CN107866266B - Catalyst for production of cyclohexylbenzene - Google Patents

Catalyst for production of cyclohexylbenzene Download PDF

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CN107866266B
CN107866266B CN201610852205.1A CN201610852205A CN107866266B CN 107866266 B CN107866266 B CN 107866266B CN 201610852205 A CN201610852205 A CN 201610852205A CN 107866266 B CN107866266 B CN 107866266B
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catalyst
solution
zeolite molecular
molecular sieve
cyclohexylbenzene
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CN107866266A (en
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刘仲能
韩亚梅
王德举
郭友娣
钱斌
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
    • B01J29/74—Noble metals
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/10—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of aromatic six-membered rings
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    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
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    • C07C2523/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of noble metals of the platinum group metals
    • C07C2523/44—Palladium
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    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
    • C07C2523/72—Copper
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
    • C07C2529/74—Noble metals
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00—Catalysts comprising molecular sieves
    • C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
    • C07C2529/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65 containing iron group metals, noble metals or copper
    • C07C2529/76—Iron group metals or copper

Abstract

The invention relates to a catalyst for producing cyclohexylbenzene, a preparation method thereof and a method for synthesizing cyclohexylbenzene by a benzene hydroalkylation one-step method, and mainly solves the technical problems of high cyclohexane yield and low cyclohexylbenzene yield of a byproduct in a reaction caused by the catalyst in the prior art. The catalyst for producing the cyclohexylbenzene comprises a carrier and the following active components: (1) 0.5-20 g/L of Pd; (2)0 to 50g/L of at least one lanthanide; (3) 0-30 g/L of at least one IB group element, wherein the carrier is a hydrogen zeolite molecular sieve, and the technical scheme has a good effect, and can be used for preparing cyclohexylbenzene by a benzene hydroalkylation one-step method.

Description

Catalyst for production of cyclohexylbenzene
Technical Field
The invention relates to a catalyst for producing cyclohexylbenzene, a preparation method thereof and a method for synthesizing cyclohexylbenzene by a benzene hydroalkylation one-step method.
Background
The cyclohexylbenzene is an important intermediate and is widely applied to the fields of liquid crystal, plastics, coatings, adhesives and the like. The cyclohexylbenzene liquid crystal has the characteristics of extremely high chemical stability, photochemical stability, low viscosity, excellent physical properties and the like, and is one of ideal materials of display devices. The cyclohexylbenzene is used as an additive of the lithium ion battery electrolyte, has the overcharge prevention performance and can improve the safety performance of the battery. In addition, phenol and cyclohexanone can be prepared through the peroxidation and decomposition reaction processes of cyclohexylbenzene, and the method is used for producing a large amount of chemical raw materials such as phenolic resin, caprolactam, nylon and the like and has a good application prospect. Process for preparing cyclohexylbenzeneThe basic information is as follows: colorless liquid with CAS number 827-52-1 and molecular weight of C12H16Density 0.95g/cm3The boiling point is 238-240 ℃, the melting point is 5 ℃, and the flash point is 98 ℃.
The preparation method of the cyclohexylbenzene comprises the following steps: biphenyl selective hydrogenation, benzene and cyclohexene alkylation, and benzene hydrogenation alkylation. Wherein, the reaction principle of preparing the cyclohexylbenzene by benzene hydroalkylation is as follows (formula 1): according to the reaction mechanism of benzene hydrogenation alkylation, benzene is subjected to hydrogenation reaction on a metal center, so that cyclohexene can be selectively generated, and part of cyclohexane and cyclohexadiene are generated at the same time; cyclohexene and cyclohexadiene undergo alkylation with benzene on an acidic center to produce cyclohexylbenzene as a main product. Therefore, the benzene hydroalkylation can be realized to produce the cyclohexylbenzene by adopting the bi-component catalyst with the hydrogenation function and the alkylation function.
Figure GDA0001212440260000011
The first study on the hydroalkylation of benzene to produce cyclohexylbenzene began in the seventies and eighties of the 20 th century. The catalyst developed in the early stage has the problem of low selectivity of cyclohexylbenzene, for example, a catalyst loaded with hydrogenation metal is developed by ExxonMobil company based on MCM-22 series molecular sieves (U.S. Pat. No. 5,2011/0015457A 1, U.S. Pat. No. 3,2011/0021841A 1) and is used for preparing cyclohexylbenzene by benzene hydroalkylation, and the selectivity of the technology to byproduct cyclohexane is high. U.S. Pat. Nos. US4094918, US4219689 and US4329531 of Phillips oil company, USA, use Ni-rare earth treated zeolite catalyst and Pd as adjuvant, and both the conversion rate of benzene and the yield of CHB are low. The method has the problems of high yield of the cyclohexane as a byproduct and relatively low yield of the cyclohexylbenzene as a product in the process of preparing the cyclohexylbenzene.
Disclosure of Invention
One of the technical problems to be solved by the invention is the problems of high yield of the byproduct cyclohexane and low yield of the main product cyclohexylbenzene in the prior art, and the catalyst for producing the cyclohexylbenzene has the advantages of low yield of the cyclohexane and high yield of the cyclohexylbenzene when being used for synthesizing the cyclohexylbenzene by reacting benzene and hydrogen.
The second technical problem to be solved by the present invention is a method for preparing the catalyst.
The invention also provides a synthesis method of cyclohexylbenzene by using the catalyst.
One of the technical solutions of the present invention to solve the above technical problems is as follows: the catalyst for producing the cyclohexylbenzene comprises a carrier and the following active components:
(1) 0.5-20 g/L of Pd;
(2)0 to 50g/L of at least one lanthanide;
(3)0 to 30g/L of at least one element of group IB;
wherein the carrier is a hydrogen type zeolite molecular sieve.
In the above technical solution, the lanthanide is preferably Nd, Eu or Dy.
In the above technical solution, it is further preferable that the lanthanoid includes Nd and Eu at the same time, or Nd and Dy at the same time, or Eu and Dy at the same time, and each two of the lanthanoid elements have a synergistic effect in improving the yield of CHB.
In the technical scheme, Nd, Eu and Dy are preferably contained at the same time, and the Nd, the Eu and the Dy have ternary synergistic action.
In the technical scheme, the IB element is preferably Cu, and Cu and lanthanide have synergistic effect in the aspect of improving CHB yield.
In the above technical scheme, the zeolite molecular sieve is preferably selected from BEA, MOR or MWW zeolite molecular sieve; more preferred zeolite molecular sieve supports are BEA zeolite molecular sieves.
In the above technical scheme, the BEA zeolite molecular sieve is preferably a binderless molded BEA zeolite molecular sieve. The mole ratio of silicon dioxide/aluminum oxide of the binderless formed BEA zeolite molecular sieve is preferably 10-100, and more preferably 20-60.
In the technical scheme, the content of the lanthanide in the catalyst is preferably more than 0 and less than or equal to 50g/L, and more preferably 4-30 g/L.
In the technical scheme, the content of the IB group element in the catalyst is preferably more than 0 and less than or equal to 30g/L, and more preferably 2-20 g/L.
To solve the second technical problem, the technical solution of the present invention is as follows: the preparation method of the catalyst in the technical scheme of one of the technical problems comprises the following steps:
a) obtaining the hydrogen-form zeolite molecular sieve;
b) preparing a compound with required amount of Pd into a solution I; the optional compound comprises one of palladium chloride, palladium nitrate, ammonium chloropalladate and ammonium chloropalladite, the solvent adopted by the solution can be water, and the pH value of the solution is adjusted to be 2.0-6.5 by hydrochloric acid or nitric acid or acetic acid, and in order to facilitate the same proportion, 1mol/L acetic acid aqueous solution is used as the solvent in the embodiment and the comparative example in the specific embodiment of the invention;
c) preparing a required amount of lanthanide compound into a solution II;
d) preparing a required amount of compound of the IB group element into a solution III;
e) loading the solution I prepared in the step b), the solution II prepared in the step c) and the solution III prepared in the step d) on the zeolite molecular sieve carrier prepared in the step a) by adopting an impregnation method, drying, and roasting at 350-550 ℃ for 3-6 hours to prepare the catalyst.
In the above technical scheme, the compound of Pd in the step b) is preferably palladium chloride.
In the above technical scheme, the lanthanide compound in step c) is preferably nitrate.
In the above technical solution, the compound of group IB element in step d) is preferably nitrate.
In the above technical scheme, the impregnation procedure of step e) adopts mixed impregnation:
and uniformly mixing the solution I, the solution II and the solution III, and then dipping, drying and roasting the mixture together. The impregnation method is mixed impregnation.
The third technical solution of the present invention to solve the above technical problems is as follows: the synthesis method of the cyclohexylbenzene takes benzene and hydrogen as reaction raw materials, and the reaction raw materials are contacted with the catalyst in any technical scheme of the technical problem to carry out benzene hydroalkylation reaction to generate the cyclohexylbenzene.
In the technical scheme, the reaction temperature is preferably 100-200 ℃, and more preferably 120-180 ℃.
In the above technical scheme, the molar ratio of benzene to hydrogen in the reaction raw material is preferably 0.5 to 2.0, and more preferably 0.5 to 1.3.
In the above-mentioned technical means, the pressure of the reaction is preferably 0.5 to 3.0MPa (gauge pressure), and more preferably 0.5 to 2.0MPa (gauge pressure).
In the technical scheme, the liquid volume space velocity of the reaction raw material benzene is preferably 0.2-2 h-1More preferably 0.2 to 1.5 hours-1。
The catalyst of the invention simultaneously adopts Pd, lanthanide and IB group elements as active components, thereby reducing the yield of the cyclohexane and increasing the yield of the p-cyclohexylbenzene. At the reaction temperature of 150 ℃, the molar ratio of benzene to hydrogen of 0.8, the pressure of 2.0MPa and the liquid volume space velocity of benzene of 0.5h-1Under the conditions, the yield of the cyclohexane can reach below 5.0 percent, the yield of the cyclohexylbenzene can reach up to 32 percent, and a better technical effect is achieved.
Detailed Description
[ example 1 ]
1. Catalyst preparation
Weighing PdCl containing 1.9g Pd2Dissolving in 1mol/L hydrochloric acid water solution to prepare 80g of solution I; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve with diameter of 1mm and length of 5mm (the mole ratio of silicon dioxide/aluminum oxide is 40); loading the solution I on a hydrogen type BEA zeolite molecular sieve, soaking for 12h at room temperature, drying for 12h at 100 ℃, and roasting for 4h at 450 ℃ to obtain the required catalyst.
2. Catalyst evaluation
10ml of the catalyst was charged into a fixed bed reactor, and activity evaluation was performed after reduction activation under the following conditions: the reaction temperature is 150 ℃, the molar ratio of benzene to hydrogen in the reaction raw material is 0.8, the reaction pressure is 2.0MPa (gauge pressure), and the liquid volume space velocity of the reaction raw material benzene is 0.5h-1。
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
Comparative example 1
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 1.6g of Nd was weighed3)3·6H2Dissolving O in water to prepare 40g of solution II; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, uniformly mixing the solution I and the solution II, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
Comparative example 2
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; weighing Eu (NO) containing 1.6g of Eu3)3·6H2Dissolving O in water to prepare 40g of solution II; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, uniformly mixing the solution I and the solution II, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
Comparative example 3
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; dy (NO) containing 1.6g Dy is weighed3)3·6H2Dissolving O in water to prepare 40g of solution II; measuring 0.1L of the product with diameter of 1mm and length of 5mm of cylindrical hydrogen type BEA zeolite molecular sieve without adhesive (the mol ratio of silicon dioxide to aluminum oxide is 40), the solution I and the solution II are evenly mixed and loaded on the hydrogen type BEA zeolite molecular sieve, the mixture is soaked for 12 hours at room temperature, dried for 12 hours at 100 ℃, and roasted for 4 hours at 450 ℃, and the needed catalyst is prepared.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
Comparative example 4
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; weighing Cu (NO) containing 1.6g of Cu3)2·3H2Dissolving O in water to prepare 40g of solution II; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, mixing the solution I and the solution II, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 2 ]
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 1.2g of Nd was weighed3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, mixing the solution I, the solution II and the solution III, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 3 ]
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; weighing Eu (NO) containing 1.2g of Eu3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, mixing the solution I, the solution II and the solution III, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 4 ]
1. Catalyst preparation
PdCl containing Pd 0.3g is weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; dy (NO) containing 1.2g Dy is weighed3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, mixing the solution I, the solution II and the solution III, loading the mixture on the hydrogen type BEA zeolite molecular sieve, soaking the mixture at room temperature for 12 hours, drying the mixture at 100 ℃ for 12 hours, and roasting the mixture at 450 ℃ for 4 hours to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 5 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.6g of Nd was weighed3)3·6H2O and Eu (NO) containing Eu 0.6g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 6 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.6g of Nd was weighed3)3·6H2O and Dy (NO) containing Dy 0.6g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 7 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; weighing Eu (NO) containing 0.6g Eu3)3·6H2O and Dy (NO) containing Dy 0.6g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 8 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.6g of Nd was weighed3)3·6H2O and Eu (NO) containing Eu 0.3g3)3·6H2O and Dy (NO) containing Dy 0.3g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 9 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.3g of Nd was weighed3)3·6H2O and Eu (NO) containing Eu 0.6g3)3·6H2O and Dy (NO) containing Dy 0.3g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 10 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.3g of Nd was weighed3)3·6H2O and Eu (NO) containing Eu 0.3g3)3·6H2O and Dy (NO) containing Dy 0.6g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (silica/alumina molar ratio is 40) with diameter of 1mm and length of 5mm, and loading the mixed solution into hydrogen typeSoaking the BEA zeolite molecular sieve at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 11 ]
1. Catalyst preparation
PdCl containing 0.3g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.4g of Nd was weighed3)3·6H2O and Eu (NO) containing Eu 0.4g3)3·6H2O and Dy (NO) containing Dy 0.4g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.4g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
As can be seen from the comparison of examples 2 to 11 with comparative examples 1 to 4, Cu and at least one selected from Nd, Eu and Dy have a synergistic effect in increasing CHB yield.
As can be seen from the comparison between examples 8 to 11 and examples 5 to 7, the ternary synergistic effect of Nd, Eu and Dy is stronger than the binary synergistic effect in improving the CHB yield.
[ example 12 ]
PdCl containing 0.5g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 1.8g of Nd was weighed3)3·6H2O and Eu1.2g of Eu (NO)3)3·6H2O and Dy (NO) containing Dy 1.2g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing Cu 2g3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 13 ]
1. Catalyst preparation
PdCl containing 0.1g Pd was weighed2Dissolving in 1mol/L hydrochloric acid water solution to prepare 40g of solution I; nd (NO) containing 0.3g of Nd was weighed3)3·6H2O and Eu 0.1g Eu (NO)3)3·6H2O and Dy (NO) containing Dy 0.1g3)3·6H2Dissolving O in water to prepare 20g of solution II; weighing Cu (NO) containing 0.2g of Cu3)2·3H2Dissolving O in water to prepare 20g of solution III; then uniformly mixing the solution I, the solution II and the solution III; weighing 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide to aluminum oxide is 40) with the diameter of 1mm and the length of 5mm, loading the mixed solution on the hydrogen type BEA zeolite molecular sieve, soaking at room temperature for 12h, drying at 100 ℃ for 12h, and roasting at 450 ℃ for 4h to obtain the required catalyst.
2. Catalyst evaluation
The catalyst evaluation method is shown in example 1.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
TABLE 1 catalyst composition and evaluation results
Figure GDA0001212440260000111
Note: in table 1, CH represents cyclohexane, and CHB represents cyclohexylbenzene.

Claims (7)

1. The catalyst for producing the cyclohexylbenzene comprises a carrier and the following active components:
(1) 0.5-20 g/L of Pd;
(2) 4-30 g/L of lanthanide;
(3) 2-20 g/L of an IB group element;
wherein the carrier is a hydrogen type zeolite molecular sieve; the lanthanide element simultaneously comprises Nd and Eu, or simultaneously comprises Nd and Dy, or simultaneously comprises Eu and Dy; the element in IB group is Cu.
2. The catalyst of claim 1, wherein said zeolite molecular sieve is selected from the group consisting of BEA, MOR and MWW zeolite molecular sieves.
3. The catalyst of claim 2 wherein the BEA zeolite molecular sieve selected is a binderless molded BEA zeolite molecular sieve.
4. The catalyst of claim 3, wherein the binderless formed BEA zeolite molecular sieve has a silica to alumina mole ratio of from 10 to 100.
5. A process for preparing the catalyst of claim 1, comprising the steps of:
a) obtaining the hydrogen-form zeolite molecular sieve;
b) preparing a compound with required amount of Pd into a solution I;
c) preparing a required amount of lanthanide compound into a solution II;
d) preparing a required amount of compound of the IB group element into a solution III;
e) loading the solution I prepared in the step b), the solution II prepared in the step c) and the solution III prepared in the step d) on the zeolite molecular sieve carrier prepared in the step a) by adopting an impregnation method, drying, and roasting at 350-550 ℃ for 3-6 hours to prepare the catalyst.
6. A method for synthesizing cyclohexylbenzene, which comprises using benzene and hydrogen as reaction raw materials, and contacting the reaction raw materials with the catalyst of any one of claims 1 to 4 to perform benzene hydroalkylation reaction to generate cyclohexylbenzene.
7. The method as set forth in claim 6, characterized in that the liquid volume space velocity of the reaction raw material benzene is 0.2-3 h-1。
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5482616A (en) * 1989-05-18 1996-01-09 Engelhard De Meern B. V. Process for hydrogenation and/or dehydrogenation
CN101998942A (en) * 2008-04-14 2011-03-30 埃克森美孚化学专利公司 Process for producing cyclohexylbenzene
CN102892733A (en) * 2010-05-20 2013-01-23 埃克森美孚化学专利公司 Hydroalkylation processes
CN105233861A (en) * 2014-07-11 2016-01-13 中国石油化工股份有限公司 Cyclohexyl benzene catalyst and synthetic method thereof
CN105439802A (en) * 2014-08-27 2016-03-30 中国石油化工股份有限公司 A method of preparing phenylcyclohexane by hydroalkylation
CN105582989A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst for synthesizing cyclohexylbenzene

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5482616A (en) * 1989-05-18 1996-01-09 Engelhard De Meern B. V. Process for hydrogenation and/or dehydrogenation
CN101998942A (en) * 2008-04-14 2011-03-30 埃克森美孚化学专利公司 Process for producing cyclohexylbenzene
CN102892733A (en) * 2010-05-20 2013-01-23 埃克森美孚化学专利公司 Hydroalkylation processes
CN105233861A (en) * 2014-07-11 2016-01-13 中国石油化工股份有限公司 Cyclohexyl benzene catalyst and synthetic method thereof
CN105439802A (en) * 2014-08-27 2016-03-30 中国石油化工股份有限公司 A method of preparing phenylcyclohexane by hydroalkylation
CN105582989A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst for synthesizing cyclohexylbenzene

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