CN205662475U - P xylene heat cascade utilization's heat transfer system - Google Patents
P xylene heat cascade utilization's heat transfer system Download PDFInfo
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- CN205662475U CN205662475U CN201620424241.3U CN201620424241U CN205662475U CN 205662475 U CN205662475 U CN 205662475U CN 201620424241 U CN201620424241 U CN 201620424241U CN 205662475 U CN205662475 U CN 205662475U
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- deheptanizer
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model provides a p xylene device heat cascade utilization system, does the system include the deheptanizer feeding deheptanizer top oil gas heat exchanger, the deheptanizer feeding liquid heat exchanger at the bottom of the deheptanizer, the deheptanizer feeding adsorption separation feeding heat exchanger and adsorption separation feeding are heavily boiled, is the feeding of deheptanizer in proper order through the deheptanizer feeding deheptanizer top oil gas heat exchanger, the deheptanizer feeding liquid heat exchanger and deheptanizer feeding at the bottom of the deheptanizer adsorption separation feeding heat exchanger links to each other with the feed inlet of deheptanizer, is the adsorption separation feeding through adsorption separation feeding reboiler and deheptanizer feeding liquid heat exchanger and adsorption separation unit connection at the bottom of the deheptanizer. The utility model discloses recoverable deheptanizer pushes up the heat of oil gas, reduces the power consumption of top of the tower air cooler, improves the heat utilization efficiency of adsorption separation feeding simultaneously, reduces the high -quality heat source consumption of finishing column.
Description
Technical field
This utility model belongs to oil-refining chemical production field, relates to a kind of xylol heat-exchange system, particularly relates to one
The heat-exchange system of xylol heat cascade utilization.
Background technology
Xylol (PX) is one of main basic organic material of petrochemical industry, chemical fibre, synthetic resin, pesticide, doctor
Numerous chemical production field such as medicine, plastics has purposes widely.P-Xylene unit is with the C in Reformed Gasoline7-C9Aromatic hydrocarbons is
Raw material, produces the products such as benzene, xylol and o-Dimethylbenzene.Complete PX device include disproportionation and transalkylation, adsorbing separation,
Isomerization and xylene fractionation unit.Wherein disproportionation and transalkylation are with reformation C7Aromatic hydrocarbons and the C of adsorption separation unit9-
C10Aromatic hydrocarbons is raw material, by disproportionation and transalkylation reaction, generates benzene and C8Aromatic hydrocarbons；Adsorption separation unit is with xylene fractionation list
The Mixed XYLENE of unit is raw material, according to adsorbing separation principle, isolates lean xylol and para-xylene product；Isomerization unit
With the lean xylol of adsorption separation unit as raw material, by isomerization reaction, obtain the product rich in xylol；Two
Toluene fractionation unit is with reformation C8The C that aromatic hydrocarbons, disproportionation and transalkylation reaction generate8The C that aromatic hydrocarbons and isomerization generate8Aromatic hydrocarbons is
Raw material, according to principles of rectification, isolates Mixed XYLENE and o-Dimethylbenzene product.
CN 204162631U discloses a kind of xylene production system, and described system includes benzenol hydrorefining, adsorbing separation
Tower, Extract tower, raffinate column, finishing column, isomerization reactor, heating furnace, deheptanizer；Anti-from xylene unit isomerization
Input and output material heat exchanger material out is answered to initially enter hot high score tank, from the hot isolated gas phase of high score tank through air cooler, water-cooled
Entering cold high score tank after device cooling and carry out gas-liquid separation, arrange outside isolated gas phase portion, part is done recycle hydrogen and is recycled；From
First feed heat exchange after hot high score tank and the cold isolated liquid-phase mixing of high score tank with isomerization reaction, change with adsorbing separation charging again
Heat, last with deheptanizer tower reactor discharging heat exchange after entrance deheptanizer；Adsorbing separation feeds first as finishing column reboiler
Thermal source, enters adsorption separation unit with after deheptanizer charging heat exchange the most again.This utility model is by optimizing isomerization reaction
Product separation process, and then optimize adsorbing separation charging heat exchange process, although finishing column thermal source consumption can be reduced, but there is also
That improvement project is relatively big, field position is the most limited, to unfavorable factors such as Reaction Separation systematic influence are uncertain.
Utility model content
For above-mentioned problems of the prior art, this utility model provides a kind of xylol heat cascade utilization
Heat-exchange system and heat-exchange method.This utility model is by feeding and absorption deheptanizer tower top oil gas, deheptanizer
The heat exchange process of separating feed is optimized, and has not only recycled the heat of deheptanizer top oil gas, reduces tower top air cooling
The power consumption of device, and the heat making adsorbing separation feed obtains cascade utilization, reduce finishing column high-quality thermal source (strippant,
Dimethylbenzene tower bottom liquid or middle pressure steam) consumption, there is obvious energy-saving effect.
For reaching this purpose, this utility model by the following technical solutions:
This utility model provides a kind of p-Xylene unit heat gradient utilization system, and described system includes that dimethylbenzene divides
Evaporating unit, isomerization unit and adsorption separation unit, isomerization unit includes that deheptanizer, adsorption separation unit include finished product
Tower, described system includes that liquid at the bottom of deheptanizer charging-deheptanizer top oil gas heat exchanger, deheptanizer charging-deheptanizer changes
Hot device, deheptanizer charging-adsorbing separation feed exchanger and adsorbing separation charging reboiler, the charging of deheptanizer warp successively
At the bottom of deheptanizer charging-deheptanizer top oil gas heat exchanger, deheptanizer charging-deheptanizer, liquid heat exchanger, deheptanizer enter
Material-adsorbing separation feed exchanger is connected with the charging aperture of deheptanizer, and adsorbing separation charging feeds reboiler through adsorbing separation
It is connected with adsorption separation unit with deheptanizer charging-adsorbing separation feed exchanger.
Following as the preferred technical scheme of this utility model, but the limit of the technical scheme provided not as this utility model
System, by the following technical programs, can preferably reach and realize technical purpose of the present utility model and beneficial effect.
As preferred version of the present utility model, described system includes that adsorbing separation feeds reboiler, described adsorbing separation
Feed after adsorbing separation charging reboiler and deheptanizer charging-adsorbing separation feed exchanger, with adsorption separation unit even
Connect.
This utility model provides above-mentioned p-Xylene unit heat stepped utilization method, and described method is:
Deheptanizer from xylene isomerization unit feeds and changes through deheptanizer charging-deheptanizer top oil gas successively
Liquid heat exchanger at the bottom of hot device, deheptanizer charging-deheptanizer and deheptanizer charging-adsorbing separation feed exchanger, respectively with
Deheptanizer is entered after liquid at the bottom of the tower top oil gas of deheptanizer, deheptanizer and adsorbing separation charging heat exchange；The tower of deheptanizer
Top oil gas enters air cooler after deheptanizer charging heat exchange；Adsorbing separation charging is first as the heat of adsorbing separation charging reboiler
After source is finishing column heat supply, enter back into deheptanizer charging-adsorbing separation feed exchanger laggard with deheptanizer charging heat exchange
Enter adsorption separation unit.
Concrete, described method is:
The deheptanizer that temperature is 30～100 DEG C from xylene isomerization unit feeds to enter through deheptanizer successively
Liquid heat exchanger, deheptanizer charging-adsorbing separation feed exchanger and deheptanizer charging-deheptanizer at the bottom of material-deheptanizer
End liquid heat exchanger, respectively with the tower top oil gas of deheptanizer, deheptanizer at the bottom of liquid and adsorbing separation charging heat exchange to 180～220
Deheptanizer is entered back into after DEG C；The temperature of deheptanizer tower top is that the oil gas of 100～200 DEG C feeds heat exchange to 80 with deheptanizer
～after 150 DEG C, enter air cooler；Temperature is that the adsorbing separation charging of 200～250 DEG C first feeds reboiler as adsorbing separation
Thermal source is that temperature is down to 160～220 DEG C after finishing column heat supply, then enters after 150～180 DEG C after deheptanizer charging heat exchange
Adsorption separation unit.
Compared with prior art, this utility model has the advantages that
This utility model is by entering the heat exchange process of deheptanizer top oil gas, deheptanizer charging and adsorbing separation charging
Row optimizes, and has not only recycled the heat of deheptanizer top oil gas, has reduced the power consumption of tower top air cooler, and make absorption divide
Heat from charging obtains cascade utilization, reduces the consumption of finishing column high-quality thermal source.Compared with prior art, this practicality is new
Type is only optimized by heat exchange process, can receive same energy-saving effect, it is to avoid isomerization reaction separation process changes instead
Answer the impact that system produces, and be not susceptible to field position impact.Further, can to reduce deheptanizer head space cold for this utility model
Device power consumption 30～60%, reduces finishing column high-quality thermal source (strippant, dimethylbenzene tower bottom liquid or middle pressure steam) simultaneously and consumes 40
～80%, there is obvious energy-saving effect.
Accompanying drawing explanation
Fig. 1 is the process chart of the xylol heat-exchange system described in this utility model embodiment 1；
Wherein, 1-finishing column, 2-deheptanizer, 3-high-quality thermal source, 4-high-quality thermal source reboiler, 5-adsorbing separation is entered
Material reboiler, liquid heat exchanger at the bottom of the charging of 9-deheptanizer and deheptanizer, the top oil gas heat exchange of 7-deheptanizer charging-deheptanizer
Device, 8-air cooler, 6-deheptanizer charging-adsorbing separation feed exchanger, 10-deheptanizer feeds, and 11-adsorbing separation is entered
Material, liquid at the bottom of 12-deheptanizer, 13-condensation reflux device.
Detailed description of the invention
For this utility model is better described, it is simple to understand the technical solution of the utility model, below to this utility model
Further describe.But following embodiment is only simple example of the present utility model, does not represent or limits this practicality
Novel rights protection scope, this utility model protection domain is as the criterion with claims.
Embodiment 1:
As it is shown in figure 1, present embodiments provide a kind of p-Xylene unit heat gradient utilization system, described system includes
Xylene fractionation unit, isomerization unit and adsorption separation unit, isomerization unit includes deheptanizer 2, adsorption separation unit
Including finishing column 1, described system include the deheptanizer charging-deheptanizer top hot device of oil gas 7, deheptanizer feed-take off heptane
Tower bottom liquid heat exchanger 9, deheptanizer charging-adsorbing separation feed exchanger 6 and adsorbing separation charging reboiler 5, deheptanizer
Charging 10 is successively through liquid heat exchanger 9 at the bottom of the deheptanizer charging-deheptanizer top hot device of oil gas 7, deheptanizer charging-deheptanizer
Being connected with the charging aperture of deheptanizer 2 with deheptanizer charging-adsorbing separation feed exchanger 6, adsorbing separation charging 11 is through inhaling
It is connected with adsorption separation unit after attached separating feed reboiler 5 and deheptanizer charging-adsorbing separation feed exchanger 6.
The tower top oil gas vent of described deheptanizer 2 successively with deheptanizer charging-deheptanizer top oil gas heat exchanger 7 and
Air cooler 8 is connected.
Described finishing column 1 thermal source includes high-quality thermal source 3 and adsorbing separation charging 11.
Embodiment 2:
As a example by 300,000 tons/year of p-Xylene unit of certain factory, present embodiments provide the xylol dress described in embodiment 1
Putting the heat-exchange method of heat gradient utilization system, described method is:
From xylene isomerization unit the deheptanizer that temperature is 100 DEG C feed 10 successively through deheptanizer feed-
After deheptanizer top oil gas heat exchanger 7 and temperature are the tower top oil gas heat exchange of deheptanizer 2 of 157 DEG C, through deheptanizer feed-
Liquid heat exchanger 9 at the bottom of deheptanizer and temperature are liquid 12 heat exchange at the bottom of the deheptanizer of 208 DEG C, then through deheptanizer charging-absorption point
From the adsorbing separation that feed exchanger 6 and temperature are 200 DEG C feed 11 heat exchange to 190 DEG C after enter deheptanizer 2；
The tower top oil gas of deheptanizer 2 and deheptanizer feed 10 heat exchange and carry out air cooling process through air cooler 8 after 120 DEG C
To 55 DEG C, then carry out subsequent treatment；
Temperature be the adsorbing separation charging 11 first thermals source as adsorbing separation charging reboiler 5 of 235 DEG C be that finishing column 1 supplies
After heat, temperature is down to 210 DEG C, then feeds 10 heat exchange to 177 DEG C with deheptanizer, enters adsorption separation unit.
Comparative example 1:
As a example by 300,000 tons/year of p-Xylene unit of certain factory, existing xylol production system is used to process, at it
Reason method is:
It is first 208 DEG C de-with temperature that the deheptanizer that temperature is 100 DEG C from xylene isomerization unit feeds 10
Heptane tower bottom liquid 12 carries out heat exchange, then feeds 11 heat exchange with the adsorbing separation that temperature is 235 DEG C to 190 DEG C, finally enters de-
Heptaner 2；The temperature of deheptanizer 2 is that the tower top oil gas of 157 DEG C is directly entered in air cooler 8 and is cooled to 55 DEG C；Temperature is 235
DEG C adsorbing separation charging 11 feed 10 heat exchange to 200 DEG C with deheptanizer, then be cooled to 177 DEG C by air cooler, enter suction
Attached separative element.
Comparative example 2 and comparative example 1 are it can be seen that use xylol heat-exchange system described in the utility model permissible
Reduce deheptanizer tower top air cooling load 6000kW, reduce air cooling power consumption 45.7% at the bottom of tower, reduce finishing column high quality heat simultaneously
Source consumes 67.9%, has obvious energy-saving effect.
The result of integrated embodiment 1-2 and comparative example 1 it can be seen that this utility model by deheptanizer top oil gas,
The heat exchange process of deheptanizer charging and adsorbing separation charging is optimized, and has not only recycled the heat of deheptanizer top oil gas
Amount, reduces the power consumption of tower top air cooler, and the heat making adsorbing separation feed obtains cascade utilization, reduce finished product tower height
The consumption of quality thermal source.Compared with prior art, this utility model can reduce deheptanizer head space cooler power consumption 30～60%,
Reduce finishing column high-quality thermal source (strippant, dimethylbenzene tower bottom liquid or middle pressure steam) simultaneously and consume 40～80%, have substantially
Energy-saving effect.
Applicant states, this utility model illustrates method detailed of the present utility model by above-described embodiment, but this reality
It is not limited to above-mentioned method detailed with novel, does not i.e. mean that this utility model has to rely on above-mentioned method detailed ability real
Execute.Person of ordinary skill in the field is it will be clearly understood that to any improvement of the present utility model, each former to this utility model product
The equivalence of material is replaced and the interpolation of auxiliary element, concrete way choice etc., all falls within protection domain of the present utility model and public affairs
Within the scope of opening.
Claims (1)
1. a p-Xylene unit heat utilization system, described system includes xylene fractionation unit, isomerization unit and suction
Attached separative element, isomerization unit includes deheptanizer (2), and adsorption separation unit includes finishing column (1), it is characterised in that institute
The system of stating includes liquid heat exchange at the bottom of deheptanizer charging-deheptanizer top oil gas heat exchanger (7), deheptanizer charging-deheptanizer
Device (9), deheptanizer charging-adsorbing separation feed exchanger (6) and adsorbing separation charging reboiler (5), deheptanizer feeds
(10) successively through liquid heat exchange at the bottom of deheptanizer charging-deheptanizer top oil gas heat exchanger (7), deheptanizer charging-deheptanizer
Device (9) is connected with the charging aperture of deheptanizer charging-adsorbing separation feed exchanger (6) with deheptanizer (2), and adsorbing separation is entered
Material (11) feeds reboiler (5) and deheptanizer charging-adsorbing separation feed exchanger (6) and adsorbing separation list through adsorbing separation
Unit connects.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620424241.3U CN205662475U (en) | 2016-05-11 | 2016-05-11 | P xylene heat cascade utilization's heat transfer system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620424241.3U CN205662475U (en) | 2016-05-11 | 2016-05-11 | P xylene heat cascade utilization's heat transfer system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205662475U true CN205662475U (en) | 2016-10-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201620424241.3U Active CN205662475U (en) | 2016-05-11 | 2016-05-11 | P xylene heat cascade utilization's heat transfer system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105777468A (en) * | 2016-05-11 | 2016-07-20 | 上海优华系统集成技术股份有限公司 | Paraxylene unit heat gradient utilization system and method |
| CN113289365A (en) * | 2021-07-01 | 2021-08-24 | 燕山大学 | Absorption heat pump rectification system based on intermediate reboiling and intermediate condensation |
-
2016
- 2016-05-11 CN CN201620424241.3U patent/CN205662475U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105777468A (en) * | 2016-05-11 | 2016-07-20 | 上海优华系统集成技术股份有限公司 | Paraxylene unit heat gradient utilization system and method |
| CN113289365A (en) * | 2021-07-01 | 2021-08-24 | 燕山大学 | Absorption heat pump rectification system based on intermediate reboiling and intermediate condensation |
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