Method of production of catalyst for conversion of carbon oxide

FIELD: production of catalysts on base of compounds of copper, zinc and aluminum for low-temperature conversion of carbon oxide with water steam; chemical, and petrochemical industries; production of ammonia and hydrogen.

SUBSTANCE: proposed method consists in mixing the solution of ammonia-carbonate complex of copper with solution of ammonia-carbonate complex of zinc and with oxide or hydroxide of aluminum; suspension thus obtained is heated to 40-50°C, then it is subjected to stirring continued for 1-2 h, after which temperature is raised to 85-97°C and purge gas is introduced, for example nitrogen or carbon dioxide and suspension is mixed at solid-to-liquid ratio of 1:(2.0-4.0); sediment is removed; mixture is dried, calcined and liquid stabilizing additives are introduced into calcined mass at solid-to-liquid ratio of 1: (0.2-1.0) and 1-1.5 mass-% of graphite is added; mixture is stirred, granulated and pelletized. Used as stabilizing additives are chromic, nitric or oxalic acids, or their salts, or carbamide.

EFFECT: enhanced activity and thermal stability.

2 cl, 1 tbl, 20 ex

 

The invention relates to a process for the preparation of catalysts based on copper compounds, zinc, aluminum for low-temperature conversion of carbon monoxide with water vapor and can be used in the chemical and petrochemical industry, for example, in the production of ammonia and hydrogen.

A known method of producing a catalyst for the conversion of carbon monoxide on the basis of the oxides of copper and zinc by adding zinc oxide to a solution of ammonium carbonate complex of copper, followed by evaporation, drying at 150°, grinding, pelletizing and activation of gas-vapor mixture at a temperature of 160-170°With (SU # 184818, B 01 J 37/00, 1965).

The disadvantage of this method is the heterogeneity of the contact mass, which leads to insufficient high activity of the catalyst.

Also known is a method of obtaining copper-zinc-aluminum catalyst for carbon monoxide conversion by mixing the oxide or aluminum hydroxide with zinc oxide and ammonium carbonate complex of copper with subsequent drying, calcination catalytic mass and molding. The alumina before the mixture is dispersed in an aqueous ammonia solution prior to the formation of aluminum hydroxide, then mixed with other components and add ammonium molybdate, the mixture is dispersed to the complete removal of ammonia, 5-15 wt.% received catalitic the Russian mass is stirred with an aqueous solution of polyvinyl alcohol powder, obtained by annealing the rest of the catalytic mass. (SU # 1524920, B 01 J 37/04, 1987).

However, the catalyst obtained by this method has poor activity.

The closest in technical essence and the achieved result is a method for preparing a catalyst for carbon monoxide conversion by mixing a solution of ammonium carbonate complex of copper with zinc oxide and aluminum oxide or aluminum hydroxide at a weight ratio of copper ammonium carbonate complex to the amount of zinc compounds and aluminum is 1:0,25-0,80, and mixing is carried out at 55-110°C, pH 13-7, followed by drying the catalyst mass at 110-120°C, annealing at 300-500°and pelletizing (SU # 596278, MKI B 01 J 37/04, 1976).

The disadvantages of this method of obtaining consist in the following.

Analysis of the phase composition showed that after mixing the components is not calcined mass consists of the phase of the basic copper carbonate, basic zinc carbonate, partly replaced by copper, and aluminum hydroxide modification type "gibbsite". During annealing the basic copper carbonate is decomposed with the formation of copper oxide, basic zinc carbonate, enriched with copper, collapses to a solid solution of copper oxide to zinc oxide and partial oxide of copper, aluminum hydroxide decomposes to "boehmite". the system obtained after calcinations, the active component is copper oxide is in different versions: free, stable in the solid solution and partially stabilized zinc oxide. Free copper oxide is easily sintered, being consolidated, which leads to loss of activity and thermostability. The calcined mass on this technology bad tabletroute.

The objective of the invention is to develop a method of producing catalyst based on copper compounds, zinc, aluminum, to ensure its high activity and stability.

This object is achieved in that the mixed solutions of ammonium carbonate complexes of copper and zinc oxide or aluminum hydroxide, the resulting suspension is heated to 40-50°C, stirred for 1.0 to 2.0 hours, raise the temperature to 85-97°serves purge gas, for example nitrogen or carbon dioxide, stirred suspension when the mass ratio of solid: liquid = 1:(2,0-4,0), the precipitate is separated, is dried at a temperature of 90-110°C, calcined at a temperature of 270-400°in the calcined mass injected liquid stabilizing additives when the mass ratio of solid: liquid = 1:(0.2 to 1.0), and 1.0-1.5% graphite by weight of the calcined mass, mix, granularit and tabletirujut.

As a liquid stabilizing additives take the rum, or nitrogen, or oxalic acid, or their salts, or urea.

The invention consists in the following.

When mixed solution of ammonium carbonate complex of copper with a solution of ammonium carbonate complex of zinc oxide or aluminum hydroxide, followed by heating the suspension up to 40-50°and stirring for 1-2 hours small portion of the aluminum present in the solution in the form of ions Al+++. Further temperature increase up 85-97°leads to the destruction of ammonium carbonate complexes of copper and zinc. Not calcined mass contains basic zinc carbonate enriched with copper and aluminum, and aluminum hydroxide. Carbonate basic copper x-ray phase analysis is not detected. To intensify the decomposition process is provided for the supply of purge gas, for example carbon dioxide or nitrogen, and maintaining a constant mass ratio of solid: liquid. The latter affects the dispersion of the mass, this in turn determines the high activity of the catalyst. During annealing the basic zinc carbonate enriched with copper and aluminum, collapses to the solid solution of copper oxide to zinc oxide and partial oxide copper-enriched aluminum and aluminum hydroxide decomposes to "boehmite". Thus, in the system, obtained after annealing the active to the ponent - the copper oxide is in a different modifications: stable in solid solution with zinc oxide and partially stabilized zinc oxide and aluminum. Free, easy sintered copper oxide x-ray phase analysis was not detected. The dispersion of the bound copper oxide in contrast to the known method higher (crystallite size 60-90 Åinstead of 120 Å prototype), which leads to high activity and thermal stability of the proposed catalyst. The introduction of liquid stabilizing additives in the calcined mass leads to their interaction with the surface with the formation of more complex compounds, stabilizing the active ingredient is copper oxide. With the introduction of the liquid stabilizing additives - chromium, or nitrogen, or oxalic acids or their salts, or urea retained high activity and thermal stability of the finished product and in some cases increases its thermostability.

Supplementation with graphite leads to a homogeneous plastic mass, and the introduction of graphite on stage tabletting helps improve the tabletting process.

The proposed method is as follows.

In a reactor with a stirrer and heating is filled with a solution of ammonium carbonate complex of copper (MACR) and a solution of ammonium carbonate complex of zinc (the AKP) and paid the required amount of oxide or hydroxide of aluminum. At this stage, the preparation of solutions determine the mass ratio of copper oxide to zinc oxide (CuO/ZnO) and the mass ratio of the amount of copper oxide and zinc oxide to aluminum oxide ((CuO+ZnO):Al2About3to control the chemical and phase composition of the catalyst. The resulting suspension is heated to 40-50°C, stirred for 1-2 hours. Next, raise the temperature in the reactor to 85-97°serves purge gas, for example nitrogen or carbon dioxide, stirred suspension when the mass ratio of solid: liquid =1:(2,0-4,0). The precipitate is separated, is dried at a temperature of 90-110°and calcined at a temperature of 270-400°C. Then calcined mass is loaded into the mixer, add the stabilizing additives - chromium, or nitrogen, or oxalic acid, or their salts, or urea in a weight ratio of solid: liquid =1:(0.2 to 1.0), and 1-1 .5% wt. graphite by weight of the calcined mass, mix, granularit, mixed with graphite and tabletirujut.

The proposed method is illustrated by the following examples.

Example No. 1. In a reactor with a stirrer and heated pour 1100 liters makrya with the content of CuO - to 136.4 g/l, NH3- 140 g/l2- 100 g/l and 2300 liters Cakra with the content of ZnO - 130 g/l, NH3- 140 g/l, CO2- 100 g/l, add 50 kg of aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at t is mperature 45° C for 1.5 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 8.4 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2,5 to a residual content of CuO in the solution to 0.8 7 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°C and annealed at 310°C. the Calcined mass of 100 kg is loaded into the mixer and add 40 kg of a solution of chromic acid (10% wt. - concentration) at a mass ratio of solid: liquid =1:0.4 and 1.5 kg of graphite, the mass is stirred at a temperature of 80°C to a residual moisture content of 1.8 wt.%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 29,20

ZnO - 58,41

Al2O3- 9,73

Cr2About3- 2,66

Example No. 2. In a reactor with a stirrer and heated pour 1100 liters makrya with the content of CuO - to 136.4 g/l, NH3- 140 g/l2- 100 g/l and 2300 liters Cakra with the content of ZnO -130 g/l, NH3- 140 g/l2- 100 g/l, add 50 kg of aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at a temperature of 40°C for 1.8 hours, then raise the temperature in the reactor to 92°C. Serves the purge gas is nitrogen with a flow rate of 8.4 m3/h and stirred suspense is th at a constant mass ratio of solid: liquid =1:2,5 to a residual content of CuO in the solution to 0.8 g/L. This forms a precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 320°C. the Calcined mass of 100 kg is loaded into the mixer and add 40 kg of a solution of chromic acid (10% wt. - concentration) at a mass ratio of solid: liquid =1: 0.4 and 1.0 kg of graphite, the mass is stirred at a temperature of 85°C to a residual moisture content of 1.8 wt.%, granularit, mixed with 2.0 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 29,20

ZnO - 58,41

Al2O3- 9,73

Cr2O3- 2,66

Example No. 3. In a reactor with a stirrer and heated pour 1100 liters makrya with the content of CuO - to 136.4 g/l, NH3- 140 g/l2- 100 g/l and 2300 liters Cakra with the content of ZnO -130 g/l, NH3- 140 g/l2- 100 g/l, add 78 kg of aluminum hydroxide (modification - "boehmite"). The resulting suspension is stirred at a temperature of 45°C for 2 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 8.4 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:3,5 to a residual content of CuO in the solution to 0.8 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 90°and calcined at 350°C. the Calcined mass of 100 kg, download the up in the mixer and add 40 kg of a solution of chromic acid (10% wt. - concentration) at a mass ratio of solid: liquid =1:0.4 and 2.0 kg of graphite, the mass is stirred at a temperature of 90°C to a residual moisture content of 1.8 wt.%, granularit, mixed with 1.0 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 29,20

ZnO - 58,41

Al2O3- 9,73

Cr2O3- 2,66

Example No. 4. In a reactor with a stirrer and heated pour 900 liters makrya with the content of CuO - 150 g/l, NH3- 135 g/l2- 105 g/l and 2400 liters Cakra with the content of ZnO - 130 g/l, NH3- 135 g/l, CO2- 105 g/l, add 55 kg aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at a temperature of 50°C for 1 hour, then raise the temperature in the reactor to 93°C. Serves purge gas is carbon dioxide with a flow rate of 11 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2.0 to a residual content of CuO in a solution of 0.5 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 320°C. the Calcined mass of 100 kg is loaded into the mixer and add 32 kg of a solution of bichromate of copper (8% wt. - concentration) at a mass ratio of solid: liquid =1:0.4 and 1.5 kg of graphite, the mass is stirred at a temperature of 90°C to a residual moisture content of 2.7 wt.%, granular is, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 26,41

ZnO - 61,03

Al2O3- 10,76

Cr2O3- 1,80

Example No. 5. In a reactor with a stirrer and heated pour 900 liters makrya with the content of CuO - 150 g/l, NH3- 135 g/l2- 105 g/l and 2 400 litres Cakra with the content of ZnO - 130 g/l, NH3- 135 g/l2- 105 g/l, add 89,5 kg of aluminum hydroxide (modification - "gibbsite"). The resulting suspension is stirred at a temperature of 50°C for 2 hours, then raise the temperature in the reactor to 87°C. Serves purge gas is carbon dioxide with a flow rate of 11 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:3,0 to a residual content of CuO in a solution of 0.5 g/l thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°C and annealed at 310°C. the Calcined mass of 100 kg is loaded into the mixer and add 32 kg of a solution of bichromate of copper (8% wt. - concentration) at a mass ratio of solid: liquid =1: 0.4 and 1.0 kg of graphite, the mass is stirred at a temperature of 87°C to a residual moisture content of 2.7 wt.%, granularit, mixed with 2 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 26,41

ZnO - 61,03

Al2O3- 10,76

Cr2O3- 1,80

Example No. 6. Reactor with a stirrer and heated pour 1200 litres makrya with the content of CuO - 137,5 g/l, NH3- 140 g/l2- 100 g/l and 2 400 litres Cakra with the content of ZnO - 130 g/l, NH3- 140 g/l2- 100 g/l, add 40 kg of aluminum oxide (modification γ - Al2O3). The resulting suspension is stirred at a temperature of 45°C for 2 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 10.3 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2.0 to a residual content of CuO in the solution to 0.2 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°C and annealed at 270°C. the Calcined mass of 100 kg is loaded into the mixer and add 45 kg of a solution of bichromate zinc (9% wt. - concentration) at a mass ratio of solid: liquid =1:0.5 and 1.5 kg of graphite, the mass is stirred at a temperature of 90°C to a residual moisture content of 2.2 wt.%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 32,17

ZnO - 57,53

Al2About3- 7,80

Cr2O3- 2,50

Example No. 7. In a reactor with a stirrer and heated pour 1200 litres makrya with the content of CuO - 137,5 g/l, NH3- 140 g/l2- 100 g/l and 2 400 litres Cakra with the content of ZnO - 130 g/l, NH3- 140 g/l2- 100 g/l, add 62,5 kg of aluminum hydroxide (mo is eficacia "boehmite"). The resulting suspension is stirred at a temperature of 40°C for 1.5 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 10.3 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:4,0 to a residual content of CuO in the solution to 0.2g/l. This forms a precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 300°C. the Calcined mass of 100 kg is loaded into the mixer and add 45 kg of a solution of bichromate zinc (9% wt. - concentration) at a mass ratio of solid: liquid =1:0.5 and 1.5 kg of graphite, the mass is stirred while heating to 85°C to a residual moisture content of 2.2 wt.%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 32,17

ZnO - 57,53

Al2About3- 7,80

Cr2O3- 2,50

Example No. 8. In a reactor with a stirrer and heated pour 1200 litres makrya with the content of CuO - 137,5 g/l, NH3- 140 g/l2- 100 g/l and 2300 liters Cakra with the content of ZnO - 128,3 g/l, NH3- 140 g/l, CO2- 100 g/l, add 40 kg of aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at a temperature of 45°C for 1 hour, then raise the temperature in the reactor to 85°C. Serves about ovocny gas carbon dioxide with a flow rate of 9.6 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2.0 to a residual content of CuO in the solution to 0.8 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°and calcined at 350°C. the Calcined mass of 100 kg is loaded into the mixer and add 20 kg of a solution of nitric acid (7% wt. - concentration) at a mass ratio of solid: liquid =1:0.2 and 15 kg of graphite, the mass is stirred at a temperature of 90°C to a residual moisture content of 1.7 wt.%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 33,00

ZnO - 59,00

Al2About3- 8,00

Example No. 9. In a reactor with a stirrer and heated pour 1200 litres makrya with the content of CuO - 137,5 g/l, NH3- 140 g/l, CO2- 100 g/l and 2300 liters Cakra with the content of ZnO - 128,3 g/l, NH3- 140 g/l2- 100 g/l, add 62,5 kg of aluminum hydroxide (modification "boehmite"). The resulting suspension is stirred at a temperature of 40°C for 2 hours, then raise the temperature in the reactor to 87°C. Serves purge gas is carbon dioxide with a flow rate of 9.6 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:3.7 to a residual content of CuO in the solution to 0.8 g/L. thus formed sieges is to, which is separated from liquid (mother liquor). The precipitate is dried at 110°and calcined at 350°C. the Calcined mass of 100 kg is loaded into the mixer and add 20 kg of a solution of nitric acid (7% wt. - concentration) at a mass ratio of solid: liquid =1: 0.2 and 1.5 kg of graphite, the mass is stirred at a temperature of 90°C to a residual moisture content of 1.7 wt.%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 33,00

ZnO - 59,00

Al2About3- 8,00

Example No. 10. In a reactor with a stirrer and heated pour 2 000 litres makrya with the content of CuO - 140 g/l, NH3- 130 g/l2- 110 g/l and 1300 liters Cakra with the content of ZnO - 140 g/l, NH3- 130 g/l, CO2- 110 g/l, add 50 kg of aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at 40°C for 2 hours, then raise the temperature in the reactor to 92°C. Serves purge gas is carbon dioxide with a flow rate of 10.3 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2,5 to a residual content of CuO in a solution of 0.7 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 370°C. the Calcined mass of 100 kg is loaded into the mixer and add 25 kg of a solution of nitric sour what about the iron (5,0% wt. - concentration) at a mass ratio of solid: liquid =1:0.5 and 1.0 kg of graphite, the mass is stirred at a temperature of 85°C to a residual moisture content of 1.6 wt.%, granularit, mixed with 2 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 35,69

ZnO - 53,54

Al2O3- to 9.91

Fe2About3- 0,86

Example No. 11. In a reactor with a stirrer and heated pour 2 000 litres makrya with the content of CuO - 140 g/l, NH3- 130 g/l2- 110 g/l and 1 300 liters Cakra with the content of ZnO - 140 g/l, NH3- 130 g/l2- 110 g/l, add 81,5 kg of aluminum hydroxide (modification of "gibbsite"). The resulting suspension is stirred at a temperature of 50°C for 2 hours, then raise the temperature in the reactor to 87°C. Serves purge gas is carbon dioxide with a flow rate of 10.3 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:3,5 to a residual content of CuO in a solution of 0.5 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°and calcined at 320°C. the Calcined mass of 100 kg is loaded into the mixer and add 21 kg of a solution of nitric acid iron (7.0% wt. - concentration) at a mass ratio of solid: liquid =1:0.3 and 1.5 kg of graphite, the mass is stirred at a temperature of 80°C to a residual moisture content of 3.7 wt.%, granules of the shape, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 54,29

ZnO - 35,23

Al2O3- 9,74

Fe2About3- 0,74

Example No. 12. In a reactor with a stirrer and heated pour 1700 liters makrya with the content of CuO - 150 g/l, NH3- 140 g/l2- 100 g/l and 1400 liters Cakra with the content of ZnO - 150 g/l, NH3- 140 g/l2- 100 g/l, add 50 kg of aluminum oxide (modification γ - Al2O3). The resulting suspension is stirred at 40°C for 1.5 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 10.7 m3per hour, stirred suspension at a constant mass ratio of solid: liquid =1:2.0 to a residual content of CuO in a solution of 0.9 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 350°C. the Calcined mass of 100 kg is loaded into the mixer and add 50 kg of a solution of oxalic acid (5% wt. - concentration) in a mass ratio of solid: liquid =1:1 and 1.0 kg of graphite, the mass is stirred at a temperature of 80°C to a residual moisture content of 1.3 wt.%, granularit, mixed with 2 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 49,50

ZnO - 40,80

Al2O3- 9,70

Example No. 13. In a reactor with a stirrer, bogre the Ohm pour 1700 liters makrya with the content of CuO - 150 g/l, NH3- 140 g/l, CO2- 100 g/l and 1400 liters Cakra with the content of ZnO - 150 g/l, NH3- 140 g/l2- 100 g/l, add 81,5 kg of aluminum hydroxide (modification of "gibbsite"). The resulting suspension is stirred at a temperature of 45°C for 2 hours, then raise the temperature in the reactor to 92°C. Serves purge gas is carbon dioxide with a flow rate of 10.7 m3per hour, stirred suspension at a constant mass ratio of solid: liquid =1:4,0 to a residual content of CuO in a solution of 0.9 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 100°and calcined at 350°C. the Calcined mass of 100 kg is loaded into the mixer and add 50 kg of a solution of oxalic acid (5% wt. - concentration) in a mass ratio of solid: liquid =1:1 and 1.5 kg of graphite, the mass is stirred at a temperature of 90° (C) to a residual moisture content of 1.3 wt. -%, granularit, mixed with 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 49,50

ZnO - 40,80

Al2About3- 9,70

Example No. 14. In a reactor with a stirrer and heated pour 1500 liters makrya with the content of CuO - 150 g/l, NH3- 135 g/l2- 105 g/l and 2100 liters Cakra with the content of ZnO - 107,1 g/l, NH3- 135 g/l, CO2- 105 g/l add 50 kg of aluminum oxide (modification γ - Al2O3). Polucheno.sostoyanie stirred at a temperature of 40° C for 1 hour, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 8.2 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:3,0 to a residual content of CuO in the solution to 1.0g/l. This forms a precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 90°and calcined at 300°C. the Calcined mass is mixed with 40 kg of solution of aluminium (10% wt. - concentration) in a mass ratio of solid: liquid =1:0.4 and 1.0 kg of graphite, is stirred at a temperature of 90°C to a residual moisture content of 4.1 wt.%, granularit, mixed with 2.0 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 48,75

ZnO - 40,19

Al2About3- 11,06

Example No. 15. In a reactor with a stirrer and heated pour 1000 liters makrya with the content of CuO - 150,0 g/l, NH3- 140 g/l2- 100 g/l and 2,000 liters Cakra with the content of ZnO - 150,0 g/l, NH3- 140 g/l2- 100 g/l, add 81,5 kg of aluminum hydroxide (modification of "gibbsite"). The resulting suspension is stirred at a temperature of 50°C for 2 hours, then raise the temperature in the reactor to 93°C. Serves purge gas is carbon dioxide with a flow rate of 10 m3per hour, stirred suspension at a constant mass ratio of solid: liquid =:3.5 to a residual content of CuO in a solution of 0.1 g/L. The resulting precipitate was separated from the liquid phase, dried at 95°C and annealed at 310°C. the Calcined mass of 100 kg is loaded into the mixer and add 40 kg of a solution of oxalic acid aluminum (concentration of 5% wt.) when the mass ratio of solid: liquid =1:0.4 and 1.5 kg of graphite, the mass is stirred at a temperature of 95°C to a residual moisture content of 1.0 wt.%, granularit add 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 29,48

ZnO - 5 8,98

Al2O3- 11,54

Example No. 16. In a reactor with a stirrer and heated pour 2000 liters makrya with the content of CuO - 140 g/l, NH3- 140 g/l2- 100 g/l and 1 300 liters Cakra with the content of ZnO - 140 g/l, NH3- 140 g/l2- 100 g/l, add 25 kg aluminum oxide (modification γ - Al2O3). The resulting suspension is stirred at a temperature of 45°C for 1.5 hours, then raise the temperature in the reactor to 85°C. Serves purge gas is carbon dioxide with a flow rate of 7 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:2.0 to a residual content of CuO in the solution to 0.2 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 95°and calcined at 400°C. the Calcined mass of 100 kg is loaded into the mixer and add 22 christwire urea (concentration - 4.5% wt.) when the mass ratio of solid: liquid =1:0.5 and 1.5 kg of graphite, the mass is stirred at a temperature of 95°C to a residual moisture content of 3.4 wt.%, granularit add 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 57,50

ZnO - 37,40

Al2O3- 5,10

Example No. 17. In a reactor with a stirrer and heated pour 2000 liters makrya with the content of CuO - 140 g/l, NH3- 140 g/l, CO2- 100 g/l and 1300 liters Cakra with the content of ZnO - 140 g/l, NH3- 140 g/l2- 100 g/l, add 41 kg of aluminum hydroxide (modification - "gibbsite"). The resulting suspension is stirred at a temperature of 50°C for 2 hours, then raise the temperature in the reactor to 90°C. Serves purge gas is carbon dioxide with a flow rate of 7 m3per hour and is stirred suspension at a constant mass ratio of solid: liquid =1:4,0 to a residual content of CuO in the solution to 0.2 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 95°and calcined at 400°C. the Calcined mass of 100 kg is loaded into the mixer and add 22 kg of urea solution (concentration of 4.5% wt.) when the mass ratio of solid: liquid =1:0.5 and 1.5 kg of graphite, is stirred at a temperature of 90°C to a residual moisture content of 3.4 wt.%, granularit add 1.5 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 57,50

ZnO - 37,40

Al2O3- 5,10

Example 18 (comparative). In a reactor with a stirrer and heated pour 1 500 litres makrya with the content of CuO - 150 g/l, NH3- 140 g/l, CO2- 100 g/l and 2100 liters Cakra with the content of ZnO - 107,1 g/l, NH3- 140 g/l2- 100 g/l, add 89 kg aluminum oxide (modification γ - Al2About3). The resulting suspension is stirred at a temperature of 40°C for 1 hour, then raise the temperature in the reactor to 97°C. Serves purge gas is carbon dioxide, stirred suspension at a constant mass ratio of solid: liquid =1:3 to a residual content of CuO in a solution of 0.7 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°and calcined at 300°C. the Calcined mass of 100 kg is loaded into the mixer, stirred at a temperature of 90°C to a residual moisture content of 4.3 wt.%, granularit, add 2 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 40,90

ZnO - 40,90

Al2About3- 18,20

Example No. 19 (comparative). In a reactor with a stirrer and heated pour 1500 liters makrya with the content of CuO - 150 g/l, NH3- 140 g/l, CO2- 100 g/l and 2100 liters Cakra with the content of ZnO - 107,1 g/l, NH3- 140 g/l, CO2- 100 g/l, add 163 kg of aluminum hydroxide (modification of "gibbsite". The resulting suspension is stirred at a temperature of 50°C for 2 hours, then raise the temperature in the reactor to 97°C. Serves purge gas is carbon dioxide, stirred suspension at a constant mass ratio of solid: liquid =1:3,0 to a residual content of CuO in a solution of 0.7 g/L. thus formed precipitate, which is separated from liquid (mother liquor). The precipitate is dried at 110°and calcined at 300°C. the Calcined mass of 100 kg is loaded into the mixer, stirred at a temperature of 90°C to a residual moisture content of 4.3 wt.%, granularit, add 2 kg of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 40,90

ZnO - 40,90

Al2About3- 18,20

Example No. 20 (prototype). In a reactor equipped with a mixer, pour 5 liters of N2Oh, is heated to 75-80°and add 2.3 liters of solution makrya with the content of CuO - 150 g/l, NH3128 g/l2- 96 g/l with a pH of 13.0. With careful stirring, poured into a solution of 140 g of aluminum hydroxide (113 g in terms of aluminum oxide) and 537 g of zinc oxide. When mixing support temperature 75-110°C. About the end of the reaction is judged by the absence of copper ions and ammonia in the filtrate and the pH of the solution is equal to 7.6-7,0. The resulting mass is dried at a temperature of 110-120°and calcined at 330-350°C. the Calcined mass in quantities of 1 kg CME is more with 20 g of graphite and tabletirujut.

Get the catalyst composition, wt.%:

CuO - 35,0

ZnO - 53,7

Al2About3- 11,3

Physico-chemical characteristics of the samples obtained by the proposed method and the prototype presented in the table.

The mass ratio of CuO/ZnO and (CuO+ZnO):Al2About3for all embodiments of the proposed method of preparation of the catalyst and the prototype are also presented in the table.

Testing of the samples on the activity in the process of conversion of CO with water vapor was conducted in a laboratory setting in the kinetic regime, far from equilibrium, under the following conditions: flow rate - 5000 hour-1; ratio of steam/gas - 0.29 to 0.31 in; the CO content in the gas and 9.8%; temperature - 140°C.

Activity was determined by the degree of conversion of carbon monoxide at 140°and thermostability of changing the degree of conversion of carbon monoxide at 140°after overheating of the sample at 350°for 2xhours.

The supply of purge gas is carbon dioxide or nitrogen in the decomposition process of hydroxocobalamin copper and zinc intensifies the formation of sludge and obtain a stable composition. In the accompanying examples, data on the supply of carbon dioxide as the purge gas, relative to the specified nitrogen example 2 for comparison, for the other examples, as in example 2, using as the PTA equivalent used purge gas the carbon dioxide and corresponds to the same physico-chemical characteristics described in examples 1-19.

The table shows that a catalyst according to the proposed method leads to high activity and thermal stability, as after overheating activity of the samples is practically unchanged, and in some cases increases in comparison with the prototype, where the activity after overheating is reduced. It should be noted that the introduced liquid stabilizing additives do not reduce the mechanical strength.

1. The method of producing catalyst for carbon monoxide conversion by mixing a solution of ammonium carbonate complex copper compounds based on zinc and aluminium, followed by drying, calcination and pelletizing, characterized in that a solution of ammonium carbonate complex of copper mixed with a solution of ammonium carbonate complex of zinc and oxide or aluminum hydroxide, the resulting suspension is heated to 40-50°C, stirred for 1-2 hours, then raise the temperature to 85-97°serves purge gas, such as nitrogen or carbon dioxide, stirred suspension when the mass ratio of solid:liquid = 1:(2,0-4,0), the precipitate is separated, dried, calcined and the calcined mass injected liquid stabilizer is the following additives in the mass ratio of solid:liquid, equal to 1:(0.2 to 1.0), and 1-1 .5 wt.% graphite by weight of the calcined mass, mix, granularit and tabletirujut.

2. The method according to claim 1, characterized in that as a liquid stabilizing additives take chrome, or nitrogen, or oxalic acid, or their salts, or urea.



 

Same patents:

FIELD: methods of storage of hydrogen in catalytic systems functioning on basis of cyclic hydrogenation/de-hydrogenation reactions of condensed and poly-nuclear aromatic compounds; hydrogen generators; hydrogen engines or plants.

SUBSTANCE: proposed catalytic composite material contains organic substrate as hydrogen source which is liable to hydrogenation/dehydrogenation reactions. Material contains heterogeneous catalyst including carbon or oxide carrier at high specific surface and metal of VIII (platinum) group applied on this surface at mass ratio of substrate and catalyst from 10:1 to 1000:1. Organic substrate contains the following aromatic hydrocarbons: condensed, poly-cyclic, poly-unsaturated, aromatic oligomers and polymers: biphenyl or its functional derivative, or terphenyl, or naphthalene, or anthracene, or functional derivative of one or other, polystyrene or its copolymer, polyacetylene or polycumulene. Proposed method consists in charging the composite material with hydrogen at high pressure and separation of hydrogen from it at low-pressure heating. Charging is carried out at contact of organic substrate and heterogeneous catalyst at temperature of from 50 to 180°C and hydrogen pressure of from 1 to 100 atm; separation of hydrogen is carried out at contact of hydrogenated of organic substrate with the same catalyst at temperature of from 200 to 350°C at atmospheric pressure.

EFFECT: enhanced efficiency.

9 cl, 2 dwg, 2 tbl, 7 ex

FIELD: industrial organic synthesis.

SUBSTANCE: synthesis gas, which is various-destination product, is generated in reactor with palladium-rhenium membrane at dimethyl ether-to-water ratio 1:1, elevated temperature, atmospheric pressure, and reactants supply speed 60 to 1200 h-1. Process allows achieving essentially complete conversion of dimethyl ether without any increase in pressure and at lower temperature, whereas resulting gas mixture contains no unreacted water steam, nitrogen, and carbon dioxide.

EFFECT: enhanced process efficiency.

4 tbl, 4 ex

FIELD: industrial organic synthesis.

SUBSTANCE: synthesis gas, which is various-destination product, is generated in reactor with palladium-rhenium membrane at dimethyl ether-to-water ratio 1:1, elevated temperature, atmospheric pressure, and reactants supply speed 60 to 1200 h-1. Process allows achieving essentially complete conversion of dimethyl ether without any increase in pressure and at lower temperature, whereas resulting gas mixture contains no unreacted water steam, nitrogen, and carbon dioxide.

EFFECT: enhanced process efficiency.

4 tbl, 4 ex

FIELD: chemical industry; methods of realization of the chemical transformations by compression of the gas-containing mixtures.

SUBSTANCE: the invention is pertaining to the chemical technology and may be used in chemical industry for realization of the different chemical transformations, for example, for the air nitrogen fixation or for production of the synthesis gas. The method of realization of the chemical transformations by compression of the gas-containing mixtures includes the two-stage superadiabatic compression of the reaction mixture in two successive strokes by the piston in the cylinder of the superadiabatic compression reactor divided into the main and additional chambers the transversal septum made with a possibility of the mixture bypassing. The second stage of the superadiabatic compression on each stroke is realized simultaneously with the bypassing of the reaction mixture into the additional chamber of the cylinder. At that the compression power is kept equal on the first and the second compression strokes by selection of the value of the relative volume of the additional chamber of the cylinder β = V2/(V1 + V2), where V1 is the volume of the main chamber, V2 is the volume of the additional chamber, which for the pressure of up to 300 atm should be of no less than 0.01, and the injection of the reaction mixture into the reactor is performed before the first stroke of the two-stage compression at the piston motion to the lower dead point. The simultaneous bypassing and compression of the mixture at the second stage of the superadiabatic compression on each stroke is performed at constant pressure. Before or in the beginning of the second compression stroke the component consisting out of the polyatomic molecules is introduced. At realization of the exothermal chemical transformations the heat-accumulating component with the developed surface is mounted in the additional chamber of the cylinder. The invention ensures the reliable and high-effective running of the chemical reactions.

EFFECT: the invention ensures the reliable and high-effective running of the chemical reactions.

4 cl, 1 dwg

FIELD: heat power generator operation methods comprising direct action of combustion products upon heated medium, possibly generation of heat power and supplying it through heat transfer agent to user.

SUBSTANCE: method comprises plasma-electrolytic action upon liquid for producing steam, hydrogen and oxygen. Said plasma-electrolytic action upon liquid (water) is realized in capillary-porous hydrophilic material. Then hydrogen is oxidized by means of oxygen in atmosphere of generated steam to which are added liquid and (or) gas phases whose quantity provides regulation of mixture temperature. Water-adsorbing matter is used in said capillary-porous hydrophilic material. Added phase is ejected by means of generated hydrogen, oxygen and steam; water is used as added liquid phase and inert gas is used as added gas phase.

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5 cl, 1 dwg, 1 ex

FIELD: chemical industry; reactor.

SUBSTANCE: the invention is pertaining to reactor. The method includes preparation of suspension of the finely dispersive powdery aluminum in water, creation in the reactor of pressure of the saturated water steams, sputtering of the suspension into the high-pressure reactor, withdrawal from the reactor of the mixture of the steams and hydrogen, and also withdrawal from the reactor of aluminum hydroxide or aluminum oxide into the receiving device, measuring of the temperature in the reactor, measuring of the gas mixture pressure in the reactor. Determine the partial pressure of the saturated water steam in the reactor, determine the partial pressure of hydrogen, determine the free volume of the reactor and, changing the mass of aluminum being introduced in the composition of the suspension according to the formula make adjustment of the pressure and temperatures in the reactor. The device contains: the source of the suspension of the finely-dispersed powdery aluminum with water and the mixer, the reactor, the condenser, the receiving device, the adjustable valve of the mixture withdrawal of the mixture of the water steams and hydrogen, the adjustable valve of withdrawal of aluminum hydroxides or oxides, the sensor of the reactor temperature, the sensor of pressure on the inlet of the suspension delivery into the reactor, the sensor of pressure on the outlet of the steam-gas mixture, and the sensor of pressure in front of the inlet of the steam- gas mixture into the condenser, the adjustable tool of the suspension delivery into the reactor, the main control unit with the inlet and the outlet. At that the source of suspension contains the adjustable tool of the water delivery and the adjustable tool of delivery of the aluminum powder. The invention allows to improve stability of the reactor operation.

EFFECT: the invention ensures the improved stability of the reactor operation.

5 cl, 3 dwg, 1 tbl

FIELD: chemical industry; methods and devices for production of molecular hydrogen.

SUBSTANCE: the invention is pertaining to the field of chemical industry, in particular, to the method and the apparatus for production of molecular hydrogen. The apparatus represents essentially the closed reactor, operation of which is not accompanied with the harmful outbursts and the pollution of atmosphere. The reactor has the first and second reaction chambers, in which at essentially different temperatures there is the same pressure. To increase the amount and to improve the purity of the produced hydrogen the reactor is supplied with the separator of the reaction products. The method includes the conversion of highly inflammable material in the reactor having the first and second chambers with utilization of the separator of the reaction products. In the reactionary layer of the first chamber conduct the response of conversion with production of hydrogen and at least one by-product, and also the reaction of interaction between the by-product and the separator of reaction products, and then transfer the separator of the reaction products into the reactionary layer of the second chamber, which is located above the reactionary layer of the first chamber. The invention ensures the increased amount and purity of the produced hydrogen.

EFFECT: the invention ensures the increased amount and purity of the produced hydrogen.

24 cl, 2 dwg

FIELD: catalyst preparation methods.

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EFFECT: prevented deactivation of copper-containing catalyst operated with process gas containing chlorine compounds.

11 cl, 3 tbl, 7 ex

FIELD: synthetic fuels.

SUBSTANCE: invention relates to a method for production of synthesis mainly containing H2 and CO for producing hydrogen, alcohols, ammonia, dimethyl ether, and ethylene, for Fischer-Tropsch processes, and also for use in chemical industry for processing hydrocarbon gases and in chemothermal systems for accumulation and transport of energy as well as in methane-methanol thermochemical water decomposition cycles. In the multistage process of invention, at least two consecutive stages are accomplished, in each of which stream containing lower alkanes having about 1 to 34 carbon atoms are passed through heating heat-exchanger and the through adiabatic reactor filled with catalyst packing. Before first stage and between the stages, stream is mixed with water steam and/or carbon dioxide and cooled in the end of each stage. Steam leaving last stage is treated to remove water steam.

EFFECT: increased conversion of lower alkanes and reduced H2/CO ratio in produced synthesis gas.

12 cl

FIELD: power industry; methods of devices for generation of electric power using carbon-containing fuels.

SUBSTANCE: the invention is pertaining to methods of devices for generation of electric power using carbon-containing fuels, more particular, to production of hydrogen and connected with it generation of electric power by a coal gasification. Hydrogen is produced out of solid or liquid carbon-containing fuels. The fuel is gasified by hydrogen producing an enriched with methane gaseous product, which then is introduced in the reaction with water and calcium oxide gaining hydrogen and calcium carbonate. The calcium carbonate may be continuously removed from the zone of the reaction producing hydrogen and the carbonization and to anneal it for regeneration of the calcium oxide, which may be repeatedly introduced into the zone of the reaction producing hydrogen and the carbonization. The method is realized in the device containing a reactor of gasification and a reactor of the carbonization for production of hydrogen. The given invention allows to use the produced hydrogen at the stage of the fuel gasification to ensure it with electric power.

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36 cl, 2 dwg

FIELD: gas treatment catalyst.

SUBSTANCE: invention relates to treatment of sulfur-containing emission gases according to Claus method and can find use in enterprises of gas, petroleum, and chemical industries as well as of ferrous and nonferrous metallurgy. Task of invention was to provide a catalyst with elevated strength and elevated activity simultaneously in three Claus process reactions: oxidation of hydrogen sulfide with sulfur dioxide; oxidation of hydrogen sulfide with sulfur dioxide in presence of oxygen; and carbonyl sulfide hydrolysis. The task is solved with the aid of sulfur-removing catalyst including titanium oxide, vanadium oxide, calcium sulfate and modifying metal compound. The latter is at least one of metal compounds selected from alkali metal (Me = K, Na, Cs or mixture thereof) oxides take at following proportions, wt %: V2O5 5.5-10.0, CaSO4 10.0-20.0, Me2O 0.1-2.0, provided that weight ratio Me2O/V2O5 = 0.01-0.36. Catalyst contains pores 10-40 nm in size in amount 50-70%. Preparation of catalyst comprises preparation of catalyst mass, extrusion, drying, and calcinations at temperature not higher than 400°C.

EFFECT: simplified catalyst preparation procedure, which is wasteless, energy efficient, and environmentally friendly.

6 cl, 2 tbl, 2 ex

FIELD: petrochemical process catalysts.

SUBSTANCE: non-oxidative conversion of methane becomes more efficient owing to increased yield of desired product obtained on Mo-containing zeolite catalyst prepared by modifying zeolite with molybdenum in solid phase. In particular, molybdenum in the form of nano-size powder (obtained according to electric explosion technique in argon atmosphere) is mixed with ZSM-type zeolite and mixture is then calcined resulting in catalyst with molybdenum level 0.5 to 6.0%.

EFFECT: increased catalyst activity in methane-to-aromatic hydrocarbons conversion process.

1 tbl, 7 ex

FIELD: chemistry of polymers, chemical technology, catalysts.

SUBSTANCE: invention relates to a method for preparing a catalyst used in polymerization of butadiene and copolymerization of butadiene with coupled dines. Method involves interaction of components comprising the compound of rare-earth element, diisobutyl aluminum hydride, triisobutyl aluminum, alkyl aluminum halide and coupled diene. Firstly, method involves mixing rare-earth element and coupled diene solutions with diisobutyl aluminum hydride solution, and the mixture is kept for 10-30 min at stirring, and then triisobutyl aluminum and alkyl aluminum halide solutions are added. After mixing all components the mixture is kept for 10-15 h in the following mole ratio of components: rare-earth element : diisobutyl aluminum hydride : triisobutyl aluminum : alkyl aluminum halide : coupled diene = 1:(3-12):(6-12):(1.5-3):(2-20), respectively, wherein rare-earth element carboxylate or alcoholate is used as a source of rare-earth element. Invention provides preparing the high-effective catalyst allowing preparing highly stereoregular polybutadiene and butadiene copolymer with the couples diene with simultaneous reducing the range of molecular-mass disposition by 3-3.5 times.

EFFECT: improved preparing method.

5 ex

FIELD: polymerization catalysts.

SUBSTANCE: catalyst preparation involves interaction of rare-earth element compound, conjugated diene, and diisobutylaluminum hydride followed by ageing of reaction mixture for 10-30 min, adding tetraisobutyl-dialumoxane and alkylaluminum hydroxide at molar ratio 1:(2-20):(3-12):(6-12):(1.5-3), respectively, and ageing resulting mixture for 10-15 h. Diene utilized is in the process is pyperilene or isoprene and rare-earth element compound is rare-earth element carboxylate or alcoholate. Catalyst can, in particular, find use in production of cis-1,4-polydienes.

EFFECT: achieved preparation of high-efficiency catalyst enabling production of highly stereospecific polybutadiene or butadiene/isoprene or butadiene/pyperilene copolymers at narrower molecular mass distribution.

4 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

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: hydrogenation-dehydrogenation catalysts.

SUBSTANCE: preparation of catalyst comprises depositing active components on γ-alumina carrier at stirring, carrier being preliminarily treated with concentrated NaOH solution. Active components are deposited consecutively in three steps. In the first step, preliminarily prepared chitosan in acetic acid solution with KCl solution is deposited for 60-65 min; in the second step, sodium tetrachloropaladate(II) trihydrate Na2PdCl4·3H2O solution is deposited for 60-65 min; and, in the third step, hydrazine hydrate solution as reducing agent is added for 180-240 min. After each step, resulting suspension is filtered off, washed, and dried at 293-303K for 1-2 h in vacuum. Catalyst can be used in chemical industry and in processing of industrial and household wastes.

EFFECT: enhanced nitrate hydrogenation efficiency.

6 cl, 1 dwg, 6 ex

FIELD: organic synthesis catalysts.

SUBSTANCE: invention relates to improved method of preparing double metal cyanide catalysts for synthesis of polyether-polyols via polyaddition alkylene oxides to starting compounds possessing active hydrogen atoms. Method comprises following steps: (i) mixing one or several solutions of water-soluble salts of Zn(II), Fe(II), Ni(II), Mn(II), Co(II), Sn(II), Pb(II), Fe(III), Mo(IV), Mo(VI), Al(III), V(V), V(IV), Sr(II), W(VI), Cu(II), or Cr(III) with solution of water-soluble cyanide ions-containing salt or acid of Fe(II), Fe(III), Co(II), Co(III), Cr(II), Cr(III), Mn(II), Mn(III), Ir(III), Ni(II), Rh(III), Ru(II), V(IV), or V(V) with the aid of mixing nozzle, preferably jet disperser; (ii) isolation of catalyst from resulting dispersion; (iii) washing; and (iv) drying.

EFFECT: increased catalytic activity, reduced particle size, and narrowed size distribution of particles in polyether-polyols production process.

8 cl, 5 dwg, 9 ex

FIELD: industrial organic synthesis and catalysts.

SUBSTANCE: invention provides catalyst for synthesis of thiophene from furan and hydrogen sulfide, which catalyst contains 3.1-4.2 wt %: boron oxide supported by alumina. Catalyst is prepared via mixing boron acid solution with aluminum hydroxide followed by extrusion and heat treatment, said aluminum hydroxide being aluminum hydroxide with pseudoboehmite structure or mixture thereof with aluminum hydroxide prepared via thermochemical activation process. Thiophene production process is accomplished via furan/hydrogen sulfide reaction in presence of above-described catalyst at 300-350 sulfate, hydrogen sulfide-to-furan molar ratio (6-11):1, and furan feed rate 3.7 to 11.1 mole/h per 1 g catalyst.

EFFECT: increased thiophene formation selectivity to 98-100%.

4 cl, 1 tbl, 7 ex

FIELD: inorganic compounds technologies.

SUBSTANCE: invention provides porous composite particles containing alumina component and residue of at least one additional crystal growth inhibitor component dispersed within alumina component, wherein indicated composite particles have (A) specific surface area at least 80 m2/g; (B) average nitrogen-filled pore diameter 60 to 1000 Å; (C) total nitrogen-filled pore volume 0.2 to2.5 cm3/g and (D) average particle size 1 to 15 μm, and where, in indicated composite particles, (i) alumina component contains at least 70 wt % of crystalline boehmite with average crystallite size 20 to 200 Å, γ-alumina obtained from indicated crystalline boehmite, or mixture thereof; (ii) residue of additional is obtained from at least one ionic compound containing ammonium, alkali metal, alkali-earth metal cation, or mixtures thereof and wherein anion is selected from group comprising hydroxyl, silicate, phosphate, sulfate, or mixtures thereof and is present in composite particles in amounts between 0.5 and 10 % of the summary weight of alumina and additional components. Invention also provides a method to obtain composite particles, agglomerated particles prepared therefrom, and a method for hydroprocessing of petroleum feed using above-mentioned agglomerates.

EFFECT: avoided unnecessary calcination before addition of metals to increase average pore size and use of organic solvents for azeotropic removal of water.

36 cl, 2 tbl, 22 ex

FIELD: industrial organic synthesis catalysts.

SUBSTANCE: invention relates to copper-containing catalysts for low-temperature synthesis of methanol in fluidized bed at high pressure and provides catalyst, whose preparation involves impregnation and which contains oxides of copper, zinc, chromium, magnesium, aluminum, boron, and barium and has following molar ratio: CuO:ZnO:Cr2O3, MgO:Al2O3:B2O3:BaO = 1:(0.7-1.1):(0.086-0.157):(0.05-0.15):(0.125-0.2):(0.018-0.029):(0.04-0.075).

EFFECT: increased mechanical strength and wear resistance of catalyst.

1 tbl

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