Patent Application
20070151902
The present invention relates to processes of desulfurizing heavy oils continuously for a long period of time. More specifically, the present invention relates to a process of desulfurizing a heavy oil such as an atmospheric residual oil continuously for a long period of time, without exchanging a catalyst.
Heavy oils such as atmospheric and vacuum residual oils produced in a petroleum refining process usually contain a few percent by mass of sulfur components and thus can not be put in markets as they are. Therefore, such heavy oils are desulfurized in the presence of high pressured hydrogen using a catalyst so as to lower the sulfur concentration. A substantial part of the reaction product resulting from desulfurization of the heavy oils is further subjected to a secondary treatment to be converted to various useful products such as gasoline, kerosene, and gas oil. The process of desulfurization of heavy oils thus takes an important role in the current petroleum refining (see, for example, Non-Patent Document 1). If the desulfurization operation is ceased, other processes are adversely affected, and in this connection, the whole refinery is adversely affected in terms of economical efficiency. Therefore, how the lifetime of a catalyst is prolonged, i.e., how the operation with a catalyst once charged can be prolonged has been a serious issue in the petroleum refining industry. It is thus necessary to operate a desulfurization unit for heavy oil stably over an extended period of time in order to improve the economical efficiency of petroleum refining.
However, under the current circumstances, the lifetime of a catalyst can not be prolonged sufficiently due to deactivation factors mainly caused by coking on the catalyst and there is thus no other choice than to cease the operation in a relatively short period of time for exchanging the catalyst. The petroleum industry has been vigorously engaged in studies to prolong the lifetime of a desulfurization catalyst so as to enable the desulfurization process of heavy oils to be operated for a long period of time and has vigorously undertaken research and development to improve the catalyst, i.e., to prolong the lifetime thereof by selecting optimum supported metals and catalyst supports (see, for example, Patent Documents 1 and 2 below). However, no satisfactory result has been attained, and a view that it is impossible to prolong the lifetime of the desulfurization catalyst for heavy oil has been dominating in the industry.
The present invention has an object to improve the economic efficiency of petroleum refining by prolonging the lifetime of a catalyst for desulfurization of heavy oils.
As a result of extensive researches and studies, the present invention was achieved by the finding that the lifetime of a desulfurization catalyst was able to be prolonged by a process of desulfurization of a heavy oil, comprising diluting the heavy oil with a dilution medium and then cracking the diluted heavy oil at a low cracking rate.
That is, the present invention relates to a process of desulfurizing a heavy oil, comprising diluting the heavy oil with a dilution medium to 90 percent by mass or less and cracking the diluted heavy oil at a cracking rate of 10 percent or less.
The present invention also relates to a process of desulfurizing a heavy oil, comprising diluting the heavy oil with a dilution medium to 90 percent by mass or less, cracking the diluted heavy oil at a cracking rate of 10 percent or less, and desulfurizing the cracked heavy oil after removal of the dilution medium therefrom.
The present invention will be described in more detail below.
The heavy oil used in the present invention denotes a heavy oil mainly composed of carbon and hydrogen and containing 90 percent by mass or more of a fraction with an initial boiling point of 300° C. or higher and a boiling point of 360° C. or higher.
There is no particular restriction on the type of heavy oil used in the present invention. Typical examples include atmospheric residual oils and vacuum residual oils, produced during a petroleum refining process.
There is no particular restriction on the dilution medium used in the present invention except that it is inactive to the heavy oil to be treated. The dilution medium is preferably compatible with the heavy oil to be treated at a cracking temperature and particularly preferably a dilution medium with a boiling point of 120° C. or higher.
Preferred examples of the dilution medium include aromatic hydrocarbons such as benzene and toluene. The use of the dilution medium can evenly dilute the heavy oil.
In the present invention, the heavy oil is diluted with the diluting medium to 90 percent by mass or less, preferably 85 percent by mass or less, and particular preferably 80 percent by mass of less. If the concentration of the heavy oil is in excess of 90 percent by mass, the effect of prolonging the lifetime of a catalyst can not be obtained sufficiently. There is no particular restriction on the lower limit concentration. However, the concentration is preferably 20 percent by mass or more and more preferably 30 percent by mass or more in view of the process efficiency.
There is no particular restriction on the method of diluting the heavy oil. However, the heavy oil is usually diluted in a mixing bath or through line-mixing. Thereupon, the mixing temperature is preferably 60° C. or higher in order to mix the dilution medium with the heavy oil with a sufficiently lowered viscosity.
Next, the heavy oil diluted to 90 percent by mass or less with the dilution medium is cracked. The cracking is necessarily carried out at a low cracking rate such as 10 percent or lower. The cracking rate used herein denotes the rate (on the basis of mass) of a fraction resulting from the cracking, which is lighter than the feedstock heavy oil (i.e. a fraction with a boiling point lower than the initial boiling point of the feedstock heavy oil but not including the diluting medium), in the produced oil.
In the present invention, the cracking rate is adjusted to 10 percent or lower and more preferably 8 percent or lower. If the cracking rate is higher than 10 percent, the effect of prolonging the lifetime of a catalyst would be insufficient. There is no particular restriction on the lower limit cracking rate. However, the lower limit cracking rate is preferably 1 percent or higher and more preferably 2 percent or higher.
In the present invention, the cracking of the heavy oil is carried out by thermal cracking. The temperature range at which the thermal cracking is carried out is preferably from 400 to 600° C. and more preferably from 420 to 540° C. The LHSV range is from 6 to 20 h-1 and more preferably from 8 to 15 h-1. There is no particular restriction on the pressure. The cracking may be carried out at a pressure ranging from atmospheric pressure to slight pressure but is usually carried out at atmospheric pressure.
As mentioned above, after the diluted heavy oil is cracked at a low cracking rate, the diluted medium is removed from the resulting oil, followed by desulfurization thereof.
There is no particular restriction on the method of removing the dilution medium. However, the dilution medium is removed using atmospheric distillation.
There is no particular restriction on the catalyst or conditions for the desulfurization. There may be used any known catalyst and conditions which are used for a conventional desulfurization reaction of heavy oils. Examples of such a catalyst include those supporting molybdenum or tungsten on alumina. Typical examples of the reaction conditions include a reaction temperature of 380 to 480° C., a reaction pressure of 5 to 20 MPa, and an LHSV of 0.1 to 2.0 h-1.
The desulfurized oil is then subjected to a secondary treatment like as usual. The resulting oil can be used as a base oil for various products such as gasoline, kerosene, gas oil, and heavy fuel oil.
As described above, the deactivation rate of the catalyst can be retarded by cracking a heavy oil diluted with a dilution medium at a low cracking rate and then desulfurizing the cracked oil, thereby making it possible to prolong the lifetime of the catalyst.
The present invention will be described in more details with reference to the following examples but is not limited thereto.
Into a tower for cracking with its inlet temperature kept at 480° C. was fed a vacuum residual oil (initial boiling point: 580° C., sulfur content: 4.3 percent by mass) diluted to 78 percent by mass with benzene at an LHSV of 10 h-1. After the benzene is distilled out, the resulting oil contained 7.7 percent by mass (cracking rate: 7.7 percent) of a cracked product with a boiling point of lower than 580° C. The resulting oil is fed together with hydrogen to a reaction tower charged with a commercially available catalyst for desulfurizing heavy oil. The reaction tower was operated for 30 days under conditions of an LHSV of 0.2 h-1 and a reaction pressure of 15 MPa, controlling the reaction temperature so that the resulting oil after the reaction was reduced in sulfur content to 0.4 percent by mass. The reaction temperature was gradually increased substantially at a constant rate, from 452.0° C. at the time of the initiation of the reaction and was higher by 1.6° C. than the initial reaction temperature when the reaction was completed. The average deactivation rate of the catalyst during the reaction was 0.053° C./day.
The operation same as that of Example 1 was carried out except for omitting the dilution and cracking steps. The reaction temperature was increased by 4.8° C. The average deactivation rate of the catalyst was 0.160° C./day.
The vacuum oil same as that used in Example 1 was cracked at a low cracking rate without using benzene, i.e., without dilution. The resulting oil contained 9.7 percent by mass of a cracked product. The resulting oil was desulfurized similarly to Example 1. The reaction temperature was increased by 3.5° C. for 30 days. The average deactivation rate of the catalyst was 0.117° C./day.
The cracking of Example 1 was carried out except that the LHSV was changed to 5 h-1. The resulting oil contained 14.7 percent by mass of a cracked product. The resulting oil was desulfurized similarly to Example 1. The reaction temperature was increased by 4.6° C. for 30 days. The average deactivation rate of the catalyst was 0.1 53° C./day.
The cracking operation same as that of Example 1 was carried out except that toluene was used instead of benzene. The resulting oil contained 8.7 percent by mass of a cracked product. The resulting oil was desulfurized similarly to Example 1. The reaction temperature was increased by 1.9° C. for 30 days. The average deactivation rate of the catalyst was 0.063° C./day.
It will be appreciated by those skilled in the art that changes could be made to the embodiments described above without departing from the broad inventive concept thereof. It is understood, therefore, that this invention is not limited to the particular embodiments disclosed, but it is intended to cover modifications within the spirit and scope of the present invention as defined by the appended claims.
| Number | Date | Country | Kind |
|---|---|---|---|
| 2004-258719 | Sep 2004 | JP | national |
This application is a Continuation of International Application No. PCT/JP2005/016572, filed Sep. 2, 2005, which was published in the Japanese language on Mar. 16, 2006, under International Publication No. WO 2006/028196 A1 and the disclosure of which is incorporated herein by reference.
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/JP05/16572 | Sep 2005 | US |
| Child | 11681991 | Mar 2007 | US |
