Fluidized bed reactor, reaction regeneration apparatus, process for preparing olefins, and process for preparing aromatic hydrocarbons

Patent metadata

Field	Value
Publication number	US-2016102033-A1
Application number	US-201514881620-A
Country	US
Kind code	A1
Filing date	Oct 13, 2015
Priority date	Oct 14, 2014
Publication date	Apr 14, 2016
Grant date	—

Abstract

A fluidized bed reactor is provided, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone. A guide plate with through holes is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof and encompassing the dense channel region. Catalysts in said fluidized bed reactor can be homogeneously distributed in the reaction zone thereof, whereby the reaction efficiency can be improved. A reaction regeneration apparatus comprising said fluidized bed reactor, and a process for preparing olefins from oxygenates and a process for preparing aromatic hydrocarbons from oxygenates using the reaction regeneration apparatus.

First claim

1 . A fluidized bed reactor, comprising an inlet zone at a lower position, an outlet zone at an upper position, and a reaction zone between the inlet zone and the outlet zone, wherein
a guide plate is disposed in the reaction zone, comprising a dense channel region in an intermediate region thereof and a sparse channel region disposed on a periphery thereof encompassing the dense channel region.

2 . The fluidized bed reactor according to claim 1 , wherein a dimension of a channel in the dense channel region is smaller than that of a channel in the sparse channel region.

3 . The fluidized bed reactor according to claim 2 , wherein a ratio of the dimension of the channel in the dense channel region to that of the channel in the sparse channel region is in a range of 1:4 to 2:3.

4 . The fluidized bed reactor according to claim 3 , wherein the dimension of the channel in the dense channel region is in a range of 0.01 m to 0.08 m.

5 . The fluidized bed reactor according to claim 1 , wherein the dense channel region and the sparse channel region each comprise a circular plate having evenly distributed pores, or a plurality of concentric ring shaped sloping panels spaced apart, or a plurality of straight panels spaced apart in parallel.

6 . The fluidized bed reactor according to claim 1 , wherein the dense channel region is round shaped and the sparse channel region is annular ring shaped, and
a ratio of a diameter of the dense channel region to a width of the sparse channel region is in a range of 2:1 to 9:1.

7 . The fluidized bed reactor according to claim 1 , wherein a plurality of guide plates is provided, which are distributed along an axial direction of the fluidized bed reactor.

8 . The fluidized bed reactor according to claim 1 , wherein an inlet for accelerating gas is disposed in the outlet zone of the fluidized bed reactor.

9 . The fluidized bed reactor according to claim 8 , wherein the inlet for accelerating gas is configured to extend obliquely from a lower position to an upper position.

10 . A reaction regeneration apparatus, comprising the fluidized bed reactor according to claim 1 , and further comprising a separation device and a catalyst regeneration device respectively connected with the fluidized bed reactor, wherein
the separation device comprises a preliminary gas-solid separator communicated with an outlet zone of the fluidized bed reactor; a vertically arranged damper, a lower region of the damper being communicated with a solid outlet of the preliminary gas-solid separator for collecting catalyst particles, and an upper region of the damper being communicated with a gas outlet of the preliminary gas-solid separator; and a fine gas-solid separator, an inlet of the fine gas-solid separator being communicated with the upper region of the damper and a solid outlet thereof being communicated with the lower region of the damper, and the catalyst regeneration device comprises a feed zone at a lower position and a discharge zone at an upper position, the feed zone being arranged lower than the lower region of the damper, and the discharge zone being arranged higher than the inlet zone of the fluidized bed reactor, wherein the lower region of the damper is communicated with the feed zone of the catalyst regeneration device through a second pipe, and the discharge zone of the catalyst regeneration device is communicated with the inlet zone of the fluidized bed reactor through a third pipe.

11 . The reaction regeneration apparatus according to claim 10 , wherein a diameter of the upper region of the damper is smaller than that of the lower region thereof.

12 . The reaction regeneration apparatus according to claim 10 , wherein both the preliminary gas-solid separator and the fine gas-solid separator are cyclone separators.

13 . The reaction regeneration apparatus according to claim 10 , wherein the preliminary gas-solid separator is a cyclone separator, and the fine gas-solid separator comprises two- or multi-stage series cyclone separators, wherein
the two or multi-stage series cyclone separators are configured so that an inlet of a first stage cyclone separator is communicated with the upper region of the damper, gas product being obtained from a gas outlet of a last stage cyclone separator, a gas outlet of an upstream cyclone separator is communicated with an inlet of an adjacent downstream cyclone separator, and solid outlets of all the cyclone separators are communicated with the lower region of the damper.

14 . The reaction regeneration apparatus according to claim 10 , wherein the lower region of the damper is configured and arranged so that it performs a stream stripping operation.

15 . The reaction regeneration apparatus according to claim 10 , wherein the third pipe is provided with a flow blocking member at a top of an inner wall thereof.

16 . The reaction regeneration apparatus according to claim 15 , wherein the flow blocking member is a baffle tilting towards the fluidized bed reactor.

17 . The reaction regeneration apparatus according to claim 16 , wherein a plurality of baffles is provided, which is arranged in parallel with respect to one another.

18 . The reaction regeneration apparatus according to claim 15 , wherein the flow blocking member is a stop pawl protruding radially inward.

19 . The reaction regeneration apparatus according to claim 18 , wherein a plurality of stop pawls is provided, which is arranged in a row along an axis of the third pipe.

20 . The reaction regeneration apparatus according to claim 19 , wherein a ratio of a length of each stop pawl to a diameter of the third pipe is in a range of 0.1 to 0.5.

21 . The reaction regeneration apparatus according to claim 10 , wherein the inlet zone of the fluidized bed reactor is disposed lower than the lower region of the damper of the separation device, and the lower region of the damper is communicated with the inlet zone of the fluidized bed reactor through a first pipe.

22 . A process for preparing olefins, using a reaction regeneration apparatus according to claim 10 , wherein an inlet zone of a fluidized bed reactor is disposed lower than a lower region of a damper of a separation device, and the lower region of the damper is communicated with the inlet zone of the fluidized bed reactor through a first pipe,
wherein the process comprises: reacting gaseous raw material containing oxygenates with catalysts in a reaction zone of the fluidized bed reactor, feeding product obtained and entrained catalysts into the separation device through an outlet zone of the fluidized bed reactor, separating the product from the entrained catalysts through the separation device, feeding a portion of catalysts obtained from the separation directly into the inlet zone of the fluidized bed reactor, subsequently regenerating the rest catalysts, and feeding regenerated catalysts into the inlet zone of the fluidized bed reactor, and mixing non-regenerated catalysts and the regenerated catalysts in the inlet zone of the fluidized bed reactor, and then feeding mixed catalysts into the reaction zone of the fluidized bed reactor.

23 . The process according to claim 22 , wherein a weight ratio of the non-regenerated catalysts to the regenerated catalysts is in a range of 0.3 to 1.5.

24 . The process according to claim 22 , wherein an operation of the separation device comprises:
preliminarily separating product from the fluidized bed react

Assignees

• China Petroleum & Chemical
• Shanghai Res Inst Petrochemical Technology Sinopec

Inventors

• Yang Weimin
• Li Xiaohong
• Zhong Siqing
• Qi Guozhen
• Xu Jun
• Yu Zhinan

Classifications

• B01J2208/00938

  Flow distribution elements · CPC title

• B01J8/24 Primary

  according to "fluidised-bed" technique (B01J8/20 takes precedence) · CPC title

• B01J8/0055 Primary

  using cyclones · CPC title

• B01J2208/00991

  Disengagement zone in fluidised-bed reactors · CPC title

• C07C1/20 Primary

  starting from organic compounds containing only oxygen atoms as heteroatoms · CPC title