Method of preparing catalyst for hydrogenation of hydrocarbon oil

Abstract: Disclosed is a method of preparing a catalyst for hydrogenation of a hydrocarbon oil, in which an aqueous solution containing a metal of the Group VI of the Periodic Table and a metal of the Group VIII of the same along with a hydroxycarboxylic acid and optionally phosphoric acid is added to a carrier substance consisting essentially of at least one of an inorganic oxide and an inorganic hydrate, and the resulting blend is kneaded, shaped and thereafter dried at a temperature not higher than 200°C. The catalyst has a high catalyst activity and is used for hydrogenation of a hydrocarbon oil, especially satisfying the requirement of reducing the sulfur content in a light oil.

Description: The present invention relates to a method of preparing an extremely highly active catalyst for hydrogenation of a hydrocarbon oil. In hydrogenation of a hydrocarbon oil in the presence of hydrogen for hydrogen addition, desulphurization, denitrogenation, decomposition or the like, a hydrogenating catalyst composed of a catalyst carrier of a porous inorganic oxide, such as alumina, titania or silica, and active metal components of the Group VI of the Periodic Table of Mo or W and the Group VIII of the same of Ni or Co, as carried on the carrier, is used. In the hydrogenation catalyst of the type, in general, the above-mentioned active metals as carried on the catalyst carrier are in the form of their oxides. Since such metal oxides are inactive as they are, the catalyst with such metal oxide could not be applied to hydrogenation. Therefore, the metal oxides are necessarily activated by converting them into the corresponding metal sulphides. Under the situation, after the above-mentioned catalyst has been filled in a device for hydrogenation of a hydrocarbon oil, an adequate presulphurization treatment is indispensable in which the catalyst layer in the device is necessarily sulphurized by introducing a hydrocarbon oil containing a sulphurizing agent as dissolved therein therethrough under heat. It is known that the active site of the thus pre-treated catalyst is formed on the surfaces of the resulting active metal sulfides so that the total number of the active sites would increase with increase of the exposed surface area of the active metal sulfides to yield, as a result, a high catalyst activity. Increase of the exposed surface area of the active metal sulfides may be attained by enhanced dispersion of the active metal sulfides as carried on the catalyst carrier or by minimization of the crystal size of the respective active metal sulfides. Method of preparing a catalyst having fine crystals of active metal sulfides as finely dispersed and carried on a carrier have been disclosed. For instance, Japanese Patent Application Laid-Open Nos. 59-102442 and 59-69147 mention a series of a method of preparing a catalyst in which a catalyst carrier such as an alumina is dipped in an aqueous solution of active metals containing a carboxylic acid, such as citric acid or malic acid, as a complexing agent for active metals and thereafter it is fired. EP 0181035(A2) mentions a method of preparing a catalyst in which an organic compound having a nitrogen-containing ligand (e.g., amino group, cyano group) such as nitriloacetic acid, ethylenediaminetetraacetic acid or diethylenetriamine is used as a complexing agent and is added to an aqueous solution of active metals, a catalyst carrier such as an alumina or silica is dipped in the resulting aqueous solution of active metals, and the catalyst composed of active metals as carried on the catalyst carrier is then dried at a temperature of not higher than 200°C without firing. In accordance with the method of adding a carboxylic acid as a complexing agent followed by firing, the carboxylic acid added is effective for elevating the stability of the active metal-dipping solution as it acts as a complexing agent for active metals and additionally the acid is also effective for inhibiting coagulation of active metals. In the method, however, the active metals would finally coagulate because of the final firing step so that the finally obtained catalyst by the method could not have a sufficiently improved catalyst activity. The method is defective in this point. On the other hand, in accordance with the method as disclosed in EP 0181035(A2), since the active metal ions such as Mo or Ni ions are firmly coordinated with the nitrogen-containing compound, such ions are carried on the carrier in the form of a highly dispersed condition. In addition, since the catalyst with the carrier is not calcined but is merely dried at a low temperature of not higher than 200°C, the dispersion of the active metals is finally maintained as it is. Further, since the active metal ions are directly formed into sulfides thereof without forming oxides thereof by pre-sulfurization, the finally obtained hydrogenation catalyst may have an extremely highly dispersed state. Because of the reasons, the catalyst prepared by the method has a higher activity than any other conventional catalysts, but it could not still have a high hydrogenation and desulfurization activity enough to meet the recent demand of reducing the sulfur content in a light oil (precisely, to 0.05 % by weight or less as the sulfur content in a light oil) for solving the problem resulting from the current legal controls on gaseous wastes. Additionally, since the catalyst contains a nitrogen-containing organic compound such as nitriloacetic acid or the like, there is a problem that the organic compound would be decomposed in the pre-sulphurization step to generate a toxic gas such as hydrogen cyanide. The object of the present invention is to provide a method of preparing a highly active catalyst which may satisfy the above-mentioned requirement of reducing the sulphur content in a light oil. The present inventor repeatedly studied for the purpose of solving the above-mentioned problems in the prior arts and of attaining the above-mentioned object and, as a result, has found that the object can be attained by adding a hydroxycarboxylic acid, as a complexing agent, to a catalyst composed of base metals and optionally phosphoric acid as carried on a carried followed by kneading and shaping the resulting carrier blend and drying the shaped carrier at a temperature not higher than 200°C before loading onto a reactor. On the basis of the finding, the inventor has achieved the present invention. Specifically, in accordance with the first embodiment of the present invention, there is provided a method of preparing a catalyst for hydrogenation of a hydrocarbon oil, in which an aqueous solution containing a metal of the Group VI of the Periodic Table and a metal of the Group VIII of the same along with a hydroxycarboxylic acid is added to a carrier substance consisting essentially of at least one of an inorganic oxide and an inorganic hydrate, and the resulting blend is kneaded, shaped and thereafter dried at a temperature not higher than 200°C before loading onto a reactor. In accordance with the second embodiment of the present invention, there is provided a method of preparing a catalyst for hydrogenation of a hydrocarbon oil, in which an aqueous solution containing a metal of the Group VI of the Periodic Table and a metal of the Group VIII of the same along with a hydroxycarboxylic acid and phosphoric acid is added to a carrier substance consisting essentially of at least one of an inorganic acid and an inorganic hydrate, and the resulting blend is kneaded, shaped and thereafter dried at a temperature not higher than 200°C before loading onto a reactor. In the present invention, at least one selected from alumina, silica, titania, zirconia, and their hydrates is used as a catalyst carrier substance in a conventional manner. As the metal of the Group VI of the Periodic Table, at least one of Mo and W is used; and as the metal of the Group VIII of the same, at least one Co and Ni is used. As examples of a hydroxycarboxylic acid usable as a complexing agent in the present invention, there are mentioned, for example, glycolic acid, hydroxypropionic acid, hydroxybutyric acid, hydroxyhexanoic acid, tartaric acid, malic acid, glyceric acid, citric acid, gluconic acid, etc. As phosphoric acid, anyone of orthophosphoric acid, metaphosphoric acid, pyrophosphoric acid, triphosphoric acid and tetraphosphoric acid can be used. A soluble salt of the acid such as nickel phosphate may also be used. The amount of the metal of Mo or W of the Group VI of the Periodic Table to be carried on the carrier is desirably from 5 to 30 % by weight as its oxide. The amount of the metal of Ni or Co of the Group VIII of the same to be carried on the carrier is desirably from 1 to 8 % by weight as its oxide. If the amounts of such active metals to be carried on the carrier are less than those falling within the above-mentioned ranges, a highly active catalyst could not be obtained by the method of the present invention. On the other hand, if they are more than those falling within the above-mentioned ranges, the pores of the carrier would be clogged with the active metals so that internal diffusion of a hydrocarbon oil in the catalyst would be inhibited and the activity of the catalyst would be poor. The amount of the hydroxycarboxylic acid to be added to the catalyst is from 0.3 to 5 molar times of the total molar number of the metals of the Group VI and the Group VIII. If the amount of the acid added is less than 0.3 molar time, it would be insufficient for forming a coordination complex of the active metals so that a highly active catalyst could not be obtained. If, however, the amount of the acid added is more than 5 molar times, the activity of the catalyst would no more increase but a carbonaceous material would rather disadvantageously precipitate to clog the pores of the catalyst. Phosphorus is desired to be in the catalyst in an amount of from 0.1 to 8 % by weight as P₂O₅, whereby the activity of the catalyst is elevated further. The drying temperature of drying the catalyst is not higher than 200°C. This is because, if the temperature is higher than 200°C, the added complexing agent would disadvantageously decompose. In accordance with the method of the present invention, an aqueous solution as obtained by blending the above-mentioned components each in a determined amount is added to the carrier substance and further kneaded and shaped and thereafter dried at a temperature not higher than 200°C before loading onto a reactor. The catalyst of the present invention thus prepared under the above-mentioned conditions is in the form of a coordination compound composed of the active metal ions of Mo, W, Ni, and/or Co ions and the added hydroxycarboxylic acid. The coordination compound is stabilized and carried on the catalyst carrier. Though not clear, the reason why the activity of the catalyst as obtained by the use of a hydroxycarboxylic acid as a complexing agent is much higher than any other conventional catalyst as prepared by the use of a nitrogen-containing compound such as nitriloacetic acid, ethylenediaminetetraacetic acid or diethylenetriamine as a complexing agent could be considered because the decomposition behaviour of the respective complexing agents would have some relation to the dispersibility of active metal sulphides since hydroxycarboxylic acids and nitrogen-containing organic compounds differ from each other in the decomposition behaviours thereof. Next, the present invention will be explained in more detail by way of the following examples, which, however, are not intended to restrict the scope of the present invention. EXAMPLE 1 500 ml of an aqueous solution of active metals, comprising 124 g of molybdenum trioxide, 36 g of cobalt carbonate (Co content: 49 % by weight), 495 g of glyceric acid as a complexing agent, and water, was added to 1000 g of alumina hydrate (water content: 60 % by weight), and kneaded under heat at 80°C. The resulting blend was shaped into a cylinder form having a diameter of 1.6 mm through an extruder. This was then dried at 100°C for 16 hours to obtain a catalyst sample (Catalyst-A). Regarding the active metal contents in Catalyst-A, Mo content therein was 22 % by weight as MoO3, and Co content therein was 4 % by weight as CoO. The amount of the glyceric acid added was 4 molar times of the total molar number of the metal of the Group VI and the metal of the Group VIII. As an activity test of Catalyst-A thus obtained, a Kuwait normal pressure light oil having the following properties was subjected to hydrogenation and desulfurization with Catalyst-A. The reaction was effected under the conditions mentioned below, using a flow reactor system. The dehydrogenation and desulfurization activity of Catalyst-A is represented by a relative value of the reaction rate constant. Precisely, a rate constant of the catalyst sample (Catalyst-A) is calculated out as the desulfurization rate is considered to be proportional to the 1.75th power of the sulfur content in the oil after the treatment, and a relative rate constant of Catalyst-A is obtained on the basis of Catalyst-L (Comparative Example 2 which will be mentioned below) having a standard rate constant of 100. EXAMPLE 2 Catalyst-B was prepared in the same manner as in Example 1, except that 27 g of 85 % phosphoric acid was further added to the aqueous solution of active metals. The activity of Catalyst-B thus prepared was tested in the same manner as in Example 1. Regarding the active metal contents in the catalyst sample, Mo content was 22 % by weight as MoO₃ , Co content was 4 % by weight as CoO and P content was 3 % by weight as P₂O₅. The amount of the glyceric acid added was 4 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample is shown in the Table mentioned below. EXAMPLE 3 400 ml of an aqueous solution of active metals, comprising 124 g of molybdenum trioxide, 36 g of cobalt carbonate (Co content: 49 % by weight), 27 g of 85 % phosphoric acid, 228 g of tartaric acid and water, was added to 1000 g of the above-mentioned alumina hydrate, and kneaded under heat at 80°C. The resulting blend was shaped into a cylinder form having a diameter of 1.6 mm through an extruder. This was then dried at 100°C for 16 hours to obtain a catalyst sample (Catalyst-C). Regarding the active metal contents in Catalyst-C, Mo content therein was 22 % by weight as MoO3, Co content therein was 4 % by weight as CoO and P content therein was 3 % by weight as P₂O₅. The amount of the tartaric acid added was 1.3 molar times of the total molar number of the metal of the Group VI and the metal of the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 4 Catalyst-D was prepared in the same manner as in Example 3, except that 119 g of glycolic acid was used as the complexing agent. Regarding the active metal contents in Catalyst-D thus obtained, Mo content was 22 % by weight as MoO3, Co content was 4 % by weight as CoO, and P content was 3 % by weight as P2O5. The amount of the glycolic acid added was 2.7 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 5 Catalyst-E was prepared in the same manner as in Example 3, except that 212.5 g of citric acid was used as the complexing agent. Regarding the active metal contents in Catalyst-E thus obtained, Mo content was 22 % by weight as MoO3, Co content was 4 % by weight as CoO, and P content was 3 % by weight as P2O5. The amount of the citric acid added was 0.87 molar time of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 6 Catalyst-F was prepared in the same manner as in Example 3, except that 205 g of malic acid was used as the complexing agent. Regarding the active metal contents in Catalyst-F thus obtained, Mo content was 22 % by weight as MoO3, Co content was 4 % by weight as CoO, and P content was 3 % by weight as P2O5. The amount of the malic acid added was 1.3 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 7 Catalyst-G was prepared in the same manner as in Example 3, except that 36 g of nickel carbonate (Ni content: 40 % by weight) was sued in place of cobalt carbonate and that 236 g of glycolic acid was used as the complexing agent. Regarding the active metal contents in Catalyst-G thus obtained, Mo content was 22 % by weight as MoO3, Ni content was 4 % by weight as NiO, and P content was 3 % by weight as P2O5. The amount of the glycolic acid added was 2.7 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 8 Catalyst-H was prepared in the same manner as in Example 7, except that 400 g of titania powder (having a specific surface area of 220 m²/g and a pore capacity of 0.45 ml/g) was used as the catalyst carrier. Regarding the active metal contents in Catalyst-H thus obtained, Mo content was 22 % by weight as MoO3, Ni content was 4 % by weight as NiO, and P content was 3 % by weight as P2O5. The amount of the glycolic acid added was 2.7 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 9 250 ml of an aqueous solution of active metals, comprising 124 g of molybdenum trioxide, 36 g of nickel carbonate (Ni content: 49 % by weight), 238 g of glycolic acid and water, was added to 400 g of γ-alumina powder (having a specific surface area of 280 m²/g and a pore capacity of 0.75 ml/g), and kneaded under heat at 80°C. The resulting blend was shaped into a cylinder form having a diameter of 1.6 mm through an extruder. This was then dried at 100°C for 16 hours to obtain a catalyst sample (Catalyst-I). Regarding the active metal contents in Catalyst-I, Mo content therein was 22 % by weight as MoO3 and Ni content therein was 4 % by weight as NiO. The amount of the glycolic acid added was 2.7 molar times of the total molar number of the metal of the Group VI and the metal of the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. EXAMPLE 10 Catalyst-J was prepared in the same manner as in Example 9, except that 27 g of 85 % phosphoric acid was added to the aqueous solution of active metals. Regarding the active metal contents in Catalyst-J thus obtained, Mo content was 22 % by weight as MoO3, Ni content was 4 % by weight as NiO, and P content was 3 % by weight as P2O5. The amount of the glycolic acid added was 2.7 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. COMPARATIVE EXAMPLE 1 In the same manner as in Example 1, 300 ml of an aqueous solution, comprising 124 g of molybdenum trioxide, 36 g of cobalt carbonate, 27 g of 85 % phosphoric acid, 222 g of EDTA, 5 g of 28 % aqueous ammonia and water, was added to 1000 g of alumina hydrate and kneaded under heat at 80°C. The resulting blend was shaped into a cylindrical form having a diameter of 1.6 mm through an extruder, which was then dried at 100°C for 16 hours to obtain a catalyst sample (Catalyst-K). Regarding the active metal contents in Catalyst-K thus obtained, Mo content was 22 % by weight as MoO3, Co content was 4 % by weight as CoO, and P content was 3 % by weight as P2O5. The amount of EDTA added was 0.6 molar time of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. COMPARATIVE EXAMPLE 2 Catalyst-L was prepared in the same manner as in Comparative Example 1, except that 182 g of ethylenediamine was used in place of EDTA. Regarding the active metal contents in Catalyst-L thus obtained, Mo content was 22 % by weight as MoO3, Co content was 4 % by weight as CoO, and P content was 3 % by weight as P2O5. The amount of the ethylenediamine added was 2.6 molar times of the total molar number of the metals of the Group VI and the Group VIII. The relative rate constant of the catalyst sample, as obtained in the same manner as in Example 1, is shown in the Table mentioned below. In accordance with the present invention, there is provided a method of preparing a catalyst for hydrogenation of a crude hydrocarbon oil, in which a hydroxycarboxylic acid is added a a complexing agent to metals of the Group VI and the Group VIII of the Periodic Table and optionally phosphoric acid is further added thereto, and the resulting blend is kneaded and shaped and then dried at a temperature not higher than 200°C before loading onto a reactor. The catalyst of the invention is usable for high hydrogenation of a hydrocarbon oil for deep desulfurization or denitrogenation of the same. Therefore, the catalyst may sufficiently satisfy the requirement of reducing the sulfur content in a light oil as one advantageous merit. As another merit, the method of the present invention is free from presulfurization of generating any harmful and toxic gas, and the catalyst of the present invention may stably be carried on the carrier.

Claims: A method of preparing a catalyst for hydrogenation of a hydrocarbon oil, in which an aqueous solution containing metals of both Group VI and Group VIII of the Periodic Table along with an hydroxycarboxylic acid is added to a carrier consisting essentially of either or both of an inorganic oxide and an inorganic hydrate, and the resulting blend is kneaded, shaped, characterised in that the resulting blend is dried at a temperature not higher than 200°C before loading onto a reactor. A method of preparing a catalyst for hydrogenation of a hydrocarbon oil, in which an aqueous solution containing metals of both Group VI and Group VIII of the Periodic Table with a hydroxycarboxylic acid and phosphoric acid is added to a carrier consisting essentially either or both of an inorganic oxide and an inorganic hydrate, and the resulting blend is kneaded, shaped and the resulting blend is dried at a temperature not higher than 200°C before loading onto a reactor. The method as claimed in claim 1 or claim 2, in which the metal of Group VI of the Periodic Table is at least one of Mo and W. The method as claimed in any preceding claim, in which the metal of Group VIII of the Periodic Table is at least one of Co and Ni. The method as claimed in any preceding claim 1, in which the hydroxycarboxylic acid is at least one of glycolic acid, hydroxypropionic acid, hydroxybutyric acid, hydroxyhexanoic acid, tartaric acid, malic acid, glyceric acid, citric acid and gluconic acid. The method as claimed in any preceding claim, in which the amount of the metal Group VI is from 5 to 30 by weight as its oxide. The method of preparing a catalyst for hydrogenation of a hydrocarbon oil as claimed in claim 1, in which the amount of the metal of Group VIII is from 1 to 8 % by weight as its oxide. The method of preparing a catalyst for hydrogenation of a hydrocarbon oil as claimed in claim 1, in which the carrier is one or more alumina, silica, titania, zirconia, and hydrates thereof. The method of preparing a catalyst for hydrogenation of a hydrocarbon oil as claimed in claim 2, in which the phosphoric acid is meta-phosphoric acid, pyro-phosphoric acid, ortho-phosphoric acid, tri-phosphoric acid, tetra-phosphoric acid or nickel phosphate. The method of preparing a catalyst for hydrogenation of a hydrocarbon oil as claimed in claim 2 or 9, in which the amount of the phosphoric acid to be in the catalyst is from 0.1 to 8 % by weight as P₂O₅. The method of preparing a catalyst for hydrogenation of a hydrocarbon oil as claimed in claim 2, 9 or 10, in which the catalyst carrier is selected from alumina, silica, titania, zirconia, and their hydrates. A method of hydrogenating a hydrocarbon oil utilising a catalyst prepared in accordance with any preceding claim.

Inventors: KAMO TETSURO, KAMO, TETSURO
Applicants: SUMITOMO METAL MINING CO, SUMITOMO METAL MINING COMPANY LIMITED
Application year: 1991
Main classification: C10G45
IPC codes: B01J31, B01J27, B01J23, B01J37, C10G45, C10G49