CN202315851U - Continuous esterification production device for plasticizer - Google Patents
Continuous esterification production device for plasticizer Download PDFInfo
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- CN202315851U CN202315851U CN2011204651338U CN201120465133U CN202315851U CN 202315851 U CN202315851 U CN 202315851U CN 2011204651338 U CN2011204651338 U CN 2011204651338U CN 201120465133 U CN201120465133 U CN 201120465133U CN 202315851 U CN202315851 U CN 202315851U
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- reaction tower
- esterification reaction
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Abstract
A continuous esterification production device for plasticizer includes a pre-esterification kettle and an esterification reactor, wherein a gas phase outlet is arranged at the top of the pre-esterification kettle, a material inlet is arranged in the middle of the pre-esterification kettle, and a pre-esterification material outlet is arranged at the bottom of the pre-esterification kettle; the esterification reactor further includes at least two esterification reaction towers which are connected in series and are internally provided with catalyst reaction beds; gas phase outlets are arranged at the tops of the esterification reaction towers, material inlets are arranged at the middle parts of the esterification reaction towers, gas phase inlets are arranged at the lower parts of the esterification reaction towers, and material outlets are arranged at the bottoms of the esterification reaction towers; and further, the material inlet of the first stage esterification reaction tower is connected with the pre-esterification material outlet of the pre-esterification kettle, and the material outlet of the previous stage esterification reaction tower is connected with the material inlet of the next stage esterification reaction tower. The continuous esterification production device for plasticizer can realize continuous esterification production of the plasticizer, improves the production efficiency, lowers the labor intensity of workers, and reduces the cost.
Description
Technical field
The utility model relates to a kind of chemical plant installations, is specifically related to a kind of continuous esterification process units of plasticizer.
Background technology
Plasticizer; Be a kind of flexibility of material or additive of material liquefaction of increasing; Plasticizer various in style; In its kind of its development period once nearly more than 1000 kinds,, and serve as maximum in the phthalate of petrochemical industry with raw material sources as the plasticizer of commodity production kind more than 200 only.
The phthalic ester plasticizer consumption is maximum in the plasticizer, accounts for 80% of plasticizer total output, and such plasticizer of China is main with dioctyl phthalate (DOP) and dibutyl phthalate (DBP) mainly.Since receive the restriction in raw alcohol source, the kind of dibutyl phthalate (DHP) (DHP), diisooctyl phthalate (DIDP), diisooctyl phthalate function admirables such as (DIOP), and output is little.
The existing adjacent benzene class plasticizer production technology of China all adopts esterification at intermittence mode to produce, and adopts phthalic anhydride and alcohol under the catalyst existence condition, to carry out esterification on the technology, and reaction unit adopts a plurality of agitated reactors that are cascaded; After the agitated reactor internal reaction of front finishes fully; This agitated reactor is shut down, and product is transferred to continuation reaction in the agitated reactor at the back, so repeatedly after the intermittent esterification reaction; The plasticizer that extraction makes from the agitated reactor of rearmost end; There is following shortcoming in this existing batch production: (1) batch production is consuming time longer, and the product quality fluctuation is big, less stable; (2) technology falls behind, and labour intensity is big; (3) esterification at intermittence energy consumption, material consumption height, product yield is low; (4) small scale can't be accomplished scale production, and has restricted the output of plasticizer.
Therefore need the continuous esterification process units of a kind of plasticizer of design, make its continuous esterification production that can realize plasticizer, thereby enhance productivity, reduced labor strength, also reduced cost.
The utility model content
The utility model technical problem to be solved provides a kind of continuous esterification process units of plasticizer, and it can realize the continuous esterification production of plasticizer, thereby eliminates defective in the above-mentioned background technology.
For solving the problems of the technologies described above, technical scheme of the present invention is:
A kind of continuous esterification process units of plasticizer comprises preparatory esterifying kettle and esterifier, and said preparatory esterifying kettle top is provided with gaseous phase outlet, and the middle part is provided with material inlet, and the bottom is provided with preparatory esterification material outlet; Said esterifier comprises at least two esterification reaction tower that connect each other, that set inside has the catalyst reaction bed; Said esterification reaction tower all is provided with gaseous phase outlet at the top; The middle part is provided with material inlet, and the bottom is provided with the gas phase import, and the bottom is provided with material outlet; Wherein, the material inlet of first order esterification reaction tower connects the preparatory esterification material outlet of said preparatory esterifying kettle, and the material outlet of previous stage esterification reaction tower connects the material inlet of back one-level esterification reaction tower.
As a kind of improvement, the upstream position of said esterification reaction tower gas phase import is provided with the preheater and the heater of the raw polyol that is used to heat up in order.
As a kind of further improvement, said esterification reaction tower bottom is provided with reboiler, and said gas phase import is arranged at the upper end of said reboiler.
As a kind of improvement, except that final stage esterification reaction tower, the equal pipeline of the gaseous phase outlet of all the other esterification reaction tower connects the treating column in order to refined alcohol.
As a kind of further improvement, the outlet of said treating column links to each other with the material inlet of said preparatory esterifying kettle.
As a kind of improvement, the gaseous phase outlet of said final stage esterification reaction tower is connected to its upper level esterification reaction tower gas phase import after through preheater and heater.
As a kind of improvement, the material outlet of said final stage esterification reaction tower connects said preheater, for the preheating raw polyol provides heat.
As a kind of improvement, said esterifier comprises first esterification reaction tower and second esterification reaction tower of mutual series connection.
Owing to adopted technique scheme, the utlity model has following beneficial effect:
The utility model comprises preparatory esterifying kettle and esterifier; Esterifier comprises at least two esterification reaction tower that connect each other, that set inside has the catalyst reaction bed; Change traditional batch (-type) esterification and produced, need not shut down in the production process and switch material, shortened the time of producing greatly; Improve production efficiency, practiced thrift lot of manpower and material resources; Simultaneously, because overheated pure gas and reaction mass have carried out countercurrent reaction on the catalyst reaction bed, overheated pure gas contacts with reaction mass very fully, and esterification is complete, and feed stock conversion is high, and product purity is high.
The utility model feeds preparatory esterification material continuously from the material inlet of first order esterification reaction tower; And the semi-finished product that generate are passed in other the esterification reaction tower of back in order continuously continue reaction; And in the gas phase import of each esterification reaction tower bottom reboiler, feed overheated pure gas; The plasticizer that generates is from the continuous extraction of final stage esterification tower bottom, and technology operates steadily, the steady quality of product.
The utility model will final stage esterification reaction tower gaseous phase outlet connect the preheater of its upper level esterification reaction tower gas phase import, the gaseous phase outlet of remaining esterification reaction tower connects treating column with the refining back recycle of alcohol, no discarded object discharge, friendly environment.
The esterification reaction tower of the utility model is used solid catalyst, and the catalytic action with the form performance esterification of fixed bed realizes the repeated use catalyst, economizes in raw materials, and reduces cost.
Description of drawings
Accompanying drawing is the structural representation of a kind of embodiment of the utility model;
Among the figure: 1. preparatory esterifying kettle, 2. first esterification reaction tower, 3. second esterification reaction tower, 4. preheater; 5. heater, 6. reboiler, 7. treating column, 8. gaseous phase outlet; 9. material inlet, 10. esterification material outlet in advance, 11. first esterification reaction tower gas phase imports, 12. second esterification reaction tower gas phase imports; 13. the first esterification reaction tower gaseous phase outlet, 14. second esterification reaction tower gaseous phase outlets, 15. first esterification reaction tower material inlets, 16. second esterification reaction tower material outlets.
The specific embodiment
For technological means, creation characteristic that the utility model is realized, reach purpose and be easy to understand understanding with effect, below in conjunction with concrete diagram, further set forth the utility model.
Shown in accompanying drawing, a kind of continuous esterification process units of plasticizer comprises preparatory esterifying kettle 1 and esterifier, and said preparatory esterifying kettle 1 top is provided with gaseous phase outlet 8, and the middle part is provided with material inlet 9, and the bottom is provided with preparatory esterification material outlet 10; Said esterifier comprises at least two esterification reaction tower that connect each other, that set inside has the catalyst reaction bed; Said esterification reaction tower all is provided with gaseous phase outlet at the top; The middle part is provided with material inlet, and the bottom is provided with the gas phase import, and the bottom is provided with material outlet; Wherein, the material inlet of first order esterification reaction tower connects the preparatory esterification material outlet 10 of said preparatory esterifying kettle 1, and the material outlet of previous stage esterification reaction tower connects the material inlet of back one-level esterification reaction tower.
In the present embodiment; Said esterifier comprises first esterification reaction tower 2 and second esterification reaction tower 3 of mutual series connection; The said first esterification reaction tower material inlet 15 connects the preparatory esterification material outlet 10 of said preparatory esterifying kettle 1; The upstream position of the first esterification reaction tower gas phase import 11 and the second esterification reaction tower gas phase import 12 all sets gradually the preheater 4 and heater 5 that is useful on the intensification raw polyol; First esterification reaction tower 2 and second esterification reaction tower, 3 bottoms are provided with reboiler 6, and the said first esterification reaction tower gas phase import 11 and the second esterification reaction tower gas phase import 12 are arranged at the upper end of said reboiler 6 respectively.Wherein, the first esterification reaction tower gaseous phase outlet, 13 pipelines connect the treating column 7 in order to refined alcohol, and the outlet of this treating column 7 links to each other with the material inlet 9 of said preparatory esterifying kettle 1; After connecting preheater 4 and heater 5, the said second esterification reaction tower gaseous phase outlet 14 is connected to the first esterification reaction tower gas phase import 11; The said second esterification reaction tower material outlet 16 connects said preheater 4, is preheating alcohol extracting heating load.
The operation principle of present embodiment is following:
(1) phthalic anhydride is mixed with raw polyol, get into intensification pre-esterification reactor in the preparatory esterifying kettle 1 from material inlet 9, the water of generation and alcohol excess steam separate from the gaseous phase outlet 8 at preparatory esterifying kettle 1 top to be removed, and obtains preparatory esterification material; (2) get raw polyol in addition and earlier be preheated to 130～150 ℃, be heated to 200～220 ℃ by heater 5 again and get overheated pure gas through preheater 4; (3) middle part of preparatory esterification material from first esterification reaction tower 2 got into continuously; Said overheated pure gas gets into from reboiler 6 upper ends of first esterification reaction tower 2; Overheated pure gas carries out countercurrent reaction with preparatory esterification material on the catalyst reaction bed; The plasticizer semi-finished product that reaction generates are discharged from the bottom of said first esterification reaction tower 2 continuously, and excessive alcohol and the water that generates are discharged in the top of first esterification reaction tower 2; (4) the plasticizer semi-finished product that will discharge from the bottom of first esterification reaction tower 2 get into from the middle part of second esterification reaction tower 3 continuously; Overheated pure gas gets into from reboiler 6 upper ends of second esterification reaction tower 3; Overheated pure gas and plasticizer semi-finished product are countercurrent reaction on the catalyst reaction bed of second esterification reaction tower 3; With phthalic anhydride and monoesters continuation that generates and the raw polyol reaction completely of unreacted in first esterification reaction tower 2; Excessive alcohol that discharge at second esterification reaction tower, 3 tops and the low amounts of water that generates, the plasticizer that the continuous extraction reaction in second esterification reaction tower, 3 bottoms obtains; This plasticizer flows through preheater 4, for the preheating raw polyol provides heat.
The utility model is not limited to the above-mentioned specific embodiment, and all are based on the technical conceive of the utility model, and the structural improvement of having done all falls among the protection domain of the utility model.
Claims (8)
1. the continuous esterification process units of a plasticizer, it is characterized in that: comprise preparatory esterifying kettle and esterifier, said preparatory esterifying kettle top is provided with gaseous phase outlet, and the middle part is provided with material inlet, and the bottom is provided with preparatory esterification material outlet; Said esterifier comprises at least two esterification reaction tower that connect each other, that set inside has the catalyst reaction bed; Said esterification reaction tower all is provided with gaseous phase outlet at the top; The middle part is provided with material inlet, and the bottom is provided with the gas phase import, and the bottom is provided with material outlet; Wherein, the material inlet of first order esterification reaction tower connects the preparatory esterification material outlet of said preparatory esterifying kettle, and the material outlet of previous stage esterification reaction tower connects the material inlet of back one-level esterification reaction tower.
2. the continuous esterification process units of a kind of plasticizer according to claim 1 is characterized in that: the upstream position of said esterification reaction tower gas phase import is provided with the preheater and the heater of the raw polyol that is used to heat up in order.
3. the continuous esterification process units of a kind of plasticizer according to claim 2, it is characterized in that: said esterification reaction tower bottom is provided with reboiler, and said gas phase import is arranged at the upper end of said reboiler.
4. the continuous esterification process units of a kind of plasticizer according to claim 1 is characterized in that: except that final stage esterification reaction tower, the equal pipeline of the gaseous phase outlet of all the other esterification reaction tower connects the treating column in order to refined alcohol.
5. the continuous esterification process units of a kind of plasticizer according to claim 4 is characterized in that: the material inlet of the said preparatory esterifying kettle of said treating column outlet connection.
6. the continuous esterification process units of a kind of plasticizer according to claim 4 is characterized in that: the gaseous phase outlet of said final stage esterification reaction tower is connected to its upper level esterification reaction tower gas phase import after through preheater and heater.
7. the continuous esterification process units of a kind of plasticizer according to claim 2, it is characterized in that: the material outlet of said final stage esterification reaction tower connects said preheater.
8. according to the continuous esterification process units of the described a kind of plasticizer of the arbitrary claim of claim 1～7, it is characterized in that: said esterifier comprises first esterification reaction tower and second esterification reaction tower of mutual series connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204651338U CN202315851U (en) | 2011-11-21 | 2011-11-21 | Continuous esterification production device for plasticizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204651338U CN202315851U (en) | 2011-11-21 | 2011-11-21 | Continuous esterification production device for plasticizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202315851U true CN202315851U (en) | 2012-07-11 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011204651338U Expired - Lifetime CN202315851U (en) | 2011-11-21 | 2011-11-21 | Continuous esterification production device for plasticizer |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202315851U (en) |
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2011
- 2011-11-21 CN CN2011204651338U patent/CN202315851U/en not_active Expired - Lifetime
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANDONG YUANLI SCIENCE AND TECHNOLOGY CO., LTD. Free format text: FORMER NAME: WEIFANG YUANLI CHEMICAL CO., LTD. |
|
| CP03 | Change of name, title or address |
Address after: 262404, Shandong province Weifang County Changle Zhu Liu Street Industrial Park (309 State Road 355 kilometers) Patentee after: Shandong Yuanli Technology Co., Ltd. Address before: 262404 No. 37 Industrial Zone, Zhu Liu street, Changle County, Shandong, Weifang Patentee before: Weifang City Yuanli Chemical Industry Co., Ltd. |
|
| CX01 | Expiry of patent term |
Granted publication date: 20120711 |
|
| CX01 | Expiry of patent term |