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Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene

A technology of mixed heat exchange and oxidative dehydrogenation, applied in chemical instruments and methods, organic chemistry, hydrocarbons, etc. Large-scale, large-diameter effect

Active Publication Date: 2016-05-04
WISON ENG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

Although the radial fixed bed reactor can theoretically reduce the pressure drop of the bed layer, in order to ensure the uniform distribution of the reaction gas in the reactor, a distributor with a low opening ratio must be used, which will inevitably lead to a large pressure drop in the distributor , not well suited for butene oxidative dehydrogenation reaction system
[0012] At present, industrial butadiene oxidative dehydrogenation plants generally use multiple axial adiabatic fixed-bed reactors connected in series. Although the structure of the reactor is simple, the capacity of a single unit is limited. The system uses radial reactors for industrial production, mainly due to the limitation of fluid distribution and has not been reported. In order to change the current situation of increasing the number of reactors to solve the production capacity, it is necessary to develop a new type of reactor that is easy to scale up

Method used

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  • Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene
  • Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene
  • Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene

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Embodiment 1

[0044] Such as figure 1 As shown, it is a large-scale axial multi-stage mixed heat exchange butene oxidative dehydrogenation reactor with a direct heat exchange section. The upper part of the reactor shell is equipped with a mixing device, and the reactor shell is equipped with two axial catalyst beds. , containing a direct heat exchange section; the direct heat exchange section is located between two axial catalyst beds, and the quench stream flows into the quench material distribution pipe in the reactor shell, and then passes through the quench nozzle and the upper axial catalyst The outlet material after the bed reaction is evenly distributed through the gas distributor, and the hot and cold streams are mixed in the mixing space of the direct heat exchange section and then enter the axial catalyst bed below it for reaction after direct heat exchange. The specific structure of the reactor as follows:

[0045] The mixing device comprises a straight cylinder or a conical cyl...

Embodiment 2

[0051] Such as figure 2 As shown, the upper part is provided with a direct heat exchange section, and the lower part is provided with a large-scale axial multi-stage mixed heat exchange type butene oxidative dehydrogenation reactor with an indirect heat exchange section in which the catalyst is installed in the tube, and a structure similar to that of Example 1 is adopted. , but the second section of the axial catalyst bed is a catalyst bed containing indirect heat exchange, and the catalyst bed containing indirect heat exchange includes heat exchange tube 18, catalyst 5 and heat exchange system, heat exchange tube 18 and axial catalyst bed The layers are arranged in a vertical manner, wherein the catalyst is filled in the heat exchange tube 18, and the heat exchange tube 18 is connected with a cooling medium to form a heat exchange system in which the heat exchange medium is connected outside the tube.

Embodiment 3

[0053] Such as image 3 As shown, the upper part is provided with a direct heat exchange section, and the lower part is provided with a large-scale axial multi-stage mixed heat exchange type butene oxidative dehydrogenation reactor with catalysts installed in the indirect heat exchange section between the tubes. structure, but the second section of the axial catalyst bed is a catalyst bed containing indirect heat exchange, and the catalyst bed containing indirect heat exchange includes heat exchange tube 18, catalyst 5 and heat exchange system, heat exchange tube 18 and axial catalyst bed The layers are arranged in parallel, wherein the catalyst is filled between the heat exchange tubes 18, and the heat exchange tubes 18 pass through the cooling medium to form a heat exchange system in which the heat exchange medium passes through the tubes.

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Abstract

The invention relates to a large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene. The reactor comprises a reactor housing, a mixing arrangement which is arranged at the upper part of the reactor housing, at least two axial catalyst bed layers in the reactor housing, and at least one direct heat exchange segment; the direct heat exchange segment is located between the two axial catalyst bed layers, a cold torrent is introduced into the direct heat exchange segment in the reactor casing, the cold torrent and outlet materials which are reacted with the axial catalyst bed layer above the direct heat exchange segment are mixed for direct heat exchange, and a mixture enters the axial catalyst bed layer below the direct heat exchange segment for carrying out a reaction. Compared with the prior art, the reactor has the advantages of large-scale, effective control of reaction temperature, reduced bed layer pressure, high energy utilization rate, and good production capacity.

Description

technical field [0001] The invention relates to the technical field of chemical reaction engineering, in particular to a large axial multi-stage mixed heat exchange type butene oxidation dehydrogenation reactor. Background technique [0002] Butadiene is the basic raw material for the production of styrene-butadiene rubber SBR, ABS resin, polybutadiene rubber BR, etc., and is also a key intermediate for the production of chemicals such as adiponitrile, chloroprene, sulfolane, and vinyl cyclohexene. a lot of uses. Oxidative dehydrogenation of butene is an important method for producing butadiene, butene mainly generates butadiene through the partial oxidative dehydrogenation of butene through the following main reaction: [0003] C 4 h 8 +0.5O 2 =C 4 h 6 +H 2 o [0004] Butene and butadiene are further oxidized through the following side reactions to produce CO by-products, respectively 2 : [0005] C 4 h 8 +6O 2 =4CO 2 +4H 2 o [0006] C 4 h 6 +5.5O 2 =4CO...

Claims

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Application Information

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IPC IPC(8): B01J8/04C07C11/167C07C5/48
CPCB01J8/0446B01J2208/00115B01J2208/00327C07C5/48C07C11/167
Inventor 张梁吕建宁李延生解建国田靖
Owner WISON ENG