JP2007270060A - Method for hydrogenating wax - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for hydrogenating wax, which improves catalytic activity deteriorating with time and obtains a fuel base having a sufficiently reduced normal paraffin content is obtained in hydrocracking FT wax for a long period of time. <P>SOLUTION: The method for hydrogenating wax comprises a process for using wax obtained by an FT synthesis as a raw material and hydrocracking the wax in the presence of hydrogen and a catalyst obtained by supporting a metal of the group VIII of the periodic table on a zeolite-containing carrier, a process for temporarily changing the raw material from the wax to a distillate obtained by distilling a mixture of the hydrocracked product of the wax obtained by the first process and the hydrocracked product of a middle distillate formed by the FT synthesis and hydrocracking the distillate in the presence of hydrogen at 160-330°C reaction temperature and a process for changing the raw material from the distillate to the wax and hydrocracking the wax in the presence of hydrogen. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a method for hydrotreating wax.

  In recent years, the regulation of sulfur content in liquid fuels such as gasoline and light oil has become stricter from the standpoint of environmental protection. For this reason, the expectation for the clean liquid fuel with low content of sulfur content and aromatic hydrocarbon is increasing. One of the methods for producing such clean fuel is a Fischer-Tropsch (FT) synthesis method using carbon monoxide and hydrogen obtained from gasification of coal or asphalt or reforming of natural gas as raw materials. .

  The fuel base material obtained by the FT synthesis method is composed of normal paraffin as a main component and contains a part of oxygen-containing compounds, so that it is difficult to use as fuel as it is. Isomerization from normal paraffin to isoparaffin is performed. In the FT synthesis method, a heavy wax fraction (FT wax) is also produced at the same time, and this FT wax is converted into an intermediate fraction (kerosene or light oil base material) rich in isoparaffin by hydrocracking. Is common.

  When a middle distillate produced by hydrocracking or FT synthesis of FT wax is used as a fuel substrate, a high yield is important from the viewpoint of economics of the process, but from the viewpoint of fuel properties, It is desirable that the normal paraffin content is low and the isoparaffin content is high. For example, in light oil, when normal paraffin content increases, low-temperature fluidity | liquidity will deteriorate, and the use as goods is restricted in the worst case. Since most of the light oil produced by FT synthesis is normal paraffin, it is difficult to use it as it is.

A technique for producing a fuel base material by hydrocracking FT wax has been studied so far. For example, hydrocracking methods using FT wax as a raw material are described in Patent Documents 1 to 3 below. ing.
International Publication No. 2004/028688 Pamphlet Japanese Patent Laid-Open No. 2004-255241 JP 2004-255242 A

  However, in the wax hydrocracking method described in Patent Documents 1 to 3, when the wax hydrocracking is performed for a long period of time, the catalytic activity of the catalyst deteriorates with time, and the fuel base material obtained There arises a problem that the normal paraffin content of the resin increases.

  Conventionally, the development of a high-performance wax hydrocracking catalyst has been centered, and there are no reports on improving the activity of the catalyst during operation, that is, extending the catalyst life. A typical method for producing middle distillate in the field of oil refining is hydrocracking vacuum gas oil, and low sulfur gas oil can be produced from this process. In this process, when the deterioration of the catalyst is greater than expected, it is common to take measures such as reducing the amount of raw material supply or reducing the decomposition rate in order to operate for a predetermined period. However, such treatment is not preferable because it reduces the operation efficiency. Therefore, there is a strong demand for the development of a catalyst reactivation method that can suppress catalyst deterioration, that is, cope with a case where catalyst deterioration occurs more than expected.

  The present invention has been made in view of the above-mentioned problems of the prior art. When hydrocracking FT wax over a long period of time, the catalytic activity that deteriorates with time is improved and the normal paraffin content is sufficiently reduced. It is an object of the present invention to provide a method for hydrotreating wax capable of obtaining a finished fuel substrate.

  In order to achieve the above object, the present invention uses a wax produced by Fischer-Tropsch synthesis as a raw material, and in the presence of hydrogen, the wax is placed on a carrier containing zeolite in the Group VIII metal in the periodic table. A first step of hydrocracking by bringing the catalyst into contact with a catalyst, and the hydrocracking product of the wax obtained by the first step from the wax temporarily, The distillate obtained by distilling the mixture of hydrocracked product of middle distillate produced by Fischer-Tropsch synthesis is switched to distillate oil, and the above distillate is obtained in the presence of hydrogen at a reaction temperature of 160 to 330 ° C. A second step of hydrocracking oil by contacting with the catalyst, and switching the raw material from the distillate oil to the wax, and in the presence of hydrogen, the wax Providing hydrotreating process of the wax, which comprises a third step of decomposing hydrogenation, the by contacting with the catalyst.

  According to the wax hydrotreating method, when the FT wax is hydrocracked using a catalyst in which a group VIII metal in the periodic table is supported on a support containing zeolite, the raw material is temporarily used. By switching to the above distillate and hydrocracking the distillate with the catalyst under the above temperature conditions, the catalytic activity of the catalyst deteriorated with time during the hydrocracking of the previous FT wax is improved. After that, by switching the raw material to FT wax again, a fuel base material in which the normal paraffin content is sufficiently reduced over a long period of time can be obtained.

  In the wax hydrotreating method of the present invention, the zeolite is preferably an ultrastable Y-type zeolite (hereinafter sometimes referred to as “USY zeolite”).

  According to the present invention, when hydrocracking FT wax over a long period of time, it is possible to improve the catalytic activity of a catalyst that deteriorates with time and to obtain a fuel base material with a sufficiently reduced normal paraffin content. The hydrotreating method can be provided.

  Hereinafter, the present invention will be described in detail with reference to preferred embodiments thereof.

  The method for hydrotreating a wax according to the present invention uses a wax produced by Fischer-Tropsch synthesis as a raw material, and in the presence of hydrogen, the wax is placed on a carrier containing zeolite with a Group VIII metal in the periodic table. A first step of hydrocracking by bringing the catalyst into contact with a supported catalyst; a hydrocracking product of the wax obtained by the first step; Switch to a distillate obtained by distillation of a mixture of hydrocracked product of middle distillate produced by Tropsch synthesis and distillate the above distillate under the conditions of reaction temperature 160-330 ° C. in the presence of hydrogen. A second step of hydrocracking by contacting the catalyst with the catalyst, and switching the raw material from the distillate oil to the wax, and in the presence of hydrogen, the wax A method which comprises a third step of decomposing hydrogenated by contacting with the catalyst.

  The wax hydrogenation treatment in the present invention can be carried out, for example, using a fixed bed reactor filled with a catalyst. The FT wax as a raw material is introduced into a fixed bed reactor and hydrocracked by contacting with a catalyst in a hydrogen atmosphere to obtain a product oil.

  Here, as the hydrocracking catalyst charged in the reactor, a catalyst obtained by supporting a Group VIII metal in the periodic table on a support containing zeolite is used. Examples of zeolite include USY zeolite, mordenite, and SAPO-11. Among these, USY zeolite is preferably used. These can be used individually by 1 type or in combination of 2 or more types.

  When USY zeolite is used as the zeolite, the molar ratio of silica to alumina in the USY zeolite (silica / alumina) is preferably 20 to 96, more preferably 25 to 60, and 30 to 45. More preferably it is.

  The upper limit of the average particle size of USY zeolite is preferably 1.0 μm, and more preferably 0.5 μm. On the other hand, the lower limit of the average particle size of USY zeolite is preferably 0.05 μm.

  The carrier may contain an amorphous solid acid such as silica alumina, silica zirconia, alumina boria, silica magnesia and the like.

  Moreover, as a support | carrier, it is preferable to use what shape | molded the pellet and the amorphous solid acid etc. which are used as needed using a binder. As the binder, for example, silica, alumina or the like can be used, and alumina is preferably used.

  In addition, examples of the Group VIII metal in the periodic table supported on the carrier include nickel, rhodium, palladium, iridium, and platinum. Of these, palladium and platinum are preferably used. These can be used individually by 1 type or in combination of 2 or more types.

  The wax used as a raw material in the first step and the third step in the wax hydrotreating method of the present invention is a wax (FT wax) produced by Fischer-Tropsch (FT) synthesis and has a carbon number. A wax containing 70% by mass or more of normal paraffin having 16 or more, preferably 20 or more carbon atoms. The carbon number distribution of the FT wax is determined by the conditions of FT synthesis, but the FT wax used in the present invention is not particularly limited in the carbon number distribution.

  The distillate used as a raw material in the second step in the wax hydrotreating method of the present invention is produced by the hydrocracking product of the FT wax obtained in the first step and the Fischer-Tropsch synthesis. The middle distillate hydrocracked product is obtained by distillation.

  The hydrocracking of middle distillate produced by FT synthesis can be performed using a fixed bed reactor. The reaction conditions at this time are not particularly limited, but it is desirable that the generation of gas and naphtha is sufficiently suppressed and the oxygen-containing compound is removed or the olefin is hydrogenated efficiently. Further, as the catalyst, for example, a group VIII metal in the periodic table, specifically, a metal selected from one or more of nickel, rhodium, palladium, iridium, and platinum is supported on a support containing a solid acid. It is preferable to use a catalyst.

  Although the distillate obtained by distilling the mixture of each said hydrocracking product is not restrict | limited, It is preferable that the carbon number is 9-25, and it is more preferable that it is 10-20. Moreover, when distilling the said mixture, for example, when dividing into a C10-C15 kerosene fraction and a C16-C20 light oil fraction, these can also be mixed and used suitably.

  In the first step, the reaction temperature immediately before performing the second step is not particularly limited. However, when the temperature is 340 ° C. or higher, the degree of recovery of the catalytic activity in the second step is reduced, so that it is less than 340 ° C. It is preferable. In other words, it is preferable to switch the raw materials (start the second step) before the reaction temperature in the first step reaches 340 ° C. due to catalyst deterioration.

  Moreover, as reaction conditions in a 2nd process, it is preferable that reaction temperature shall be 160-330 degreeC normally, and it is more preferable to set it as 170-320 degreeC normally. When the reaction temperature is lower than 160 ° C or higher than 330 ° C, the catalyst activity is not sufficiently recovered.

In the second step, the liquid space velocity (LHSV) of the light paraffin with respect to the catalyst in the fixed bed reactor is preferably 0.1 to 10.0 h ^−1, and preferably 0.5 to 5.0 h ^−. More preferably, it is ¹ . If the liquid space velocity is less than 0.1 h ⁻¹ , it takes time to sufficiently improve the catalyst activity, which is not preferable.

  Furthermore, in the second step, the pressure during the reaction is preferably 1 to 12 MPa, and more preferably 2 to 6 MPa.

  In the second step, the hydrogen oil ratio is not particularly limited, but is usually preferably 100 to 850 NL / L, and more preferably 200 to 650 NL / L.

  By performing the wax hydrogenation process through the first to third steps described above, the catalytic activity of the catalyst that deteriorates with time can be improved by performing the second step, and the normal paraffin content over a long period of time. It is possible to obtain a fuel base material with sufficiently reduced.

  EXAMPLES Hereinafter, although this invention is demonstrated more concretely based on an Example and a comparative example, this invention is not limited to a following example.

Example 1
FT wax (carbon number 20 to 80, normal paraffin content: 96 mass%) was prepared as a raw material for hydrocracking. Further, USY zeolite, silica alumina (alumina content: 17 mol%) and alumina binder were mixed at a mass ratio of 3:57:40, and molded into a cylindrical shape having a diameter of about 1.5 mm and a length of 3 mm, and then 500 The catalyst carrier was obtained by calcination at 1 ° C. for 1 hour. In addition, as said USY zeolite, the molar ratio of the silica and alumina in this USY zeolite is 37, and the average particle diameter is 0.82 micrometer. The obtained catalyst carrier was impregnated with an aqueous solution of dichlorotetraammineplatinum (II), dried at 120 ° C. for 3 hours, and then calcined at 500 ° C. for 1 hour, so that the platinum on the catalyst carrier was 0. A hydrocracking catalyst supported by 8% by mass was prepared.

Next, 300 ml of the catalyst was packed in a fixed bed reaction tower, and metal (platinum) was reduced under a hydrogen stream at 345 ° C. for 4 hours before the reaction. Thereafter, the decomposition rate of the raw material becomes 70% by mass under the conditions of the liquid space velocity of the raw material with respect to the catalyst of 2.0 h ⁻¹ (600 ml / h as the liquid flow rate), the pressure of 3.0 MPa, and the hydrogen oil ratio of 570 NL / L. In this way, the raw material was subjected to hydrogenation treatment continuously for 45 days while always adjusting the reaction temperature (first step). The product oil obtained during this time was distilled together to obtain a hydrocracked product A (normal paraffin content: 60% by mass) having 10 to 20 carbon atoms.

On the other hand, the middle distillate produced by the FT synthesis is treated with an alumina catalyst in which 0.2 mass% of platinum is supported on the basis of the total amount of the catalyst, at a temperature of 230 ° C., a liquid space velocity of 1.0 h ⁻¹ , and a pressure of 2. Hydrorefining was carried out under conditions of 8 MPa and a hydrogen oil ratio of 380 NL / L. The product thus obtained was distilled to obtain a hydrocracked product B (normal paraffin content: 60% by mass) having 10 to 20 carbon atoms. Next, the hydrocracking product A and the hydrocracking product B are mixed at a mass ratio of 40:60, and the resulting mixture is distilled to obtain a distillate oil (10 to 20 carbon atoms, containing normal paraffin). Amount: 60% by mass) was obtained.

45 days after the start of the hydrotreating operation in the first step, the raw material was switched from the FT wax to the distillate, and the distillate was hydrotreated for two days (second step). The reaction conditions in this treatment were a reaction temperature of 310 ° C., a liquid space velocity of 2.5 h ⁻¹ , a pressure of 3.0 MPa, and a hydrogen oil ratio of 350 NL / L.

  After the distillate oil hydrogenation treatment, the raw material was returned to the FT wax again, and the hydrogenation treatment was performed under the same conditions as in the first step (third step).

  As the reaction temperature in the above-described series of hydrotreating processes, the temperature at the start of the reaction (reaction start temperature), the temperature immediately before switching the raw material from FT wax to distillate (temperature before the second step), and the raw material as light paraffin Table 1 shows the temperature immediately after switching from FT to FT wax again (temperature after the second step). This reaction temperature is an indicator of the catalyst activity, and the lower the reaction temperature, the better the catalyst activity. Table 1 shows the normal paraffin content (index of isomerization) of the product oil having 10 to 20 carbon atoms among the product oils obtained by the hydrotreating process after switching the raw material from distillate oil to FT wax again. Shown in

(Comparative Example 1)
The hydrogenation process of the said 1st-3rd process was performed like Example 1 except having made the reaction temperature in the hydrogenation process of the distillate oil in the 2nd process into 130 degreeC. Table 1 shows each reaction temperature in the above-described series of hydrotreating and the normal paraffin content (an index of isomerization) of the product oil having 10 to 20 carbon atoms.

(Comparative Example 2)
As a raw material in the second step, instead of distillate oil, an unrefined middle distillate produced by FT synthesis (carbon number 10 to 20, alcohol content: 8.2 mass%, normal paraffin content: 80 .6 mass%) was used in the same manner as in Example 1 except that the hydrogenation treatment in the first to third steps was performed. Table 1 shows each reaction temperature in the above-described series of hydrotreating and the normal paraffin content (an index of isomerization) of the product oil having 10 to 20 carbon atoms.

As is apparent from the results shown in Table 1, when hydrocracking wax over a long period of time, a specific distillate (FT wax hydrogenation) is temporarily used during hydrocracking operation under specific conditions. The distillate obtained by distilling the cracked product and the hydrocracked product of the middle distillate produced by the FT synthesis at the same time), the activity of the catalyst deteriorated over time can be improved, It was confirmed that a fuel substrate rich in isoparaffin (low in normal paraffin) can be obtained.

Claims (2)

A wax produced by Fischer-Tropsch synthesis is used as a raw material, and in the presence of hydrogen, the wax is brought into contact with a catalyst formed by supporting a Group VIII metal in the periodic table on a support containing zeolite. A first step of chemical decomposition;
A mixture of the hydrocracking product of the wax obtained by the first step and the hydrocracking product of the middle distillate produced by Fischer-Tropsch synthesis from the wax temporarily from the wax. A second step of switching to a distillate obtained by distillation and hydrocracking by contacting the distillate with the catalyst in the presence of hydrogen at a reaction temperature of 160 to 330 ° C;
A third step in which the raw material is switched from the distillate oil to the wax and hydrocracked by contacting the wax with the catalyst in the presence of hydrogen;
A method for hydrotreating a wax, comprising: 2. The wax hydrotreating method according to claim 1, wherein the zeolite is an ultrastable Y-type zeolite.