CN107930682B - Catalyst for cyclohexylbenzene and preparation method thereof - Google Patents

Catalyst for cyclohexylbenzene and preparation method thereof Download PDF

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CN107930682B
CN107930682B CN201610894540.8A CN201610894540A CN107930682B CN 107930682 B CN107930682 B CN 107930682B CN 201610894540 A CN201610894540 A CN 201610894540A CN 107930682 B CN107930682 B CN 107930682B
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catalyst
cyclohexylbenzene
molecular sieve
benzene
hydrogen
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CN107930682A (en
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韩亚梅
刘仲能
王德举
郭友娣
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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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
    • B01J29/76—Iron group metals or copper
    • B01J29/7615—Zeolite Beta
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/74—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition with simultaneous hydrogenation
    • 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
    • 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
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

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Abstract

The invention relates to a catalyst of 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 yield of cyclohexane serving as a byproduct and low yield of cyclohexylbenzene serving as a main product in a reaction caused by the catalyst in the prior art. The invention provides a catalyst adopting cyclohexylbenzene, which comprises a carrier and an active component loaded on the carrier; the active component comprises a noble metal and iron; the noble metal includes at least one selected from platinum and palladium; the technical scheme that the carrier is selected from a hydrogen type zeolite molecular sieve obtains better effect, and can be used for preparing cyclohexylbenzene by a benzene hydroalkylation one-step method.

Description

Catalyst for cyclohexylbenzene and preparation method thereof
Technical Field
The invention relates to a catalyst of 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. The basic information for cyclohexylbenzene 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 GDA0001221298460000011
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 invention provides a cyclohexylbenzene catalyst which has the advantages of low yield of the cyclohexane and high yield of the cyclohexylbenzene when being used for synthesizing the cyclohexylbenzene by the reaction of 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.
In order to solve one of the above technical problems, the technical solution of the present invention is as follows:
a catalyst for cyclohexylbenzene, the catalyst comprising a carrier and an active component supported on the carrier; the active component comprises a noble metal and iron; the noble metal includes at least one selected from platinum and palladium; the carrier is selected from hydrogen type zeolite molecular sieve.
In the technical scheme, the content of the noble metal is preferably 0.5-20 g/L.
In the technical scheme, the content of the iron is preferably 1-25 g/L.
In the above technical scheme, the hydrogen type zeolite molecular sieve is preferably selected from BEA, MOR or MWW zeolite molecular sieves.
In the above technical solution, the hydrogen type zeolite molecular sieve is preferably a binder-free molded zeolite molecular sieve.
The invention uses iron to replace part of noble metal, thus saving the consumption of noble metal.
In the above technical solution, it is more preferable that the noble metal includes both platinum and palladium, and at this time, the noble metal and iron have a significant synergistic effect in increasing the yield of CHB, and we find that neither platinum alone nor palladium alone has a synergistic effect with iron.
The specific ratio of each of platinum and palladium is not particularly limited as long as platinum and palladium are simultaneously present in the catalyst, and both have synergistic effects in the same ratio, for example, but not limited to, the active components in the catalyst include:
the platinum content is: 0.5-20 g/L; the content of palladium is: 0.5-20 g/L; the content of iron is: 1-25 g/L.
In the above technical solution, the mole ratio of silica/alumina of the hydrogen-type zeolite molecular sieve is preferably 10 to 100, for example, but not limited to, 20, 30, 40, 50, 60, 70, 80, 90, and the like.
To solve the second technical problem, the technical solution of the present invention is as follows:
a process for preparing a catalyst as claimed in any one of claims 1 to 6, comprising the steps of:
(1) mixing required amounts of solutions of Pt compounds, Pd compounds and Fe compounds with the hydrogen-form zeolite molecular sieve;
(2) standing and drying;
(3) and roasting in an air atmosphere to obtain the catalyst.
In the above technical solution, the drying process conditions are not particularly limited, for example, but not limited to, the drying temperature is 70-120 ℃ (for non-limiting example, within this range, 80 ℃, 90 ℃, 100 ℃, 110 ℃, etc.), and the drying time is, for example, but not limited to, at least 6 hours, for example, 6-14 hours (for non-limiting example, within this range, 7, 8, 9, 10, 11, 12, etc.); the roasting temperature is preferably 350-550 ℃, and the roasting time is preferably 3-6 hours.
In the above technical solution, the Pt-containing compound in step (1) is preferably at least one selected from chloroplatinic acid, platinum chloride, and palladium nitrate.
In the above technical solution, the Pd-containing compound in step (1) is preferably at least one selected from palladium acetate, palladium nitrate, palladium chloride, and palladium sulfate.
In the above technical solution, the Fe-containing compound in step (1) is preferably at least one selected from iron sulfate, iron nitrate, and iron chloride.
In the technical scheme, the solvent adopted in the solution in the step (1) can be water and is adjusted to pH 3-6.5 by hydrochloric acid or nitric acid or acetic acid, and in order to facilitate the same proportion, the examples and comparative examples in the specific implementation mode of the invention are both adjusted to pH 6 by water and acetic acid.
To solve the third technical problem, the technical scheme of the invention 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 5.0MPa (gauge pressure), and more preferably 0.5 to 4.0MPa (gauge pressure).
In the technical scheme, the liquid volume of the reaction raw material benzene is preferably 0.2-3 h-1More preferably 0.2 to 1.5 hours-1。
The catalyst of the invention adopts Pt, Pd and Fe as active components, thus reducing the yield of cyclohexane as a byproduct, and obviously improving the yield of the target product CHB under the condition of simultaneously comprising Pt, Pd and Fe. At the reaction temperature of 150 ℃, the molar ratio of benzene to hydrogen of 0.8, the pressure of 2.0MPa and the mass 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 30 percent, and a better technical effect is achieved. The invention is further illustrated by the following examples.
Detailed Description
[ COMPARATIVE EXAMPLE 1 ]
Preparing a catalyst: weighing PtCl containing 1.0g of Pt4·5H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pt content of the catalyst was 10 g/L. The benzene conversion was calculated to be 72.56%, the yield of CH was 4.97%, and the yield of CHB was 25.98%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ COMPARATIVE EXAMPLE 2 ]
Preparing a catalyst: PdCl containing 1.0g Pd was weighed2Dissolving in 1mol/L acetic acid water solution to prepare 80g solution; measurement ofTaking 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pd content of the catalyst was 10 g/L. The benzene conversion was calculated to be 68.56%, the yield of CH was 4.25%, and the yield of CHB was 26.13%, and the composition of the catalyst and the evaluation results are shown in table 1 for convenience of illustration and comparison.
[ COMPARATIVE EXAMPLE 3 ]
Preparing a catalyst: fe (NO) containing 1.0g Fe was weighed out3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Fe content of the catalyst was 10 g/L. The calculated benzene conversion was 0%, the yield of CH was 0%, and the yield of CHB was 0%, and the composition of the catalyst and the evaluation results are shown in table 1 for convenience of illustration and comparison.
[ COMPARATIVE EXAMPLE 4 ]
Preparing a catalyst: separately weigh 0.5g Pt in PtCl4·5H2O and PdCl containing 0.5g Pd2Dissolving in 1mol/L acetic acid water solution to prepare 80g solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 catalyst has a Pt content of 5g/L and a Pd content of 5 g/L. The benzene conversion was calculated to be 49.29%, the yield of CH was 1.68%, and the yield of CHB was 26.76%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ example 1 ]
Preparing a catalyst: separately weigh 0.8g Pt in PtCl4·5H2O and Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution I; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pt content of the catalyst is 8g/L, and the Fe content is 2 g/L. The benzene conversion was calculated to be 45.58%, the yield of CH was 2.35%, and the yield of CHB was 21.36%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ example 2 ]
Preparing a catalyst: PdCl containing 0.8g Pd was weighed out2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution I; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pd content of the catalyst is 8g/L, and the Fe content is 2 g/L. The benzene conversion was calculated to be 46.86%, the yield of CH was 1.82%, and the yield of CHB was 20.92%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ example 3 ]
Preparing a catalyst: separately weigh 0.2g Pt in PtCl4·5H2O, PdCl containing 0.6g Pd2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pt content of the catalyst is 2g/L, the Pd content is 6g/L, and the Fe content is 2 g/L. The benzene conversion was calculated to be 50.87%, the yield of CH was 1.84%, and the yield of CHB was 28.88%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ example 4 ]
Preparing a catalyst: separately weigh 0.3g Pt in PtCl4·5H2O, PdCl containing 0.5g Pd2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 Pt content of the catalyst is 3g/L, the Pd content is 5g/L, and the Fe content is 2 g/L. The benzene conversion was calculated to be 51.58%, the yield of CH was 1.65%, and the yield of CHB was 29.55%, and the composition of the catalyst and the results of the evaluations are shown in Table 1 for ease of illustration and comparison.
[ example 5 ]
Preparing a catalyst: separately weigh 0.4g Pt in PtCl4·5H2O, PdCl containing 0.4g Pd2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 10ml of catalyst was taken and charged in a fixed bed reactor,after reduction activation, activity evaluation was performed 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 catalyst has Pt content of 4g/L, Pd content of 4g/L and Fe content of 2 g/L. The benzene conversion was calculated to be 51.47%, the yield of CH was 1.70%, and the yield of CHB was 29.23%, and the composition of the catalyst and the evaluation results are shown in table 1 for convenience of illustration and comparison.
[ example 6 ]
Preparing a catalyst: separately weigh 0.5g Pt in PtCl4·5H2O, PdCl containing 0.3g Pd2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 catalyst has Pt content of 5g/L, Pd content of 3g/L and Fe content of 2 g/L. The benzene conversion was calculated to be 51.22%, the yield of CH was 1.44%, and the yield of CHB was 28.44%, and the composition of the catalyst and the evaluation results are shown in table 1 for convenience of illustration and comparison.
[ example 7 ]
Preparing a catalyst: separately weigh 0.6g Pt in PtCl4·5H2O, PdCl containing 0.2g Pd2And Fe (NO) containing 0.2g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecules with diameter of 1mm and length of 5mmSieve (silica/alumina molar ratio 30); loading the solution 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.
Evaluation of catalyst: 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 Pt content of the catalyst is 6g/L, the Pd content is 2g/L, and the Fe content is 2 g/L. The benzene conversion was calculated to be 51.12%, the yield of CH was 1.52%, and the yield of CHB was 28.16%, and the composition of the catalyst and the evaluation results are shown in table 1 for convenience of illustration and comparison.
[ example 8 ]
Preparing a catalyst: separately weigh 0.5g Pt in PtCl4·5H2O, PdCl containing 1.0g Pd2And Fe (NO) containing 2.0g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 100 ℃, the molar ratio of benzene to hydrogen in the reaction raw material is 0.5, the reaction pressure is 0.5MPa (gauge pressure), and the liquid volume space velocity of the reaction raw material is 0.2h-1。
The catalyst has Pt content of 5g/L, Pd content of 10g/L and Fe content of 20 g/L. The benzene conversion was calculated to be 47.49%, the yield of CH was 2.11%, and the yield of CHB was 22.36%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
[ example 9 ]
CatalysisPreparation of the agent: separately weigh 0.1g Pt in PtCl4·5H2O, PdCl containing 0.3g Pd2And Fe (NO) containing 0.1g Fe3)3·9H2Dissolving O in 1mol/L acetic acid water solution to prepare 80g of solution; measuring 0.1L of binderless cylindrical hydrogen type BEA zeolite molecular sieve (the molar ratio of silicon dioxide/aluminum oxide is 30) with the diameter of 1mm and the length of 5 mm; loading the solution 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.
Evaluation of catalyst: 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 200 ℃, the molar ratio of benzene to hydrogen in the reaction raw material is 2.0, the reaction pressure is 3.0MPa (gauge pressure), and the liquid volume space velocity of the reaction raw material is 2.0h-1。
The Pt content of the catalyst is 1g/L, the Pd content is 3g/L, and the Fe content is 1 g/L. The benzene conversion was calculated to be 34.15%, the yield of CH was 1.36%, and the yield of CHB was 17.92%, and the composition of the catalyst and the evaluation results are shown in table 1 for ease of illustration and comparison.
TABLE 1 catalyst composition and evaluation results
Figure GDA0001221298460000091
Note: in table 1, CH represents cyclohexane, and CHB represents cyclohexylbenzene.

Claims (9)

1. A method for synthesizing cyclohexylbenzene comprises the steps of taking benzene and hydrogen as reaction raw materials, enabling the reaction raw materials to contact with a cyclohexylbenzene catalyst to carry out benzene hydroalkylation reaction to generate cyclohexylbenzene, wherein the catalyst comprises a carrier and an active component loaded on the carrier; the active component comprises a noble metal and iron; the noble metal comprises both platinum and palladium; the carrier is selected from hydrogen type zeolite molecular sieve.
2. The synthesis method according to claim 1, wherein the noble metal content is 0.5-20 g/L.
3. The synthesis method according to claim 1, wherein the iron content is 1-25 g/L.
4. The synthesis process according to claim 1, characterized in that the zeolitic molecular sieve is selected from the group consisting of BEA, MOR or MWW zeolitic molecular sieves.
5. The synthesis method according to claim 4, wherein the hydrogen form zeolite molecular sieve is a binderless formed zeolite molecular sieve.
6. A synthesis method according to claim 4, characterized in that the silica/alumina molar ratio of the hydrogen-form zeolite molecular sieve is 10-100.
7. A synthesis process according to any one of claims 1 to 6, characterised in that the catalyst is prepared by a process comprising the steps of:
(1) mixing required amounts of solutions of Pt compounds, Pd compounds and Fe compounds with the hydrogen-form zeolite molecular sieve;
(2) standing and drying;
(3) and roasting in an air atmosphere to obtain the catalyst.
8. The synthesis method according to claim 1, wherein the reaction temperature is 100-200 ℃.
9. The synthesis method according to claim 1, wherein the liquid volume space velocity of the reaction raw material benzene is 0.2-3 h-1。
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Citations (2)

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Publication number Priority date Publication date Assignee Title
CN102513145A (en) * 2011-11-14 2012-06-27 天津大学 Fe molecular sieve catalyst for purifying NOx in acrylonitrile oxidization tail gas and preparation method of Fe molecular sieve catalyst
CN105233862A (en) * 2014-07-11 2016-01-13 中国石油化工股份有限公司 Cyclohexyl benzene catalyst and preparation method therefor

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Publication number Priority date Publication date Assignee Title
CN102513145A (en) * 2011-11-14 2012-06-27 天津大学 Fe molecular sieve catalyst for purifying NOx in acrylonitrile oxidization tail gas and preparation method of Fe molecular sieve catalyst
CN105233862A (en) * 2014-07-11 2016-01-13 中国石油化工股份有限公司 Cyclohexyl benzene catalyst and preparation method therefor

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