Selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow

A technology for selective hydrogenation and phenylacetylene, applied in chemical instruments and methods, hydrocarbons, chemical/physical processes, etc., can solve problems such as excess hydrogen and increased styrene loss, and ensure utilization and consistency sexual effect

Active Publication Date: 2010-08-25
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0010] The technical problem to be solved by the present invention is that there is excess hydrogen in the selective hydrogenation process of phenylacetylene in t

Method used

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  • Selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow
  • Selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow
  • Selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow

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Embodiment 1

[0028] According to Figure 1, Figure 2 and Figure 7, the diameter of the gas-liquid-solid three-phase multi-stage fixed bubbling bed reactor is 1000 mm, and the catalyst bed is 2 layers. Catalyst 0.5% by weight Pd / Al 2 o 3 palladium-containing catalyst. Dendritic gas distributor distributed in parallel, each branch pipe is arranged at equal intervals in the same section of the reactor, and there are two rows of small holes on the branch pipe, and the small holes are evenly distributed along the length of the pipe. The diameter of the main pipe is 100 mm, and there are 4 branch pipes with a diameter of 50 mm. The small holes on the branch pipes are circular with a diameter of 5 mm. into an angle of 30°. Hydrogen is a mixture of hydrogen and nitrogen, and the molar ratio of nitrogen to hydrogen is 0.5. A C8 hydrocarbon fraction comprising 25% by weight of styrene, 11% by weight of ethylbenzene and 1500ppm phenylacetylene is added to the bottom of the reactor, a part of hydro...

Embodiment 2

[0030] According to Figure 1, Figure 2 and Figure 9, the diameter of the gas-liquid-solid three-phase multi-stage fixed bubbling bed reactor is 1500 mm, and the catalyst bed is 2 layers. Catalyst 1.5 wt% Ni / Al 2 o 3 nickel-containing catalysts. Dendritic gas distributor distributed in parallel, each branch pipe is arranged at equal intervals in the same section of the reactor, with two rows of open short pipes on the branch pipe, and the open short pipes are staggered and evenly distributed along the length of the pipe. The diameter of the main pipe is 100 mm, and there are 8 branch pipes with a diameter of 40 mm. The small holes on the short pipe with holes are circular with a diameter of 4 mm. The reactor axis forms an included angle of 60°. Hydrogen is pure hydrogen. A C8 hydrocarbon cut comprising 30% by weight of styrene, 10.5% by weight of ethylbenzene and 3500ppm phenylacetylene is added to the bottom of the reactor, a part of hydrogen is also added to the bottom of...

Embodiment 3

[0032] According to Figure 1, Figure 2 and Figure 5, the diameter of the gas-liquid-solid three-phase fixed bubbling bed reactor is 1000 mm, and the catalyst bed is 2 layers. Catalyst 1.5 wt% Ni / Al 2 o 3 nickel-containing catalysts. Dendritic gas distributor distributed in parallel, each branch pipe is arranged at equal intervals in the same section of the reactor, the small holes on the branch pipe are 1 row, and the holes are opened along the axial direction of the reactor, and the small holes are evenly distributed along the length of the pipe. The diameter of the main pipe is 80 mm, and there are 12 branch pipes with a diameter of 30 mm. The small holes are circular with a diameter of 5 mm. The total area of ​​the holes is 1.5 times the cross-sectional area of ​​the branch pipes. Hydrogen is a mixture of hydrogen and nitrogen, and the molar ratio of nitrogen to hydrogen is 0.3. A C8 hydrocarbon cut comprising 35% by weight of styrene, 8% by weight of ethylbenzene and 10...

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Abstract

The invention relates to a selective hydrogenation method for phenylacetylene in phenylacetylene-containing styrene material flow, which mainly solves the problem that excessive hydrogen in the selective hydrogenation process for the phenylacetylene possibly transforms the phenylacetylene and the styrene into an unexpected unsaturated product ethylbenzene so as to cause loss increment of the styrene. The invention adopts the technical scheme that raw materials and a palladium or nickel-containing catalyst in a catalyst bed layer undergo contact reaction in a gas-liquid-solid three-phase multi-section fixed bubbling bed reactor, wherein a gas distributor is arranged between the bottom of the fixed bubbling bed reactor and the catalyst bed layer; and the gas distributor comprises a gas mainand branch pipes, and the branch pipe is provided with at least one row of pores or the branch pipe is provided with at least one row of open short pipes, so the problem is well solved. The method can be used in the selective hydrogenation industrial production for the phenylacetylene in the phenylacetylene-containing styrene material flow.

Description

technical field [0001] The invention relates to a method for selective hydrogenation of phenylacetylene in a styrene stream containing phenylacetylene. Background technique [0002] Styrene is an important monomer for the production of polystyrene, ABS resin and styrene-butadiene rubber. At present, the production methods of styrene in the world mainly include ethylbenzene dehydrogenation method, propylene oxide-styrene (PO / SM) co-production method, pyrolysis gasoline extraction distillation recovery method and butadiene synthesis method, etc. Although, the ethylbenzene dehydrogenation method is the main method of producing styrene at home and abroad at present. However, in recent years, with the scale-up of ethylene, it has become an effective way to recover styrene from pyrolysis gasoline by-product of steam cracking ethylene unit. [0003] For the method of recovering styrene from pyrolysis gasoline, it is generally believed that extractive distillation is feasible at p...

Claims

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Application Information

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IPC IPC(8): C07C15/46C07C7/167B01J8/04
Inventor 孙凤侠朱志焱王万民李蕾
Owner CHINA PETROLEUM & CHEM CORP
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