CN111377820B - Preparation method of 2-methylpentanediamine - Google Patents
Preparation method of 2-methylpentanediamine Download PDFInfo
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- CN111377820B CN111377820B CN202010327061.4A CN202010327061A CN111377820B CN 111377820 B CN111377820 B CN 111377820B CN 202010327061 A CN202010327061 A CN 202010327061A CN 111377820 B CN111377820 B CN 111377820B
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/44—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers
- C07C209/48—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers by reduction of nitriles
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Abstract
The invention provides a preparation method of 2-methyl pentanediamine, which comprises the steps of taking 2-methyl glutaronitrile as a raw material, doping Ru and Mo metals in a Raney nickel catalyst to form a composite catalyst, diluting the 2-methyl glutaronitrile by a solvent, and then realizing hydrogenation reaction in a bubble flow reactor under the action of the composite catalyst, thereby obtaining a target product, namely the 2-methyl pentanediamine. According to the preparation method of 2-methyl pentanediamine, provided by the invention, the Raney nickel catalyst is doped with metal ruthenium (Ru), so that the selectivity of the target product 2-methyl pentanediamine in the final product can be effectively improved, the bubble flow reactor is adopted, the production efficiency is improved, and the conversion rate of 2-methyl glutaronitrile can be higher in a short time.
Description
Technical Field
The invention belongs to the technical field of chemical production, and particularly relates to a preparation method of 2-methyl pentanediamine.
Background
Adiponitrile is a main raw material for producing nylon-66, and nylon-66 has wide application in the fields of electronics, light industry and other organic synthesis, has excellent mechanical material characteristics, is suitable for the military field of special tires such as airplanes, fighters and the like, is one of indispensable important materials for national defense, and is also a metal substitute for lightening the vehicle weight and reducing the consumption in a new generation of automobiles. The technology for preparing adiponitrile by directly hydrocyanating butadiene is the adiponitrile preparation technology which has high adiponitrile yield, short reaction path and low energy consumption, is a very ideal adiponitrile production technology, but can produce a large amount of 2-methylglutaronitrile as a byproduct. How to improve the added value of the byproduct 2-methylglutaronitrile and optimize the whole process flow becomes more and more important.
2-methylpentanediamine is widely used industrially. It can be used for producing polyamide plastics, films, fibers, polyamide adhesives, printing resins, epoxy resin curing treatment agents (such as coatings, floors and the like), organic chemical products (such as pesticides and the like) and the like; it can also be used for chain expansion of isonitrile acid ester, polyhydric alcohol, etc.; the poly (hexamethylene diamine) is also an important chain extender in the production of polyurethane, elastic fiber spandex and high-modulus fiber aramid fiber, is also an important chemical and medical intermediate, and can be used as a polyamide monomer to partially replace hexamethylene diamine to prepare nylon 66. The 2-methylglutaronitrile can be used for preparing 2-methylglutaronitrile by catalytic hydrogenation, so that the adiponitrile industrial chain is prolonged, and the additional value of the byproduct 2-methylglutaronitrile is increased.
The nitrile compound is catalyzed and hydrogenated to prepare amine compound, and the commonly used catalyst is a skeletal nickel/cobalt catalyst. The literature reports that the catalytic hydrogenation performance of the dinitrile compound of the Raney nickel catalyst can be obviously improved by doping a small amount of Mo, cr or Fe auxiliary agent, the high-efficiency Raney nickel catalyst can be obtained by optimizing the doping amount of the auxiliary agent, and the yield of the aliphatic diamine product is improved. Patent CN107365257A discloses a method for preparing 2-methyl pentanediamine and methyl piperidine by hydrogenating 2-methyl glutaronitrile, which adopts ytterbium-doped Raney nickel catalyst at 30-100 ℃, hydrogenation reaction pressure of 2-8 MPa, and realizes 100% conversion of 2-methyl glutaronitrile under optimal conditions, product 2-methyl pentanediamine selectivity is 67%, and the method has long reaction time and low overall 2-methyl pentanediamine selectivity.
The doping among metals is characterized in that multiple-metal alloy phases of various types are formed in local microscopic regions, and certain specific alloy phases have high activity and high selectivity for specific reactions, such as the hydrogenation reaction of Raney nickel catalysts on nitriles. The reactors for preparing 2-methylpentanediamine reported in the literature at present mostly adopt a kettle reactor, such as CN107365257A. The kettle reactor is generally used for batch reaction and is suitable for the production of products with small batch, multiple varieties and longer reaction time. The bubble flow reactor is a reactor for high-efficiency continuous production, but the gas-phase bubbles are difficult to uniformly and stably exist in the reactor, so the popularization and the application are limited. Wherein, the reasonable gas-liquid-air speed ratio in the reactor is an important parameter for ensuring stable bubbling.
In order to improve the additional value of a byproduct 2-methylglutaronitrile in the adiponitrile production process, reduce the preparation cost of an important organic intermediate of 2-methylglutaronitrile and improve the selectivity of the 2-methylglutaronitrile in a final product, a raney nickel catalyst needs to be further doped, the catalytic hydrogenation reaction process is further improved, finally, the catalyst and reaction process parameters are optimized and coupled, so that the 2-methylglutaronitrile is utilized more efficiently, the catalytic hydrogenation condition and the product high yield which are more optimized than those in the prior art are realized, and the capacity maximization in unit time is realized.
Disclosure of Invention
In order to solve the defects of the prior art, the invention provides a preparation method of 2-methyl pentanediamine, which is used for improving the selectivity of the 2-methyl pentanediamine and improving the production efficiency.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a preparation method of 2-methylpentanediamine comprises the following specific steps: doping Ru and Mo metals in a Raney nickel catalyst to form a composite catalyst, diluting 2-methylglutaronitrile by a solvent, and carrying out a hydrogenation reaction in a bubble flow reactor under the action of the composite catalyst to obtain 2-methylglutaronitrile; preferably, the specific operation mode is as follows: mixing raw materials in a raw material tank, wherein the raw material tank is connected with the bubbling reactor through a pipeline, and after the raw materials are mixed in the raw material tank, a reaction liquid in the raw material tank is conveyed into a vertical pipe of the bubbling reactor through the bottom of the bubbling reactor by a metering pump; introducing nitrogen from the other position at the bottom through a pipeline, purging with the nitrogen for several times to exhaust air, then switching the nitrogen into hydrogen, driving the reaction liquid to move from the lower end of the vertical pipe to the upper end of the vertical pipe by gas-phase bubbling, arranging an outlet at the upper end of the vertical pipe, overflowing the product liquid from the outlet to enter a downstream gas-liquid separation device, rectifying and purifying the 2-methylpentanediamine product liquid in the downstream device, and purifying and boosting the separated gas-phase hydrogen to return to the inlet of the bubbling reactor for recycling.
Further, the mass ratio of Ru, mo and Raney nickel catalyst in the composite catalyst is as follows: (0.2-2.5): (0.1-2.5): (95-99.7).
Further, the total mass of Ni and Al in the Raney nickel catalyst accounts for 94.7-99.7% of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: (78-95): (1.4-11.4).
Further, the ratio of the air speed of the gas in the standpipe of the bubble flow reactor to the flow rate of the liquid is as follows: 10-20.
Further, the reaction time of the hydrogenation reaction is 15 min-50 min.
Further, the reaction temperature of the hydrogenation reaction is as follows: 70-100 ℃; the reaction pressure is as follows: 2.3MPaG to 6MPaG.
Further, the solvent is alcohol, wherein the alcohol is selected from one of ethanol and ethylene glycol.
Further, diluting the 2-methylglutaronitrile by using a solvent, and adding a base to adjust the pH value to be between 11.5 and 12.5, wherein the base is selected from KOH, naOH or NH 4 One of OH.
Compared with the prior art, the preparation method of the 2-methylpentamethylenediamine provided by the invention has the following advantages: according to the method, the Raney nickel catalyst is doped with Ru and Mo metals, and the selectivity of the target product 2-methylpentamethylenediamine is effectively improved by doping the Ru (Ru) metal; meanwhile, the proportion of the air speed of the gas in the vertical pipe of the bubbling flow reactor to the flow speed of the liquid is controlled, stable bubbling in the reactor can be realized, the reaction efficiency is improved, and the higher conversion rate of the 2-methylglutaronitrile can be realized in a shorter time, so that the target product with higher selectivity can be obtained in the whole reaction in a shorter time.
Detailed Description
The present invention will be described in detail with reference to examples.
Comparative example 1:
according to the weight ratio of 1.5:2: the ruthenium, molybdenum and Raney nickel catalyst are added in a proportion of 96.5 to form the composite catalyst, the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 30kg of an ethanol solution containing 40% of 2-methylglutaronitrile and 25% of NH was charged into a stainless steel tank reactor 3 1kg of ammonia water solution is adjusted to have the pH value: 11.7, and finally 1.5kg of the composite catalyst is added. The reactor was sealed with high pressure nitrogen (around 4.3 MPaG) and purged several times with nitrogen to exhaust air. When the reactor is upWhen the temperature reaches 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. And sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 150min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 100% and the selectivity of conversion to 2-methylpentamethylenediamine was 55%.
Comparative example 2:
according to the weight ratio of 1.5:2: the ruthenium, molybdenum and Raney nickel catalyst are added in a proportion of 96.5 to form the composite catalyst, the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (around 3.7 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 3.7 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Ensuring the ratio of the air speed of gas in the vertical pipe of the reactor to the flow speed of liquid to be 5:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 87% and the selectivity of conversion to 2-methylpentamethylenediamine was 62%.
Comparative example 3:
according to the weight ratio of 1.5:2:96.5, adding ruthenium, molybdenum and Raney nickel catalyst to form the composite catalyst, wherein the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of a basic solution containing 32% KOH are added in a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (around 3.7 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 3.7 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 30:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 70% and the selectivity of conversion to 2-methylpentanediamine was 50%.
Comparative example 4:
the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, wherein the mass percentages of Ni and Al are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and containing 25% of NH were introduced into a bubble flow reactor (DN 40) 3 Adjusting the pH value of 10g of ammonia water solution to be: 11.7, and finally 15g of the above Raney nickel catalyst. The reactor was sealed with high pressure nitrogen (about 4.3 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 12:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 100% and the selectivity of conversion to 2-methylpentamethylenediamine was 63%.
Comparative example 5:
according to the weight ratio of 3.2:2: ruthenium, molybdenum and Raney nickel catalyst are added in a proportion of 94.8 to form the composite catalyst, the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9% of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (about 4.3 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 12:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile amine was 100% and the selectivity of conversion to 2-methylglutaronitrile amine was 75%.
Example 1:
according to the proportion of 1.5:2:96.5, adding ruthenium, molybdenum and Raney nickel catalyst to form the composite catalyst, wherein the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and containing 25% of NH were introduced into a bubble flow reactor (DN 40) 3 10g of ammonia solution is adjusted to have a pH value of: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (about 4.3 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 12:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 100% and the selectivity of conversion to 2-methylpentamethylenediamine was 72%.
Example 2:
according to the weight ratio of 1.5:2:96.5, adding ruthenium, molybdenum and Raney nickel catalyst to form the composite catalyst, wherein the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (around 3.7 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 3.7 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 10:1. and sampling and collecting a reacted solution at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 97% and the selectivity of conversion to 2-methylpentamethylenediamine was 65%.
Example 3:
according to the weight ratio of 1.5:2:96.5, adding ruthenium, molybdenum and Raney nickel catalyst to form the composite catalyst, wherein the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (around 3.7 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 3.7 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 20:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 95% and the selectivity of conversion to 2-methylpentamethylenediamine was 67%.
Example 4:
according to the weight ratio of 0.2:2:97.8, adding ruthenium, molybdenum and Raney nickel catalyst to form the composite catalyst, wherein the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (about 4.3 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 12:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 100% and the selectivity of conversion to 2-methylpentamethylenediamine was 66%.
Example 5:
according to the proportion of 2.2:2: the ruthenium, molybdenum and Raney nickel catalyst are added according to the proportion of 95.8 to form the composite catalyst, the total mass of Ni and Al in the Raney nickel catalyst accounts for 96.9 percent of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: 94.3:2.6; 300g of an ethanol solution containing 40% of 2-methylglutaronitrile and 5g of an aqueous alkali solution containing 32% KOH are introduced into a bubble flow reactor (DN 40) to adjust the pH to: 11.7, and finally 15g of the above composite catalyst was added. The reactor was sealed with high pressure nitrogen (about 4.3 MPaG) and purged several times with nitrogen to exhaust air and complete the material circulation process under nitrogen atmosphere. When the temperature of the reactor is raised to 82 ℃, the high-pressure nitrogen is switched into high-pressure hydrogen (about 4.3 MPaG), the hydrogen flow rate is controlled, the reaction heat is taken away by adopting circulating water, and the temperature of the reactor is maintained at 82 ℃. Controlling the ratio of the air speed of gas in the vertical pipe of the reactor to the flow rate of liquid in the vertical pipe of the reactor to be 12:1. and sampling and collecting the solution after reaction at regular intervals and carrying out gas chromatography analysis. When the reaction time was 20min, it was found from the results of product analysis that the conversion of 2-methylglutaronitrile was 100% and the selectivity of conversion to 2-methylpentamethylenediamine was 74%.
As can be seen from comparative examples 1, 2 and 3 and examples 1, 2 and 3, the higher conversion rate of 2-methylglutaronitrile can be achieved by adopting the bubbling flow reactor and controlling the air speed of the gas in the vertical pipe and the flow rate of the liquid in a certain proportional range for reacting for 20 min; as can be seen from the comparative example 4 and the examples 1, 4 and 5, the catalyst doped with the metal ruthenium (Ru) can effectively improve the selectivity of the 2-methylpentamethylenediamine; as can be seen from comparative example 5 and example 5, when the mass percentage of ruthenium exceeds a certain ratio, the selectivity of the target product, 2-methylpentamethylenediamine, is not obviously improved.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (8)
1. The preparation method of the 2-methylpentanediamine is characterized by comprising the following steps: doping Ru and Mo metals in a Raney nickel catalyst to form a composite catalyst, diluting 2-methylglutaronitrile by a solvent, and carrying out a hydrogenation reaction in a bubble flow reactor under the action of the composite catalyst to obtain 2-methylglutaronitrile;
the ratio of the air speed of the gas in the vertical pipe of the bubble flow reactor to the flow speed of the liquid is as follows: 10 to 20.
2. The method for preparing 2-methylpentanediamine, according to claim 1, wherein: the mass ratio of Ru to Mo to Raney nickel in the composite catalyst is as follows: (0.2 to 2.5): (0.1 to 2.5): (95 to 99.7).
3. The method for preparing 2-methylpentanediamine, according to claim 1, wherein: the total mass of Ni and Al in the Raney nickel catalyst accounts for 94.7-99.7% of the total mass of the Raney nickel catalyst, and the mass percentages of Ni and Al in the Raney nickel catalyst are as follows: (78 to 95): (1.4 to 11.4).
4. The method for preparing 2-methylpentanediamine according to claim 1, wherein: the reaction time of the hydrogenation reaction is 15min to 50min.
5. The method of claim 1, wherein the method comprises the steps of: the reaction temperature of the hydrogenation reaction is as follows: 70-100 ℃.
6. The method for preparing 2-methylpentanediamine, according to claim 1, wherein: the reaction pressure of the hydrogenation reaction is as follows: 2.3MPaG to 6MPaG.
7. The method of claim 1, wherein the method comprises the steps of: the solvent is alcohol, and the alcohol is selected from one of ethanol and ethylene glycol.
8. The process for producing 2-methylpentanediamine, according to claim 1, wherein: diluting 2-methylglutaronitrile with a solvent, adding a base to adjust the pH value to be between 11.5 and 12.5, wherein the base is selected from KOH, naOH or NH 4 One of OH groups.
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| CN1483016A (en) * | 2000-12-23 | 2004-03-17 | �������¹ɷ�����˾ | Method for producing amines by catalytic hydrogenation of nitrites or imines |
| CN101298420A (en) * | 2007-03-07 | 2008-11-05 | 赢创德固赛有限责任公司 | Method for production of trimethylhexamethylenediamine |
| CN105555752A (en) * | 2013-09-13 | 2016-05-04 | 因温斯特技术公司 | Hydrogenation of dinitriles for the preparation of diamines |
| CN109456200A (en) * | 2018-11-23 | 2019-03-12 | 万华化学集团股份有限公司 | A kind of preparation method of m-xylene diamine |
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