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Regeneration method of paraffin dehydrogenation catalyst

A dehydrogenation catalyst and alkane dehydrogenation technology, applied in the direction of catalyst regeneration/reactivation, chemical instruments and methods, metal/metal oxide/metal hydroxide catalysts, etc., can solve the problem of affecting the performance of low-carbon alkane dehydrogenation regeneration catalysts It has the effect of improving regeneration stability, easy operation, and prolonging the service life and service life.

Inactive Publication Date: 2016-07-27
LIAONING UNIVERSITY OF PETROLEUM AND CHEMICAL TECHNOLOGY
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

When these two methods are used for catalyst regeneration, water vapor is introduced, which will not only cause the crystal phase transformation of the alumina carrier, but also cause the loss of alkali metal in the low-carbon alkane catalyst, and also cause metal aggregation to a certain extent.
[0008] It can be seen from the regeneration method of the above-mentioned noble metal-based dehydrogenation catalyst that oxygen, halogen or water vapor are usually introduced purposefully during the regeneration process. Although it has a certain effect, it often brings other side effects, especially The introduced water vapor will cause the loss of alkali additives on the noble metal-based dehydrogenation catalyst, which will inevitably affect the performance and life of the regenerated catalyst for dehydrogenation of low-carbon alkanes

Method used

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  • Regeneration method of paraffin dehydrogenation catalyst
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Examples

Experimental program
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Effect test

Embodiment 1

[0030] Weigh a commercially available alumina carrier (γ phase, spherical, 0.5 mm in diameter, 0.71 cm in pore volume) 3 / g, specific surface area 224m 2 / g) 30g, deionized water was added dropwise to the initial moistening, and the volume of water consumed was 27mL. According to the weight content of Sn element in the final catalyst of 0.4%, stannous chloride containing 0.12g Sn was weighed and dissolved in ethanol, and the volume was made up to 27mL with ethanol. The prepared Sn-containing ethanol solution was added to 30 g of alumina carrier, mixed evenly, and aged at room temperature for 2 hours. It was dried at 80°C for 8h, and then calcined at 600°C for 4h.

[0031] According to the weight content of Pt element in the final catalyst of 0.5%, chloroplatinic acid containing 0.18 g of Pt was weighed and dissolved in deionized water, the volume was adjusted to 27 mL, added to the alumina carrier containing Sn, mixed evenly, and aged at room temperature for 4 h. Dry at 100...

Embodiment 2

[0034] Weigh a commercially available alumina carrier (γ phase, spherical, 0.5 mm in diameter, 0.71 cm in pore volume) 3 / g, specific surface area 224m 2 / g) 30g, deionized water was added dropwise to the initial moistening, and the volume of water consumed was 27mL. According to the weight content of Sn element in the final catalyst of 0.6%, stannous chloride containing 0.18g Sn was weighed and dissolved in ethanol, and the volume was made up to 27mL. The prepared Sn-containing ethanol solution was added to 30 g of alumina carrier, mixed evenly, and aged at room temperature for 4 hours. It was dried at 100°C for 6h, and then calcined at 500°C for 6h.

[0035] According to the weight content of Pt element in the final catalyst of 0.7%, chloroplatinic acid containing 0.12 g of Pt was weighed and dissolved in deionized water, and the volume was adjusted to 27 mL. Dry at 120°C for 4h and calcinate at 500°C for 6h. The samples obtained in the above steps were treated at 700°C ...

Embodiment 3

[0038] After the C-1 fresh agent reacted for 72 hours, the feed gas was switched to pure hydrogen gas and purged for 1 hour; then the temperature was lowered to 470°C, switched to a nitrogen-oxygen mixed gas with an oxygen content of 15v%, and treated for 2 hours; then the temperature was raised to 530°C , switch to a nitrogen-oxygen mixed gas with an oxygen content of 21v%, and treat for 2h; then continue to heat up to 580 °C, switch to a nitrogen-oxygen mixed gas with an oxygen content of 35v%, and treat for 3h.

[0039] After the charcoal is burned, switch to nitrogen, cool down to 400 ° C, and introduce a nitrogen-oxygen mixed gas with an oxygen content of 10v%, and H 2 The molar ratio of O / Cl is 60:1 containing carbon dichloride water vapor, the carbon dichloride water vapor is introduced for 10h, and the total amount of water vapor introduced is 4000 μg per gram of catalyst.

[0040] After the oxychlorination of the deactivated catalyst was updated, it was switched to ni...

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Abstract

The invention discloses a regeneration method of a paraffin dehydrogenation catalyst. The method includes the following steps of firstly, carbon-burning an inactivated dehydrogenation catalyst in an oxygen-containing atmosphere; secondly, conducting oxychlorination treatment on the catalyst carbon-burned in the first step; thirdly, conducting vapor dechlorination treatment on the catalyst subjected to oxychlorination treatment in the second step; fourthly, conducting alkaline metal promoter compensation treatment on the catalyst subjected to vapor treatment in the third step; fifthly, conducting high-temperature air treatment on the catalyst obtained in the fourth step to obtain the regenerated catalyst. By means of the method, alkali metal lost in the reaction process and the regeneration process can be effectively compensated for, the dehydrogenation activity of the regenerated catalyst can reach the level of a fresh catalyst, operation is easy, and the service life of the catalyst is prolonged.

Description

technical field [0001] The invention relates to a regeneration method of a low-carbon alkane dehydrogenation catalyst, in particular to a regeneration method of a noble metal-based catalyst for the dehydrogenation of propane and isobutane. Background technique [0002] The shale revolution in North America has brought a large amount of low-carbon alkane resources, resulting in the lightening of the feedstock of the ethylene cracker and the sharp drop in the production of propylene. At the same time, under the background of the increasing scarcity of petroleum resources, the production of propylene has changed from relying solely on petroleum as raw material to the technical route of diversifying raw material sources, and has gradually become a trend. Dehydrogenation of propane by-product in natural gas (conventional natural gas, shale gas, coalbed methane, combustible ice, etc.) to produce propylene is an effective way to solve this problem. In recent years, the technology ...

Claims

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Application Information

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IPC IPC(8): B01J38/02B01J38/44B01J38/06B01J38/48B01J23/96C07C11/06C07C5/333
CPCY02P20/52Y02P20/584B01J38/02B01J23/96B01J38/06B01J38/44B01J38/485C07C5/333
Inventor 张海娟王卫强王海彦王国付李小玲孙林
Owner LIAONING UNIVERSITY OF PETROLEUM AND CHEMICAL TECHNOLOGY
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