CN109647456B - Hydrogenation catalyst for synthesizing cyclohexylamine - Google Patents
Hydrogenation catalyst for synthesizing cyclohexylamine Download PDFInfo
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Abstract
The invention relates to a hydrogenation catalyst for synthesizing cyclohexylamine, which mainly solves the problems of low yield and low selectivity of synthesizing cyclohexylamine by catalytic hydrogenation of aniline in the prior art. The hydrogenation catalyst for synthesizing cyclohexylamine comprises a carrier and an active component, wherein the carrier is phosphorus modified Al2O3The active component comprises Co element and promoter element; the catalyst promoter element comprises at least one metal element selected from alkali metals and IIB group metals, so that the problem is solved well, and the catalyst promoter element can be used in the industrial production of cyclohexylamine.
Description
Technical Field
The invention relates to a hydrogenation catalyst for synthesizing cyclohexylamine.
Background
Cyclohexylamine, also known as hexahydroaniline and aminocyclohexane, is a colorless transparent liquid, has strong fishy amine smell, and can be mixed and dissolved with water and common organic solvents. It is an important organic chemical raw material and fine chemical intermediate, and is mainly used in rubber auxiliary agent, food additive, anticorrosion, paper-making, plastic processing and textile industry.
Overseas production and application are mainly concentrated in western developed countries and regions, and main manufacturers include unequal-scale manufacturers such as American air products company, Seranies company, Germany Basff company, Bayer company and the like. However, in europe, cyclohexylamine is in a state of shortage because of the limitation of the hydrogen feed. The capacity of producing cyclohexylamine in China is close to 10 ten thousand tons per year, and main manufacturers thereof comprise: qingdao Jintian factories, Hebei Jizhong Weifang Zhenxing and Shandong Hengda. In 2010, the consumption capacity of the cyclohexylamine in China is 7 ten thousand tons per year, and with the rapid development of food additive sodium cyclamate and rubber industries, the consumption of the cyclohexylamine is increased by more than 10 percent every year.
The preparation process of cyclohexylamine has many routes, and mainly comprises aniline catalytic hydrogenation, nitrocyclohexane reduction, chlorocyclohexane catalytic ammonolysis, cyclohexanol vapor phase ammonification and cyclohexanone catalytic ammonolysis.
Reducing nitrocyclohexane: according to the method, nitrocyclohexane and hydrogen are used as raw materials, a reducing agent is used for generating cyclohexylamine, and the nitrocyclohexane raw materials are difficult to obtain, so that the method is basically eliminated. ② catalytic ammonolysis of chlorocyclohexane: the method takes chlorocyclohexane and ammonia as raw materials to carry out catalytic reaction on the chlorocyclohexane and the ammonia. The process route is longer, the selectivity of cyclohexylamine is poorer, and the reaction product contains hydrogen chloride, so the requirement on equipment is high. ③ cyclohexanol vapor phase ammonification method: under the action of a nickel/silicon dioxide catalyst, cyclohexanol and ammonia are subjected to liquid phase hydrogenation to generate cyclohexylamine and dicyclohexylamine, the yield of the product cyclohexylamine and dicyclohexylamine is 3:1, the conversion rate of cyclohexanol is about 70%, and no industrial report is found in China. The aniline catalytic hydrogenation method: the process of producing cyclohexylamine with benzene as material includes two steps of producing aniline directly with one benzene step and catalytic hydrogenation of aniline. The catalytic aniline hydrogenation process has two technological routes of normal pressure and pressurization. Both processes have the advantages of mature process and easily obtained raw materials, but the device has small universality, only can produce single cyclohexylamine, and cannot be used for producing other organic amines; and the process has the defects of low single pass conversion rate of the aniline, poor selectivity of the cyclohexylamine and the like.
However, the aniline catalytic hydrogenation has more operable space from the viewpoints of raw material source, cost advantage and process simplicity advantage and prospect, so the method is favored by domestic and foreign research institutions. A plurality of methods for preparing Ni catalysts are introduced and researched by Mink and the like of Hungarian science research institute in the "Hydrogenation of aniline to cyclic hexylamine amine on NaOH-promoted or Lanthana supported Nickel", and the discovery shows that in the gas phase reaction for preparing cyclohexylamine by catalytic Hydrogenation of aniline, the traditional Ni catalyst is added into a NaOH auxiliary agent, so that the initial selectivity of cyclohexylamine can be improved by about 5%; DE1975457(Hydrogenation processes and chemosynthesis catalysts for the preparation of mixtures of cyclohexylamine and dicyclohexylamine from aniline) teaches that the Hydrogenation of aniline to a mixture of cyclohexylamine and dicyclohexylamine at 100-350 ℃ and 1-40 MPa gives very high yieldsYield and selectivity. The carrier of the heterogeneous catalyst adopted in the reaction is Al2O3The active components are 0.50 to 10 percent of Ru and Pd. At present, many research institutions make articles on the aniline catalytic hydrogenation catalyst in an effort, but the effect is not obvious, and the technical barriers and obstacles of the aniline catalytic hydrogenation catalyst are difficult to break successfully. Namely, the prior methods have the problems of low yield and low selectivity of the cyclohexylamine in the process of synthesizing the cyclohexylamine.
Disclosure of Invention
One of the technical problems to be solved by the invention is the problem that the yield and the selectivity of the cyclohexylamine are low, and the invention provides a novel hydrogenation catalyst for synthesizing the cyclohexylamine, which has the characteristics of high yield and high selectivity of the cyclohexylamine.
The second technical problem to be solved by the invention is the preparation method of the hydrogenation catalyst.
The third technical problem to be solved by the invention is the application of the hydrogenation catalyst.
In order to solve one of the above technical problems, the technical solution adopted by the present invention is as follows: the hydrogenation catalyst for synthesizing cyclohexylamine comprises a carrier and an active component, wherein the carrier is phosphorus modified Al2O3The active component comprises Co element and promoter element; the promoter element includes at least one metal element selected from alkali metals and group IIB metals.
In the technical scheme, the content of the phosphorus element in the carrier is preferably 0.10-3.00 g/L, such as but not limited to 0.152, 0.202, 0.302, 0.402, 0.502, 0.602, 0.792, 0.902, 1.02, 1.302, 1.502, 1.602, 1.702, 1.802, 1.902, 2.02, 2.52, 2.92 and the like, and more preferably 0.792-2.02 g/L.
In the above technical solution, the alkali metal in the hydrogenation catalyst is preferably at least one selected from Li, Na, K, Rb and Cs, and more preferably both Na and Li. Na and Li have synergistic effect in improving the yield and selectivity of cyclohexylamine. The ratio of Na to Li is not particularly limited, for example, but not limited to, the weight ratio of Na to Li is 0.102 to 10.00, and more specific non-limiting examples of the weight ratio within this range may be 0.202, 0.402, 0.502, 0.602, 0.802, 1.002, 1.202, 1.402, 1.602, 1.802, 2.002, 2.502, 3.002, 3.502, 4.002, 4.502, 5.002, 5.502, 6.002, 6.502, 7.002, 7.502, 8.002, and the like.
In the above technical solution, the group IIB metal in the hydrogenation catalyst is preferably at least one of Zn, Cd and Hg, and more preferably both Zn and Cd. Zn and Cd have synergistic effect in improving the yield of cyclohexylamine and the selectivity of cyclohexylamine. The ratio of Zn to Cd is not particularly limited, for example, but not limited to, the weight ratio of Zn to Cd is 0.102-10.00, and non-limiting examples of more specific weight ratios within this range may be 0.202, 0.402, 0.502, 0.602, 0.802, 1.002, 1.202, 1.402, 1.602, 1.802, 2.002, 2.502, 3.002, 3.502, 4.002, 4.502, 5.002, 5.502, 6.002, 6.502, 7.002, 7.502, 8.002, and the like.
In the above technical solution, the promoter element preferably includes at least one selected from alkali metal elements and at least one selected from group IIB metal elements at the same time, and at this time, there is a synergistic effect between the metal element in the alkali metal and the metal element in the group IIB metal in the aspect of improving the yield of cyclohexylamine and the selectivity of cyclohexylamine. By way of non-limiting example, such as but not limited to, lithium in conjunction with cadmium, lithium in conjunction with zinc, and the like. In this case, the ratio of the alkali metal element to the group IIB metal element is not particularly limited, and for example, but not limited to, the weight ratio of the alkali metal element to the group IIB metal element is 0.102 to 10.00, and more specific non-limiting examples of the weight ratio in this range may be 0.202, 0.402, 0.502, 0.602, 0.802, 1.002, 1.202, 1.402, 1.602, 1.802, 2.002, 2.502, 3.002, 3.502, 4.002, 4.502, 5.002, 5.502, 6.002, 6.502, 7.002, 7.502, 8.002, and the like.
In the technical scheme, the content of Co in the hydrogenation catalyst is preferably 1.00-8.00 g/L, such as but not limited to 1.4922g/L, 2.002g/L, 2.502g/L, 3.002g/L, 3.502g/L, 4.002g/L, 4.502g/L, 5.002g/L, 5.502g/L, 6.002g/L, 6.502g/L, 7.002g/L, 7.502g/L and the like, and more preferably 1.492-5.00 g/L.
In the technical scheme, the content of the promoter element in the hydrogenation catalyst is preferably 0.50-10.00 g/L, such as but not limited to 0.702g/L, 0.802g/L, 0.982g/L, 1.502g/L, 2.002g/L, 2.502g/L, 3.002g/L, 3.502g/L, 4.002g/L, 4.502g/L, 5.002g/L, 5.502g/L, 6.002g/L, 6.502g/L, 7.002g/L, 7.502g/L, 8.002g/L, 8.502g/L, 9.002g/L, 9.502g/L and the like; more preferably 0.982 to 6.00 g/L.
In the above technical solution, the vector is preferably obtained by a method comprising the following steps:
(1) preparing the compound containing phosphorus into an aqueous solution to impregnate Al2O3Drying to obtain the carrier precursor I;
(2) and roasting the carrier precursor I in a reducing and/or inert atmosphere to obtain the modified carrier.
In the above technical solution, the phosphorus-containing compound is preferably selected from phosphoric acid and ammonium phosphate ((NH)4)3PO4) Diammonium hydrogen phosphate ((NH)4)2HPO4And phosphorus pentoxide. Wherein the phosphoric acid is preferably at least one selected from hypophosphorous acid, phosphorous acid, orthophosphoric acid, pyrophosphoric acid and polyphosphoric acid, and preferably at least one selected from orthophosphoric acid, pyrophosphoric acid and polyphosphoric acid.
In the technical scheme, the drying temperature in the step (1) is preferably 100-120 ℃, such as but not limited to 105 ℃, 110 ℃ and 115 ℃; the drying time in step (1) is preferably 3 to 10 hours, such as but not limited to 4 hours, 5 hours, 6 hours, 7 hours, 8 hours, 9 hours and the like.
In the above technical solution, the gas in the step (2) is not particularly required, the inert atmosphere may be an inert gas (at least one of helium, neon and argon) of group 0 of the periodic table of elements and/or nitrogen, and the reducing gas may be hydrogen.
In the above technical scheme, the baking temperature in the step (2) is preferably 500-700 ℃, for example, but not limited to 550 ℃, 600 ℃, 650 ℃, and the like. The time for calcination is preferably 3 to 10 hours, such as but not limited to 4 hours, 5 hours, 6 hours, 7 hours, 8 hours, 9 hours, and the like.
To solve the second technical problem, the technical solution of the present invention is as follows:
the method for preparing a hydrogenation catalyst according to any of the preceding technical problems, comprising the steps of:
(i) mixing a solution containing cobalt element and promoter element with a carrier according to the composition of the catalyst to obtain a catalyst precursor;
(ii) drying to obtain the catalyst.
In the above-mentioned technical solution, as a non-limiting example, the specific compound corresponding to the cobalt element in the step (i) is preferably at least one selected from cobalt acetate, cobalt ammonium sulfate, cobalt chloride, cobalt nitrate, cobalt oxalate, cobalt sulfate, cobalt carbonate and cobalt phosphate; more preferably cobalt ammonium sulfate.
In the above technical solution, as a non-limiting example, when the specific compound corresponding to the alkali metal element in the step (i) is preferably at least one selected from the group consisting of alkali metal oxide, alkali metal hydroxide, alkali metal chloride, alkali metal sulfate, alkali group metal nitrate and alkali metal acetate; more preferably at least one of an alkali metal acetate; most preferably at least one selected from the group consisting of sodium acetate and lithium acetate.
In the above technical solution, as a non-limiting example, the specific compound corresponding to the group IIB metal element in step (i) is preferably at least one selected from zinc citrate, zinc gluconate, zinc acetate, zinc nitrate, cadmium acetate, cadmium chloride, cadmium nitrate, mercury acetate, mercurous nitrate, and mercury sulfate; more preferably at least one of zinc citrate and cadmium acetate.
In the above technical scheme, the drying temperature in step (ii) is preferably 30 to 120 ℃, for example, but not limited to, 60 ℃, 70 ℃, 80 ℃, 90 ℃, 100 ℃, 110 ℃, more preferably 80 to 120 ℃; the drying time in step (ii) is preferably 1 to 5 hours, such as but not limited to 1.5 hours, 2.0 hours, 2.5 hours, 3.0 hours, 3.5 hours, 4.0 hours, 4.5 hours, and the like.
To solve the third technical problem, the technical scheme of the invention is as follows:
the use of a catalyst according to any of the preceding technical solutions for the synthesis of cyclohexylamine.
The key to the present invention is the choice of catalyst, which can be reasonably determined by one skilled in the art for the specific process conditions to be applied and without inventive effort.
For example, the specific application method may be:
according to the synthesis method of the cyclohexylamine, in the presence of the hydrogenation catalyst in any one of the technical schemes in one of the technical problems, hydrogen and aniline react to obtain the cyclohexylamine.
In the above technical scheme, the raw material ratio is preferably: the molar ratio of hydrogen to aniline is (20.0 to 40.0)/1.0, and the most preferable raw material ratio is (25.0 to 35.0)/1.0.
In the technical scheme, the temperature of the hydrogenation reaction is preferably 120-300 ℃, and more preferably 185-220 ℃.
In the technical scheme, the preferred volume space velocity of the hydrogenation reaction is 1800-3000 h-1More preferably 2100 to 2800h-1。
In the technical scheme, the pressure of the hydrogenation reaction is preferably 0.05-0.50 MPa.
Unless otherwise specified, the pressures described herein are in terms of gauge pressure.
Aniline is commercially available or can be synthesized by ammoxidation of benzene. In the method for synthesizing cyclohexylamine according to the present invention, it is well known to those skilled in the art to select a suitable catalyst for the ammoxidation reaction of benzene and to determine a suitable reaction temperature, time and material ratio. For example, but not limited to, the active component of the catalyst is mainly Ni or Cu, and Ti, Cr and the like are added as auxiliary components. The carrier used can be activated carbon, alumina gel, silica gel or molecular sieve.
Ni-Ti/SiO is preferred in the present invention2Is a catalyst for direct ammoniation and oxidation reaction of benzene by one-step method. Suitable Ni-Ti/SiO2The content of the nickel element in the catalyst is preferably 2.50-5.00 g/L, and more preferably 3.00-4.50 g/L; the content of titanium element is preferably 0.50 to 3.00g/L, more preferably 1.00 to 2.00 g/L. The temperature of the appropriate ammoniation oxidation reaction is preferably 80-350 ℃; the pressure of the ammoniation oxidation reaction is preferably 8.0-50.0 MPa; the time of the ammoniation oxidation reaction is preferably 0.5-5 h; the molar ratio of benzene to hydroxylamine hydrochloride is preferably 0.5 to 3.0. After the completion of the ammoxidation of benzene, the reaction mixture may be subjected toThe mixture of the benzene amination and oxidation reaction is separated to obtain the target product aniline, and then catalytic hydrogenation is carried out, or the aniline is generated by benzene amination and oxidation and then catalytic hydrogenation is directly carried out without separation. However, in order to eliminate other impurities to cause the system to be complicated and convenient for comparison, the specific embodiment of the invention adopts pure aniline for catalytic hydrogenation.
The product mixture of the hydrogenation reaction can be separated to obtain the target product cyclohexylamine.
The product after hydrogenation reaction is analyzed by a gas chromatography-MASS spectrometer (GC-MASS), and the yield and selectivity of cyclohexylamine are calculated according to the following formula:
compared with the prior art, the hydrogenation catalyst provided by the invention improves the yield and selectivity of cyclohexylamine.
Experimental results show that when the method is adopted, the yield of the cyclohexylamine reaches 81.55%, the selectivity reaches 91.56%, and a better technical effect is achieved. Particularly, when the hydrogenation catalyst carrier is modified by phosphorus, and the active component of the hydrogenation catalyst simultaneously comprises cobalt, at least one metal element selected from alkali metals and at least one metal element selected from group IIB metals, more outstanding technical effects are obtained. The invention is further illustrated by the following examples.
Detailed Description
[ example 1 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and an aqueous solution of 1.88g Li-containing lithium acetate (LiOAc) 200ml were immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L and a Li content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.55% and the selectivity 91.56%, and for ease of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 2 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Standing for 24h at 110 deg.CDrying for 4 hours to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and zinc citrate containing 1.88g Zn (Zn)3(C6H5O7)2·2H2O) 200ml of an aqueous solution was immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L and a Zn content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.32% and the selectivity 91.74%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of cyclohexylamine and the selectivity are shown in tables 1 and 2, respectively.
[ COMPARATIVE EXAMPLE 1 ]
Are comparative examples of [ example 1 ] and [ example 2 ].
Preparation of hydrogenation catalyst:
(i) will contain 2.18g of cobalt ammonium Co sulfate ((NH)4)2Co(SO4)2·6H2O) 200ml of the aqueous solution was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3To obtain a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The Co content of the catalyst was determined by ICP to be 2.18 g/L.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 70.18% and the selectivity 83.21%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
Compared with the examples 1-2, the catalyst which adopts the phosphorus-containing compound to modify the carrier and hydrogenate has the active components containing Co and Li and Co and Zn better than the catalyst containing Co, shows that the active components of the hydrogenation catalyst simultaneously contain Co and at least one metal element selected from alkali metals and IIB group metals, is favorable for improving the activity and stability of the hydrogenation catalyst, and has high yield and selectivity of cyclohexylamine.
[ COMPARATIVE EXAMPLE 2 ]
Comparative example [ comparative example 1 ].
Modified supportP/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) 200ml of an aqueous solution, immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The Co content of the catalyst was determined by ICP to be 2.18 g/L.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 72.69% and the selectivity 85.34%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
As can be seen from comparison with comparative example 1, the present invention employs phosphorusModified Al2O3The prepared hydrogenation catalyst is more than that of directly using Al2O3The performance of the prepared hydrogenation catalyst is better, which indicates that P/Al is used2O3Is beneficial to the catalytic hydrogenation of aniline, and has high yield and selectivity of cyclohexylamine.
[ example 3 ]
Modified support P/Al2O3The preparation of (1):
(1) ammonium phosphate (NH) containing 0.80g P4)3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was determined to be 0.80g/L by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and 200ml of an aqueous solution containing 1.88g K potassium acetate (KOAc) were immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L and a K content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. The mixed gas after reaction is reactedThe bottom of the reactor enters a condenser for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.45% and the selectivity 91.48%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 4 ]
Modified support P/Al2O3The preparation of (1):
(1) diammonium hydrogen phosphate ((NH) containing 2.00g P4)2HPO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 2.00g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and an aqueous solution of 1.88g Rb of rubidium acetate (RbOAc) 200ml were immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L and an Rb content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1Enters a reactor at a space velocity of the volume and reactsThe temperature was 187 ℃ and the reaction pressure (gauge pressure) was 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.46% and the selectivity 91.47%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 5 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and an aqueous solution 200ml of rubidium acetate (CsOAc) containing 1.88g Cs were immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The Co content of the catalyst is 2.18g/L and the Cs content is 1.88g/L through ICP measurement.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the raw gas is mixed with 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.40% and the selectivity 91.50%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 6 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and an aqueous solution of 1.88g of Na rubidium acetate (NaOAc) 200ml were immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L and a Na content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
filling 35ml of catalyst into a micro reactor, adopting nitrogen leakage test to ensure that no leakage point exists in the system, then introducing aniline into a vaporizer through a metering pump for vaporization, controlling the vaporization temperature of the vaporizer to be 190 ℃, introducing hydrogen into the vaporizer along the direction vertical to the flow direction of the aniline, mixing the hydrogen and the aniline to obtain a feed gas, and adding hydrogen into the feed gasAniline/aniline is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.43% and the selectivity 91.59%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 7 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co4)2Co(SO4)2·6H2O) and cadmium acetate (Cd (OA) containing 1.88g of CdC)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L and a Cd content of 1.88g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro-reactor, nitrogen is adopted for leakage test, aniline enters a vaporizer for vaporization through a metering pump after no leakage point of the system is ensured, and steam is controlledThe vaporization temperature of the vaporizer is 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of aniline, and the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio) after being mixed by the vaporizer. Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.35% and the selectivity 91.69%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 8 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 1.50g of Co4)2Co(SO4)2·6H2O) and mercury acetate (Hg (OA) containing 1.00g HgC)2·2H2O) was dissolved in cold water to obtain 200ml of an immersion liquid and the immersion liquid was immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 1.50g/L and an Hg content of 1.00g/L as determined by ICP.
Synthesis of cyclohexylamine:
charging 35ml of catalyst into a microreactorAnd (3) adopting nitrogen leakage testing to ensure that a leakage point does not exist in the system, introducing aniline into a vaporizer through a metering pump to vaporize, controlling the vaporization temperature of the vaporizer to be 190 ℃, introducing hydrogen into the vaporizer in a direction vertical to the flow direction of the aniline, and mixing the hydrogen and the aniline through the vaporizer to obtain a feed gas, wherein the molar ratio of the hydrogen to the aniline in the feed gas is 30.0/1.0. Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 79.95% and the selectivity 90.89%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of cyclohexylamine and the selectivity are shown in tables 1 and 2, respectively.
[ example 9 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 5.00g of Co4)2Co(SO4)2·6H2O) and Zinc acetate containing 6.00g Zn (OA)C)2·2H2O) 200ml of an aqueous solution was immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 3.00g/L and a Zn content of 6.00g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 81.17% and the selectivity 90.20%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 10 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 0.98g of Zn and 0.90g of Cd4)2Co(SO4)2·6H2O), zinc citrate (Zn)3(C6H5O7)2·2H2O) and cadmium acetate (Cd (OA)C)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Zn content of 0.98g/L and a Cd content of 0.90g/L determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 82.28% and the selectivity 92.39%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of cyclohexylamine and the selectivity are shown in tables 1 and 2, respectively.
As can be seen from the comparison between example 10 and examples 2 and 7, in the hydrogenation catalyst used in the present invention, the metal element Zn and the metal element Cd in the group IIB metal have a better synergistic effect in increasing the yield and selectivity of cyclohexylamine.
[ example 11 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 1.02g of Li and 0.86g of Na4)2Co(SO4)2·6H2200ml of an aqueous solution of O), lithium acetate (LiOAc) and sodium acetate (NaOAc) was immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst had a Co content of 2.18g/L, a Li content of 1.02g/L and a Na content of 0.86g/L as determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 82.48% and the selectivity 92.16%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
From the comparison between example 11 and examples 1 and 6, it can be seen that in the hydrogenation catalyst used in the present invention, the metallic element Li and the metallic element Na in the alkali metal have a better synergistic effect in increasing the yield and selectivity of cyclohexylamine.
[ example 12 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution of (1L) in diameter6mm, pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 0.92g of Li and 0.96g of Zn)4)2Co(SO4)2·6H2O), lithium acetate (LiOAc) and zinc citrate (Zn)3(C6H5O7)2·2H2O) 200ml of an aqueous solution was immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Li content of 0.92g/L and a Zn content of 0.96g/L as measured by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 83.11% and the selectivity 92.79%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
From the comparison between example 12 and examples 1 and 2, it can be seen that in the hydrogenation catalyst used in the present invention, the metallic element Zn in the group IIB metal and the metallic element Li in the alkali metal have a better synergistic effect in increasing the yield and selectivity of cyclohexylamine.
[ example 13 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 0.92g of Li and 0.96g of Cd4)2Co(SO4)2·6H2O), lithium acetate (LiOAc) and cadmium acetate (Cd (OA)C)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Li content of 0.92g/L and a Cd content of 0.96g/L determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature was 187 ℃ and the reaction pressure (gauge pressure) was 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 83.21% and the selectivity 92.67%, and for ease of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
From the comparison between example 13 and examples 1 and 7, it is shown that in the hydrogenation catalyst used in the present invention, the metallic element Cd in the group IIB metal and the metallic element Li in the alkali metal have a better synergistic effect in increasing the yield and selectivity of cyclohexylamine.
[ example 14 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 0.92g of Li, 0.54g of Zn and 0.42g of Cd4)2Co(SO4)2·6H2O), lithium acetate (LiOAc), zinc citrate (Zn)3(C6H5O7)2·2H2O) and cadmium acetate (Cd (OA)C)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Li content of 0.92g/L, a Zn content of 0.54g/L and a Cd content of 0.42g/L determined by ICP.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 84.45% and the selectivity 93.76%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the yield of cyclohexylamine and the selectivity are shown in tables 1 and 2, respectively.
From the comparison between example 14 and examples 12 and 13, it can be seen that in the hydrogenation catalyst used in the present invention, the metallic elements Zn and Cd in the group IIB metal and the metallic element Li in the alkali metal have a better synergistic effect in increasing the yield and selectivity of cyclohexylamine.
[ example 15 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) 2.18g of Co, containing0.92g Na, cobalt ammonium sulfate ((NH) containing 0.54g Zn and 0.42g Cd4)2Co(SO4)2·6H2O), sodium acetate (NaOAc), zinc citrate (Zn)3(C6H5O7)2·2H2O) and cadmium acetate (Cd (OA)C)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Na content of 0.92g/L, a Zn content of 0.54g/L and a Cd content of 0.42g/L through ICP determination.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 84.54% and the selectivity 93.54%, and for convenience of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed amount, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
[ example 16 ]
Modified support P/Al2O3The preparation of (1):
(1) phosphoric acid (H) containing 1.48g P3PO4) 180ml of the aqueous solution (A) was immersed in 1L of a solution having a diameter of 6mm and a pore volume of 0.92cm3A specific surface area of 200 cm/g2Al in g2O3Then, the mixture is kept still for 24 hours and dried for 4 hours at 110 ℃ to obtain the carrier precursor I.
(2) Roasting the carrier precursor I for 5h at 630 ℃ in the atmosphere of nitrogen gas to obtain the modified carrier P/Al2O3。
The P content in the carrier was 1.48g/L as determined by ICP.
Preparation of hydrogenation catalyst:
(i) cobalt ammonium sulfate ((NH) containing 2.18g of Co, 0.48g of Li, 0.44g of Na, 0.54g of Zn and 0.42g of Cd4)2Co(SO4)2·6H2O), lithium acetate (LiOAc), sodium acetate (NaOAc), zinc citrate (Zn)3(C6H5O7)2·2H2O) and cadmium acetate (Cd (OA)C)2·2H2O) was dissolved in an aqueous solution of acetic acid having a concentration of 10 wt% to obtain 200ml of an immersion liquid immersed in P/Al2O3Obtaining a catalyst precursor I;
(ii) drying at 110 ℃ for 4 hours to obtain the catalyst.
The catalyst has a Co content of 2.18g/L, a Li content of 0.48g/L, a Na content of 0.44g/L, a Zn content of 0.54g/L and a Cd content of 0.42g/L through ICP determination.
Synthesis of cyclohexylamine:
35ml of catalyst is filled in a micro reactor, nitrogen leakage test is adopted, after no leakage point of the system is ensured, aniline enters a vaporizer through a metering pump to be vaporized, the vaporization temperature of the vaporizer is controlled to be 190 ℃, hydrogen enters the vaporizer along the direction vertical to the flow direction of the aniline, and the aniline and the hydrogen are mixed through the vaporizer to obtain feed gas, wherein the hydrogen/aniline in the feed gas is 30.0/1.0 (molar ratio). Then, the feed gas is used for 2400h-1The reaction temperature is 187 ℃, and the reaction pressure (gauge pressure) is 0.28 MPa. And the reacted mixed gas enters a condenser from the bottom of the reactor for condensation, and the product is analyzed.
The yield of cyclohexylamine was analytically calculated to be 85.18% and the selectivity 94.33%, and for ease of illustration and comparison, the support modification of the hydrogenation catalyst, the preparation of the hydrogenation catalyst, the reaction conditions, the feed rates, the cyclohexylamine yield and selectivity are shown in tables 1 and 2, respectively.
From the comparison between example 16 and examples 14 and 15, it is shown that in the hydrogenation catalyst used in the present invention, the metallic elements Zn and Cd in group IIB metals and the metallic elements Li and Na in alkali metals have a good synergistic effect in increasing the yield and selectivity of cyclohexylamine.
TABLE 1
TABLE 2
Claims (8)
1. The hydrogenation catalyst for synthesizing cyclohexylamine comprises a carrier and an active component, wherein the carrier is phosphorus modified Al2O3The active component comprises Co element and promoter element; the promoter elements include Na in alkali metals and Zn and Cd in Li and IIB group metals.
2. The hydrogenation catalyst according to claim 1, wherein the carrier contains 0.10 to 3.00g/L of phosphorus.
3. The hydrogenation catalyst according to claim 1, wherein the content of Co element in the hydrogenation catalyst is 1.00-8.00 g/L.
4. The hydrogenation catalyst according to claim 1, wherein the content of the promoter element in the hydrogenation catalyst is 0.50 to 10.00 g/L.
5. Hydrogenation catalyst according to claim 1, characterized in that the support is obtained with a process comprising the following steps:
(1) preparing the compound containing phosphorus into an aqueous solution to impregnate Al2O3Drying to obtain the carrier precursor I;
(2) and roasting the carrier precursor I in a reducing and/or inert atmosphere to obtain the modified carrier.
6. A hydrogenation catalyst according to claim 5, characterised in that the phosphorus-containing compound is selected from at least one of phosphoric acid, ammonium phosphate, diammonium phosphate and phosphorus pentoxide.
7. A process for preparing a hydrogenation catalyst as claimed in claim 1, comprising the steps of:
(i) mixing a solution containing cobalt element and promoter element with a carrier according to the composition of the catalyst to obtain a catalyst precursor;
(ii) drying to obtain the catalyst.
8. Use of the catalyst of any one of claims 1 to 6 in the synthesis of cyclohexylamine.
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| CN1149287A (en) * | 1994-05-27 | 1997-05-07 | 希巴-盖吉股份公司 | Process for the preparation of unsaturated amino compounds |
| CN1469851A (en) * | 2000-10-13 | 2004-01-21 | �����ɷ� | Method for the hydrogenation of unsubstituted or alkyl substituted aromatics |
| AU2014285704A1 (en) * | 2013-07-05 | 2015-10-15 | Cadila Healthcare Limited | Synergistic compositions |
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| CN1149287A (en) * | 1994-05-27 | 1997-05-07 | 希巴-盖吉股份公司 | Process for the preparation of unsaturated amino compounds |
| CN1469851A (en) * | 2000-10-13 | 2004-01-21 | �����ɷ� | Method for the hydrogenation of unsubstituted or alkyl substituted aromatics |
| AU2014285704A1 (en) * | 2013-07-05 | 2015-10-15 | Cadila Healthcare Limited | Synergistic compositions |
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