Paraffin hydrogenation process and process for obtaining fuel base

FIELD: oil and gas industry.

SUBSTANCE: paraffin hydrotreating method involves the first stage at which paraffin with content C21 or higher of normal paraffins 70% wt or higher is used as basic material, and paraffin contacts with catalyst at reaction temperature of 270-360 °C in presence of hydrogen for hydrocracking, catalyst consisting of metal of group VIII of the Periodic Table, which is put on carrier containing amorphous solid acid; the second stage at which raw material from paraffin is replaced for some time with light paraffin with content C9-20 of paraffins 60% wt or higher, and light paraffin contacts with catalyst at reaction temperature of 120-335 °C in presence of hydrogen for hydrocracking; and the third stage at which raw material of light paraffin is replaced with paraffin and paraffin contacts with catalyst at reaction temperature of 270-360 °C in presence of hydrogen for hydrocracking. Also, invention refers to method for obtaining material of fuel system, which involves the above method.

EFFECT: use of this invention allows improving activity of hydrocracking catalyst, which deteriorates with time.

6 cl, 1 tbl, 4 ex, 1 dwg

 

The technical field

The present invention relates to a process for the hydrogenation of paraffin and to the process of obtaining material of the fuel base.

Prior art

Recent years have shown rapid growth restrictions on the sulphur content in liquid fuel, such as gasoline or light oil, for the purposes of environmental protection. This helped to lead to the development of cleaner liquid fuels with low contents of sulphur and aromatic hydrocarbons. One of the processes of production of this clean fuel is the Fischer-Tropsch synthesis (FT), which is used as raw material hydrogen and carbon monoxide from the gasification of bitumen or coal or natural gas cleaning. Synthesis CFT allows fundamentals of liquid fuel, rich in paraffins and containing no sulfur, also simultaneously, allowing you to get paraffins (paraffins CFT). The FT paraffins become sredneetazhnye fraction (kerosene or light oil by hydrocracking.

When sredneetazhnye fraction produced by hydrocracking of paraffin or FT synthesis, used as fuel material basis, it is important to achieve a high yield from the point of view of efficiency of the process, but from the point of view of the properties of the fuel, preferably the izkuyu the content of normal paraffins, while the content isoparaffins, in contrast, preferably high. In the case of light oil, for example, a high content of normal paraffins reduces low-temperature rheological properties, at times limiting their use as a commercial product in extreme cases. Since the light oil produced by the FT synthesis, are almost entirely composed of normal paraffins, they cannot easily be applied in this form.

Methods of obtaining materials fuel basis hydrocracking of paraffins were already known and, for example, hydrocracking processes using paraffin CFT disclosed in the following Patent documents 1-3.

[Patent document 1] international patent publication No. 2004/028688

[Patent document 2] Japanese Publication of unexamined patent application No. 2004-255241

[Patent document 3] Japanese Publication of unexamined patent application No. 2004-255242

Disclosure of invention

Problems to be solved by the inventions

However, when solid hydrocarbons are subjected to hydrocracking over a long period through hydrocracking processes described in Patent documents 1 to 3 mentioned above, the catalytic activity of the catalyst deteriorates with time, and the content of normal paraffin is in the resulting material fuel bases increases, or may decrease the output of the fuel material basis.

Traditionally, the development of efficient catalysts for hydrocracking of paraffin was the main goal, while in fact there is no message about the existence of superior catalytic activity during the process, i.e. the prolongation of the life of the catalyst. The typical process of obtaining a middle distillate fractions in the refining comprises hydrocracking the vacuum light oil fractions, and this process can be obtained low-sulfur light oil. In cases when wear of the catalyst during the process more than expected, then simply include reducing the amount of raw materials supplied in the planned period of the process, and the lowering of the rigidity of coking. However, such measures are not preferred because of the low efficiency. Therefore, a highly desirable goal is the development of process catalyst reactivation, which can be used to inhibit the deterioration of the catalyst, i.e. the wear of the catalyst, which exceeds expectations.

The aim of the present invention, which is improved in light of the above problems of the prior art is the provision of a Hydrotreating process paraffins and process of obtaining fuel material base, what exploits which catalyst activity, which worsens with time during the process of hydrocracking of solid hydrocarbons in long periods increases, and may be satisfactory when the output of the fuel material basis with a corresponding reduced content of normal paraffins.

Resolving problems

In order to achieve the objective set forth above, the invention provides a process for Hydrotreating paraffin, characterized by the inclusion of the first stage at which the paraffin content of C16 or more normal paraffins 70% mass or higher, is used as a raw material, and the wax is in contact with the catalyst in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid; a second step in which the raw material from the state of paraffin-temporarily replaced by light paraffin content of C9-21 paraffin 60% mass or higher, and light paraffin is in contact with the catalyst in the presence of hydrogen for hydrocracking; and a third step in which a raw material of a light paraffin replaced with paraffin, and paraffin wax in contact with the catalyst in the presence of hydrogen for hydrocracking.

According to this process of Hydrotreating the wax when the wax is subjected to hydrocracking is with the use of a catalyst, consisting of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid, a raw material temporarily replaced by light paraffin, and light paraffin is subjected to hydrocracking by catalyst, thereby making it possible to improve the catalytic activity of the catalyst, which has worsened with time during the preliminary hydrocracking of paraffin, after which the raw material is replaced back on the wax so that it can be the fuel material basis with a corresponding reduced content of normal paraffins with a satisfactory output for prolonged periods.

In the Hydrotreating process of paraffin according to the invention, the paraffin is preferably paraffin FT produced by the Fischer-Tropsch synthesis (FT). Using paraffin FT as raw material, will tend to increase the yield of middle distillate fractions.

Light paraffin used in the Hydrotreating process of paraffin according to the invention also preferably produced by Fischer-Tropsch synthesis. The use of light paraffin will allow the reaction temperature in the third stage reduced to a more reasonable level.

Also the second stage Hydrotreating process of paraffin according to the invention preferably is carried out at 150-320 is C. By carrying out Hydrotreating of light paraffin at the reaction temperature 150-320°C as possible to satisfactorily improve the catalytic activity of the catalyst, which worsens over time, and to get a higher output fuel material basis with a more appropriate reduced content of normal paraffins in prolonged periods.

The invention further provides a process for obtaining a material of the fuel framework characterized by the inclusion of the first stage at which the paraffin content of C16 or higher normal paraffins 70% mass or more is used as a raw material, and the wax is in contact with the catalyst in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid; a second step in which the raw material from paraffin temporarily replace a light paraffin content of C9-21 paraffin 60% mass or more, and a light paraffin is in contact with the catalyst in the presence of hydrogen for hydrocracking; a third step in which the raw material of a light paraffin replaced with paraffin, and paraffin wax in contact with the catalyst in the presence of hydrogen for hydrocracking; and a fourth step in which the obtained srednebelaya fraction of about botanova product, get on stages one through three. According to this production process, it is possible to improve the catalytic activity of the catalyst, which worsens over time during the hydrocracking of solid hydrocarbons in the long periods, and to get the fuel material basis with a suitable reduced content of normal paraffins with a satisfactory output.

The results of the inventions

According to the present invention, it becomes possible to provide a Hydrotreating process of the paraffin and the process of obtaining fuel material basis, which can improve the catalytic activity of the catalyst, which worsens over time during the hydrocracking of paraffin in the long periods, and can obtain satisfactory output of the fuel material basis with a corresponding reduced content of normal paraffins.

Brief description of drawings

The drawing shows a process flow diagram showing an example of a preferred device for the material of the fuel base for carrying out the process of obtaining material fuel bases according to the invention.

Description character references

10: the reaction column 12: the layer of catalyst for hydrocracking, 20: distillation column 100: the device receiving fuel material basis.

The best way to implement is subramania

Now will be described in detail preferred embodiments of the invention.

The Hydrotreating process of paraffin according to the invention is a process characterized by the inclusion of the first stage at which the paraffin content of C16 or higher normal paraffins 70% mass or more is used as a raw material, and the wax is in contact with the catalyst in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid; a second step in which the raw material from paraffin temporarily replace a light paraffin content of C9-21 paraffin 60% mass or higher, and a light paraffin is in contact with the catalyst in the presence of hydrogen for hydrocracking; and a third step in which the raw material of light replaced by paraffin wax, and paraffin wax in contact with the catalyst in the presence of hydrogen for hydrocracking.

Hydrotreating the wax according to the invention can be carried out using, for example, a reactor with a fixed bed filled with a catalyst. Paraffin feedstock is introduced into a reactor with a fixed bed and in contact with the catalyst in an atmosphere of hydrogen for hydrocracking, to obtain the target product.

The catalyst for hydrocracking, the which is loaded into the reactor for use, can be such, which consists of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid. The carrier preferably is an amorphous solid acid, which is compressed into tablets using a binder.

As examples of the amorphous solid acids there may be mentioned silica-alumina, zirconiasilicate, lumbricidae and mahavairocana, among which the aluminosilicate and lumbricidae preferred. They can be used singly or in combination of two or more. The content of amorphous solid acid catalyst, preferably 20-100% mass, and more preferably 50-100% of the mass relative to the total weight of the catalyst.

The binder component may be, for example, silicon dioxide, dioxide, aluminum and the like, and aluminum dioxide is preferred. The content of the binder component in the catalyst is preferably 0-80% mass and more preferably 0-50% mass relative to the total weight of the catalyst.

The metal of group VIII of the Periodic Table, which is placed on the carrier may be, for example, Nickel, rhodium, palladium, iridium, platinum or the like, among which palladium and platinum are preferred. They can be used singly or in combination of two or more. When image quality is as a raw material is paraffin GAC, containing an oil component, it is particularly preferable to apply a combination of palladium and platinum on a carrier. The content of the metal of group VIII in the catalyst is preferably from 0.01 to 2.0% of mass and more preferably 0.1 to 1.0% of the mass relative to the total weight of the catalyst.

The paraffin used as raw material in stages from the first to the third Hydrotreating process of paraffin according to the invention is a paraffin oil-based or synthetic, containing at least 70% of the mass C16 or higher, preferably C20 or higher and more preferably C21 or higher normal paraffins. As examples of paraffin oil-based there may be mentioned paraffin GAC and microoperation, and as examples of synthetic waxes there may be mentioned "the FT paraffins, which are obtained by the FT synthesis. The FT paraffins most preferred.

Light paraffin used as raw material in the second stage Hydrotreating process of paraffin according to the invention, fuel is a material basis with the content of C9-21 paraffin 60% mass or more, preferably the material of the fuel framework with the content of C9-20 paraffin 60% mass or more, even more preferably the material of the fuel framework with the content of C9-20 paraffin 70% mass or more, most of predpochtitel the major C9-20 oil synthesis FT.

As the reaction conditions in the first and third stages, for most purposes, the reaction temperature is preferably 270-360°C and more preferably 300-350°C. If the reaction temperature below 270°C., the content of normal paraffins will tend to be higher, and if above 360°C, the output srednemotornoy fraction will tend to be lower. In particular, reaction temperatures above 370°C leads to greater extraction of aromatic compounds than when the temperature is within the limits specified above, and therefore it is not preferable from the viewpoint of obtaining pure material fuel basis.

On the first and third stages hourly space velocity of liquid product (LHSV) of paraffin in relation to the catalyst in the reactor with a porous layer is preferably 0.1 to 5.0 h-1and more preferably 0.3 to 3.0 HR-1. If the volumetric rate of fluid below 0.1 h-1the content of normal paraffins produced srednemotornoy fraction will tend to be higher, and if it is above 5,0 h-1the output srednemotornoy fraction will tend to be lower.

Also the pressure of the reaction on the first and third stages affect catalyst activity and, therefore, is in the range of preferably 1.0 to 10.0 MPa, and more preferably 2.0 to 7.0 MPa. Pressure is e below 1.0 MPa will seek to promote the wear of the catalyst, while the pressure is higher than 10.0 MPa will tend to reduce output srednemotornoy faction.

The ratio of hydrogen/oil on the first and third stages is not severely limited, but as a rule, should be preferably 50 NL/L or more. The ratio of hydrogen/oil less than 50 NL/L will tend to lead to more olefins in the resulting srednemotornoy fraction, thereby reducing the oxidative stability of the fuel.

As for the reaction conditions of the second phase, the preferred reaction temperature 150-320°C. and more preferred 180-310°C. If the reaction temperature below 150°C, light paraffins can be resistant to isomerization, the improvement of catalytic activity may be insufficient, and the content of normal paraffins in the fuel material bases obtained in the third stage, will tend to increase, at the same time, if it is higher than 320°C, the raw light paraffins will be to reduce weight, tending to lead to a lower exit end of the fuel material basis.

Volumetric hourly rate of liquid product (LHSV) of light paraffins relative to the catalyst in the reactor with a fixed bed during the second stage is preferably of 0.1 h-1or more and more preferably 0.5 h-1or more. Hours is the volumetric rate of liquid product is preferably not less than 0.1 h -1because more time will be necessary to adequately improve catalyst activity.

There is not particular restrictions on the pressure during the reaction of the second stage, but preferably it is in the same row and in the first phase, and during the control operation is more preferable to maintain the same pressure as the first stage. Also for the second stage there is not particular restrictions on the ratio of hydrogen/oil, but they are preferred in the same limit of the ratio of hydrogen/oil that at the first stage, and during the control operation is more preferable to maintain the same ratio of hydrogen/oil that at the first stage.

Carrying out the hydrotreatment of paraffin through stages one through three, described above, is possible by means of the second stage to improve the catalytic activity of the catalyst, which worsens over time, and thus can get the fuel material basis with a suitable reduced content of normal paraffins at a high yield in prolonged periods.

Now will be explained the process of production of material fuel bases according to the invention. The production process of the fuel material basis according to the invention is characterized by the inclusion of the first stage at which paraffins content of C16 or higher normal paraffins 70% mass or more is used as a raw material, and the paraffin is in contact with the catalyst in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic Table, placed on media containing amorphous solid acid; a second step in which the raw material from paraffin temporarily replace a light paraffin content of C9-21 paraffin 60% mass or higher, and a light paraffin is in contact with the catalyst in the presence of hydrogen for hydrocracking; a third step in which the source material of a light paraffin replace paraffin, and paraffin wax in contact with the catalyst in the presence of hydrogen for hydrocracking; and a fourth step in which the fraction obtained srednebelaya of the treated product obtained in stages one through three.

From the first to the third stages for hydrocracking feedstock is preferably carried out according to the same process as the process of Hydrotreating the wax according to the invention.

Srednebelaya fraction obtained in the fourth stage, can fraktsionirovanija with a boiling point within 145-360°C.

Now will be explained, the device for receiving the material of the fuel base, used for carrying out the process of obtaining material of the fuel base. The drawing is a process flow diagram showing an example of a preferred device according to the teachings of the material of the fuel base for carrying out the process of obtaining material of the fuel base. The device receiving fuel material basis 100 shown in the drawing, is constructed from the reaction column 10 and the distillation column 20 for distillation of the reaction products obtained from the reaction column 10 (processed product obtained by hydrocracking of raw material). The reaction column 10 is the reaction column with a fixed layer, including inside the catalyst bed hydrocracking 12 containing a catalyst consisting of a metal of group VIII of the Periodic Table, placed on a carrier comprising amorphous solid acid, as explained above. In the reaction column 10 raw material is subjected to hydrocracking by Hydrotreating process according to the invention, as described above. At the top of the reaction column 10 is attached, the line L1 for supplying the raw material into the reaction column 10, while line L2 for supplying hydrogen attached upstream from the connection line L1 with the reaction column 10. At the bottom of the reaction column joins the line L3 to remove the reaction product from the reaction column 10, the other end of the line L3 is attached to the distillation column of normal pressure to 20.

The distillation column 20 is used for fractionation of the reaction product obtained by the reaction in the reaction column 10, on a separate f the shares with specific limits boiling points. The reaction product from the distillation column 20 may be subjected to fractional distillation at a gas fraction (C4 and below light hydrocarbons), heavy naphtha fraction (fraction with a boiling point 80-145°C), kerosene fraction (fraction with a boiling point 145-260°C), the fraction of light petroleum products (fraction with a boiling point of 260-360°C) and cubic fraction (fraction with a boiling point of 360°C and above), to obtain the desired fuel material basis. Distilled fraction obtained from the distillation column 20, each transported to a lower stage of the process via line (L4-L8), connected to the distillation column 20.

Examples

The present invention will now be explained in more detail by examples and comparative examples, with the understanding that the invention is not limited to the examples.

(Example 1)

Paraffin CFT (the content of C20-80, C21 or higher normal paraffins: 95% mass) was prepared as a raw material for hydrocracking. Separately, the aluminosilicate (aluminum content: 0,16 mol%) and alumina binder were combined in a weight ratio of 80:20, and after pressing in a cylindrical shape with a diameter of about 1.5 mm and a length of about 3 mm they burnt at 500°C for 1 hour to obtain a catalyst carrier. The obtained catalyst carrier was impregnated with the mixture of water plants is ora, containing hexachloroplatinic acid and tetraamminepalladium, and dried at 120°C for three hours, after which it was fired at 500° for 1 hour to obtain a hydrocracking catalyst comprising platinum and palladium in a weight ratio of 90:10 when the content of 0.8% of the mass relative to the total weight of the catalyst, applied to the catalyst carrier.

Next, 200 ml of the catalyst were placed in a reactor with a fixed bed, and metals (platinum and palladium) was subjected to reduction treatment at 345°C for 4 hours under a hydrogen stream prior to reaction. The raw material was subjected to continuous Hydrotreating in 30 days under the conditions with hourly volumetric rate of liquid product 1.5 h-1the source material with respect to the catalyst (300 ml/h based on volumetric flow rate), pressure of 2.8 MPa and a ratio of hydrogen/oil 570 NL/L, at the same time, by adjusting the reaction temperature for hard coking conditions of the source material - 80% of the mass (the first stage). The target product, obtained in the course of this procedure were collected and converted to obtain a C10-20 light paraffin (paraffin content: 99% mass).

On 30 day after initiation of the Hydrotreating source material from the FT paraffin was replaced by a light paraffin and light paraffin And subjected the very the hydrocracking for 24 hours (second stage). The reaction conditions of this treatment were: reaction temperature of 310°C, the volumetric rate of liquid product is 2.5 h-1the pressure of 2.8 MPa and a ratio of hydrogen/oil - 350 NL/L.

After Hydrotreating of light paraffin And raw material was replaced back on the FT paraffin and subjected to Hydrotreating in the initial conditions (conditions for rigidity coking 80% of the mass, as in the first stage)(second stage).

Table 1 shows the reaction temperature for these series of steps of Hydrotreating in the form of temperature at the beginning of the reaction

(the temperature of the start of the reaction), the temperature immediately before the replacement of the original material from the FT paraffin for light paraffin And

(temperature before processing a light oil) and temperature directly after replacing the original material of a light paraffin back on wax FT (temperature after processing a light oil). The reaction temperature is a measure of catalyst activity, with lower reaction temperature is more satisfactory catalytic activity. Table 1 also shows the content of normal paraffins (reflection isomerization) and the output of petroleum with a boiling point 145-360°C, oil product, obtained by Hydrotreating after replacing the original material of a light paraffin back to paraf the N. FT.

(Example 2)

Hydrotreating the first to the third steps described above were conducted in the same manner as in example 1, except that the C9-22 srednebelaya fraction (wax content C9-20: 89% mass)produced by the FT synthesis, was used instead of a light paraffin And as raw material in the second stage. Table 1 shows the reaction temperature for these series of steps of Hydrotreating, the content of normal paraffin oil with a boiling point 145-360°C (figure isomerization) and exit.

(Example 3)

The Hydrotreating stages from the first to the third, described above, was conducted in the same manner as in example 1 except that the reaction temperature Hydrotreating of light paraffin And the second stage was 335°C. table 1 shows the reaction temperature for these series of steps of Hydrotreating, the content of normal paraffin oil with a boiling point 145-360°C (figure isomerization) and exit.

(Example 4)

The Hydrotreating stages from the first to the third, described above, was conducted in the same manner as in example 1, except that the reaction temperature Hydrotreating of light paraffin And the second stage was 120°C. table 1 shows the reaction temperature for these series of steps of Hydrotreating, the content of normal paraffin oil with a point of Kipen what I 145-360°C (figure isomerization) and exit.

(Comparative example 1)

Hydrotreating the wax CFT was conducted in the same manner as in example 1, except that the first stage was long, without the second stage. Table 1 shows the reaction temperature after 30 days from the start of the operation of the Hydrotreating paraffin CFT as temperature before processing a light oil and reaction temperature after an additional 24 hours as the temperature after processing a light oil". Table 1 also shows the content of the normal paraffin oil with a boiling point 145-360°C (figure isomerization) and the output received after 31 days from the start of the operation.

As clearly evident from the results shown in table 1, it was confirmed that the temporary introduction of a light paraffin during the operation for hydrocracking of paraffin for a prolonged period can improve the catalyst activity, which worsens over time, and can produce isoparaffin enriched (with low content of normal paraffins, the fuel material basis for a satisfactory output.

Industrial applicability

As explained above, the present invention can provide a process for Hydrotreating the wax and the process of obtaining fuel material basis, which can improve the catalytic AK is Yunosti catalyst, which worsens with time during the hydrocracking of paraffin in the long periods, and can provide satisfactory output of the fuel material basis with a suitable reduced content of normal paraffins.

1. The method of Hydrotreating paraffin, characterized by the inclusion of the first stage at which the paraffin contents C21 or higher normal paraffins 70 wt.% or more is used as the source material, and the wax is in contact with the catalyst at the reaction temperature 270-360°C in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic table, placed on media containing amorphous solid acid,
the second step in which the raw material from paraffin temporarily replace a light paraffin, containing C9-20 paraffin 60 wt.% or more, and a light paraffin is in contact with the catalyst at the reaction temperature 120-335°C in the presence of hydrogen for hydrocracking, and
the third step in which the raw material is easily replaced by paraffin wax, and paraffin wax in contact with the catalyst at the reaction temperature 270-360°C in the presence of hydrogen for hydrocracking.

2. The method of Hydrotreating the wax according to claim 1, characterized in that the wax produced by the Fischer-Tropsch synthesis.

3. The method of Hydrotreating the wax according to claim 1, characterized in that h is of a light paraffin obtained by a Fischer-Tropsch synthesis.

4. The method of Hydrotreating paraffin according to any one of claims 1 to 3, characterized in that the second stage is conducted at a reaction temperature of 150-320°C.

5. The method of Hydrotreating the wax according to claim 2, characterized in that the light paraffin is obtained from the product of the hydrocracking obtained by hydrocracking of paraffin.

6. The method of obtaining material of the fuel base, characterized in that it includes
the first stage at which the paraffin contents C21 or higher normal paraffins 70 wt.% or more is used as a raw material, and the wax is in contact with the catalyst at the reaction temperature 270-360°C in the presence of hydrogen for hydrocracking, the catalyst consisting of a metal of group VIII of the Periodic table, placed on media containing amorphous solid acid,
the second stage in which the raw material from paraffin temporarily replace a light paraffin content of C9-20 paraffin 60 wt.% or more, and a light paraffin is in contact with the catalyst at the reaction temperature 120-335°C in the presence of hydrogen for hydrocracking,
the third stage in which the raw material is easily replaced by paraffin wax, and paraffin wax in contact with the catalyst at the reaction temperature 270-360°C in the presence of hydrogen for hydrocracking, and
the fourth stage on which of the treated product obtained in the third step, is obtained with enditerate fraction.



 

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20 cl, 31 ex, 17 tbl, 22 dwg

FIELD: petrochemical processes and catalysts.

SUBSTANCE: middle distillates are obtained, in particular, from paraffin charge prepared by Fischer-Tropsch synthesis wherein hydrocracking/hydroisomerization catalyst is utilized including at least one hydrocracking/hydroisomerization element selected from group constituted by group VIII metals, non-zeolite silica-and-alumina-based carrier (more than 5% and less than or equal to 95% SiO2) and having: average pore size measured by mercury porometry within a range 20 to 140 Å; total pore volume measured by mercury porometry 0.1-0.6 mL/g; total pore volume measured by nitrogen porometry 0.1-0.6 mL/g; specific surface BET between 100 and 550 m2/g; pore volume for pores with diameter above 140 Å measured by mercury porometry less than 0.1 mL/g; pore volume for pores with diameter above 160 Å measured by mercury porometry less than 0.1 mL/g; pore volume for pores with diameter above 200 Å measured by mercury porometry less than 0.1 mL/g; pore volume for pores with diameter above 500 Å measured by mercury porometry less than 0.01 mL/g; x-ray diffraction pattern containing at least principal characteristic lines of at least one transition aluminum oxides (alpha, rho, chi, eta, kappa, teta, and delta). Processes of obtaining middle distillates from paraffin charge obtained ny Fischer-Tropsch synthesis (options) using above indicated procedure are also described.

EFFECT: improved catalytic characteristics in hydrocracking/hydroisomerization processes and improved quality and yield of middle distillates.

18 cl, 6 dwg, 3 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to a method of hydrofining synthetic oil, realised by bringing synthetic oil, obtained via Fischer-Tropsch synthesis and having content of C-9-21 hydrocarbons greater than or equal to 90 wt %, into contact with a hydrofining catalyst which has a support which contains one or more solid acids selected from ultra-stable Y-(USY) zeolite, aluminosilicate, zirconia-silicate and aluminium-bromine oxide catalyst and at least one metal selected from a group comprising group VIII metals, deposited on the support, in the presence of hydrogen with regulation of the reaction temperature when the hydrofining catalyst is in contact with the synthetic oil, in order to hydrofine the synthetic oil such that content (wt %) of C8 or lower hydrocarbons in the synthetic oil after contact is 3-9 wt % higher than before contact. The invention also relates to a method of producing base fuel material.

EFFECT: obtaining base oil with excellent low-temperature rheological properties with good output of the middle fraction of the synthetic oil.

6 cl, 8 ex, 2 tbl, 1 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to a method of purifying lower alkanes from methanol through contact between the raw material and a catalyst which contains aluminium oxide at high temperature and pressure. The method is characterised by that the catalyst used is an aluminiuim-platinum catalyst and contact takes place at temperature of 180-400°C, pressure of 1.5-4.0 MPa, volume rate of supply of material of 0.4-4 h-1 and volume ratio of material : hydrogen equal to 1:(5-900).

EFFECT: invention increases degree of purity of lower alkanes from methanol.

3 cl, 9 ex

FIELD: chemistry, organic, processing of hydrocarbons.

SUBSTANCE: invention is related to an improved method for hydroprocessing of hydrocarbon raw stock containing sulphur- and/or nitrogen-bearing contaminants. The method comprises the first contact interaction of hydrocarbon raw stock with hydrogen in the presence of at least one first catalyst based on VIII group metals on an acidic carrier, the carrier being selected from the group of zeolites and zeolite-bearing carriers, and then the flow leaving the first catalyst directly contacts hydrogen in the presence of at least one second catalyst based on a VIII group metal on a less acidic solid carrier, said solid carrier being selected from the group of carriers based on silicon dioxide-aluminium oxide and other solid carriers that are not zeolites. Said combination of two catalyst layers allows processing of raw stock with a high content of contaminating impurities without high-level cracking that involves the use of highly acidic carriers.

EFFECT: processing of hydrocarbon raw stock with contaminating impurities without high-level cracking.

14 cl, 1 ex

FIELD: petroleum processing and catalysts.

SUBSTANCE: field of invention is production of catalysts for catalytic hydrotreatment (desulfurization) of gasoline fractions, e.g. straight-run gasoline. Herein disclosed is block-type high-porosity cellular catalyst for hydrotreatment of straight-run gasoline having porosity at least 90-93% and microporosity up to 30%, average pore size being ranging from 0.5 to 2.0 μm. Catalyst consists of α-alumina-based carrier and active catalyst portion containing sulfated zirconium dioxide and metallic palladium in concentration 0.5-0.9 wt %. Catalyst preparation method is also claimed and is as follows. Carrier is prepared from reticular polyurethane foam and impregnated with slurry containing more than 30 wt % α-alumina, after which calcined at 1300-1500°C, impregnated with water-soluble zirconium salts, dried at 100-200°C, calcined at 450-950°C, treated with 5-10% sulfuric acid, dried, calcined at 500-550°C, treated with palladium nitrate, dried, and calcined at 400-450°C, whereupon palladium oxide is reduced to metallic palladium.

EFFECT: lowered pressure and temperature of hydrotreatment process, considerably reduced process duration, lowered sulfur level in straight-run gasoline due to developed surface of catalyst, and prevented crumbling and loss of catalyst due to cellular structure and high strength.

FIELD: oil refining industry and petrochemistry; hydrorefining of petroleum distillates.

SUBSTANCE: hydrorefining of petroleum distillates is carried out at elevated temperature and increased pressure in presence of catalyst containing carrier - highly porous cellular material on base of aluminum α-oxide modified by aluminum γ-oxide or sulfated zirconium dioxide; used as active component is palladium or palladium modified by palladium nano-particles or palladium in mixture with zinc oxide in the amount of 0.35-20.0 mass-%. The process is carried out at temperature of 150-200°C and pressure of 0.1-1.0 Mpa.

EFFECT: enhanced efficiency; facilitated procedure; possibility of hydrorefining of gasoline and diesel distillates.

2 cl, 1 tbl

FIELD: desulfurization and hydrogenation catalysts.

SUBSTANCE: invention relates to preparing hydrodesulfurization and dearomatization catalysts useful in processes of deep purification of motor fuels from sulfur-containing compounds and aromatics. A sulfur-resistant catalyst is provided including active component deposited on porous inorganic support including montmorillonite or alumina and characterized by that support is composed of zeolite H-ZSM-5 with Si/Al atomic ratio 17-45 (80-65%) and montmorillonite or alumina (20-35%), while active component is platinum or palladium, platinum and palladium in quantities, respectively, 0.2-2.0, 0.2-1,5. and 0.4-0.2% based on the total weight of catalyst. Described is also catalyst comprising platinum (0.2-2.0%) or palladium (0.2-1.5%), or platinum and palladium (0.4-2.0%) supported by Ca or Na form of montmorillonite, and also catalyst with the same active components supported by zeolite H-ZSM-5 with Si/Al atomic ratio 17-45.

EFFECT: increased sulfur-caused deactivation resistance of catalyst at moderate temperatures and under conditions efficiency in hydrodesulfurization and aromatics hydrogenation processes.

8 cl, 4 tbl, 30 ex

The invention relates to the petrochemical industry, particularly to a method of liquid-phase hydrogenation of unsaturated hydrocarbons in the part of the light fraction of pyrolysis tar
The invention relates to the field of petrochemicals, and particularly to a method of Hydrotreating a liquid hydrocarbon fractions

The invention relates to a catalyst used in the methods of hydroconversion hydrocarbons, which contain small amounts of metals

The invention relates to the refining and can be used in the process of cleaning catalytic reforming products from olefin hydrocarbons

FIELD: chemistry.

SUBSTANCE: invention relates to processes of generating catalysts for hydrogenation of plant oil and fat. The invention describes a method of regenerating a spent palladium-containing catalyst for hydrogenating plant oil and fat through treatment with sodium hydroxide solution and washing with a condensate, where the catalyst is pre-washed with steam condensate until there are no traces of fat while simultaneously bubbling with hydrogen. Treatment is carried out with 10% solution of sodium hydroxide while blowing with hydrogen at the same time. Washing is carried out with steam condensate until there are completely no traces of alkali and soap and drying is carried out in a hydrogen stream at 145-150°C for 8-9 hours.

EFFECT: attaining high degree of purification and regeneration of the catalyst.

2 ex

FIELD: petrochemical industry; methods of production of the ethylene non-saturated halogen-containing aliphatic hydrocarbons.

SUBSTANCE: the invention is pertaining to the method of production of the ethylene non-saturated halogen-containing aliphatic hydrocarbons by the thermal fission of the saturated halogen-containing aliphatic hydrocarbons. The initial gas stream introduce into the reactor having, at least, one entering in its internal part feeding line, through which the heated gas formed from the fission promoters and containing the radicals comes into the reactor. The invention is also pertaining to the reactor used for realization of the method. At that generation of the radicals is exercised outside the reactor. The technical result of the invention is the increased output of the fission reaction.

EFFECT: the invention ensures the increased output of the fission reaction.

36 cl, 1 ex, 9 dwg

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