CN209368154U - A kind of aromatics seperation heat integration goes into operation optimization system - Google Patents
A kind of aromatics seperation heat integration goes into operation optimization system Download PDFInfo
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- CN209368154U CN209368154U CN201822175574.9U CN201822175574U CN209368154U CN 209368154 U CN209368154 U CN 209368154U CN 201822175574 U CN201822175574 U CN 201822175574U CN 209368154 U CN209368154 U CN 209368154U
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Abstract
It goes into operation optimization system the utility model discloses a kind of aromatics seperation heat integration, including benzenol hydrorefining, toluene tower, benzene column, it is disproportionated stripper, heavy aromatics tower, toluene tower bottom reboiler, benzene column bottom reboiler and disproportionation stripper bottom reboiler, benzenol hydrorefining top exit connects toluene tower bottom reboiler and disproportionation stripper bottom reboiler by pipeline, toluene tower top exit connects benzene column bottom reboiler by pipeline, benzene column outlet at bottom connects toluene tower by pipeline, toluene tower top exit connects disproportionation stripper by pipeline, it is disproportionated stripper outlet at bottom and benzene column is connected by pipeline, toluene tower outlet at bottom connects benzenol hydrorefining by pipeline, xylene column bottoms outlet connects heavy aromatics tower by pipeline, the outlet of heavy aromatics top of tower connects disproportionation stripper by pipeline.The structure design of the utility model is reasonable, can be realized five towers circulation, guarantees that realization system sufficiently recycles, and realizes synchronous heating.
Description
Technical field
The utility model relates to aromatics seperations to integrate heat integration technology field, relate generally to a kind of aromatics seperation heat connection
Run work optimization system jointly.
Background technique
Aromatic hydrocarbons is widely used in the industries such as chemical industry, light industry, weaving, medicine, printing and dyeing, rubber and pesticide, at present aromatics seperation collection
At heat integration process, using benzenol hydrorefining as the center of heat integration, top gaseous phase does heat source to multiple towers, and realizes heat source and concentrate
Management, but not can be carried out multitower circulation heating.The benzenol hydrorefining of aromatics seperation, heavy aromatics tower, benzene column, toluene in the prior art
Tower, each tower single column self-loopa of disproportionation stripper, heating, but since the thermal center (-tre) of heat integration is in benzenol hydrorefining, so only diformazan
When benzene column is warming up to tower top and has enough gas phases, remaining tower can just be started to warm up, and cause the temperature difference larger, and heating is difficult.
Aromatics seperation integrates heat integration process complexity at present, and on-stream time is long, and there are each towers of heat integration cannot synchronize liter
There is liquid hammer scene in temperature after heating, equipment and equipment safety operation are seriously affected, when to solve to go into operation because of aromatic hydrocarbons heat integration
Heating cannot be synchronized, the problems such as on-stream time is long, and the cold and hot temperature difference is big, the utility model has carried out related improvement.
Utility model content
The utility model provides a kind of aromatics seperation heat integration and goes into operation optimization system, realizes five towers circulation, synchronous rises
Temperature.To realize above-mentioned technical purpose and the technique effect, the utility model is achieved through the following technical solutions.
A kind of aromatics seperation heat integration goes into operation optimization system, including benzenol hydrorefining, toluene tower, benzene column, disproportionation stripper, again
Aromatic hydrocarbons tower, toluene tower bottom reboiler, benzene column bottom reboiler and disproportionation stripper bottom reboiler, the benzenol hydrorefining top
Outlet connects toluene tower bottom reboiler and disproportionation stripper bottom reboiler by pipeline, and the toluene tower top exit passes through
Pipeline connects benzene column bottom reboiler, and the benzene column outlet at bottom connects toluene tower, the toluene tower top exit by pipeline
Disproportionation stripper is connected by pipeline, the disproportionation stripper outlet at bottom connects benzene column, the toluene tower bottom by pipeline
Outlet connects benzenol hydrorefining by pipeline, and the xylene column bottoms outlet connects heavy aromatics tower, the heavy aromatics by pipeline
Top of tower outlet connects disproportionation stripper by pipeline.
Preferably, during a kind of aromatics seperation heat integration goes into operation optimization system, the benzenol hydrorefining top is connected by pipeline
There is return tank I, the toluene tower top is connected with return tank II by pipeline, and heavy aromatics tower top is connected with by pipeline
Return tank III.
Preferably, a kind of aromatics seperation heat integration goes into operation in optimization system, between the toluene tower bottom and return tank II
It is connected with the cross-line I that goes into operation, is connected with the cross-line II that goes into operation between the heavy aromatics tower bottom and return tank III.
Preferably, a kind of aromatics seperation heat integration goes into operation in optimization system, on go into operation cross-line I and the cross-line II that goes into operation
It is provided with tower bottom drawing pump.
Preferably, during a kind of aromatics seperation heat integration goes into operation optimization system, the benzenol hydrorefining is aromatics seperation heat integration
The heat integration center of the optimisation technique that goes into operation transformation research and development.
The beneficial effects of the utility model are:
The structure design of the utility model is reasonable, and aromatics seperation dimethylbenzene top gaseous phase is to toluene bottom reboiler, disproportionation vapour
Mention bottom reboiler and do heat source, toluene top gaseous phase does heat source to benzene column bottom reboiler, increase after two cross-lines that go into operation
It can be realized five towers circulation when low temperature, recycle oil can bring heat to each when guaranteeing that realization system sufficiently recycles, while heating up
A tower realizes synchronous heating.
Detailed description of the invention
In order to illustrate more clearly of the technical solution of the utility model embodiment, make required for being described below to embodiment
Attached drawing is briefly described, it should be apparent that, the drawings in the following description are merely some embodiments of the present invention,
For those of ordinary skill in the art, without creative efforts, it can also be obtained according to these attached drawings
Other attached drawings.
Fig. 1 is the process flow diagram of the utility model.
Specific embodiment
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art are without creative efforts
All other embodiment obtained, fall within the protection scope of the utility model.
Refering to Figure 1, the present embodiment is that a kind of aromatics seperation heat integration goes into operation optimization system, including benzenol hydrorefining 1,
Toluene tower 2, benzene column 3, disproportionation stripper 4, heavy aromatics tower 5, toluene tower bottom reboiler 6, benzene column bottom reboiler 7 and disproportionation vapour
Stripper bottom reboiler 8,1 top exit of benzenol hydrorefining connect toluene tower bottom reboiler 6 and disproportionation stripper tower by pipeline
Bottom reboiler 8,2 top exit of toluene tower connect benzene column bottom reboiler 7 by pipeline, and 3 outlet at bottom of benzene column is connected by pipeline
Toluene tower 2 is connect, 2 top exit of toluene tower connects disproportionation stripper 4 by pipeline, and disproportionation 4 outlet at bottom of stripper passes through pipeline
Benzene column 3 is connected, 2 outlet at bottom of toluene tower connects benzenol hydrorefining 1 by pipeline, and 1 outlet at bottom of benzenol hydrorefining is connected by pipeline
Heavy aromatics tower 5,5 top exit of heavy aromatics tower connect disproportionation stripper 4 by pipeline.
1 top of benzenol hydrorefining is connected with return tank I 9 by pipeline, and 2 top of toluene tower is connected with return tank II by pipeline
10,5 top of heavy aromatics tower is connected with return tank III 11 by pipeline.
The cross-line I 12 that goes into operation, 5 bottom of heavy aromatics tower and return tank III are connected between 2 bottom of toluene tower and return tank II 10
The cross-line II 13 that goes into operation is connected between 11.
It goes into operation and cross-line I 12 and goes into operation and be provided with tower bottom drawing pump on cross-line II 13.
Benzenol hydrorefining 1 be aromatics seperation heat integration go into operation optimisation technique transformation research and development heat integration center.
Specific embodiment of the present utility model are as follows:
When aromatics seperation, 1 top gaseous phase of benzenol hydrorefining is to toluene tower bottom reboiler 6, disproportionation stripper bottom reboiler 7
Heat source is done, 2 top gaseous phase of toluene tower does heat source, 3 materials at bottom of tower of benzene column to 2 tower bottom of toluene tower, toluene to benzene column bottom reboiler 7
2 tower top material of tower is disproportionated 4 materials at bottom of tower of stripper to benzene column 3,2 materials at bottom of tower of toluene tower separately divides all the way extremely to disproportionation stripper 4
Benzenol hydrorefining 1,1 materials at bottom of tower of benzenol hydrorefining to heavy aromatics tower 5,5 tower top material of heavy aromatics tower to disproportionation stripper 4, therefore discrimination
The material for changing stripper 4 is to need toluene tower 2 and heavy aromatics tower 5 to have foot from 5 tower top of 2 tower top of toluene tower and heavy aromatics tower
Just can guarantee that disproportionation stripper 4 is fed after enough temperature, so cannot achieve circulation when going into operation initial stage cold stage, by
Toluene tower 2 and the increase of heavy aromatics tower 5, which go into operation, cross-line I 12 and to go into operation cross-line II 13, in low temperature by tower bottom drawing pump open across
Line realizes the charging of disproportionation stripper 4, meets circulation and requires, and recycle oil can when guaranteeing that realization system sufficiently recycles, while heating up
Bringing heat to each tower, synchronous heating is realized.
In the description of this specification, the description of reference term " one embodiment ", " example ", " specific example " etc. means
Particular features, structures, materials, or characteristics described in conjunction with this embodiment or example are contained at least one of the utility model
In embodiment or example.In the present specification, schematic expression of the above terms be not necessarily referring to identical embodiment or
Example.Moreover, particular features, structures, materials, or characteristics described can be in any one or more embodiment or examples
In can be combined in any suitable manner.
The preferred embodiment in the utility model disclosed above is only intended to help to illustrate the utility model.Preferred embodiment is simultaneously
There is no the details that detailed descriptionthe is all, also not limiting the utility model is only the specific embodiment.Obviously, according to this theory
The content of bright book can make many modifications and variations.These embodiments are chosen and specifically described to this specification, is in order to preferably
The principles of the present invention and practical application are explained, so that skilled artisan be enable to better understand and utilize this
Utility model.The utility model is limited only by the claims and their full scope and equivalents.
Claims (5)
- The optimization system 1. a kind of aromatics seperation heat integration goes into operation, it is characterised in that: including benzenol hydrorefining (1), toluene tower (2), benzene Tower (3), disproportionation stripper (4), heavy aromatics tower (5), toluene tower bottom reboiler (6), benzene column bottom reboiler (7) and disproportionation vapour Stripper bottom reboiler (8), benzenol hydrorefining (1) top exit pass through pipeline connection toluene tower bottom reboiler (6) and discrimination Change stripper bottom reboiler (8), toluene tower (2) top exit connects benzene column bottom reboiler (7) by pipeline, described Benzene column (3) outlet at bottom connects toluene tower (2) by pipeline, and toluene tower (2) top exit connects disproportionation vapour by pipeline Stripper (4), disproportionation stripper (4) outlet at bottom connect benzene column (3) by pipeline, and toluene tower (2) outlet at bottom is logical Pipeline connection benzenol hydrorefining (1) is crossed, benzenol hydrorefining (1) outlet at bottom connects heavy aromatics tower (5) by pipeline, the heavy virtue Hydrocarbon tower (5) top exit connects disproportionation stripper (4) by pipeline.
- The optimization system 2. a kind of aromatics seperation heat integration according to claim 1 goes into operation, it is characterised in that: the dimethylbenzene Tower (1) top is connected with return tank I (9) by pipeline, and toluene tower (2) top is connected with return tank II by pipeline (10), heavy aromatics tower (5) top is connected with return tank III (11) by pipeline.
- The optimization system 3. a kind of aromatics seperation heat integration according to claim 2 goes into operation, it is characterised in that: the toluene tower (2) cross-line I (12) that goes into operation, heavy aromatics tower (5) bottom and return tank III are connected between bottom and return tank II (10) (11) cross-line II (13) that goes into operation is connected between.
- The optimization system 4. a kind of aromatics seperation heat integration according to claim 3 goes into operation, it is characterised in that: it is described go into operation across Tower bottom drawing pump is provided on line I (12) and the cross-line II (13) that goes into operation.
- The optimization system 5. a kind of aromatics seperation heat integration according to claim 1 goes into operation, it is characterised in that: the dimethylbenzene Tower (1) be aromatics seperation heat integration go into operation optimisation technique transformation research and development heat integration center.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112500889A (en) * | 2020-12-28 | 2021-03-16 | 大连福佳·大化石油化工有限公司 | Adsorption plant to isomerization unit feed system |
| CN112625741A (en) * | 2020-12-28 | 2021-04-09 | 大连福佳·大化石油化工有限公司 | Isomerization reaction system |
-
2018
- 2018-12-24 CN CN201822175574.9U patent/CN209368154U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112500889A (en) * | 2020-12-28 | 2021-03-16 | 大连福佳·大化石油化工有限公司 | Adsorption plant to isomerization unit feed system |
| CN112625741A (en) * | 2020-12-28 | 2021-04-09 | 大连福佳·大化石油化工有限公司 | Isomerization reaction system |
| CN112500889B (en) * | 2020-12-28 | 2024-02-20 | 大连福佳·大化石油化工有限公司 | Adsorption unit to isomerization unit feed system |
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