CN202342929U - Catalytic rectifying tower - Google Patents
Catalytic rectifying tower Download PDFInfo
- Publication number
- CN202342929U CN202342929U CN2011205227780U CN201120522778U CN202342929U CN 202342929 U CN202342929 U CN 202342929U CN 2011205227780 U CN2011205227780 U CN 2011205227780U CN 201120522778 U CN201120522778 U CN 201120522778U CN 202342929 U CN202342929 U CN 202342929U
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- catalyst
- filling material
- tower
- beds
- catalytic rectifying
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- Physical Or Chemical Processes And Apparatus (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a catalytic rectifying tower, which belongs to the field of chemical equipment. The catalytic rectifying tower is characterized by comprising a tower body, filling material layers, catalyst bed layers and liquid distributors, wherein the filling material layers and the catalyst bed layers are uniformly and alternately arranged in the tower body, and the liquid distributor is respectively arranged at the upper end of each filling material layer. After the structure is adopted, filling material is regularized to form a pure rectifying element, and when a catalyst is replaced, only the catalyst in the bed layers needs to be replaced and the filling material does not need to be replaced; compared with the etherifying baled catalyst, the operation cost of the catalyst is greatly saved; and a stainless steel corrugated silk screen is adopted for regularizing the filling material, the separation efficiency is higher than that of a plate type tower, the shortcomings of excessive reaction and insufficient rectification of a bulk structure of the original plate type tower are solved, the relation between rectification and reaction is also considered, and the utilization rate of the catalyst is improved.
Description
Technical field
The utility model relates to a kind of catalytic rectifying tower, belongs to the chemical industry equipment field.
Background technology
Catalytic distillation is applied to be widely used in comprising multiple balanced reactions such as esterification, etherificate, isomerization, alkylation, lamination process, olefine selective hydrogenation, oxidative dehydrogenation, C-1 chemistry, hydrolysis, ester exchange and other courses of reaction in methyl tertiary butyl ether(MTBE) (MTBE) and the ethyl tert-butyl ether (ETBE) synthesis techniques such as (ETBE) the earliest at present.
Different with the coupled modes of rectifying by reaction, catalytic rectifying tower is divided into 2 kinds of versions: a kind of is that reaction and rectifying are carried out simultaneously, and chemical reaction occurs on the column plate or has in the packing layer of catalytic action; Another kind is that catalytic reaction and rectifying separation hocket, and in the conversion zone reaction, product gets into rectifying section again and carries out rectifying earlier for catalytic rectifying tower conversion zone and rectifying section reactant.
Reaction and rectifying carry out simultaneously that catalyst loading pattern is the most commonly used to be the bale packing catalyst loading pattern, and this type of feed is that catalyst is packed in the pouch that glass fibre processes, and with the covering of stainless steel ripple silk screen, is rolled into cylinder again, and bag is tied up in formation.This structure is easy to loading and unloading, and its intensity is very high, and the size of catalyst structure is changeable, and the ripple silk net of adjacent two layers catalyst structure trend staggers when mounted, makes uniform gas-liquid distribution.Shortcoming one is that catalyst is being wrapped by one deck glass cloth, and catalyst bag inner transmission matter resistance is big in the catalytic distillation process, so catalyst efficiency can not be given full play to; The 2nd, its rectifying element (stainless steel ripple silk screen) combines with catalyst; Catalyst can not be changed separately, and catalyst needs to change with stainless steel ripple silk screen, for example as far as etherificate bale packing catalyst; Stainless steel ripple silk screen accounts for its total cost more than 70%; At every turn more during catalyst changeout, not only expensive, and dead catalyst difficult treatment.
It is the catalyst bulk structure that reaction and rectifying separation hocket the most commonly used; If be characterized in conversion zone is divided into some beds, a board-like plate is installed between two beds, catalyst directly fills in the beds of conversion zone with bulk form; Be positioned at plate column downspout below; Distributor of each bed top band, catalyst can directly be packed into by loading port, and used catalyst can directly draw off from unloading outlet.Shortcoming one is that beds and board-like plate each have its hydraulics characteristic, and design features such as board-like plate plate efficiency is low, liquid phase short circuit, causes its separative efficiency poor, and catalyst utilization is low, i.e. reaction is had a surplus, and rectifying is not enough; The 2nd, adopt board-like tower tray, liquid phase must increase the liquid phase redistributor from the beds of tower tray downspout inflow conversion zone, makes logistics evenly through beds, causes the catalyst bed sheaf space little, the filling of unfavorable replacing catalysis.
Summary of the invention
According to the deficiency of prior art, the technical problem that the utility model will solve is: a kind of catalytic rectifying tower is provided, reduces the operating cost of catalyst, improve the utilization rate of catalysis, simplify the structural shape of tower, make things convenient for the loading and unloading of catalyst.
The utility model solves the technical scheme that its technical problem adopted: a kind of catalytic rectifying tower is provided; It is characterized in that comprising: tower body, packing layer, beds and liquid distribution trough; Evenly be arranged alternately packing layer and beds in the tower body, wherein the packing layer upper end is provided with liquid distribution trough.
Described packing layer adopts the structured packing of stainless steel ripple silk screen.
Described beds both sides are respectively arranged with gas phase channel, and the gas phase channel upper end is provided with baffle plate.Baffle plate is for being obliquely installed, and baffle plate one end is fixed on the tower body, and lower edge is arranged on beds top.
The structural shape that the catalytic distillation tower structure adopts structured packing and beds to hocket, structured packing adopt stainless steel ripple wire packing, and catalyst adopts to loose to stow fills out structure.
The beneficial effect of the utility model is: after adopting this structure, structured packing is simple rectifying element, more during catalyst changeout, only changes catalyst in the bed, need not change filler, compares with etherificate bale packing catalyst, saves the operating cost of catalyst greatly;
Adopt the structured packing of stainless steel ripple silk screen, separative efficiency is higher than plate column, solves former plate column bulk structure reaction and has a surplus, and the shortcoming that rectifying is not enough is taken into account the relation between rectifying and the reaction, improves the utilization rate of catalyst;
Regular wire packing has good in distributivity, and beds does not need liquid phase distributor, and the loading and unloading of catalyst are convenient.
Description of drawings
Fig. 1 is the structural representation of the utility model;
1 is tower body among the figure; 2 is packing layer; 3 is beds; 4 is liquid distribution trough; 5 is gas phase channel; 6 is baffle plate.
The specific embodiment
Below in conjunction with accompanying drawing the embodiment of the utility model is done and to further describe:
As shown in Figure 1, the utility model comprises: tower body 1, packing layer 2, beds 3 and liquid distribution trough 4, evenly be arranged alternately packing layer 2 and beds 3 in the tower body 1, and wherein packing layer 3 upper ends are provided with liquid distribution trough 4.
Beds 3 both sides are respectively arranged with gas phase channel 5, and gas phase channel 5 upper ends are provided with baffle plate 6.
This structural shape is applied to grand celebration medium blue company 80,000 tons of/year MTBE devices capacity expansion revamping, and one feeding is driven successfully, the MTBE product that output is qualified, and isobutene conversion is greater than 99.8%.
Claims (3)
1. catalytic rectifying tower; It is characterized in that comprising: tower body (1), packing layer (2), beds (3) and liquid distribution trough (4); Evenly be arranged alternately packing layer (2) and beds (3) in the tower body (1), wherein packing layer (3) upper end is provided with liquid distribution trough (4).
2. catalytic rectifying tower according to claim 1 is characterized in that described packing layer (2) adopts the structured packing of stainless steel ripple silk screen.
3. catalytic rectifying tower according to claim 1 is characterized in that described beds (3) both sides are respectively arranged with gas phase channel (5), and gas phase channel (5) upper end is provided with baffle plate (6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205227780U CN202342929U (en) | 2011-12-14 | 2011-12-14 | Catalytic rectifying tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011205227780U CN202342929U (en) | 2011-12-14 | 2011-12-14 | Catalytic rectifying tower |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202342929U true CN202342929U (en) | 2012-07-25 |
Family
ID=46531956
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011205227780U Expired - Fee Related CN202342929U (en) | 2011-12-14 | 2011-12-14 | Catalytic rectifying tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202342929U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107519824A (en) * | 2017-10-10 | 2017-12-29 | 天津市新天进科技开发有限公司 | A kind of combined type high flux catalytic distillation tower member |
-
2011
- 2011-12-14 CN CN2011205227780U patent/CN202342929U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107519824A (en) * | 2017-10-10 | 2017-12-29 | 天津市新天进科技开发有限公司 | A kind of combined type high flux catalytic distillation tower member |
| CN107519824B (en) * | 2017-10-10 | 2023-09-15 | 天津市新天进科技开发有限公司 | Composite high-flux catalytic distillation tower component |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120725 Termination date: 20201214 |