CN111604060B - Preparation method of hydrogenation catalyst carrier and product - Google Patents

Preparation method of hydrogenation catalyst carrier and product Download PDF

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CN111604060B
CN111604060B CN201910133798.XA CN201910133798A CN111604060B CN 111604060 B CN111604060 B CN 111604060B CN 201910133798 A CN201910133798 A CN 201910133798A CN 111604060 B CN111604060 B CN 111604060B
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mixture
alumina powder
mass
carrier
hydrogenation catalyst
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CN111604060A (en
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张瑜平
傅骐
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Yichang Supeng Technology Co ltd
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Yichang Supeng Technology Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/892—Nickel and noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • B01J21/04—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/89—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals
    • B01J23/8933—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/8986—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with noble metals also combined with metals, or metal oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with manganese, technetium or rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/635—0.5-1.0 ml/g
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/63—Pore volume
    • B01J35/638—Pore volume more than 1.0 ml/g
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a preparation method and a product of a hydrogenation catalyst carrier, relates to the field of catalyst carriers, and aims to solve the problem that the carrier of the existing hydrogenation catalyst is poor in use effect. The method comprises the following specific steps: step one, mixing two kinds of active alumina powder with different pore structures, adding nitric acid, acetic acid, citric acid and water into the mixture, and stirring the mixture at a high speed to obtain a first mixture; heating and preserving heat, cooling and sieving the first mixture, adding urotropine water solution into the first mixture, stirring while adding, ageing at low temperature, oil bath forming, and drying and roasting to obtain the finished product. The preparation process is reasonable, different active alumina powder is used as raw materials for preparing the catalyst carrier, and compared with the similar carrier, the prepared carrier has the advantages of large specific surface area, high strength and low bulk density, and is more suitable for being used as the carrier of the hydrogenation catalyst taking noble metal as an active component.

Description

Preparation method of hydrogenation catalyst carrier and product
Technical Field
The invention relates to the field of catalyst carriers, in particular to a preparation method of a hydrogenation catalyst carrier.
Background
The catalyst is a substance which can change the chemical reaction rate (increase or decrease) of a reactant in a chemical reaction without changing chemical equilibrium, and the quality and chemical properties of the catalyst are not changed before and after the chemical reaction. Catalysts are extremely important in the modern chemical industry, for example, iron catalysts are used in the production of ammonia, vanadium catalysts are used in the production of sulfuric acid, and different catalysts are used in the production of three synthetic materials such as ethylene polymerization and rubber made from butadiene.
The catalyst has various types, the industry rapidly develops, the demand is continuously increased, people consider how to fully exert the catalytic efficiency of the catalyst, the catalyst carrier is realized to have a critical effect on the performance of the catalyst, the performance of the carrier is mainly the strength, the stacking density, the specific surface and the pore volume of the carrier, and the catalyst carrier is a key for improving the performance of the catalyst.
The hydrogenation catalyst is a common catalyst, but the existing hydrogenation catalyst has low carrier strength, small pore volume and poor use effect.
Disclosure of Invention
The invention aims to provide a preparation method of a hydrogenation catalyst carrier, which aims to solve the problems in the background technology.
In order to achieve the above purpose, the present invention provides the following technical solutions:
a preparation method of a hydrogenation catalyst carrier comprises the following specific steps:
step one, mixing two kinds of active alumina powder with different pore structures, adding nitric acid, acetic acid, citric acid and water into the mixture, and stirring the mixture at a high speed to obtain a first mixture;
heating the first mixture to 75-86 ℃ and preserving heat for 4-12 minutes, cooling and sieving with a 60-90 mesh sieve to obtain a second mixture, adding urotropine water solution into the second mixture, stirring while adding, aging at low temperature and forming in an oil bath at 80-90 ℃, and then drying and roasting to obtain the finished product.
As a further scheme of the invention: the two active alumina powders with different pore structures in the first step comprise a first active alumina powder and a second active alumina powder, wherein the dry basis bulk density of the first active alumina powder is 0.20-0.35g/mL, and the specific surface area is 300-550m 2 Per g, pore volume of 0.85-1.20cm 3 Per gram, the dry bulk density of the second activated alumina powder is 0.28-0.35g/mL, and the specific surface area is 330-390m 2 Per g, pore volume of 0.8-0.9cm 3 /g。
As a further scheme of the invention: the mass ratio of the first activated alumina powder to the second activated alumina powder is 1-8:1.
As a further scheme of the invention: in the first step, the mass of nitric acid is 1-3% of the mass of the first mixture, the mass of acetic acid is 0.1-1% of the mass of the first mixture, and the mass of citric acid is 0.05-2% of the mass of the first mixture.
As a further scheme of the invention: the mass of urotropine in the urotropine aqueous solution in the second step is 0.45-2.25% of the total mass of the urotropine aqueous solution and the second mixture.
As a further scheme of the invention: the cooling temperature in the second step is 8-12 ℃, the low-temperature aging temperature is 1-15 ℃ and the time is 4-36 hours.
As a further scheme of the invention: and in the second step, the drying temperature is 110-128 ℃, the roasting temperature is 780-840 ℃, and the roasting time is 3-5.5 hours.
The nitric acid, acetic acid and citric acid are all industrial acids.
Compared with the prior art, the invention has the beneficial effects that:
the preparation process is reasonable, different active alumina powder is used as raw materials for preparing the catalyst carrier, and compared with similar carriers, the prepared carrier has the advantages of large specific surface area, high strength and low bulk density, is more suitable for being used as a carrier of a hydrogenation catalyst taking noble metal as an active component, and has wide application prospect.
Detailed Description
The technical scheme of the patent is further described in detail below with reference to the specific embodiments.
The invention takes noble metals of ruthenium, rhodium, palladium and platinum as active components, the mass of the active components is 0.1-5.0% of the mass of the catalyst, nickel, cobalt and manganese are selected as auxiliary agents, the mass of the auxiliary agents is 0.05-5.0% of the mass of the catalyst, and the preparation of the catalyst and the evaluation of the performance thereof are carried out.
Example 1
A preparation method of a hydrogenation catalyst carrier comprises the following specific steps: adding 545 kg of water, 150 kg of 11.5% nitric acid solution, 5 kg of industrial grade 99% acetic acid and 8 kg of industrial grade 99.5% citric acid into a high-speed disperser, opening the high-speed disperser, adding 300 kg of first active alumina powder and 75 kg of second active alumina powder into the high-speed disperser, heating to 80 ℃, preserving the temperature for 5 minutes, cooling to 11 ℃, sieving the mixture to a reaction kettle by using a 80-mesh filter screen, adding 34.2 kg of urotropine aqueous solution containing 15.3 kg of urotropine, aging for 13 hours at 5 ℃, then oil-injecting the mixture into an oil bath at 84 ℃ by using a 12-gauge needle, drying and sieving spherical carriers of phi 1.9, and roasting the spherical carriers at 800 ℃ for 4 hours to obtain the carrier A1.
Application example 1:
250 g of carrier A1 is taken, treated and immersed into an aqueous solution which has the temperature of 80 ℃ and contains 0.73 g of noble metal palladium and 0.5 g of nickel, and the catalyst A1 is obtained after standing for 18 minutes, taken out, dried and roasted.
Example 2
A preparation method of a hydrogenation catalyst carrier comprises the following specific steps: adding 160 kg of water, 160 kg of nitric acid solution with the mass fraction of 11.5%, 4 kg of acetic acid with the mass fraction of 99% and 6 kg of citric acid with the mass fraction of 99.5% into a high-speed disperser, opening the high-speed disperser, adding 275 kg of first active alumina powder and 100 kg of second active alumina powder, heating to 80 ℃, preserving the temperature for 5 minutes, cooling to 11 ℃, sieving to a reaction kettle by using a 80-mesh filter screen, adding 34 kg of urotropine aqueous solution containing 15.4 kg of urotropine, aging for 24 hours at the temperature of 12 ℃, and then performing oil injection molding in an oil bath with the temperature of 86 ℃ by using a 12-gauge needle. And (3) drying and screening the spherical carrier phi 2.5, and roasting at 800 ℃ for 4 hours to obtain a carrier A2.
Application example 2
250 g of carrier A2 is taken, treated and immersed into an aqueous solution which has the temperature of 80 ℃ and contains 0.75 g of noble metal palladium, 0.5 g of nickel and 0.6 g of manganese, and the catalyst B2 is obtained after standing for 22 minutes, taking out, drying and roasting.
Example 3
A preparation method of a hydrogenation catalyst carrier comprises the following specific steps: adding 545 kg of water, 150 kg of 11.5% nitric acid solution, 3 kg of industrial grade 99% acetic acid and 6 kg of industrial grade 99.5% citric acid into a high-speed disperser, opening the high-speed disperser, adding 225 kg of first active alumina powder and 150 kg of second active alumina powder, heating to 80 ℃, preserving the temperature for 10 minutes, and then cooling to 8 ℃. Sieving with a 80-mesh filter screen, adding 35 kg of urotropine aqueous solution containing 14.5 kg of urotropine into a reaction kettle, aging at 12 ℃ for 15 hours, and then oil-injection molding in an oil bath at 90 ℃ by using a 12-gauge needle. And (3) drying and screening the spherical carrier phi 2.7, and roasting at 800 ℃ for 4 hours to obtain a carrier A3.
Application example 3
250 g of carrier A3 is taken, treated, immersed into an aqueous solution with the temperature of 80 ℃ and containing 0.75 g of noble metal palladium, 0.5 g of nickel and 0.6 g of manganese, and kept stand for 25 minutes, taken out, dried and roasted to obtain the catalyst B3.
Comparative example 1:
adding 575 kg of water, 165 kg of 11.5% nitric acid solution and 6 kg of industrial grade 99.5% citric acid into a high-speed disperser, opening the high-speed disperser, adding 375 kg of first active alumina powder, heating to 80 ℃, preserving heat for 0 min, and cooling to 10 ℃. Sieving with a 80-mesh filter screen, adding 35 kg of urotropine aqueous solution containing 15.5 kg of urotropine into a reaction kettle, aging at 12 ℃ for 16 hours, and then oil-injection molding in an oil bath at 85 ℃ with a 12-gauge needle. And (3) drying and screening the spherical carrier phi 2.0, and roasting at 800 ℃ for 4 hours to obtain a carrier A4.
250 g of carrier A4 is taken, treated, immersed into an aqueous solution with the temperature of 80 ℃ and containing 0.75 g of noble metal palladium and 0.5 g of nickel, kept stand for 25 minutes, taken out, dried and roasted to obtain the catalyst B4.
Comparative example 2:
adding 575 kg of water, 165 kg of 11.5% nitric acid solution and 6 kg of industrial grade 99.5% citric acid into a high-speed disperser, opening the high-speed disperser, adding 375 kg of second active alumina powder, heating to 80 ℃, preserving heat for 0 min, and cooling to 12 ℃. Sieving with a 80-mesh filter screen, adding 35 kg of urotropine aqueous solution containing 14.5 kg of urotropine into a reaction kettle, aging at 15 ℃ for 28 hours, and then oil-injection molding in an oil bath at 86 ℃ with a 12-gauge needle. And (3) drying and screening the spherical carrier phi 2.4, and roasting at 800 ℃ for 4 hours to obtain a carrier A5.
250 g of carrier A5 is taken, treated, immersed into an aqueous solution with the temperature of 80 ℃ and containing 0.75 g of noble metal palladium and 0.5 g of nickel, kept stand for 30 minutes, taken out, dried and roasted to obtain the catalyst B5.
The products of examples 1-3, application examples 1-3 and comparative examples 1-2 were subjected to performance tests, and the test results are shown in Table 1.
TABLE 1
As can be seen from Table 1, the bulk density of A4 in comparative example 1 is close to that of examples 1-3, but the average intensity is only 15.4N/p; the average A5 strength in comparative example 2 was 31.5N/P, but the bulk density was 0.512g/ml. Therefore, only by mixing two different active alumina powders according to a proper proportion, a more ideal result can be obtained, and the strength of the corresponding catalyst is basically unchanged.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Furthermore, it should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is provided for clarity only, and that the disclosure is not limited to the embodiments described in detail below, and that the embodiments described in the examples may be combined as appropriate to form other embodiments that will be apparent to those skilled in the art.

Claims (4)

1. The preparation method of the hydrogenation catalyst carrier is characterized by comprising the following specific steps:
step one, mixing two kinds of active alumina powder with different pore structures, wherein the two kinds of active alumina powder with different pore structures comprise a first active alumina powder and a second active alumina powder, the dry bulk density of the first active alumina powder is 0.20-0.35g/mL, and the specific surface area is 300-550m 2 Per g, pore volume of 0.85-1.20cm 3 Per gram, the dry bulk density of the second activated alumina powder is 0.28-0.35g/mL, and the specific surface area is 330-390m 2 Per g, pore volume of 0.8-0.9cm 3 And/g, wherein the mass ratio of the first activated alumina powder to the second activated alumina powder is 1-8:1, and nitric acid, acetic acid, citric acid and water are added into the mixture and stirred at a high speed to obtainTo a first mixture;
heating the first mixture to 75-86 ℃ and preserving heat for 4-12 minutes, cooling and sieving with a 60-90 mesh sieve to obtain a second mixture, adding urotropine water solution into the second mixture, stirring while adding, aging at low temperature and forming in an oil bath at 80-90 ℃, and then drying and roasting to obtain a finished product;
in the first step, the mass of nitric acid is 1-3% of the mass of the first mixture, the mass of acetic acid is 0.1-1% of the mass of the first mixture, and the mass of citric acid is 0.05-2% of the mass of the first mixture;
the temperature of drying in the second step is 110-128 ℃, the roasting temperature is 780-840 ℃, and the roasting time is 3-5.5 hours.
2. The method for preparing a hydrogenation catalyst carrier according to claim 1, wherein the mass of urotropine in the urotropine aqueous solution in the second step is 0.45-2.25% of the total mass of the urotropine aqueous solution and the second mixture.
3. The method for preparing a hydrogenation catalyst carrier according to claim 1, wherein the cooling temperature in said step two is 8-12 ℃, the low temperature aging temperature is 1-15 ℃ and the time is 4-36 hours.
4. A product prepared by the method for preparing a hydrogenation catalyst support according to any one of claims 1 to 3.
CN201910133798.XA 2019-02-22 2019-02-22 Preparation method of hydrogenation catalyst carrier and product Active CN111604060B (en)

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CN114644351B (en) * 2020-12-17 2024-02-13 中国石油化工股份有限公司 Superfine alumina spherical particles and preparation method thereof
CN113731385B (en) * 2021-08-20 2023-11-28 宜昌苏鹏科技有限公司 Catalyst carrier for preparing hydrogen peroxide by fixed bed anthraquinone method and preparation method of catalyst

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