The catalyst for refining of gasoline, the method of its preparation and method of refining gasoline

 

(57) Abstract:

Usage: oil refining and petrochemical industry. The inventive catalyst contains 0.05 to 80 wt. sverkhkriticheskogo zeolite type pentasil a molar ratio of SiO2/Al2O3equal 25-150, optionally 0.005 to 80 wt. zeolite MeNaY, where Me-H, Zn, Mn, Ga, and binding-rest. As a binder, the catalyst may contain amorphous metroselect-aluminosilicate or zirconosilicate, or miniserial, or conciliate. When this catalyst has the following chemical composition, wt. the metal oxide in metallasiloxanes binder 0,5-8,5; aluminum oxide 1,6-17,6; the metal oxide in the composition of the zeolite of 0.05-2.5; sodium oxide of 0.05-0.5; silica rest. The catalyst may contain a binder alumina. When this catalyst has the following composition, wt. the metal oxide in the composition of the zeolite of 0.05-2.5; sodium oxide of 0.05-0.5; silicon oxide 22,1 is 72.1, alumina rest. The catalyst may have a ball or microspheric form or shape of the extrudate. The preferred content sverkhkriticheskogo zeolite type pentasil in the catalyst pellet forms of 0.05-50 wt. Method of refining gasoline on the proposed catalinmarian gasoline over zeolite catalysts and may find application in the refining and petrochemical industries.

Known zeolite-containing catalyst for refining of gasoline, representing servicecompany zeolite (ICS) with silicate module 30 in amorphoussilicon binder. The catalyst is prepared by mixing a solution of water glass, aluminum sulfate and water suspension sverkhvysokochastotnogo zeolite at pH 7.8 and 8.1, coagulation, syneresis in aqueous solution ammonium salts, washing the obtained hydrogel, drying and calcination. This catalyst allows for the improvement of thermal cracking gasoline to flow laboratory setting at a temperature of 480aboutWith, duration of experience, 1H, mass feed rate of the raw material 4,4-6,7 h-1and the resultant catalysate 75 wt. to increase the octane number by the motor method from 62 up to 76.4-79,6% [1]

The disadvantage of this catalyst and method of its preparation is not sufficiently high activity of the catalyst, which leads to insufficient high resultant catalysate and its octane number.

Also known zeolite-containing catalyst for refining of gasoline, representing servicecompany zeolite with silica module 30 in the binder is alumina. The catalyst was prepared by the method of hydrocarbon-Ammi is karasti feed 1 h-1contact times of 1 h and the content of 5 wt. Swcc in the binder is 72 wt. Data on the octane number catalyzate in the work of the absent [2]

This catalyst also does not have a sufficiently high activity.

The objective of the invention is to develop a catalyst for refining of gasoline and ways of cooking, allowing to obtain a catalyst with higher activity, which allows to increase the output of the catalyst and the octane number of gasoline.

The problem is solved, we offer zeolite-containing catalyst for refining of gasoline containing servicecompany zeolite type pentasil a molar ratio of SiO2/Al2O3equal 25-150, and zeolite MeNaY, where Me-H, Zn, Mn, Ga and having the following composition, wt.

Sverkhvisokimi - terrestrial 0,05-80 Zeolite MeNaY 0,05-80 the Rest of the Binder

The catalyst may contain a binder amorphous metroselect-aluminosilicate, or zirconosilicate, or miniserial, or conciliate. When this catalyst has the following chemical composition, wt.

The metal oxide in

metallasiloxanes binder of 0.5-8.5 aluminum Oxide 1,6-17,6

The metal oxide in the composition of the zeolite 0.05-2.5 Oxide on the and this he has the following chemical composition, wt. The metal oxide 0.05-2.5 Oxide, 0.05-0.5 sodium Oxide silicon 22,1 is 72.1 alumina Rest

The catalyst can be obtained in a ballpoint or microspheric form or in the form of extrudates. The catalyst in ball form preferably contains servicecompany zeolite type pentasil in the amount of 0.05-50 wt.

The task is also solved by a method of preparation metallasiloxanes zeolite catalyst for refining gasoline, comprising mixing in an aqueous solution of metal joints, sodium silicate and suspensions of zeolite, coagulation, syneresis and/or activation of an aqueous solution of ammonium salt, washing the obtained hydrogel, drying and calcination, the distinctive feature of which is that as the metal joining using an aqueous solution of a salt of one of the following metals: aluminum, zirconium, magnesium, zinc, as a suspension of zeolite a mixture of sverkhkriticheskogo zeolite type pentasil a molar ratio of SiO2/Al2O3equal 25-150, and zeolite MeNaY, where IU-N, Zn, Mn, Ga, in water, or mixture of zeolites high type pentasil and NaY in an aqueous salt solution of one of the following metals: zinc, manganese, gallium. When atomnoi drying and calcination.

The task is also solved by a method of preparation of zeolite-containing catalyst for refining gasoline, comprising mixing the aqueous suspension of the zeolite with aluminum hydroxide, forming, drying, calcining, the distinctive feature of which is that as the suspension of zeolite a mixture of zeolites of type pentasil a molar ratio of SiO2/Al2O3equal 25-150, and zeolite MeNaY, where Me-H, Zn, Mn, Ga, in water, or mixture of zeolites sverkhvysokochastotnogo zeolite type pentasil a molar ratio of SiO2/Al2O3= 25-150 and NaY in an aqueous salt solution of one of the following metals zinc, manganese, gallium, and aluminum hydroxide use aluminum hydroxide pseudoboehmite patterns. In this case, to obtain a catalyst in microspherical form a mixture of zeolite and aluminum hydroxide is subjected to spray drying and calcination.

The task is also solved by a method of refining gasoline on zeolite-containing catalyst containing sverhkrupnyh zeolite at elevated temperatures and pressures, the distinctive feature of which is that as the catalyst use of catalyst with the following composition 25-150, 0,05-80; zeolite MeNaY, where IU-N, Zn, Mn, Ga, 0.05 to 80; the rest of the binder.

Characteristics of the binder and the chemical composition of the catalyst set forth in the description of the catalyst composition. The invention consists in the following.

Metallogenically zeolite catalyst pellet form is prepared as follows: mixing an aqueous solution of an aluminum salt or zirconium, or magnesium, or zinc containing 1,5-26,2 kg/m3metal oxide and 60 to 120 kg/m3H2SO4, an aqueous solution of sodium silicate (liquid glass) concentration of NaOH 1.4 to 1.8 chequ/m3and suspension sverkhvysokochastotnogo (ICS) zeolite type pentasil a molar ratio of SiO2/Al2O3=25-150 and zeolite MeNaY, where Me=Zn or Mn, or Ga containing 0.25-250 kg/m3CRS-zeolite and 0.25-250 kg/m3zeolite MeNaY. For mixing with the above-mentioned aqueous solutions it is possible to use a mixture of high zeolite type pentasil a molar ratio of SiO2/Al2O3equal 25-150, and NaY zeolite in an aqueous solution of metal salt of zinc, or manganese, or gallium containing 100 kg/m3CRS-zeolite, 25 kg/m3zeolite NaY and 7.5 kg/m3a metal oxide. The mixture produced in the mixer with the formation of Satem hydrogel may be subject to syneresis when 20-60aboutC for 6-24 h and/or ion exchange with an aqueous solution of ammonium sulfate concentration of 5-25 kg/m3when 20-60aboutWith in 12-24 hours and Then washed with condensate water at 20-60aboutWith in 12-24 hours from sulfation, dried at 110-190aboutC and calcined at 500-600aboutC for 6-24 h in air flow. The resulting catalyst contains 0.05-50 wt. CRS-zeolite, of 0.05-50 wt. zeolite MeNaY (where Me-H, or Zn, or Mn, or Ga) and 49.95-75 wt. metallasiloxanes basis matrix and has the following chemical composition, wt.

The metal oxide (in the binder) of 0.05-8.5 aluminum Oxide 1,6-11,0 Oxide sodium 0,2-0,6

Oxide cream of the Rest (up to 100)

Methylsilicone zeolite-containing catalyst in microspherical form get similar catalyst in ball form. After washing the condensate water, the hydrogel is subjected to dispersion with suspension CRS-zeolite or zeolite MeNaY (where IU-N, Zn, Mn, Ga) or by suspension CRS-zeolite in an aqueous solution of the salt of zinc or manganese, or gallium. Then hold the spray drying at 400-600aboutWith, calcining at 500-600aboutC for 6-12 h in air flow. The resulting catalyst contains 0.05 to 80 wt. CRS-zeolite, 0.05 to 80 wt. zeolite MeNaY (where Me-H, or Zn, or Mn, or Ga) and the rest (up to 100) metallocene is,5 aluminium Oxide a 4.7-17.6 Oxide sodium 0,2-0,6

Oxide cream of the Rest (up to 100)

Alumina zeolite-containing catalyst in the form of extrudate prepared as follows: aqueous suspension of aluminum hydroxide pseudoboehmite structures containing between 100 and 900 kg/m3aluminium oxide is dispersed with an aqueous suspension of zeolite MeNaY (where IU-N or Zn, or Mn, or Ga) and CRS-zeolite type pentasil a molar ratio of SiO2/Al2O3=25-150 containing 0.2 to 320 kg/m3zeolite MeNaY and 0.2-320 kg/m3CRS-zeolite, and passed through the extruder. The resulting extrudate is dried at 110-190aboutC, calcined at 500-600aboutC for 6-24 h in air flow. The resulting catalyst contains 0.05 to 80 wt. CRS-zeolite, 0.05 to 80 wt. zeolite MeNaY (where IU-N or Zn, or Mn, or Ga) and the rest of the alumina binder and has the following chemical composition, wt.

The metal oxide

(Zn, or Mn, or Ga) 0.05-2.5 sodium Oxide is 0.2 to 0.6 silicon Oxide 22,1 is 72.1

The aluminium oxide of the Rest (up to 100)

For mixing, you can use the suspension CRS-zeolite and zeolite NaY in an aqueous solution of nitrate of metal (zinc, or manganese, or gallium).

Alumina zeolite-containing catalyst in microspherical form receive the same catalyst in the form of extrudates. After dispersancy catalyst contains 0.05 to 80 wt. CRS-zeolite, 0.05 to 80 wt. zeolite MeNaY (where IU-N or Zn, or Mn, or Ga) and the rest of the alumina binder and has a chemical composition similar to the composition of the extrudate.

Method of refining gasoline with the proposed catalyst is carried out at a temperature of 350-450aboutC, a pressure of 0.1-1 MPa and a flow rate of 1-2 .5 h-1. As raw materials can be used straight-run gasoline, gasoline, thermal cracking, etc.

P R I m e R 1. An aqueous solution of aluminum sulfate containing 20 kg/m3Al2O3and 80 kg/m3H2SO4, an aqueous solution of sodium silicate (liquid glass) concentration of NaOH 1.6 chequ/m3and suspension sverkhvysokochastotnogo (ICS) zeolite type pentasil a molar ratio of SiO2/Al2O3=45 and NaY zeolite containing 100 kg/m3CRS-zeolite and 25 kg/m3zeolite NaY, are mixed in the mixer with the formation of a Hydrosol, which is coagulated with 10aboutC and pH=8.1 in the hydrogel pellet form in a layer of mineral oil, then the hydrogel treated with an aqueous solution of ammonium sulfate concentration of 10 kg/m3at the 50aboutC for 18 h, washed with condensate water at 50aboutC for 18 h from sulfate ions, dried at 150

Aluminum oxide (in binder) 6.5 aluminum Oxide 1.8 Oxide sodium 0,2

Oxide cream of the Rest (up to 100)

P R I m m e R 2. An aqueous solution of aluminum sulfate containing 1.5 kg/m3Al2O3and 120 kg/m3H2SO4, an aqueous solution of sodium silicate concentration of 1.4 chequ/m3and suspension CRS-zeolite type pentasil a molar ratio of SiO2/Al2O3= 25 and NaY zeolite containing 250 kg/m3CRS-zeolite and 0.25 kg/m3zeolite NaY, are mixed in the mixer with the formation of a Hydrosol, which is coagulated at the 15aboutC and pH 7.8 in the hydrogel pellet form in a layer of mineral oil. Then the hydrogel is subjected to syneresis at 60aboutC for 6 hours Then the hydrogel treated with an aqueous solution of ammonium sulfate concentration of 5 kg/m3at 60aboutC for 12 h, washed with condensate water at 60aboutC for 12 h from sulfation, dried at 110aboutC and calcined at 500aboutC for 24 h in air flow. The resulting catalyst contains 50 wt. CRS-zeolite, 0,05 wt. zeolite, NaY and 49.95 wt. amorphous aluminosilicate framework binder and imeet

Silica Rest

P R I m e R 3. An aqueous solution of aluminum sulfate contains 26,2 kg and 60 kg/m3H2SO4, an aqueous solution of sodium silicate concentration of 1.8 chequ/m3and suspension CRS-zeolite type pentasil a molar ratio of SiO2/Al2O3=150 and NaY zeolite containing 0.25 kg/m3CRS-zeolite and 250 kg/m3zeolite NaY, are mixed in the mixer with the formation of a Hydrosol, which is coagulated in 5aboutC and a pH of 8.4 in the hydrogel pellet form in a layer of mineral oil. Then the hydrogel is subjected to syneresis at 20aboutC for 24 h Then the hydrogel treated with an aqueous solution of ammonium sulfate concentration of 25 kg/m3at 20aboutC for 24 h, washed with condensate water at 20aboutC for 24 h from sulfate ions, dried at 190aboutC and calcined at 600aboutC for 6 h in air flow. The resulting catalyst contains 0.05 wt. CRS-zeolite, 50 wt. zeolite, NaY and 49.95 wt. amorphous aluminosilicate framework matrix and has the following chemical composition, wt.

Aluminum oxide (in binder) 8.5 aluminum Oxide 11,0 Oxide sodium 0.6 silica Rest

P R I m e R s 4-6. The catalysts prepared as in examples 1-3. Instead of NaY zeolite used price is -3. Instead of NaY zeolite used zeolite MnNaY. The composition of the catalysts are given in table.1.

P R I m e R 10-12. The catalysts prepared as in examples 1-3. Instead of NaY zeolite used zeolite GaNaY. The composition of the catalysts are given in table.1.

P R I m e R s 13-24. The catalysts prepared as in examples 1-12. Instead of an aqueous solution of aluminum sulfate is used an aqueous solution of zirconium sulfate. The composition of the catalysts are given in table.1.

P R I m e R s 25-36. The catalysts prepared as in examples 1-12. Instead of an aqueous solution of aluminum sulfate is used an aqueous solution of magnesium sulfate. The composition of the catalysts are given in table.1.

P R I m e R s 37 to 48. The catalysts prepared as in examples 1-12. Instead of an aqueous solution of aluminum sulfate is used an aqueous solution of zinc sulfate. The composition of the catalysts are given in table.1.

P R I m e R 49. The catalyst was prepared as in example 1. As slurry is used, the suspension CRS-zeolite and zeolite NaY in an aqueous solution of zinc sulfate containing 100 kg/m3CRS-zeolite, 25 kg/m3zeolite NaY and 7.5 kg/m3of zinc oxide. Further according to the example 1. The composition of the catalyst are given in table.1.

P R I m e R 50. The catalyst was prepared as in example 1. As suspension use suspe the3zeolite NaY and 7.5 kg/m3oxide of manganese. Further according to the example 1. The composition of the catalyst are given in table.1.

P R I m e R 51. The catalyst was prepared as in example 1. As slurry is used, the suspension CRS-zeolite and zeolite NaY in aqueous gallium nitrate solution containing 100 kg/m3CRS-zeolite, 25 kg/m3zeolite NaY and 7.5 kg/m3gallium oxide. Further according to the example 1. The composition of the catalyst are given in table.1.

P R I m e R 52. The catalyst was prepared as in example 2. After washing the condensate water, the hydrogel is subjected to dispersion with suspension CRS-zeolite and spray-dried at 400aboutC and calcining at 600aboutWith 6 hours in air flow. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 53. The catalyst was prepared as in example 3. After washing, the hydrogel is subjected to dispersion with a suspension of zeolite HNaY and spray-dried at 600aboutC and calcining at 500aboutWith 12 hours in air flow. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 54. The catalyst was prepared as in example 14. After washing, the hydrogel is subjected to dispersion with suspension CRS-zeolite in an aqueous solution of zinc nitrate, spray-dried at 400about

P R I m e R 55. The catalyst was prepared as in example 15. After washing, the hydrogel is subjected to dispersion with a suspension of zeolite ZnNaY and spray-dried at 600aboutC and calcining at 500aboutWith 12 hours in air flow. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 56. The catalyst was prepared as in example 26. After washing, the hydrogel is subjected to dispersion with suspension CRS-zeolite in an aqueous solution of manganese nitrate, spray-dried at 400aboutC and calcining at 600aboutWith the current of air. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 57. The catalyst was prepared as in example 27. After washing, the hydrogel is subjected to dispersion with a suspension of zeolite MnNaY and spray-dried at 600aboutC and calcining at 500aboutWith 12 hours in air flow. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 58. The catalyst was prepared as in example 38. After washing, the hydrogel is subjected to dispersion with suspension CRS-zeolite in an aqueous solution of gallium nitrate, spray-dried at 400aboutC and calcining at 600aboutWith the current of air. The catalyst has the microspheric form, the composition is shown in table.1.

th zeolite GaNaY and spray-dried 600aboutC and calcining at 500aboutWith 12 hours in air flow. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 60. Aqueous suspension of aluminum hydroxide pseudoboehmite structure containing 400 kg/m3aluminium oxide is dispersed with a water suspension CRS-zeolite type pentasil with a molar ratio of SiO2/Al2O3=45 and zeolite HNaY containing 80 kg/m3CRS-zeolite and 20 kg/m3zeolite, NaY, and passed through the extruder. The resulting extrudate is dried at 150aboutC, calcined at 550aboutC for 12 h in air flow. The catalyst containing 20 wt. CRS-zeolite, 5 wt. zeolite HNY and 75 wt. alumina binder and has the following chemical composition, wt.

Aluminum oxide (in binder) 75 sodium Oxide 0.2 silica 22,1

Oxide Alu - MINIA Rest (up to 100)

P R I m e R 61. Aqueous suspension of aluminum hydroxide pseudoboehmite structure containing 900 kg/m3of aluminum oxide and 5 kg/m3nitric acid, is dispersed with a water suspension CRS-zeolite type pentasil a molar ratio of SiO2/Al2O3=25 and zeolite HNaY, containing 320 kg/m3CRS-zeolite and 0.2 kg/m3The NaY, and passed through the extruder. Palatalization contains 80 wt. CRS-zeolite, 0,05 wt. zeolite HNaY and 19.95 wt. alumina binder and has the following chemical composition, wt.

Aluminum oxide (in binder) 19,95 Oxide sodium 0.4 silicon Oxide 72,1 alumina Rest

P R I m e R 62. Aqueous suspension of aluminum hydroxide pseudoboehmite structures containing 100 kg/m3aluminum oxide and 0.5 kg/m3nitric acid, is dispersed with a water suspension CRS-zeolite type pentasil a molar ratio of SiO2/Al2O3=150 and zeolite HNaY containing 0.2 kg/m3CRS-zeolite and 320 kg/m3HNaY, and passed through the extruder. The resulting extrudate is dried at 190aboutC, calcined at 600aboutC for 6 h in air flow. The resulting catalyst contains 0.05 wt. CRS-zeolite, 80 mass. zeolite HNaY and 19.95 wt. alumina binder and has the following chemical composition, wt.

Aluminum oxide (in binder) 19,95 Oxide sodium 0.6 silicon Oxide 51,8 alumina Rest

P R I m e R 63. The catalyst was prepared as in example 61. As suspension CRS-zeolite and zeolite NaY in an aqueous solution of zinc nitrate, containing 320 kg/m3CRS-zeolite, 0.2 kg/m3zeolite NaY and 0.2 kg/m3of zinc oxide. Further in example 61. The composition of the catalyst privezi SPCS-zeolite and zeolite ZnNaY, contains 0.2 kg/m3CRS-zeolite and 320 kg/m3zeolite ZnNaY. Further in example 62. The composition of the catalyst are given in table.1.

P R I m e R 65. The catalyst was prepared as in example 61. As slurry is used, the suspension CRS-zeolite and zeolite NaY in an aqueous solution of manganese nitrate, containing 320 kg/m3CRS-zeolite, 0.2 kg/m3zeolite NaY and 0.2 kg/m3oxide of manganese. Further in example 61. The composition of the catalyst are given in table.1.

P R I m e R 66. The catalyst was prepared as in example 62. As slurry is used, the suspension CRS-zeolite MnNaY containing 0.2 kg/m3CRS-zeolite and 320 kg/m3zeolite MnNaY. Further in example 62. The composition of the catalyst are given in table.1.

P R I m e R 67. The catalyst was prepared as in example 61. As slurry is used, the suspension CRS-zeolite and zeolite NaY in an aqueous solution of gallium nitrate, containing 320 kg/m3CRS-zeolite, 0.2 mg/m3zeolite NaY and 0.2 kg/m3gallium oxide. Further in example 61. The composition of the catalyst are given in table.1.

P R I m e R 68. The catalyst was prepared as in example 62. As slurry is used, the suspension CRS-zeolite and zeolite GaNaY, containing 0.2 kg/m3CRS-zeolite and 320 kg/m3zeolite GaNaY. Further in example 62.e dispersion mixture is subjected to spray drying and calcining under the condition of example 54. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R s 72-77. The catalysts prepared as in examples 63-68. After dispersion, the mixture is subjected to spray drying and calcination under the conditions of example 55. The catalyst has the microspheric form, the composition is shown in table.1.

P R I m e R 78 (for comparison). The catalyst prepared according to [1] the catalyst containing 10 wt. CRS-zeolite with a molar ratio of SiO2/Al2O3= 30 and 90 wt. amorphous silica-alumina base (binder) and has the following chemical composition, wt. Aluminum oxide 6.1 Oxide sodium Oxide 0.2 silica Rest

P R I m e R 79 (for comparison). The catalyst prepared according to [1] After washing the hydrogel dispersion make, spray drying at 600aboutC and calcination at 600aboutAt 6 a.m. the resulting catalyst has a composition as in example 78.

Ball-type catalysts and catalysts in the form of extrudates of examples 1-51, 60-68, 78 were tested in the process of refining gasoline on running the installation with a fixed catalyst bed at atmospheric pressure, temperature 350aboutC, space velocity of the raw material 1 h-1and duration of experience 0.5 hours

aboutWith 35-190 sulfur Content, wt. 0,1 Octane number (m m) 50,4

Group hydrocarbon composition, wt. Unsaturated 4 Paraffin-naphthenic 87 Aromatic 9

The test results are presented in table.2. Resulting catalysts according to examples 52-59, 69-77, 79 were tested in the process of refining gasoline, thermal cracking at atmospheric pressure, a temperature of 350aboutC, space velocity of the raw material 1 h-1and duration of experience 0.5 hours

thermal cracking gasoline had the following characteristics; Density, g/cm30,74

Limits boiling GOST,aboutWith 60-180 sulfur Content, wt. 0,3 Octane number (m m) 62,7

Group hydrocarbon composition, wt. Unsaturated 38 Paraffin-naphthene Aromatic 51 11

The test results are presented in table.3.

P R I m e R 80. The preparation of the catalyst and its composition is similar to example 16.

P R I m e R 81. The preparation of the catalyst and its composition is similar to example 56. Ball catalysts in examples 78 and 80 were tested in the process of refining gasoline at a pressure of 1.0 MPa, a temperature of 450aboutC, space velocity of the raw materials 2.5 h-1and the continuation of the experience 0.5 hours Characteristics the definition of the catalysts in examples 79 and 81 were tested in the process of refining gasoline, thermal cracking at a pressure of 1.0 MPa, temperature 450aboutC, space velocity of the raw materials 2.5 h-1and the continuation of the experience 0.5 H. Characteristics of gasoline above. The test results are presented in table.3 after the asterisk.

P R I m e R 82. The catalyst was prepared as in example 1. As slurry is used, the suspension CRS-zeolite and zeolite NaY, containing 0.25 kg/m3CRS-zeolite and 0.25 kg/m3zeolite NaY. Further according to the example 1. The resulting catalyst contains 0.05 wt. CRS-zeolite, 0,05 wt. zeolite HNaY and 99.9 wt. amorphous aluminosilicate framework-matrix and has the following chemical composition, wt.

Aluminum oxide (in binder) 6.5 aluminum Oxide 0.01 sodium Oxide 0.2 silica Else.

P R I m e R 83. The catalyst was prepared as in example 60. As slurry is used, the suspension CRS-zeolite and zeolite HNaY containing 0.2 kg/m3CRS-zeolite and 0.2 kg/m3zeolite HNaY. Further in example 60. The resulting catalyst contains 0.05 wt. CRS-zeolite, 0,05 wt. zeolite HNaY and 99.9 wt. alumina-matrix and has the following chemical composition, wt.

Aluminum oxide (in binder) 99,9 Oxide sodium 0.001 alumina 0.01 silicon Oxide 0,09

The catalysts according to examples 82,83 were tested in the process of refining is to increase the resultant catalysate to 87,0-94,4 wt. and to increase its octane number up to 80.8 m m

1. The catalyst for refining of gasoline containing servicecompany zeolite and a binder, characterized in that it contains servicecompany zeolite type pentasil a molar ratio of SiO2/Al2O325 150, and optionally a zeolite MeNaY, where Me-H,Zn,Mn,Ga, at the following content, wt.

Servicecompany zeolite 0,05 80,0

Zeolite MeNaY 0,05 80,0

Binder 19,95 99,9

2. The catalyst p. 1, characterized in that it contains as a binder amorphous metroselect.

3. The catalyst p. 2, characterized in that as amorphous metroselect it contains aluminosilicate, or zirconosilicate, or miniserial, or conciliate.

4. The catalyst PP.2 and 3, characterized in that it has the following chemical composition, wt.

The metal oxide in metallasiloxanes binder 0,5 8,5

The aluminum oxide of 1.6 to 17.6

The metal oxide in the zeolite 0,05 2,5

The sodium oxide 0,05 0,5

Silica Rest

5. The catalyst p. 1, characterized in that it contains aluminum oxide.

6. The catalyst p. 5, characterized in that it has the following chemical status is aluminum Else

7. The catalyst p. 1 to 6, characterized in that it has a ball or microspheric form or shape of the extrudate.

8. The catalyst PP.1 and 7, characterized in that in ball form, it contains servicecompany zeolite type pentasil in the amount of 0.05 to 50 wt.

9. The preparation method of catalyst for refining of gasoline comprising mixing in an aqueous solution of metal joints, sodium silicate and suspensions of zeolite, coagulation, syneresis and/or activation of an aqueous solution of ammonium salt, washing the obtained hydrogel, drying and calcination, wherein as the metal joining using salt of one of the following metals aluminum, zirconium, magnesium, zinc, as a suspension, a mixture of sverkhvysokochastotnogo zeolite type pentasil a molar ratio of SiO2/Al2O325 150, and zeolite MeNaY, where Me-H,Zn,Mn,Ga, in water or a mixture of high zeolite type pentasil a molar ratio of SiO2/Al2O325 150, and NaY zeolite in an aqueous solution of salt of one of the metals zinc, manganese, gallium.

10. The preparation method of catalyst for refining of gasoline, comprising mixing the aqueous suspension of the zeolite is form a mixture sverkhvysokochastotnogo zeolite type pentasil a molar ratio of SiO2/Al2O325 150, and zeolite MeNaY, where Me-H,Zn,Mn,Ga, in water or a mixture sverkhvysokochastotnogo zeolite type pentasil a molar ratio of SiO2/Al2O325 150, and NaY zeolite in an aqueous solution of salt of one of the metals zinc, manganese, gallium and aluminum hydroxide use aluminum hydroxide pseudoboehmite patterns.

11. The method according to p. 9, characterized in that to obtain a catalyst in microspherical form the washed hydrogel is subjected to dispersion, spray drying and calcination.

12. The method according to p. 10, characterized in that to obtain a catalyst in microspherical form a mixture of zeolite and aluminum hydroxide is subjected to spray drying and calcination.

13. Method of refining gasoline over zeolite catalyst comprising servicecompany zeolite and a binder, at elevated temperature and pressure, characterized in that the use of catalyst containing servicecompany zeolite type pentasil a molar ratio of SiO2/Al2O325 150 and optionally a zeolite MeNaY, where Me - H,Zn,Mn,Ga, having the following composition, wt.

Servicecompany zeolite 0,05 80,0

CE is containing as a binder amorphous metroselect.

15. The method according to PP.13 and 14, characterized in that the use of a catalyst containing as amorphous metroselect aluminosilicate, or zirconosilicate, or miniserial, or conciliate.

16. The method according to PP.13 to 15, characterized in that use a catalyst having the following chemical composition, wt.

The metal oxide in metallasiloxanes binder 0,5 8,5

The aluminum oxide of 1.6 to 17.6

The metal oxide in the composition of the zeolite 0,05 2,5

The sodium oxide 0,05 0,5

Silica Rest

17. The method according to p. 13, characterized in that the use of a catalyst containing as the binder is alumina.

18. The method according to p. 17, characterized in that use a catalyst having the following chemical composition, wt.

The metal oxide in the composition of the zeolite 0,05 2,5

The sodium oxide 0,05 0,5

The silicon oxide 22,1 72,1

Alumina Rest

 

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4 dwg, 1 tbl, 2 ex

FIELD: chemistry.

SUBSTANCE: nanotubular materials crystallising in the system of K2O-TiO2-X-H2O (X=NiO, MgO, Al2O3, Cr2O3, CO2O3, Fe2O3) are characterized by the fact that in their composition up to 10% of ions Ti4+ is replaced by doping two- or trivalent metal. The method of synthesis of nanotubular materials is characterized by the fact that the synthesis of the samples is carried out by hydrothermal treatment of a pre-prepared mixture of hydroxide in KOH solution, to produce the initial mixtures of hydroxides, a solution of titanyl chloride synthesised by reaction of TiCl4 with chilled distilled water, is mixed with aqueous solutions of salts of finished elements in a predetermined ratio, and then the precipitation of hydroxides is produced by adding NH4OH to the aqueous solution mixture at pH=9-9.5 followed by washing with distilled water, drying at 70-90C and mechanical crushing, then the crushed precipitate is mixed with 10 M KOH solution and subjected to a hydrothermal treatment at 170-180C for, at least, 24 hours, after which the resulting product is washed with distilled water.

EFFECT: invention makes it possible to synthesise potassium-titanate nanotubes with an average outer diameter of 5 to 12 nm.

2 cl, 5 dwg, 2 ex

FIELD: chemistry.

SUBSTANCE: method of growing diamond single-crystals doped with nitrogen and phosphorus at high pressures of 5.5-6.0 GPa and temperatures of 1600-1750C is carried out on the seed crystal, which is pre-pressed into a substrate of cesium chloride and separated from the source of carbon, nitrogen, and phosphorus with the metal-solvent, which is used as an alloy of iron, aluminium, and carbon. Between the source of carbon, nitrogen, and phosphorus and the seed crystal, a temperature difference of 20-50C is created. The alloy of iron, aluminium, and carbon in the metal-solvent is taken with the following component ratio, wt %: iron 92.5-95.0; aluminium 2.5-0.5; carbon 5.0-4.0. The mixture of the source of carbon, nitrogen, and phosphorus is taken with the following component ratio, wt %: carbon (graphite) 95.0-97.0; phosphorus 5.0-3.0; adsorbed nitrogen 0.0010.0005. Heating is carried out up to the initial temperature in a zone of growth at 100-250C higher the melting temperature of the alloy of the metal-solvent, the exposure is produced at this temperature for 50 to 150 h. The mass flow rate of crystal growth is more than 2 mg/h. The technical result consists in the controlled doping the diamond single- crystal grown on the seed with impurities of phosphorus and nitrogen in the conditions of influence of high pressure and temperature.

EFFECT: resulting large diamond single-crystals contain a nitrogen admixture in the concentration of 0,1-17,8 parts per million of carbon atoms and phosphorus in a concentration of 0,5-5 parts per million of carbon atoms.

2 dwg, 3 ex

FIELD: chemistry.

SUBSTANCE: urea-containing solution (13) is produced in the section (10) of synthesis, the solution is purified in the section (14) of extraction, and an aqueous solution (15) containing mostly urea and water, which is produced from the above-mentioned section of the extraction is subjected to the concentration process. Herewith the concentration process includes a separation step through an elective membrane.

EFFECT: improvement of the current urea production process.

9 cl, 1 dwg

FIELD: chemistry.

SUBSTANCE: anti-photobleaching additive is polyester-modified polysiloxane, methyl ether of polyethylene glycol, or polyoxyethylenesorbitan. The anti-photobleaching additive is selected to reduce photobleaching while maintaining the photocatalytic activity of the composition to at least 90%. In the photocatalytic composition, the said additive is present in a series of 1-35 vol.%. The photobleaching index (AL) of the said composition is less than 6. A photocatalytic coating, a building panel, and a method for applying a photocatalytic composition are also described.

EFFECT: obtaining a composition with reduced photobleaching and with the stored photocatalytic activity.

25 cl, 10 dwg, 3 tbl, 6 ex

FIELD: transportation.

SUBSTANCE: method involves transporting the polymer to a polymer storage container along a supply line using a carrier medium. The container is a container for the seed layer for the gas phase polymerization process. Then, at least a portion of the polymer in the container is recirculated by means of recovering the polymer from the container and supplying the recovered polymer to said supply line. Recycling is carried out simultaneously with transportation. During the transportation and recycling, cooling the polymer to a temperature not exceeding 50C is provided.

EFFECT: expanding the range of technological tools.

14 cl, 3 dwg

FIELD: petroleum processing.

SUBSTANCE: petroleum feedstock hydrocracking catalyst is prepared by compounding zeolite Y with aluminonickel(cobalt)-molybdenum(tungsten) oxide system. Specifically, low-alkalinity zeolite Y having silicate modulus 5.5-7.0 and crystallinity at least 70% is mixed with aluminum hydroxide having pseudoboehmite structure in proportion (1-9):1. Thus obtained mix is molded, dried, and calcined under water steam atmosphere to give molded thermally treated zeolite. The latter is impregnated with aqueous Ni(Co) and Mo(W) salt solutions or ground and compounded with aluminonickel(cobalt)-molybdenum(tungsten) oxide system by mixing with aluminum hydroxide and Ni(Co) and Mo(W) salts, after which follow molding and impregnation with aqueous Ni(Co) and Mo(W) salt solutions.

EFFECT: expanded catalyst preparation possibilities.

2 cl, 5 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: unsupported catalyst composition for hydrocracking contains one or more group VIb metals, one or more group VIII base metals, one or more zeolites and optionally heat-resistant oxide material. The said composition is obtained through deposition of group VIb metals, group VIII base metals and optionally heat-resistant oxide material in the presence of a zeolite. The method of preparing the said catalyst composition, in which one or more compounds of group VIb metals are combined with one or more compounds of group VIII base metals, and with zeolite, in the presence of a proton-containing liquid and an alkaline compound, and the catalyst composition is extracted after deposition.

EFFECT: obtaining a catalyst composition with very high activity during hydrogenation of monoaromatic compounds, significantly better selectivity towards middle distillate products.

15 cl, 13 ex, 4 tbl

FIELD: oil and gas production.

SUBSTANCE: invention refers to certain catalytic compositions and processes used for decreasing of sulphur derivatives, usually found in a petrol fraction of liquid-phase catalytic cracking processes. The invention represents a cracking catalyst composition containing zeolite or a component containing zeolite, containing Na2O in amount 0.3 wt % or less combined with a component containing Lewis acid, and a cracking catalyst composition contains Na2O in number of 0.2 % or less, and a component containing Lewis acid within 3 to 75 wt %. Besides the invention involves an advanced method of catalytic cracking of raw hydrocarbons containing organic sulphur derivatives, involves a method for decreasing of sulphur content in gasoline and a method for preparing the cracking catalytic composition.

EFFECT: it is established that amount of sulphur compounds in hydrocarbon supplied at the stage of liquid-phase catalytic cracking can be decreased by at least 15% in comparison with effect of the same composition not containing a component comprising.

59 cl, 14 tbl, 8 dwg, 5 ex

FIELD: process engineering.

SUBSTANCE: invention relates to petrochemistry, particularly, to production of zeolite-based catalyst for alkylation of isobutane by olefins and may be used in oil processing. Invention covers catalyst of alkylation of isobutane by zeolite-based olefins that contains aluminium oxide and silicon dioxide at silicon dioxide-to-aluminium oxide molar ratio equal to 2.8-7.0, sodium oxide, rare-earth element, oxides of active metals, which contains oxides of platinum and/or palladium and/or rhenium and/or ruthenium at the following ratio of components, in wt %: sodium oxide - 0.26-0.8, calcium oxide - 0.8-4.2, rare earth element oxide - 12.0-20.0,oxides of platinum and/or or palladium and/or molybdenum and/or nickel and/or cobalt - 0.02-2.0, zeolite with SiO2/Al2O3 equal to 2.8-7.0, making the rest. It covers also two versions of the method of catalyst production comprising zeolite treatment by water solutions of salts of calcium, rare earth element and ammonium at increased temperature and pressure of saturated vapors for time period required for conversion of zeolite into rare-earth calcium zeolite, its washing, drying and calcinating. In compliance with this method, first, rare-earth calcium zeolite is impregnated with unipolar water unless air escapes from zeolite pores and, then, processing is performed by impregnation with water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or molybdenum and/or nickel and/ or cobalt taken in amount that ensures said content of metal oxide in finished catalyst. It comprises also drying, calcinating, or applying on rare-earth metal calcium zeolite of water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or molybdenum and/or nickel and/or cobalt. The process includes two stages: first, cold impregnation at not over 30C, and, second, at, at least, 70C, and finally drying, tabletting and calcinating.

EFFECT: increase in catalyst activity approximating to 100 wt %, isotope selectivity approximating to 73.5 wt %, yield of target alkyl benzene by 10-15 wt %.

16 cl, 10 ex, 2 tbl

FIELD: process engineering.

SUBSTANCE: invention relates to petrochemistry, particularly, to production of zeolite-based catalyst for alkylation of isobutane by olefins and may be used in oil processing. Invention covers catalyst of alkylation of isobutane by zeolite-based olefins that contains aluminium oxide and silicon dioxide at silicon dioxide-to-aluminium oxide molar ratio equal to 2.8-7.0, sodium oxide, rare-earth element, oxides of active metals, which contains oxides of platinum and/or palladium and/or rhenium and/or ruthenium at the following ratio of components, in wt %: sodium oxide - 0.26-0.8, calcium oxide - 0.8-4.2, rare earth element oxide - 12.0-20.0, oxides of platinum and/or palladium and/or rhenium and/or ruthenium - 0.02-2.0, zeolite with SiO2/Al2O3 equal to 2.8-7.0, making the rest. It covers also two versions of the method of catalyst production comprising zeolite treatment by water solutions of salts of calcium, rare earth element and ammonium at increased temperature and pressure of saturated vapors for time period required for conversion of zeolite into rare-earth calcium zeolite, its washing, drying and calcinating. In compliance with this method, first, rare-earth calcium zeolite is impregnated with unipolar water unless air escapes from zeolite pores and, then, processing is performed by impregnation with water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or rhenium and/or ruthenium taken in amount that ensures said content of metal oxide in finished catalyst. It comprises also drying, calcinating, or applying on rare-earth metal calcium zeolite of water solutions of salts of oxides of active metals, which contains oxides of platinum and/or palladium and/or rhenium and/or ruthenium in unipolar water taken in amount that ensures aforesaid content of metal oxide in finished catalyst, drying, tabletting and calcinating.

EFFECT: increase in catalyst activity to 100 wt %, in isooctane selectivity to 75,7 wt % and in yield of target alkyl benzene by 10-15 wt %.

14 cl, 10 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to petrochemistry, particularly to production of a zeolite-based catalyst for alkylation of isobutane with olefins and can be used in oil refining industry. Described is a zeolite-based catalyst for alkylation of isobutane with olefins which contains aluminium oxide and silicon dioxide with molar ratio of silicon dioxide to aluminium oxide equal to 2.8-7.0, sodium and rare-earth element oxides and active metal oxides in form of platinum oxide and/or palladium oxide and/or rhenium oxide and/or rhodium oxide and/or halogen - chlorine or fluorine, with the following ratio of components in wt %: sodium oxide 0.26-0.8, calcium oxide 0.8-4.2, rare-earth element oxide 12.1-20.0, platinum oxide and/or palladium oxide and/or rhenium oxide and/or rhodium oxide 0.02-2.0, and/or chlorine 0.05-0.8 and/or chlorine 0.005-0.5, a zeolite with ratio SiO2/Al2O3 equal to 2.8-7.0 being the balance. Disclosed also are two versions of the method of producing a zeolite-based catalyst for alkylation of isobutane with C2-C4 olefins, involving treatment thereof with aqueous solutions of salts of calcium, a rare-earth element and ammonium at high temperature and pressure of saturated vapour for a period of time necessary to convert the zeolite into a rare-earth calcium zeolite, and depositing active metal oxides onto it by saturation with aqueous solutions containing active metals, followed by washing, drying and calcination, where at the beginning, the obtained rare-earth calcium zeolite is saturated with unipolar water until the release of air from zeolite pores stops, and then depositing active metal oxides: platinum oxide and/or palladium oxide and/or rhenium oxide and/or rhodium oxide and/or halogen - chlorine or fluorine, taken in amounts which ensure said content of the oxide of the corresponding metal and halogen in the ready product, or deposition of active metal oxides - platinum oxide and/or palladium oxide and/or rhenium oxide and/or rhodium oxide and/or halogen - chlorine or fluorine - onto the rare-earth calcium zeolite is carried out from solutions containing the corresponding metals or halogen in unipolar water, taken in amounts which ensure said content of oxide of the oxide of the corresponding metal in the ready catalyst, wherein in both versions, deposition of active metals and halogen is carried out in two steps: at the first step via cold saturation at temperature not higher than 30C for 1 hour, at the second step - at temperature not lower than 70C for 1 hour, after which treatment with an organic acid is carried out in the presence of 30% aqueous hydrogen peroxide solution, followed by drying, tableting and calcination. Described is a method for liquid-phase alkylation of isobutane with olefins in the presence of the catalyst described above.

EFFECT: longer stable operation of the catalyst with activity thereof up to almost 100 wt % and isooctane selectivity of up to 75,7 wt %.

20 cl, 10 ex, 2 tbl

FIELD: chemistry.

SUBSTANCE: invention relates to hydrofining catalysts. Described is a bead catalyst for hydrofining oil fractions, which consists of an aluminium oxide support, active components - molybdenum, nickel or cobalt compounds in form of oxides and/or sulphides and, optionally, additional zeolite Y in hydrogen form, which is in form of spherical or elliptical granules, characterised by that the catalyst granules have packed density of 0.4-0.5 g/ml and pore volume of not less than 1.2 ml/g. Described is a method of preparing said catalyst, involving peptisation of the starting powder - an aluminium oxide source with aqueous solution of an organic acid to obtain a pseudo-sol, moulding the obtained pseudo-sol in ammonia solution, drying and calcination of the support with subsequent embedding of active components therein, with optional embedding of zeolite Y in hydrogen form, drying and calcination of the catalyst in an air current, wherein the starting powder - aluminium oxide source used is weakly crystalline pseudo-boehmite; peptisation thereof is carried out using aqueous solution of an organic acid with concentration of 1-15 wt % and granulation (moulding) is carried out by drip moulding with the solid to liquid ratio in the pseudo-sol of not less than 1:2 and pH of the ammonia solution of not less than 11.0.

EFFECT: high activity, selectivity and stability of the catalyst.

3 cl, 1 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: described is a bead cracking catalyst which contains 10-35 wt % fine zeolite ReHY, 30-80 wt % kaolin and 60-5 wt % aluminium oxide, the source of which is a mixture of components of thermally activated aluminium oxide and basic aluminium chloride in weight ratio of 1:(0.25-0.95). Described is a method of producing said catalyst.

EFFECT: high catalytic activity.

2 cl, 1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to the oil-refining and petrochemical industry and specifically to preparation of catalysts for heavy catalytic cracking of oil fractions for producing C2-C4 olefins and high-octane gasoline. The invention particularly relates to a microsphere cracking catalyst obtained from a suspension which contains, based on dry residue, 25-35 wt % fine zeolite ReHY, 30-40 wt % kaolin, 25-44 wt % aluminium oxide sources and 1-10 wt % fine silicon dioxide. The invention also relates to a method of producing a microsphere cracking catalyst, which includes steps of preparing a suspension of fine zeolite ReHY, kaolin, aluminium oxide sources and fine silicon dioxide with concentration of the suspension, based on dry residue, of 450-600 g/l, moulding by spraying the suspension in a medium of flue gases at temperature of 140-170C and calcining the obtained microspheres at temperature of 550-650C in a revolving calcining furnace.

EFFECT: obtaining a microsphere cracking catalyst with high wear-resistance and catalytic activity.

4 cl, 1 tbl, 5 ex

FIELD: chemistry.

SUBSTANCE: invention relates to oil refining, particularly catalysts for hydroisomerisation of oil stock. The disclosed catalyst includes a hydrogenating metal component on a support comprising zeolite and aluminium oxide. The hydrogenating metal component used is base metals Ni, Mo, W or mixtures thereof and noble metals Pd and Ir, and the zeolite is a mixture of medium-pore zeolite TSVN with a pentasil structure and a wide-pore ultrastable zeolite USY. Content of acidic sites in the disclosed catalyst is in the range of 400-600 mcmol/g. The catalyst further contains a boron oxide or phosphorus oxide promoter. The disclosed catalyst has the following ratio of components, wt %: base metals - 7-12, noble metals - 0.1-1.0; zeolite mixture - 60-70; promoter - 0.5-4.0; aluminium oxide - up to 100. The invention also relates to a method for hydroisomerisation of oil stock in the presence of said catalyst.

EFFECT: disclosed catalyst and method for isomerisation of oil stock using said catalyst enable to obtain high-quality winter and arctic grade diesel fuels with high output.

5 cl, 2 tbl, 4 ex

FIELD: petrochemical processes.

SUBSTANCE: high-octane fuels and propane-butane fraction are obtained via conversion of hydrocarbon feedstock on contact with hot catalyst placed in reactor, into which diluting gas is supplied at elevated pressure. Catalyst is Pentasil-type zeolite with general formula xM2/nO,xAl2O3,ySiO2,zMe2/mO wherein M represents hydrogen and/or metal cation, Me group II or VII metal, n is M cation valence, m is Me metal valence, x, y, z are numbers of moles of Al2O3, SiO2, and Me2/mO, respectively, and y/x and y/z ratios lie within a range of 5 to 1000. Metal oxide Me2/mO is formed during calcination, in presence of oxygen, of Me-containing insoluble compound obtained in zeolite reaction mixture.

EFFECT: increased octane number of gasoline fractions with propane-butane fraction as chief component of gas products, and prolonged inter-regeneration time of catalyst.

11 cl, 4 dwg, 3 tbl, 16 ex

FIELD: petrochemical processes.

SUBSTANCE: alkylation is carried out at 250-425°C, pressure 0.1 to 2.5 MPa, benzene/ethylene molar ratio 1-5, and volume flow rate of raw material 0.5 to 3.5 h-1 in presence of spherical zeolite-containing catalyst having following composition: 5-55 wt % high-silica ZSM-5-type zeolite with silica/alumina molar ratio 20-150 and 45-95 wt % amorphous aluminosilicate carrier. Chemical analysis of catalyst, wt %: aluminum oxide 3.0-9.5, rare-earth element oxides 0.4-5, calcium oxide 1.0-5.0, sodium oxide 0.1-0.6, silicon oxide - the balance.

EFFECT: increased yield of ethylbenzene and alkylation selectivity.

2 cl, 1 tbl, 5 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: method of preparing catalyst based on high-silica zeolite comprises calcination of zeolite and treating it with ammonium salt solutions at 120-150°C followed by mixing with binder, drying, and calcination. High-silica zeolite utilized is ZSM-5 zeolite, which is treated with aqueous ammonium solutions at equivalent ratio NH4+:Na+ = (1.5-2.9):1.0 to degree of Na+ cation substitution above 99%.

EFFECT: increased catalytic activity and selectivity in benzene-ethylene alkylation process.

1 tbl, 7 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: method of preparing catalyst based on high-silica zeolite comprises calcination of zeolite and treating it with ammonium salt solutions at 160-200°C followed by mixing with binder, drying, and calcination. High-silica zeolite utilized is ZSM-5 zeolite, which is treated with aqueous ammonium solutions until degree of Na+ cation substitution above 99% is attained.

EFFECT: increased catalytic activity and selectivity in benzene-ethylene alkylation process.

1 tbl, 6 ex

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