Patent Application
20100304963
The present invention relates to a catalyst developed for hydroprocessing of heavy oil and residue, and particularly relates to a catalyst used in a hydrodemetallization step of a multistage process for hydroconversion of heavy crude oils and residue.
The catalysts synthesized in a present invention considerably improve the hydrodemetallization activity and are not deactivated quickly by the contaminants, particularly metals such as nickel and vanadium (Ni or and V) that are present in heavy crude oil feedstock. This process not only removes the adverse impurities such as metals, sulfur, nitrogen, etc, but also can crack heavy fraction into high value components with low boiling point.
The heavy crude oil contains a substantial proportion of asphaltenes and other hydrocarbons which are associated with large amount of sulfur, nitrogen and metals. In past times, these heavy fractions were usually found to be applicable in paving materials and converted to the valuable product using thermal processes. Today, due to the cost and enormous demands for petroleum, these fractions require to be processed to form more valuable products, which are relatively low sulfur and lower boiling hydrocarbon that can be used as clean fuels. It is known in the art that this reduction in metal, sulfur and conversion to lower boiling hydrocarbons can be carried out with hydrogen and a solid catalyst at elevated temperatures and pressure. There are few previous arts, which report the catalysts close to the present invention.
The patent WO 0,253,286 claims a hydroprocessing catalyst for the conversion of the heavy oil hydrocarbons, which contains a transition metal of group VI in a concentration of 7 to 20 weight % and a metal of group VIII in a concentration of 0.5-6 weight % in a calcined catalyst, which correspond to oxide composition over a support of alumina. The invention also claims a process for the hydroprocessing of heavy hydrocarbon feedstock with the catalyst of the invention in fixed or ebullated bed.
U.S. Pat. No. 4,225,421 discloses a process for hydrodemetallation and hydrodesulfurization of hydrocarbon feedstocks containing asphaltenes and metals by contacting the feedstock with hydrogen and a bimodal catalyst consisting essentially of a Group VIB hydrogenation metal on a support comprising alumina wherein said catalyst has a surface area of about 140-300 m2/g and a total pore volume of about 0.4-1.0 cc/g. Out of that total pore volume, 0.06-0.3 cc/g can be in pores having a radius greater than 60 nm. U.S. Pat. No. 4,746,419 discloses a bimodal catalyst characterized by a surface area of 75-400 m2/g and a total pore volume of 0.5-1.5 cc/g. Out of that total pore volume, 0.2-0.3 cc/g are in pores greater than 60 nm radius and not more than 0.15 cc/g in pores greater than 200 nm radius. Although U.S. Pat. Nos. 4,225,421 and 4,746,419 disclose that high surface area, bimodal catalyst are desirable for hydroprocessing heavy hydrocarbon feedstocks, these patents fail to understand that the manner in which the pore volume is distributed throughout the range of pores that are less than 60 nm radius can make a difference in catalyst performance.
U.S. Pat. No. 5,545,602 claims a catalyst with a composition containing very high amount of group VIII and group VIB metals along with phosphorus oxide, with a surface area of 150-240 m2/g, total pore volume of 0.7-0.98 cm3/g, and a pore volume distribution where less than 20% corresponds to the micro-pore zone with diameter of 10 nm, around 34-74 corresponds to pores within the 10-20 nm interval, from 26-46% corresponds to the region of meso-pores with pore diameter of 20 nm, 22-32% with pore diameters of 25 nm, and the macro-pore region with diameters of 100 nm contributes with 14-22%. This patent mainly claims the process for residua feedstock having 4-6° API gravity.
U.S. Pat. No. 6,218,333 discloses a detailed method for the preparation of a catalyst by means of a porous support (alumina, silica-alumina, silica, titanium, boron, zeolites, zirconium, magnesium and their combinations) with one or more active metals (Mo, W, Co, Ni and their oxides, sulfides and mixtures of them). The aim of this patent is to find out the proper method of activation before catalytic activities.
U.S. Pat. No. 4,687,757 claims an alumina support which can contain compounds of transition metals titanium and one of molybdenum having a surface area in the 100-250 m2/g interval, while they are neither claiming the interval of pore volume nor the average pore diameter, both of which are very important properties particularly when the hydrotreating feedstock are residues and/or heavy crude oils. In the detailed description of the patent they reveal a volume of pore of 0.2-2.0 cm3/g, which was determined in mercury penetration equipment. From these data it is evident that the catalyst of the referred patent is used mainly in the hydrodemetallization stage, which contains titania in the support.
On the other hand, in present invention to balance catalyst textural properties to provide a catalyst that admits a maximum amount of treatable hydrocarbons into the pores of the catalyst while at the same time providing access to a maximum number of active catalytic sites on the surface as well as in-side the pores without diffusion limitations.
In addition, the present inventions provide a catalyst affording higher conversion of heavy hydrocarbon feedstocks along with sufficient stability with time on stream. Thus, a catalyst development is appreciated that is economically attractive to maximize the balance of catalyst life and activity of hydroprocessing. This entity is accomplished herein by variation support composition (different alumina) or different pore diameter of the catalyst.
The above representative patents examples disclosed the catalyst formulations and other catalyst useful components along with their entirety of process conditions. All of them are with the alumina catalysts of the present invention.
The performance of heavy oil hydroprocessing catalysts is often affected by pore diffusion limitations generated due to the carbon and metal deposition. The variation of support composition is a way to find out the optimum pore diameter of the catalyst. The reason behind the optimum pore diameter is to obtain more selective activity, which depends on the active metal dispersion as well as pore diameter of the catalysts. However, heavy oils fraction contains high amounts of sulfur and other contaminants that exhibit different reactivity during hydroprocessing, and depending on their complexity, can affect the course of reactions differently; to the point that they can even deactivate the catalyst at a very fast rate. Therefore, before hydroprocessing heavy oil, there are two main concerns that need to be considered: i) environmental specification, and ii) product selectivity. The later case involves the different functionalities of the hydrotreating catalyst, i.e., hydrogenolysis, hydrogenation and hydrocracking, which have an impact on the final product quality depending on both feed and catalyst compositions. Thus, to satisfy both concerns, upgrading of heavy oil is mandatory. Alternatively, refiners are facing a dilemma in trying to keep oil prices more or less steady in spite of treating the crude with more expensive processing methods.
To solve the aforesaid problems existing in the prior art, an object of the present invention is to provide a catalyst for hydroconvertion of a heavy hydrocarbon feedstock.
Another objective of present investigation is to obtained a catalyst that has a high metal retention capacity during the operation of heavy oil and residues, thereby prolonging the operation lifetime of the hydroprocessing units as well as protect subsequent process catalysts in a multi-reactor system.
An additional objective of the present invention is to develop an HDM catalyst located in the front reactor; to remove metals; and to protect high activity downstream HDS, hydrogenation, and HDN catalysts, which are loaded in subsequent reactors of a multi reactor system.
Therefore, the design of pore structure of catalysts should handle complex metal compounds of large molecular size. In general the HDM catalyst (first reactor) is designed with high porosity and low surface area, while the subsequent catalysts are characterized by higher surface area and moderate pore size distribution. Apart from this, the large pore catalysts enhance diffusion of asphaltene into the interior surface of the catalyst.
The detail of the above said objectives of present invention is given in the following sections.
The manner in which the foregoing and other objects are achieved in accordance with the present invention will be better understood in view of the following detailed description and accompanying drawings, which form a part of this specification, and wherein:
The catalyst is adopted for fixed bed hydroprocessing units. The invention is characterized for having a large pore diameter catalyst principally for hydrodemetallization of heavy oil and residue in a first reactor of a multi-reactor process. The catalyst has high demetallizing activity and high metal deposition capacity which results in good stability with time on stream (TOS). The hydrorefining catalyst is obtained by kneading a porous starting powder principally composed of gamma-alumina and having a pore capacity of 0.3-0.6 ml/g or larger and a mean pore diameter of 10 to 26 nm, extrudating and calcining, and after that supported with active metals component of elements belonging to groups VIIIB and VIB of the periodic table.
Our invention is entitled “Catalyst for a first-step hydrodemetallization in a multi-reactor hydroprocessing system for upgrading of heavy and extra-heavy crude oils” for improved textural properties of catalysts and their evaluation, the step wise drawing shows the detail preparation method of catalyst.
The preparation of support and catalysts are depicted in the
Required quantity of aluminum oxyhydroxide (boehmite) is first dried at 120° C. for 5 h (A). The following steps are dry mixing of different boehmite (B), and mixing continuously with 3.5% (volume/volume) of HNO3 and distilled H2O(C). The mixture is then added to the mixer slowly with continuous mixing with the amount of deionized water necessary to obtain an homogeneous paste adequate to be extruded (D). The extrudates obtained with the paste are maintained at 20-25° C. during 12-18 h, then they are dried at 100-120° C. during 2-6 h, and calcined at 500-600° C. during 3-5 h, using a heating ramp of 2° C./min to obtain gamma alumina (E). The calcined support was impregnated with the active metal in a sequential impregnation method (F) using typical group IV metal in first step and second step group VIIIB as promoters. The catalysts were dried at room temperature, 120° C. for 12 h, and finally calcined at 450° C. for 4 hours (G). The catalysts prepared with this method with variation of support composition and their physico-chemical properties are those presented in Table 1.
The reactor was operated in a fixed bed mode using up-flow and down flow modes.
The selected conditions for the evaluation of catalysts at micro plant and bench scale are those presented in Table 3. At bench scale level the operating conditions for evaluation of the catalysts are more severe than at micro-plant level, the run time was increased to 1000 h and the amounts of catalyst and inert material were 100 and 50 mL respectively.
The following examples are provided to illustrate the behavior of the catalyst of the present invention and its use in hydroprocessing of heavy crude oil and residua. These examples should not be considered as limitations of the invention, but should merely teach how to make the appropriate support, catalyst and their evaluation, reflecting the present invention. The reactor had a fixed bed of a particulate supported transitions metal hydroprocessing catalyst. The reactor was run at a total pressure of 5.4-7 MPa. The liquid weight throughput based on catalyst volume was 1 h−1, and the hydrogen throughput was equivalent to 891 m3/m3.
A support hydroprocessing catalyst containing the reference aluminas from Table 1 was prepared per following procedure. The dried 50 parts of catapal C1 alumina (Catapal C1 from Condea) and 50 parts pseudoboehmite alumina (Catapal 200 from Condea) were well mixed in equal proportion considering 25% moisture in both samples. To the mix, diluted HNO3 acid and sufficient amount of de-ionized water were added to form an extrudable paste (3-5 wt % HNO3 to the total powders). These weights are on 100% solids basis. The paste was extruded in 1/16″ cylinder, and dried at 100-120° C. overnight. The dried extrudates were calcined at 500-550° C. for 4 hour with purging excess dry air to obtain a gamma alumina support, and cooled down to room temperature.
Impregnation of Co and Mo was done using a solution containing ammonium heptamolybdate and cobalt nitrate to the target metal loadings of 2.2 wt % CoO and 10 wt % MoO3 in the finished catalyst. The total volume of the solution matched the 100% water pore volume of the base extrudate sample (incipient wetness method). The metal solution was added to the support extrudates gradually while tumbling the extrudates. When the solution addition was complete, the soaked extrudates were aged for over night. Then the extrudates were dried at 120° C. for 12 h. The dried extrudates were calcined at 450° C. for 4 hour with purging excess dry air, and cooled down to room temperature. This catalyst is named Catalyst 1 (Cat-1) and its physical properties are summarized in Table 1 where it is observed that catalyst contains mesoporous.
The catalyst of the present invention was loaded to a reactor and used as first-stage hydrodemetallization catalyst. The run was carried out in a bench-scale test unit having automatic controls for pressure, flow of reactants, and temperature. The reactor specifications are reported in the Table 3. During the reaction the reactor temperatures were controlled at different height of reactor through outside as well as inside thermo-well extended up through the center of the reactor. The hydrocarbon feedstock was fed to the unit by means of a LDC pump, a positive-displacement pump. The activity products of the run were obtained from the product receiver and were analyzed for relevant analysis. Catalyst activities for HDS, HDN, HDM and HDAs are shown in
Catalyst 2, a CoMo catalyst containing alumina of the invention, was prepared using a procedure similar to Catalyst 1. For Catalyst 2, catapal 200 alumina of the invention from Example 1 was used to prepare the base extrudates. This catalyst is named Catalyst 2 (Cat-2) and its physical properties are summarized in Table 1. The texturales property of the catalyst (Cat-2) is shown in Table 1 where it is observed that catalyst contains mesoporous.
Catalyst activities for HDS, HDM and HDAs were slightly higher than HDN. These activities were decreased with time-on-stream almost at similar magnitude as shown in
Catalyst 3, a CoMo catalyst containing alumina of the invention, was prepared using a procedure similar to Catalyst 1. For Catalyst 3, 50 parts alumina (Pural SB, from Condea) of the invention from example 1 and 50 parts pural TH alumina (Pural TH 100, from Sasol) were used to prepare the base extrudates. This catalyst is named Catalyst 3 (Cat-3) and its physical properties are summarized in Table 1. The texturales property of the catalyst (Cat-2) is shown in Table 1 where it is observed that catalyst contains mesoporous.
The catalyst showed almost similar activity for HDS, HDM and HDAs. These activities were decreased with time-on-stream almost at similar magnitude as shown in
The catalysts activities were compared for three different catalysts after 120 h time-on-stream as shown in
Based on the balanced HDS and HDM activities results obtained in the evaluation of catalyst (Cat-1) at micro-plant scale after 120 hours of time-on-stream, this catalyst was evaluated at bench scale during 1000 h of time-on-stream. The reaction conditions were mentioned previously (Table 3). The behavior of Cat-1 at bench scale is presented in
The experiment of Example I is repeated with two changes. As base feedstock is used a pure Maya crude having a sulfur content of 3.52%, a metals content of 322 ppm and a gravity of about 21.3. Results illustrating the effectiveness of the invention similar to those of Example I would be observed.
Apart from the above conversion the hydrotreated product oil improved API gravity by 6-8 degree along with low metal and sulfur content. Such kind of feedstock can be directly used for hydrocracking or fluid catalytic cracking. During the HDM, catalyst retains Ni and V sulfides as shown in
It has been described above that the present invention has its novelty and therefore, the following claims have been proposed.
| Number | Date | Country | Kind |
|---|---|---|---|
| MX/A/2007/009504 | Aug 2007 | MX | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/MX2008/000064 | 5/26/2008 | WO | 00 | 3/23/2010 |
