Pt, Au, Cr, Mo, or W.

22. The method of claim 1, wherein said zeolite comprises from 1-80 mass % of said catalyst.

23. The method of claim 22, wherein said zeolite comprises from 5-50 mass % of said catalyst.

Description

BRIEF DESCRIPTION OF THE FIGURES

[0013] FIG. 1 presents XRD data to show structural integrity of the catalists of the invention.

[0014] FIG. 2 depicts UV-Vis spectra for the base zeolite and the final catalyst of the invention.

[0015] FIG. 3 shows, graphically, differences in total acidity and acidity strength between USY based catalysts, and the *BEA catalysts of the invention.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

[0016] The invention is a method for hydrocracking a petroleum based, hydrocarbon feedstock under hydrocracking conditions with a catalyst, said catalyst comprising an active phase metal compound carried on a support which comprises a beta zeolite having a *BEA framework, wherein a portion of aluminum atoms in said framework have been substituted/replaced by from 0.1-5 wt % of each of Ti and Zr, wherein the weights are calculated on an oxide basis. Optionally, 0.1-5 wt % of Hf can be used to substitute Al as well. Active phase metal comprises one or more of Fe, Co, Ni, Rh, Pd, Ag, In, Pt, Au, Cr, Mo, or W. In some embodiments, the amount of Ti and Zr is 0.1-2.0 mass % on an oxide basis. In further embodiments, the amount of Hf present is from 0.1-2.0 mass % on an oxide basis.

[0017] The modified beta zeolite framework containing Ti and Zr atoms of the invention preferably possesses one or more, and most preferably all, of the following characteristics: [0018] (a) a crystal lattice constant of a=1.260 to 1.270 nm, h=1,260 to 1.270 mu, and c=26,200 to 26.500 nm; [0019] (b) a specific surface area of 400 to 800 m.sup.2/g, preferably 500-700 m.sup.2.g, and [0020] (c) a molar ratio of 10 to 200 (preferably 10-100, and more preferably, 30-70) in terms of SiO.sub.2 to Al.sub.2O.sub.3.

[0021] The “specific surface area” referred to supra relates to the modified zeolite itself, as do all of the other properties listed. The zeolite containing catalyst support has a specific surface area of 15-500 m.sup.2/g, and more preferably 150-450 m.sup.2/g.

[0022] In the hydrocracking catalyst for hydrocarbon oil according to the present invention, a specific surface area thereof which falls preferably in a range of 15-500 m.sup.2/g, preferably 150 to 400 m.sup.2/g; a volume of pores having a diameter of 600 Å or less, which falls preferably in a range of 0,40 to 0.75 ml/g; and an amount of the active phase metal component in a range of 0.01 to 40% by mass, preferably from 10-35 mass % on an oxide basis. The amount of TiZr beta zeolite in the catalyst ranges from 1-80 wt % of the catalyst weight, and preferably 5-50 wt %. In some embodiments, the catalyst is on an inorganic support, preferably one which contains alumina and silica.

[0023] The method for producing the hydrocracking catalyst of the invention comprises substituting a part of aluminum atoms of the Beta zeolite with *BEA framework with zirconium atoms and titanium atoms, followed by firing the zeolite at a temperature of from 55-700° C. The Beta zeolite with *BEA framework with zirconium and titanium atoms of the invention has a. crystal lattice constant falling in a range of a=1.260 to 1,270 nm, b=1.260 to 1.270 nm, and c=2.6.200 to 26,500 nm, a specific surface area of 400 to 800 m.sup.2/g and a molar ratio of SiO.sub.2 to Al.sub.2O.sub.3 of 10 to 200, preferably 10-100, and more preferably 30-70, preparing a suspension having a mass ratio of 5 to 15 in terms of liquid/solid from the above fired zeolite, adding an inorganic acid or an organic acid thereto so that a pH of the above suspension is less than 2.0, subsequently adding a zirconium compound and/or a titanium compound and mixing them and then neutralizing the suspension.

[0024] In another method for producing a hydrocracking catalyst of the invention, a zeolite as described supra, is used to prepare a suspension having a mass ratio of 5 to 15 in terms of liquid/solid zeolite, adding an inorganic acid or an organic acid thereto so that the pH of the suspension is less than 2.0, adding a zirconium compound and titanium compound, mixing, and then neutralizing the mixed solution to secure the catalyst.

[0025] A third aspect of the present invention is a method for hydrocracking a petroleum based hydrocarbon feedstock, such as hydrocarbon oil with the hydrocracking catalyst described above, in the presence of hydrogen and appropriate reaction conditions.

[0026] Preferably, the method for hydrocracking a petroleum based hydrocarbon feedstock according to the invention comprise placing a reactor vessel of a hydrocracking apparatus which is a flow reactor with the catalyst of the invention., and treating the feedstock having a boiling point of 300° C. to 833° C. in the presence of hydrogen at a reactor temperature of 300° C. to 450° C., a hydrogen pressure of 4 to 30 MPa, a liquid hourly space velocity (LHSV) of 0.1 to 10 h and a Hydrogen/oil ratio of 500 to 2500 Nm.sup.3/m.sup.3.

[0027] Preferably, the method for hydrocracking hydrocarbon oil according to the invention involves treating a feedstock with a boiling point of 375-650° C. with the catalyst, and in the presence of hydrogen at a reactor temperature of 330° C. to 450″ C., a hydrogen pressure of 7 to 15 MPa, a liquid hourly space velocity (LHSV) of 0.2 to 1.5 h.sup.−1, and a hydrogen/oil ratio of 1000 to 2000 Nm.sup.3/m.sup.3 to yield a middle distillate. Preferably this middle distillate is rich in kerosene and gas oil.

[0028] In the method for hydrocracking hydrocarbon oil according to the present invention, the flow reactor described above is preferably a flow reactor selected from the group consisting of a stirring bath type reactor, a. boiling bed type reactor, a baffle-equipped slurry bath type reactor, a fixed bed type reactor, a rotary tube type reactor and a slurry bed type reactor.

[0029] In the method for hydrocracking a petroleum feedstock according to the invention, the hydrocarbon feedstock described above preferably contains refined oil obtained from (1) crude oil, (2) synthetic crude oil, (3) bitumen, (4) oil sand, (5) shell oil or (6) coal liquid.

[0030] In the method for hydrocracking hydrocarbon oil according to the present invention, the hydrocarbon oil described above contains refined oil obtained from crude oil, synthetic crude oil, bitumen, oil sand, shell oil or coal liquid, and the above refined oil is preferably any of a) vacuum gas oil (VGO), b) deasphalted oil (DAO) obtained from a solvent deasphalting process or demetalized oil, c) light coker gas oil or heavy coker gas oil obtained. from a coker process, d) cycle oil obtained from a fluid catalytic cracking (FCC) process or e) gas oil obtained from a visbraking process.

[0031] The hydrocracking catalyst for hydrocarbon oil according to the present invention comprises a hydrogenative metal component carried on a support containing a Beta zeolite of *BEA type, which a part of aluminum atoms constituting the framework thereof is substituted with zirconium atoms and titanium ions.

[0032] Accordingly, the hydrocracking catalyst of the present invention makes it easy to diffuse heavy hydrocarbons such as VGO, DAO and the like into mesopores thereof as compared with conventional hydrocracking catalysts.

[0033] FIG. 3 shows the results of tests to determine the acidity of catalysts of the invention and the prior art.

EXAMPLE 1

[0034] A beta zeolite of *BEA framework, having a silica/alumina ratio (“SAR” hereafter) of 28.5 was used. A total of 51.4 g of this zeolite was suspended in 450 g of deionized water, and heated to 40° C. A total of 14.8 g of H.sub.2SO.sub.4 (25 wt %) was added, together with 10.0 g of an aqueous solution of titanium sulfate (equivalent to 5 wt % TiO.sub.2). The solution contained 8.48 g deionized water and 1.52 g titanium sulfate (equivalent to 33 wt % TiO.sub.2). An additional. aqueous zirconium sulfate solution (2.8 g, constituting 18 wt % ZrO.sub.2) was added, and the mixture was stirred for 4 hours, then filtered and washed with 1.5 liters of deionized water. This took place at 60° C. The resulting zeolite was dried at 110° C. to yield a framework substituted, Ti/Zr beta zeolite.

[0035] The XRD data for the *BEA zeolite before framework substitution, and after, are shown in FIG. 1. It can be seen that the structural integrity of the zeolite remained.

EXAMPLE 2

[0036] The *BEA zeolite and framework substituted *BEA zeolite were analyzed, and the results follow in Table 1.

TABLE-US-00001 TABLE 1 Compositional analysis of zeolite Beta before and after Ti/Zr treatment. SiO.sub.3/Al.sub.2O.sub.3 ratio TiO.sub.2 ZrO.sub.2 Surface Area Zeolite mol/mol % % m.sup.2/g β-Zeolite 28.5 — — 623 β-Zeolite + Ti/Zr 53.5 0.84 0.31 614

[0037] Additional data are shown in FIG. 2, which presents UV-Vis spectra of the original β zeolite, and the framework substituted β zeolite. One sees a Ti 4-coordinated species and a wavelength of about 250 nm. If 6-coordinated species were present, one would expect a shift to a higher wavelength, at about 285 nm, This did not occur, as shown by FIG. 2.

EXAMPLE 3

[0038] Experiments were carried out to determine what impact substitution of alumina framework by Ti and Zr would have on the acidity of the zeolite.

[0039] Both USY and *BEA zeolites were tested for acidity, unmodified, and modified by substitution of Ti & Zr.

[0040] FIG. 3 presents these results where total acidity is shown by the height of the bars, while the horizontal bars show weak (100-200° C.), medium (200-400° C.), and strong (400-500° C.) acid site content.

[0041] Other features of the invention will be clear to the skilled artisan and need not be reiterated here.

[0042] The terms and expression which have been employed are used as terms of description and not of limitation, and there is no intention in the use of such terms and expression of excluding any equivalents of the features shown and described or portions thereof, it being recognized that various modifications are possible within the scope of the invention.