CN111054353A - Catalyst for preparing butadiene by oxidative dehydrogenation of butylene - Google Patents

Catalyst for preparing butadiene by oxidative dehydrogenation of butylene Download PDF

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CN111054353A
CN111054353A CN201811201472.8A CN201811201472A CN111054353A CN 111054353 A CN111054353 A CN 111054353A CN 201811201472 A CN201811201472 A CN 201811201472A CN 111054353 A CN111054353 A CN 111054353A
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catalyst
oxidative dehydrogenation
butadiene
butylene
solution
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曾铁强
缪长喜
吴文海
樊志贵
姜冬宇
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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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    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/83—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with rare earths or actinides
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    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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    • B01J23/8892—Manganese
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
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    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/42—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor
    • C07C5/48—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with a hydrogen acceptor with oxygen as an acceptor
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
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    • C07C2523/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
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Abstract

The invention relates to a catalyst for preparing butadiene by oxidative dehydrogenation of butylene, which mainly solves the problems of high steam unit consumption, large wastewater generation amount and high energy consumption in the existing production process for preparing butadiene by oxidative dehydrogenation of butylene. The invention relates to a catalyst for preparing butadiene by oxidative dehydrogenation of butylene and a process method thereof, wherein the catalyst comprises the following components: a) me in spinel StructureⅡFe2O4Is a main active component, wherein Me is selected from Zn, Mg, Ni, Co or MnAt least one of; b) with the chemical formula of AaBbCombined oxides as auxiliaries: wherein A is selected from Zn; b is at least one of lanthanide elements, so that it can effectively and stably prepare butadiene product, reduce energy consumption, reduce steam consumption and waste water production quantity, and can be used in industrial production of butadiene by using butylene oxidative dehydrogenation.

Description

Catalyst for preparing butadiene by oxidative dehydrogenation of butylene
Technical Field
The invention relates to a catalyst for preparing butadiene by oxidative dehydrogenation of butylene.
Background
1, 3-butadiene is an important monomer for chemical products such as synthetic rubber and resin, and plays an important role in petrochemical olefin raw materials. The industrial production method of butadiene mainly comprises two methods of carbon four extraction separation and butylene dehydrogenation which are co-produced in the process of preparing ethylene by steam cracking. The method for obtaining butadiene by adopting the carbon four extraction method is economically advantageous, and the pyrolysis carbon four extraction process is adopted in the vast majority of butadiene production capacity in the world at present. However, butadiene is obtained as a by-product of the cracking unit, and it is difficult to increase its yield by adding the cracking unit. Moreover, as refinery feedstocks are upgraded, butadiene production will be reduced, creating a continuing bias in global butadiene supply.
With the rapid development of the synthetic rubber and resin industry and the wider and wider application of butadiene, the market demand of butadiene is continuously increased. Butadiene obtained by extracting naphtha cracking products cannot meet market demands, but butadiene products cannot be provided in the new energy field, coal chemical industry and large-scale shale gas development, so people pay attention to other butadiene production methods, and research on butylene oxidative dehydrogenation technology is wide.
The carbon four-fraction of the refinery contains a large amount of butylene, the carbon four-fraction has low use added value as civil fuel, and the high-selectivity conversion of the butylene into butadiene has obvious economic benefit and has important significance for the comprehensive utilization of carbon four-fraction resources. The process route for producing butadiene by oxidative dehydrogenation of butylene has great application prospect.
The catalysts currently used in the industrial production of butadiene by oxidative dehydrogenation of butene can be mainly classified into the following two types: bismuth molybdate systems and ferrite systems. The bismuth molybdate system catalyst is a multi-component catalyst based on Mo-Bi oxide. Bismuth molybdate catalyst for preparing butane by oxidative dehydrogenation of buteneThe main disadvantages of the diene are the high amount of by-product oxygenates, especially organic acids, and the serious pollution of three wastes. In the molybdenum series composite oxide catalyst, the main reaction for removing butylene from oxidative dehydrogenation to butadiene and the complete combustion to generate CO2In addition to the side reactions, 8-10% of the butenes are converted into oxidation products such as furan, aldehyde, ketone, acid, etc. This problem is particularly acute today where clean production is currently of increasing importance. Having a spinel structure (A)2+B2 3+O4) Ferrite catalysts such as ZnFe2O4、MnFe2O4、MgFe2O4、ZnCrFeO4And Mg0.1Zn0.9Fe2O4The method has the advantages of high activity and selectivity for oxidative dehydrogenation of butene, less oxygen-containing byproducts, long service life, high economic benefit, less three-waste pollution and the like. The butylene is oxidized and dehydrogenated on the catalyst, the conversion rate can reach more than 70 percent, and the selectivity can reach more than 90 percent. The ferrite catalyst with a spinel structure has better effect in the reaction of preparing butadiene by oxidative dehydrogenation of butylene (CN104226352A, CN103102238A, CN103079695A and the like).
The Oxo-D process of the American TPC group (formerly Texas Petrochemical) and the O-X-D process of Philips are typical processes for preparing butadiene through oxidative dehydrogenation of butene. The oxidative dehydrogenation of butene is a strongly exothermic reaction, and in order to achieve a good catalytic effect, a large amount of water vapor needs to be mixed into a reaction raw material to be used as a diluent gas and a heat carrier. For example, the Oxo-D process employs a ferrite catalyst with a water vapor to butene molar ratio of 10: 1.
the domestic processes for preparing butadiene by oxidative dehydrogenation of butylene, which are used for industrial production, mainly comprise an adiabatic fixed bed reaction process adopting a B-02 iron-based catalyst and a fluidized bed reaction process adopting an H-198 iron-based catalyst as a representative, wherein the molar ratio of steam to butylene is about 10: 1-16: 1.
the existing production process for preparing butadiene by oxidative dehydrogenation of butylene has high steam unit consumption, large wastewater generation amount and high energy consumption, and the amount of steam needs to be reduced as much as possible along with the improvement of the requirements on environmental protection, energy conservation and emission reduction. However, the current relevant patent literature reports that the research on the low water ratio catalyst for preparing butadiene by oxidative dehydrogenation of butene has less mention. The development of high-activity and low-water-ratio catalysts is the key of the low-water-ratio and low-energy-consumption butylene oxidative dehydrogenation technology.
Disclosure of Invention
The invention aims to solve the technical problems of high steam unit consumption, large wastewater generation amount and high energy consumption in the existing production process of preparing butadiene by oxidative dehydrogenation of butylene, and provides a novel catalyst for preparing butadiene by oxidative dehydrogenation of butylene. The second technical problem to be solved by the present invention is to provide a method for preparing a catalyst corresponding to the first technical problem, wherein the method for preparing the catalyst is simple. The third technical problem to be solved by the invention is to provide a process method for preparing butadiene by oxidative dehydrogenation of butylene, which corresponds to one of the technical problems, the butadiene product is efficiently and stably prepared in the oxidative dehydrogenation reaction of butylene, the energy consumption is reduced, the steam unit consumption and the waste water production are reduced, and the method has the advantages of high butadiene selectivity and high catalyst activity and stability.
In order to solve the first technical problem, the technical scheme adopted by the invention is as follows: a catalyst for preparing butadiene by oxidative dehydrogenation of butylene comprises the following components:
a) me in spinel StructureⅡFe2O4Is a main active component, wherein Me is at least one selected from Zn, Mg, Ni, Co or Mn;
b) with the chemical formula of AaBbCombined oxides as auxiliaries, in molar ratio, with MeⅡFe2O4Has the chemical formula of MeⅡFe2O4·AaBbOxThe composition of (1), wherein:
a is selected from Zn;
b is selected from at least one of lanthanides;
the value range of a is 0.02-2;
the value range of b is 0.01-1;
x is the total number of oxygen atoms required to satisfy the valence state of each element in the catalyst.
In the above technical solution, the divalent metal Me is preferably selected from at least one of Zn and Mg.
In the technical scheme, the value range of a is 0.02-1; the value of a is more preferably in the range of 0.05-0.5.
In the above technical solution, preferably, the lanthanoid is selected from at least one of La or Ce.
In the technical scheme, the value range of b is 0.01-0.5.
In order to solve the technical problem II, the invention adopts the following steps to prepare the catalyst:
a) preparing a mixed solution containing a catalyst component and fully stirring;
b) co-precipitating the mixed solution with an alkaline solution at a suitable pH value;
c) the precipitated product is worked up.
In the above technical scheme, the component precursor of the catalyst can be selected from one of chloride or nitrate; the pH value in the precipitation process is 6-12, the washing temperature is 10-80 ℃, the drying temperature is 90-150 ℃, the drying time is 1-24 hours, the roasting temperature is 400-650 ℃, the preferred roasting temperature is 500-650 ℃, and the roasting time is 1-24 hours; the alkaline solution is selected from one of ammonia water, sodium hydroxide or potassium hydroxide, wherein the ammonia water is the best, and the concentration of the ammonia water is preferably 10-30%.
In order to solve the third technical problem, the butadiene production method provided by the invention can adopt the following process steps:
the method takes the mixed gas of butylene, air or oxygen and water vapor as raw materials, the inlet temperature of a reactor is 300-550 ℃, and the mass space velocity of butylene is 1.0-6.0 h-1And the raw materials are contacted with a catalyst for reaction to obtain butadiene.
Butene in the reactants: oxygen: the volume ratio of water vapor is 1: (0.1-20): (1-10), preheating water into steam before entering the reactor, and fully mixing the steam with the raw material gas.
In the above technical scheme, butene: the volume ratio of the water vapor is preferably 1: (2-10), and the more preferable scheme is 1: (4-8).
The catalyst can be shaped in different modes and is used in a fixed bed or a fluidized bed reactor.
Compared with the prior art, the invention has obvious advantages and outstanding effects. The traditional butene oxidative dehydrogenation catalyst needs higher water-olefin molar ratio, and the catalytic performance is obviously reduced under the condition of low water ratio. The catalyst with strong hydrophilicity can improve the utilization efficiency of the water vapor, thereby reducing the using amount of the water vapor and achieving the purposes of energy conservation and emission reduction. The invention adopts the spinel structure ferrite with high catalytic performance as the main active component, and the auxiliary agent improves the utilization efficiency of the water vapor and reduces the consumption of the water vapor. Through the adjustment and optimization of the catalyst composition and the proportion among the components, the catalyst is not only suitable for the butylene oxidative dehydrogenation reaction under a higher water ratio, but also very suitable for the butylene oxidative dehydrogenation reaction to prepare butadiene under a low water ratio condition. The catalyst has the advantages of simple preparation method, high butadiene selectivity, high catalyst activity and high stability, reduces the unit consumption of steam and the generation amount of wastewater, and reduces the energy consumption.
The butylene oxidative dehydrogenation reaction is carried out on a micro catalytic reaction device of a continuous flow quartz tube reactor. Analysis of products the contents of alkane, alkene, butadiene, etc. in the dehydrogenated product were analyzed on-line using HP-5890 gas chromatograph (HP-AL/S capillary column, 50 m.times.0.53 mm.times.15 μm; FID detector) and the conversion of the reaction and the product selectivity were calculated. The catalyst prepared by the method provided by the invention is used for butylene oxidative dehydrogenation, has good catalytic activity under the conditions of higher and lower water-olefin molar ratio, has butadiene selectivity of 96 percent, and has good performance and high stability, and good technical effect is obtained.
The invention is further illustrated by the following examples.
Detailed Description
[ example 1 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 1, and grinding the catalyst 1 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 1 was Mg0.8Zn0.2Fe2O4·Zn0.2Ce0.1Ox。
[ example 2 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 2, and grinding the catalyst 2 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the element composition of the catalyst 2 is Mg0.8Zn0.2Fe2O4·Zn0.2Ce0.01Ox。
[ example 3 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then the solution is mixed with 20% ammonia water solutionCoprecipitation was carried out, the precipitation pH was maintained at 9.5 and the precipitation temperature was room temperature, then a solid sample in the precipitated product was separated by a centrifuge, washed with 4L of deionized water, and the resulting solid was dried in an oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 3, and grinding the catalyst 3 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 3 is Mg0.8Zn0.2Fe2O4·Zn0.2Ce0.05Ox。
[ example 4 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 4, and grinding the catalyst 4 into particles of 40-60 meshes for catalyst evaluation. Catalyst 4 had an elemental composition in a molar ratio of Mg0.8Zn0.2Fe2O4·Zn0.2Ce0.5Ox。
[ example 5 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then coprecipitating the above solution with 20% ammonia water solution, maintaining the pH value of the precipitate at 9.5 and the precipitation temperature at room temperature, separating the solid sample in the precipitate with a centrifugal separator, washing with 4L deionized water, and drying the obtained solidDried in oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 5, and grinding the catalyst 5 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 5 is Mg0.8Zn0.2Fe2O4·Zn0.2Ce1.0Ox。
[ example 6 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 6, and grinding the catalyst 6 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 6 is Mg0.8Zn0.2Fe2O4·Zn0.02Ce0.1Ox。
[ example 7 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 7, and grinding the catalyst 7 into particles of 40-60 meshes for catalyst evaluation. Elemental composition of catalyst 7In a molar ratio of Mg0.8Zn0.2Fe2O4·Zn0.05Ce0.1Ox。
[ example 8 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 8, and grinding the catalyst 8 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 8 is Mg0.8Zn0.2Fe2O4·Zn0.5Ce0.1Ox。
[ example 9 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 9, and grinding the catalyst 9 into particles of 40-60 meshes for catalyst evaluation. Catalyst 9 had an elemental composition in molar ratio of Mg0.8Zn0.2Fe2O4·Zn1.0Ce0.1Ox。
[ example 10 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 500 ℃ for 4 hours to obtain the catalyst 10, and grinding the catalyst 10 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 10 is Mg0.8Zn0.2Fe2O4·Zn2.0Ce0.1Ox。
[ example 11 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and lanthanum nitrate (La (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 10% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 6.0, the precipitation temperature is 10 ℃, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 24 hours at the temperature of 90 ℃. And roasting the dried sample in a muffle furnace at 400 ℃ for 24 hours to obtain the catalyst 11, and grinding the catalyst 11 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 11 is Mg0.8Zn0.2Fe2O4·Zn0.2La0.1Ox。
[ example 12 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and praseodymium nitrate (Pr (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 30% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 12, the precipitation temperature is 80 ℃, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 1 hour at 150 ℃. And roasting the dried sample in a muffle furnace at 650 ℃ for 1 hour to obtain a catalyst 12, and grinding the catalyst 12 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 12 is Mg0.8Zn0.2Fe2O4·Zn0.2Pr0.1Ox。
[ example 13 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O), lanthanum nitrate (La (NO)3)3·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then the catalyst precursor solution and 15% ammonia solution were coprecipitated, the precipitation pH was maintained at 8.0 and the precipitation temperature was 40 ℃, then a solid sample in the precipitated product was separated with a centrifuge, washed with 4L deionized water, and the resulting solid was dried in an oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 13, and grinding the catalyst 13 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 13 is Mg0.8Zn0.2Fe2O4·Zn0.2La0.05Ce0.05Ox。
[ example 14 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then the catalyst precursor solution and 25% ammonia water solution were coprecipitated, the precipitation pH was maintained at 10.0 and the precipitation temperature was 60 ℃, then a solid sample in the precipitated product was separated with a centrifuge, washed with 4L of deionized water, and the resulting solid was dried in an oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 14, and grinding the catalyst 14 into particles of 40-60 meshes for catalyst evaluation. The elemental composition molar ratio of catalyst 14 is MgFe2O4·Zn0.2Ce0.1Ox。
[ example 15 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 15, and grinding the catalyst 15 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of the catalyst 15 is ZnFe2O4·Zn0.2Ce0.1Ox。
[ example 16 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), zinc chloride (ZnCl)2) Magnesium chloride (MgCl)2) And cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then the solution and 3M KOH solution are coprecipitated, the precipitation pH value is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitation product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. The dried sample was then heated in a muffle furnace at 60 deg.CRoasting at 0 ℃ for 4 hours to obtain a catalyst 16, and grinding into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 16 is Mg0.9Zn0.1Fe2O4·Zn0.2Ce0.1Ox。
[ example 17 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 17, and grinding the catalyst 17 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 17 is Mg0.1Zn0.9Fe2O4·Zn0.2Ce0.1Ox。
[ example 18 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 18, and grinding the catalyst 18 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 18 is Mg0.5Zn0.5Fe2O4·Zn0.2Ce0.1Ox。
[ example 19 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O), cobalt nitrate (Co (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 19, and grinding the catalyst 19 into particles of 40-60 meshes for catalyst evaluation. Catalyst 19 has an elemental composition in a molar ratio of Mg0.8Co0.2Fe2O4·Zn0.2Ce0.1Ox。
[ example 20 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O), manganese nitrate (Mn (NO)3)2·4H2O), and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain the catalyst 20, and grinding the catalyst 20 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 20 is Mg0.8Mn0.2Fe2O4·Zn0.2Ce0.1Ox。
[ example 21 ]
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O), nickel nitrate (Ni (NO)3)2·4H2O), and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst 21, and grinding the catalyst 21 into particles of 40-60 meshes for catalyst evaluation. The molar ratio of the elemental composition of catalyst 21 is Mg0.8Ni0.2Fe2O4·Zn0.2Ce0.1Ox。
Comparative example 1
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) was dissolved in 4L of distilled water and stirred well to form a solution. Then, the above solution was coprecipitated with a 20% aqueous ammonia solution, the pH of the precipitate was maintained at 9.5, the precipitation temperature was room temperature, then a solid sample in the precipitated product was separated by a centrifugal separator, washed with 4L of distilled water, and the resulting solid was dried in an oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst comparative example 1, and grinding the catalyst comparative example 1 into particles of 40-60 meshes for catalyst evaluation. Catalyst comparative example 1 elemental composition Mg0.8Zn0.2Fe2O4。
Comparative example 2
An appropriate amount of zinc nitrate (Zn (NO) was weighed3)2·6H2O) was dissolved in 4L of distilled water and stirred well to form a solution. Then will beThe above solution was coprecipitated with 20% aqueous ammonia solution, the pH of the precipitate was maintained at 9.5 and the precipitation temperature was room temperature, then a solid sample in the precipitated product was separated by a centrifuge, washed with 4L distilled water, and the resulting solid was dried in an oven at 110 ℃ for 4 hours. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst comparative example 2, and grinding the catalyst comparative example 2 into particles of 40-60 meshes for catalyst evaluation. The elemental composition of catalyst comparative example 2 was ZnO.
Comparative example 3
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O), zinc nitrate (Zn (NO)3)2·6H2O) and cerium nitrate (Ce (NO)3)3·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. And roasting the dried sample in a muffle furnace at 600 ℃ for 4 hours to obtain a catalyst comparative example 3, and grinding the catalyst comparative example 3 into particles of 40-60 meshes for catalyst evaluation. Catalyst comparative example 3 had a molar ratio of elemental composition of Mg0.8Zn0.2Fe2O4·Ce0.1Ox。
Comparative example 4
An appropriate amount of ferric nitrate (Fe (NO) was weighed3)3·9H2O), magnesium nitrate (Mg (NO)3)2·6H2O) and zinc nitrate (Zn (NO)3)2·6H2O) is dissolved in 4L of deionized water and stirred uniformly to form a solution. Then, the solution and 20% ammonia water solution are subjected to coprecipitation, the pH value of the precipitate is kept at 9.5, the precipitation temperature is room temperature, then a solid sample in the precipitate product is separated by a centrifugal separator, 4L deionized water is used for washing, and the obtained solid is dried in an oven for 4 hours at 110 ℃. The dried sample was calcined in a muffle furnace at 600 ℃ for 4 hours to obtain comparative catalyst example 4, which was groundThe particles of 40-60 meshes are used for catalyst evaluation. Catalyst comparative example 4 had a molar ratio of elemental composition of Mg0.8Zn0.2Fe2O4·Zn0.2Ox。
[ example 22 ]
0.5g of the catalysts of examples 1 to 21 and comparative examples 1 to 4 were used for evaluation of oxidative dehydrogenation of butene. The feed gas is a mixture of butylene, oxygen and water vapor, wherein the ratio of butylene: the oxygen is in a molar ratio of 1: 0.75, butene: the compositional molar ratios of water are shown in the following table. The raw material gas is fully mixed and then introduced into a reactor for oxidative dehydrogenation. The inlet temperature of the reactor is 420 ℃; the reaction pressure is normal pressure; the mass space velocity of the butylene is 1.2h-1. The catalytic reaction was carried out under the above conditions, and the reaction product was analyzed by gas chromatography. The reaction results are shown in Table 1.
TABLE 1
Figure BDA0001830108610000121
Figure BDA0001830108610000131
Butene conversion and butadiene selectivity over 10 hours of reaction
[ example 23 ]
0.5g of catalyst 1 and comparative example 1 were taken for the evaluation of oxidative dehydrogenation of butene. The feed gas is a mixture of butylene, oxygen and water vapor, wherein the ratio of butylene: the oxygen is in a molar ratio of 1: 0.75, water: the composition molar ratio of butene is shown in table 2, and the raw material gases are first mixed thoroughly and then introduced into the reactor for oxidative dehydrogenation. The inlet temperature of the reactor is 420 ℃; the reaction pressure is normal pressure; the mass space velocity of the butylene is 1.2h-1. The catalytic reaction was carried out under the above conditions, and the reaction product was analyzed by gas chromatography. The reaction results are shown in Table 2.
TABLE 2
Figure BDA0001830108610000141
[ example 24 ]
0.5g of catalyst 1 and comparative example 1 were taken for the evaluation of oxidative dehydrogenation of butene. The feed gas is a mixture of butylene, oxygen and water vapor, wherein the ratio of butylene: oxygen: the composition molar ratio of water is 1: 0.75: and 6, fully mixing the raw material gases, and introducing the raw material gases into the reactor to perform oxidative dehydrogenation. The inlet temperature of the reactor is 420 ℃; the reaction pressure is normal pressure; the mass space velocity of the butylene is 1.2h-1. The catalytic reaction was carried out under the above conditions, and the reaction product was analyzed by gas chromatography. The reaction results are shown in Table 3.
TABLE 3
Figure BDA0001830108610000142

Claims (10)

1. A catalyst for preparing butadiene by oxidative dehydrogenation of butylene comprises the following components:
a) me in spinel StructureⅡFe2O4Is a main active component, wherein Me is at least one selected from Zn, Mg, Ni, Co or Mn;
b) with the chemical formula of AaBbCombined oxides as auxiliaries, in molar ratio, with MeⅡFe2O4Has the chemical formula of MeⅡFe2O4·AaBbOxThe composition of (1), wherein:
a is selected from Zn;
b is selected from at least one of lanthanides;
the value range of a is 0.02-2;
the value range of b is 0.01-1;
x is the total number of oxygen atoms required to satisfy the valence state of each element in the catalyst.
2. The catalyst for the oxidative dehydrogenation of butene to butadiene according to claim 1, wherein Me is selected from at least one of Zn and Mg.
3. The catalyst for preparing butadiene through oxidative dehydrogenation of butene according to claim 1, wherein a is in the range of 0.02 to 1.
4. The catalyst for preparing butadiene through oxidative dehydrogenation of butene according to claim 3, wherein a is in the range of 0.05-0.5.
5. The catalyst for the oxidative dehydrogenation of butene to butadiene according to claim 1, wherein said lanthanide is selected from at least one of La or Ce.
6. The catalyst for preparing butadiene through oxidative dehydrogenation of butene according to claim 1, wherein the value of b is in the range of 0.01-0.5.
7. A preparation method of a catalyst for preparing butadiene by oxidative dehydrogenation of butylene, which adopts the catalyst of any one of claims 1-6, and is characterized by comprising the following steps:
a) preparing a mixed solution containing a catalyst component and fully stirring;
b) co-precipitating the mixed solution with an alkaline solution at a suitable pH value;
c) the precipitated product is worked up.
8. The method for preparing the catalyst according to claim 7, wherein the pH value in the precipitation process is 6 to 12, the washing temperature is 10 to 80 ℃, the drying temperature is 90 to 150 ℃, the drying time is 1 to 24 hours, the roasting temperature is 400 to 650 ℃, and the roasting time is 1 to 24 hours.
9. A process for preparing butadiene by oxidative dehydrogenation of butene by using the catalyst of any one of claims 1 to 8, wherein the ratio of butene: oxygen: the volume ratio of water vapor is 1: (0.1-20): (1-10).
10. The process for preparing catalyst for the oxidative dehydrogenation of butene to butadiene as claimed in claim 9, wherein the ratio of butene: the volume ratio of water vapor is 1: (2-10).
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114073959A (en) * 2020-08-19 2022-02-22 中国石油化工股份有限公司 Butene oxidative dehydrogenation catalyst and preparation method and application thereof
CN114377687A (en) * 2022-01-27 2022-04-22 淄博市翔力致高新材料有限责任公司 Iron-based butylene oxidative dehydrogenation catalyst and preparation method thereof

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105582959A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst and process method used for preparing butadiene through butene oxidative dehydrogenation
CN105582960A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst used for producing butadiene through butene oxidative dehydrogenation, and application method thereof
CN107537535A (en) * 2016-06-29 2018-01-05 中国石油化工股份有限公司 Catalyst for Oxidative Dehydrogenation of Butene into Butadiene under low-water ratio conditions and preparation method thereof and process
CN107970954A (en) * 2016-10-21 2018-05-01 中国石油化工股份有限公司 Catalyst for Oxidative Dehydrogenation of Butene into Butadiene and preparation method thereof

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105582959A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst and process method used for preparing butadiene through butene oxidative dehydrogenation
CN105582960A (en) * 2014-10-24 2016-05-18 中国石油化工股份有限公司 Catalyst used for producing butadiene through butene oxidative dehydrogenation, and application method thereof
CN107537535A (en) * 2016-06-29 2018-01-05 中国石油化工股份有限公司 Catalyst for Oxidative Dehydrogenation of Butene into Butadiene under low-water ratio conditions and preparation method thereof and process
CN107970954A (en) * 2016-10-21 2018-05-01 中国石油化工股份有限公司 Catalyst for Oxidative Dehydrogenation of Butene into Butadiene and preparation method thereof

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114073959A (en) * 2020-08-19 2022-02-22 中国石油化工股份有限公司 Butene oxidative dehydrogenation catalyst and preparation method and application thereof
CN114073959B (en) * 2020-08-19 2023-08-29 中国石油化工股份有限公司 Butene oxidative dehydrogenation catalyst and preparation method and application thereof
CN114377687A (en) * 2022-01-27 2022-04-22 淄博市翔力致高新材料有限责任公司 Iron-based butylene oxidative dehydrogenation catalyst and preparation method thereof
CN114377687B (en) * 2022-01-27 2024-02-06 淄博市翔力致高新材料有限责任公司 Iron-based butene oxidative dehydrogenation catalyst and preparation method thereof

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