A kind of preparation method of propane oxidative dehydrogenation to propylene catalyst

An oxidative dehydrogenation and catalyst technology, applied in metal/metal oxide/metal hydroxide catalysts, physical/chemical process catalysts, molecular sieve catalysts, etc. It can avoid further oxidation, improve the conversion rate and selectivity of propylene, and reduce the cost of catalysts.

Active Publication Date: 2018-02-09
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The oxidative dehydrogenation of propane to propylene is still a fast reaction (this kind of fast reaction is generally carried out under the condition of mass transfer control), and the reaction is completed when the reactants reach the outer surface of the catalyst, so the inner surface of the catalyst is relatively The target reaction does not contribute much, which results in lower metal utilization in the pores of the support, increases the cost of the catalyst, and also accelerates the deep oxidation of the product

Method used

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  • A kind of preparation method of propane oxidative dehydrogenation to propylene catalyst
  • A kind of preparation method of propane oxidative dehydrogenation to propylene catalyst

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] Weigh 2.97g of nickel nitrate and 0.55g of ammonium tungstate and dissolve them in an appropriate amount of deionized water to obtain solution A; use the equal volume impregnation method to load 20g of alumina (pore volume is 0.72ml / g, specific surface area is 242m 2 / g, strip shape, equivalent diameter 1.5mm) carrier, aged at room temperature for 4h, dried at 80°C for 12h, and calcined at 700°C for 4h to obtain catalyst precursor B, wherein Ni accounted for 3% of the weight of the carrier by element, and W by element Accounting for 2% of the weight of the carrier; catalyst precursor B is activated in a mixed atmosphere containing hydrogen, the volume content of hydrogen in the mixed gas is 80%, the reduction condition is 450 ° C, 0.2 MPa (absolute pressure), and the reduction time is 4 hours; after the reduction activation The catalyst precursor B and 300mL of sorbitol solution with a mass concentration of 10% were added to the autoclave, sealed and replaced with hydrog...

Embodiment 2

[0029] Weigh 2.97g of nickel nitrate and 0.55g of ammonium tungstate and dissolve them in an appropriate amount of deionized water to obtain solution A; use the equal volume impregnation method to load 20g of silicon oxide (pore volume 1.06ml / g, specific surface area 387m 2 / g, spherical, equivalent diameter 0.5mm) carrier, aged at room temperature for 4h, dried at 80°C for 12h, and calcined at 700°C for 4h to obtain catalyst precursor B, wherein Ni accounted for 3% of the carrier weight by element, and W accounted for The weight of the carrier is 2%; the catalyst precursor B is activated in a mixed atmosphere containing hydrogen. Catalyst precursor B and 300mL sorbitol solution with a mass concentration of 10% were added to the autoclave, sealed and replaced with hydrogen for 3 times, then adjusted the hydrogen pressure to 3MPa, and reacted at 220°C for 4h; The final mixture was placed for 2h, filtered, and the resulting solid sample was dried at room temperature until there w...

Embodiment 3

[0031] Weigh 2.97g of nickel nitrate and 0.55g of ammonium tungstate and dissolve them in an appropriate amount of deionized water to obtain solution A; use an equal volume impregnation method to load 20g of SBA-15 (the pore volume is 1.23ml / g, and the specific surface area is 701m 2 / g, strip shape, equivalent diameter 1.5mm) carrier, aged at room temperature for 4h, dried at 80°C for 12h, and calcined at 700°C for 4h to obtain catalyst precursor B, wherein Ni accounted for 3% of the weight of the carrier by element, and W by element Accounting for 2% of the weight of the carrier; catalyst precursor B is activated in a mixed atmosphere containing hydrogen, the volume content of hydrogen in the mixed gas is 80%, the reduction condition is 450 ° C, 0.2 MPa (absolute pressure), and the reduction time is 4 hours; after the reduction activation The catalyst precursor B and 300mL of sorbitol solution with a mass concentration of 10% were added to the autoclave, sealed and replaced w...

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Abstract

The invention relates to a preparation method of a catalyst for oxidative dehydrogenation of propane to propylene. The catalyst includes an active component, a first auxiliary agent, a second auxiliary agent and a carrier; the preparation method of the catalyst first prepares the active component precursor, the first The auxiliary agent precursor is dissolved in water to obtain a solution A; the catalyst precursor B is obtained after adding a carrier, aging, drying, and roasting; the catalyst precursor B is reduced using a reducing atmosphere; the reduced catalyst precursor B is mixed with polyol The solution is added to the reaction kettle for hydrogenation reaction; the reaction effluent is placed, filtered and dried to obtain catalyst precursor C; the active component precursor and the second auxiliary agent precursor are dissolved in water to obtain solution D, and catalyst precursor C is added , after drying and roasting, the catalyst is obtained. The method of the invention promotes the dispersion of more active components on the carrier surface, not only improves the utilization rate of active metals, but also improves the conversion rate of propane and the selectivity of propylene.

Description

technical field [0001] The invention relates to a preparation method of a catalyst for oxidative dehydrogenation of propane to propylene, in particular to a preparation method of a supported nickel-based catalyst for oxidative dehydrogenation of propane to propylene. Background technique [0002] Propylene is an extremely important organic chemical raw material, widely used in the production of a series of important chemical products such as polypropylene, polyacrylonitrile, phenol, oxo alcohol, propylene oxide, acrolein and acrylic acid. [0003] At present, propylene is mainly produced by catalytic cracking of petroleum and catalytic dehydrogenation of propane. The production process of propane catalytic dehydrogenation to propylene is controlled by thermodynamic equilibrium, the reaction conditions are harsh, and there are problems such as rapid deactivation of the catalyst due to carbon deposition. The oxidative dehydrogenation of propane is a new way to prepare propyle...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): B01J23/888B01J29/035C07C11/06C07C5/48
CPCY02P20/52
Inventor 孙晓丹张舒冬张信伟刘继华
Owner CHINA PETROLEUM & CHEM CORP
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