CN109092295B - Isopropyl benzene catalyst and preparation method thereof - Google Patents
Isopropyl benzene catalyst and preparation method thereof Download PDFInfo
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- CN109092295B CN109092295B CN201710473479.4A CN201710473479A CN109092295B CN 109092295 B CN109092295 B CN 109092295B CN 201710473479 A CN201710473479 A CN 201710473479A CN 109092295 B CN109092295 B CN 109092295B
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- 239000003054 catalyst Substances 0.000 title claims abstract description 110
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 238000002360 preparation method Methods 0.000 title abstract description 20
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 16
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical compound CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 8
- 229910052751 metal Inorganic materials 0.000 claims abstract description 6
- 239000002184 metal Substances 0.000 claims abstract description 6
- 238000000034 method Methods 0.000 claims description 18
- 239000011148 porous material Substances 0.000 claims description 14
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 13
- 238000001354 calcination Methods 0.000 claims description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 6
- 229910052783 alkali metal Inorganic materials 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 239000012018 catalyst precursor Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 150000001339 alkali metal compounds Chemical class 0.000 claims description 3
- 150000001340 alkali metals Chemical class 0.000 claims description 3
- 150000002941 palladium compounds Chemical class 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 239000005078 molybdenum compound Substances 0.000 claims description 2
- 150000002752 molybdenum compounds Chemical class 0.000 claims description 2
- 238000011156 evaluation Methods 0.000 description 36
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 20
- 239000000243 solution Substances 0.000 description 19
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 18
- 239000007864 aqueous solution Substances 0.000 description 14
- 239000000203 mixture Substances 0.000 description 13
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 9
- 239000011609 ammonium molybdate Substances 0.000 description 9
- 229940010552 ammonium molybdate Drugs 0.000 description 9
- 235000018660 ammonium molybdate Nutrition 0.000 description 9
- 229910000027 potassium carbonate Inorganic materials 0.000 description 9
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 7
- 238000001035 drying Methods 0.000 description 7
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- -1 alkali metal salt Chemical class 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000003638 chemical reducing agent Substances 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000002195 synergetic effect Effects 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 241001147665 Foraminifera Species 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 150000007942 carboxylates Chemical class 0.000 description 1
- 238000009903 catalytic hydrogenation reaction Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- UOUJSJZBMCDAEU-UHFFFAOYSA-N chromium(3+);oxygen(2-) Chemical class [O-2].[O-2].[O-2].[Cr+3].[Cr+3] UOUJSJZBMCDAEU-UHFFFAOYSA-N 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000007613 slurry method Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/44—Palladium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/652—Chromium, molybdenum or tungsten
- B01J23/6525—Molybdenum
-
- B01J35/615—
-
- B01J35/633—
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- 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
- C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
-
- 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
Abstract
The invention relates to a cumene catalyst and a preparation method thereof, which mainly solve the technical problems of low AMS conversion rate and low cumene selectivity of the catalyst in the prior art.A technical scheme of adopting the cumene catalyst comprises a carrier and active components of (1) metal palladium or an oxide thereof and 0.05-10 g/L and (2) Mo or an oxide thereof and 0-5.00 g/L better solves the technical problems and can be used for the reaction of preparing cumene by hydrogenation of α -methyl styrene.
Description
Technical Field
The invention relates to a cumene catalyst, a preparation method thereof and application of the catalyst in preparation of cumene from α -methyl styrene through hydrogenation.
Background
At present, the global yield of the cumene is about ten million tons, more than 90 percent of the cumene is used for producing phenol and acetone, a byproduct α -methyl styrene (AMS) is usually generated in the process, the AMS is difficult to separate and remove in the subsequent refining process, but the cumene can be converted into raw material through hydrogenation and then returned to an oxidation process for use, so that the unit consumption of the cumene is reduced, the yield of the phenol is improved, the raw material cost is saved, and the like, so that the consumption of the raw material propylene and benzene can be reduced, and the technical and economic indexes of a device can be improved.
An annual phenol/acetone production apparatus of 1 ten thousand tons can produce 500 tons of AMS as a by-product, and AMS hydrogenation units are arranged in foreign phenol/acetone production apparatuses. The traditional method for preparing cumene through AMS hydrogenation is a slurry method, a Reney nickel catalyst is used, and the method has the defects of complex flow, low catalyst selectivity, short service cycle and the like. Slurry processes are gradually being replaced by fixed bed processes, where the performance of the hydrogenation catalyst is very critical. Many catalysts for preparing isopropylbenzene by AMS hydrogenation have been reported: the experiment of catalytic hydrogenation of AMS with platinum group metal as catalyst was studied in Zhai Teng; west German phenol chemical company adopted Cu2Cr2AMS hydrogenation of Ni, high-temp sintering of Pd/alumina catalyst by Chongheng, Pd/C catalyst for α -methyl styrene hydrogenation by Franco C, and Ni, Pt, Pd, Co and Cr by Little2O3And AMS selective hydrogenation performance of several metal alloy catalysts; in contrast, the activity and selectivity of a non-palladium catalyst are not high, and in recent years, a catalyst containing palladium as a main or sole component has attracted attention. AMS is active and has poor stability, and thus it is desirable that hydrogenation catalysts have high low temperature activity and selectivity, and adequate impurity resistance to increase the catalyst regeneration cycle and thus prolong the catalyst life.
U.S. Pat. No. 3,3646235 discloses the use of nickel, platinum, palladium, cobalt, chromium oxides and mixed metal catalysts for AMS hydrogenation, preferably Pd catalysts having a metal content of 1 to 5% by weight at 24 to 50 ℃ and 0.17 to 0.45 MPa.
Chinese patent CN1793089A discloses a method for selective hydrogenation of AMS to cumene using a combined catalyst system of nickel-based catalyst and noble metal catalyst. The catalyst combination is filled in a market, 70-95% of AMS conversion is realized in the first reaction zone, and at least 95% of AMS conversion is realized in the second reaction zone.
The catalysts used in the prior art processes have to be improved in terms of AMS conversion and cumene selectivity.
Disclosure of Invention
One of the technical problems to be solved by the invention is to solve the problems of low AMS conversion rate and low cumene selectivity of the catalyst in the prior art, and provide a cumene catalyst which has the characteristics of high AMS conversion rate and high cumene selectivity.
The second technical problem to be solved by the invention is the preparation method of the catalyst.
The third technical problem to be solved by the invention is the application of the catalyst.
In order to solve one of the above technical problems, the technical solution of the present invention is as follows:
the cumene catalyst comprises a carrier and the following active components:
(1) 0.05-10 g/L of metal palladium or oxide thereof;
(2) mo or an oxide thereof in an amount of 0 to 5.00 g/L.
In the above technical solutions, it is preferable that the content of the component (2) is more than 0g/L and not more than 5.00g/L, in which case the component (1) and the component (2) have a synergistic effect in improving the AMS conversion and the selectivity to cumene.
In the above technical scheme, the carrier is not particularly limited, and those well known in the art can be selected, for example, but not limited to, the carrier is selected from at least one of alumina, silica, titania and activated carbon.
In the technical scheme, the BET specific surface area of the carrier is preferably 60-200 m2Per gram, more preferably 80 to 150 m2Per gram.
In the above technical scheme, the pore volume of the carrier is preferably 0.2-0.7 ml/g, and more preferably 0.3-0.5 ml/g.
In the technical scheme, the content of the component (1) is preferably 0.5-5.0 g/L.
In the technical scheme, the content of the component (2) is further preferably 0.05-5.00 g/L.
In the above-mentioned embodiment, the catalyst further preferably contains the component (3), an alkali metal or an oxide thereof in an amount of more than 0g/L and not more than 60 g/L. At this time, in the presence of the component (1), the component (2) and the component (3) have a synergistic effect in enhancing the conversion of AMS and the selectivity of cumene.
In the above technical solution, the alkali metal is preferably at least one of Li, Na, and K, and more preferably K.
In the technical scheme, the content of the component (3) is preferably 0.1-5.0 g/L.
To solve the second technical problem, the technical solution of the present invention is as follows:
the method for preparing the catalyst according to any of the preceding technical solutions, comprising the steps of:
(i) mixing a solution containing a molybdenum compound with a carrier, and roasting to obtain a catalyst precursor I;
(ii) the solution of the palladium compound is mixed with the catalyst precursor I and calcined.
In the technical scheme, the roasting temperature in the step (i) and the roasting temperature in the step (ii) are independently selected from 400-600 ℃.
In the technical scheme, the roasting time of the step (i) and the step (ii) is 3-8 hours.
In the technical scheme, the roasting atmosphere is not particularly limited, and the comparable technical effect can be achieved, so that the air atmosphere is used for economic consideration. For convenience, the air atmosphere is adopted in the specific embodiment of the invention.
When the catalyst of the present invention contains the component (3), it is preferred that the solution of the molybdenum-containing compound in the step (i) is a solution of a molybdenum-containing compound and an alkali metal compound.
As will be appreciated by those skilled in the art, in order to obtain a catalyst with better strength, it is preferable to dry the catalyst before the calcination step in step (i) and/or step (ii), and the drying conditions are not particularly limited, for example, but not limited to, the drying temperature in step (i) and/or step (ii) is 80 to 120 ℃, and the drying time in step (i) and/or step (ii) is 2 to 6 hours.
In the above technical scheme, the alkali metal compound is not particularly limited, such as but not limited to an alkali metal salt or an alkali metal hydroxide. Alkali metal salts such as carbonates, nitrates, and carboxylates of C1-C4.
In the above technical solution, the palladium compound may be palladium chloride, palladium nitrate, chloropalladic acid, ammonium chloropalladate, and a soluble complex of palladium.
In the above-mentioned embodiment, any solvent that can dissolve the compound may be used for the solution preparation of the catalyst, but water is preferred as the solvent in view of economic efficiency, environmental protection, and the like. Wherein the pH of the solution of step (ii) is preferably 2.0-4.0.
The Pd in the catalyst can be reduced to be simple substance and directly used in the reaction of α -methyl styrene hydrogenation to prepare isopropylbenzene, or can also exist in the form of Pd oxide, so that the catalyst is stable for storage and transportation, but needs to be activated by a reducing agent before use, and the reducing agent for activation can be hydrogen or a material containing hydrogen.
To solve the third technical problem, the technical scheme of the invention is as follows:
the application of the catalyst in the technical scheme of one of the technical problems in the preparation of the isopropylbenzene by the hydrogenation of α -methyl styrene.
The technical key of the invention is the selection of the catalyst, and under the condition of determining the catalyst, the technical personnel of the invention know how to reasonably select the applied process conditions. For example, the specific application method may be:
the method for preparing the isopropylbenzene comprises the steps of taking hydrocarbon material containing α -methyl styrene and hydrogen as raw materials in a fixed bed reactor, contacting the raw materials with a catalyst, and reacting to generate the isopropylbenzene.
In the technical scheme, the reaction pressure is preferably 0.2-1.0 MPa, and more preferably 0.3-0.8 MPa.
In the technical scheme, the reaction temperature is preferably 30-100 ℃, and more preferably 35-90 ℃.
The preferred volume airspeed of hydrocarbon material among the above-mentioned technical scheme is 0.3 ~ 3.0 hours-1More preferably 0.5 to 2.5 hours-1。
In the technical scheme, the molar ratio of the hydrogen to the α -methylstyrene is preferably 1.0-5.0, and more preferably 1.2-3.0.
In the technical scheme, the hydrocarbon material containing α -methylstyrene contains 1-25% of α -methylstyrene and 75-99% of cumene by weight.
The catalyst of the invention has higher activity and selectivity when being used for preparing cumene. When the catalyst is used for preparing the cumene, the conversion rate of AMS can reach 99.97%, the selectivity of the cumene can reach 99.60%, and the effect is good.
The invention is further illustrated by the following examples. These examples are not intended to limit the scope of the present invention in any way.
Detailed Description
[ example 1 ]
1. Catalyst preparation
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2G, pore volume 0.46 ml/g) 1L, with 500 ml of potassium carbonate aqueous solution containing 0.30 g of K, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content 2.7 g/L, K content 0.30 g/L).
2. Catalyst evaluation
40ml of the catalyst was charged in a fixed bed reactor, activated at 50 ℃ for 4 hours in a hydrogen atmosphere of 0.4MPa, and then reacted. The reaction conditions were as follows: the reaction temperature was 45 ℃ and the reaction pressure was 0.3MPa, the molar ratio of hydrogen to AMS in the reaction feed was 1.2, and the liquid space velocity of the reaction feed (containing 21% AMS and 79% cumene) was 1.0h-1And the reaction was carried out for 72 hours.
The composition of the catalyst and the evaluation results are shown in Table 1 for convenience of comparison.
[ example 2 ]
1. Catalyst preparation
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume of 0.46 ml/g) 1L, and 500 ml of an ammonium molybdate aqueous solution containing 0.30 g of Mo, drying at 80 ℃ for 4 hours, calcining at 450 ℃ for 4 hours, then mixing with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusting the pH to 3 with hydrochloric acid, drying at 80 ℃ for 4 hours, and calcining at 450 ℃ for 4 hours to obtain the desired catalyst (the Pd content is 2.7 g/L, and the Mo content is 0.30 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume of 0.46 ml/g) 1L, and potassium carbonate containing 0.24 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.06 g of Mo, drying at 80 ℃ for 4 hours, calcining at 450 ℃ for 4 hours, then mixing with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, drying at 80 ℃ for 4 hours, and calcining at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content of 2.7 g/L, K content of 0.24 g/L, and Mo content of 0.06 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume of 0.46 ml/g) 1L, and potassium carbonate containing 0.18 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.12 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content of 2.7 g/L, K content of 0.18 g/L, and Mo content of 0.12 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume 0.46 ml/g), with potassium carbonate containing 0.15 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.15 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ and driedRoasting for 4 hours at 450 ℃ to obtain the required catalyst (the Pd content is 2.7 g/L, the K content is 0.15 g/L, and the Mo content is 0.15 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume of 0.46 ml/g) 1L, and potassium carbonate containing 0.12 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.18 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content of 2.7 g/L, K content of 0.12 g/L, Mo content of 0.18 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume of 0.46 ml/g) 1L, and potassium carbonate containing 0.06 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.24 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content of 2.7 g/L, K content of 0.06 g/L, Mo content of 0.24 g/L).
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
A cylindrical titanium dioxide support (specific surface area: 129 m) having a length of 5mm and a diameter of 2mm was placed2G, pore volume 0.41 ml/g) 1L, and was mixed with potassium carbonate containing 0.18 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.12 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, and then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours, to obtain the desired catalyst (Pd content 2.7 g/L, K content 0.18 g/L, Mo content 0.12 g/L).
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
A cylindrical silica support 5mm in length and 2mm in diameter (specific surface area 130 m)2Pore volume of 0.43 ml/g) was added to 1L, mixed with potassium carbonate containing 0.18 g of K and 500 ml of an aqueous ammonium molybdate solution containing 0.12 g of Mo, dried at 80 ℃ for 4 hours, calcined at 450 ℃ for 4 hours, then mixed with 500 ml of an aqueous solution containing 2.7 g of Pd and adjusted to pH 3 with hydrochloric acid, dried at 80 ℃ for 4 hours, and calcined at 450 ℃ for 4 hours to obtain the desired catalyst (Pd content of 2.7 g/L, K content of 0.18 g/L, Mo content of 0.12 g/L).
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 1
1. Catalyst preparation
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2Pore volume 0.46 ml/g) 1L, with 500 ml of an aqueous solution containing 3.00 g of Pd in palladium chloride adjusted to pH 3 with hydrochloric acid, and dried at 80 ℃ for 4 hoursThen, the catalyst is roasted for 4 hours at the temperature of 450 ℃, and the required catalyst (the content of Pd is 3.00 g/L) is obtained.
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2G, pore volume of 0.46 ml/g) 1L, and is mixed with 500 ml of potassium carbonate aqueous solution containing 3.00 g of K, dried for 4 hours at 80 ℃, and roasted for 4 hours at 450 ℃, thus obtaining the required catalyst (the K content is 3.00 g/L).
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
A cylindrical alumina carrier (specific surface of 125 m) having a length of 5mm and a diameter of 2mm was prepared2G, pore volume of 0.46 ml/g) 1L, and is mixed with 500 ml of ammonium molybdate aqueous solution containing 3.00 g of Mo, dried for 4 hours at 80 ℃, and roasted for 4 hours at 450 ℃, thus obtaining the required catalyst (the Mo content is 3.00 g/L).
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
Claims (9)
1. The application of a cumene catalyst in the reaction of α -methyl styrene hydrogenation to prepare cumene, the cumene catalyst comprises a carrier and the following active components:
(1) 0.05-10 g/L of metal palladium or oxide thereof;
(2) mo or an oxide thereof, more than 0g/L and not more than 5.00 g/L;
(3) an alkali metal or an oxide thereof in an amount of more than 0g/L and not more than 60 g/L.
2. The method of claim 1, wherein the carrier is at least one selected from the group consisting of alumina, silica, titania and activated carbon.
3. The method according to claim 1, wherein the carrier has a BET specific surface area of 60 to 200 m2Per gram.
4. The use according to claim 1, wherein the carrier has a pore volume of 0.2 to 0.7 ml/g.
5. Use according to claim 1, characterized in that the content of component (1) is 0.5 to 5.0 g/L.
6. Use according to claim 1, characterized in that the content of component (2) is 0.05 to 5.0 g/L.
7. Use according to any one of claims 1 to 6, characterized in that the cumene catalyst is prepared by a process comprising the steps of:
(i) mixing a solution containing a molybdenum compound and an alkali metal compound with a carrier, and roasting to obtain a catalyst precursor I;
(ii) the solution of the palladium compound is mixed with the catalyst precursor I and calcined.
8. The method according to claim 7, wherein the calcination temperature in step (i) and step (ii) is selected from 400 to 600 ℃.
9. The method as claimed in claim 7, wherein the calcination time in step (i) and step (ii) is 3-8 hours.
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CN1876231A (en) * | 2006-07-14 | 2006-12-13 | 谷育英 | Catalyst and its preparing process and usage method and use |
WO2013110995A2 (en) * | 2012-01-25 | 2013-08-01 | Council Of Scientific & Industrial Research | A process for hydrogenation of olefinic or acetylenic bonds |
CN104151129A (en) * | 2013-05-16 | 2014-11-19 | 中国石油化工股份有限公司 | Alpha-methyl styrene selective hydrogenation method |
CN105618082A (en) * | 2014-10-28 | 2016-06-01 | 中国石油天然气股份有限公司 | Reformate selective hydrogenation catalyst, and preparation method and application thereof |
CN106582820A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Catalyst for synthesis of ethylene method vinyl acetate |
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CN1876231A (en) * | 2006-07-14 | 2006-12-13 | 谷育英 | Catalyst and its preparing process and usage method and use |
WO2013110995A2 (en) * | 2012-01-25 | 2013-08-01 | Council Of Scientific & Industrial Research | A process for hydrogenation of olefinic or acetylenic bonds |
CN104151129A (en) * | 2013-05-16 | 2014-11-19 | 中国石油化工股份有限公司 | Alpha-methyl styrene selective hydrogenation method |
CN105618082A (en) * | 2014-10-28 | 2016-06-01 | 中国石油天然气股份有限公司 | Reformate selective hydrogenation catalyst, and preparation method and application thereof |
CN106582820A (en) * | 2015-10-19 | 2017-04-26 | 中国石油化工股份有限公司 | Catalyst for synthesis of ethylene method vinyl acetate |
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