CN204162631U - A kind of xylene production system - Google Patents
A kind of xylene production system Download PDFInfo
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- CN204162631U CN204162631U CN201420633375.7U CN201420633375U CN204162631U CN 204162631 U CN204162631 U CN 204162631U CN 201420633375 U CN201420633375 U CN 201420633375U CN 204162631 U CN204162631 U CN 204162631U
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Abstract
The utility model provides a kind of xylene production system, and described system comprises benzenol hydrorefining, absorptive separation column, Extract tower, raffinate column, finishing column, isomerization reactor, process furnace, deheptanizer; First hot high score tank is entered from xylene unit isomerization reaction input and output material interchanger material out, after air cooler, water cooler cooling, enter cold high score tank from the isolated gas phase of hot high score tank and carry out gas-liquid separation, isolated gas phase portion is arranged outward, and part is done recycle hydrogen and recycled; First with isomerization reaction charging heat exchange, enter deheptanizer again with after fractionation by adsorption charging heat exchange, last and deheptanizer tower reactor discharging heat exchange after hot high score tank and the isolated liquid-phase mixing of cold high score tank; Fractionation by adsorption charging first as finishing column reboiler thermal source, and then with deheptanizer charging heat exchange after enter adsorption separation unit.System described in the utility model achieves cancels finishing column to the consumption of outside higher-grade thermal source.
Description
Technical field
The utility model relates to aromatic hydrocarbons xylene production system, especially relates to a kind of xylene production system of novel energy-conserving.
Background technology
PX(p-Xylol) be a kind of important basic organic chemical industry raw material, be mainly used in producing terephthalic acid (PTA) and dimethyl terephthalate (DMT) (DMT), and then produce polyester.Therefore, PX can be described as the tap of polyester product chain, is important industrial chemicals, has extremely important importance and functions in national economy.By the end of 2011, the PX output of China, more than 6,000,000 tons/year, became one of maximum in the world producing country.
Current PX produces main with C
8aromatic hydrocarbons (m-xylene, o-Xylol and ethylbenzene) is raw material, can obtain highly purified PX product by isomerization reaction, fractionation by adsorption and rectifying separation process.The function of isomerization unit is with the C of poor PX
8mixture is raw material, is obtained the reaction product being rich in PX by isomerization reaction; The function of adsorption separation unit obtains highly purified PX product by fractionation by adsorption and rectifying means, isolates the C of poor PX simultaneously
8mixture is as the raw material of isomerization reaction unit; The function of xylene distillation unit realizes C
8a and C
9+ clear cutting, C
8a is as fractionation by adsorption charging.
Summary of the invention
For the deficiencies in the prior art, the purpose of this utility model is to provide a kind of energy-saving xylene production system, and can significantly improve device energy level, unit consumption of energy significantly declines.
The utility model provides a kind of xylene production system, and described system comprises benzenol hydrorefining, adsorption tower, Extract tower, raffinate column, finishing column, isomerization reactor, process furnace, deheptanizer, the tower top outlet of described benzenol hydrorefining is successively through finishing column reboiler, be connected with adsorption tower after fractionation by adsorption feed exchanger, the Extract mouth of adsorption tower is connected with Extract tower through pipeline, the raffinate mouth of adsorption tower is connected with raffinate column through pipeline, the upper outlet of described Extract tower is connected with finishing column through pipeline, Extract tower is connected with adsorption tower through finishing column reboiler with the tower bottom outlet of raffinate column, the upper outlet of raffinate column is successively through reaction feed interchanger, input and output material interchanger, be connected with the entrance of isomerization reactor after process furnace, the outlet of isomerization reactor is connected with hot high score tank through input and output material interchanger, the upper outlet of hot high score tank is through air cooler, be connected with the entrance of cold high score tank after water cooler, the upper outlet of cold high score tank divides two-way, wherein a road is connected with input and output material interchanger through compressor, arrange outside another road, through reaction feed interchanger after the outlet at bottom of hot high score tank and cold high score tank converges, fractionation by adsorption feed exchanger, deheptanizer input and output material interchanger is connected with deheptanizer, the tower bottom outlet of deheptanizer is connected with benzenol hydrorefining entrance through deheptanizer input and output material interchanger.
In system described in the utility model, described compressor is screw or reciprocation compressor, is preferably screw-type compressor.
In system described in the utility model, described input and output material interchanger can be around tubular type, shell and tube or shell-and-plate(heat)exchanger, is preferably shell-and-plate(heat)exchanger.
In system described in the utility model, described benzenol hydrorefining is pressurized operation, and working pressure is 0.5 ~ 2.5 Mpa, and be preferably 0.8 ~ 1.0 Mpa, benzenol hydrorefining is preferably tray column, and stage number is 150 ~ 200.
In system described in the utility model, described deheptanizer is tray column, and stage number is 20 ~ 50, and deheptanizer is pressurized operation, and working pressure is 0.5 ~ 2.5 Mpa, is preferably 0.7 ~ 1.0 Mpa,
In system described in the utility model, described Extract tower, raffinate column, finishing column are tray column, stage number 30 ~ 70; Atmospheric operation.
In system described in the utility model, described adsorption tower inside filling has the sorbent material of highly selective to p-Xylol, ADS-27, ADS-37 or ADS-47 type sorbent material that sorbent material can be produced for Uop Inc., adsorption tower service temperature is preferably 170 ~ 190 DEG C.
In system described in the utility model, the operational condition of hot high score tank is service temperature 100 ~ 120 DEG C, pressure 0.6 ~ 1.2 MPa.
In system described in the utility model, the operational condition of cold high score tank is service temperature 35 ~ 40 DEG C, and pressure is 0.5 ~ 1.1 MPa.
Compared with prior art, the utility model provides xylene production system by adopting hot high division technique and reasonably optimizing heat exchange process, achieve and cancel finishing column to the consumption of outside higher-grade thermal source, reach really energy-conservation object, the utility model flow process can not cause detrimentally affect to production operation, there is obvious energy saving effect and economic benefit, proving to adopt the utility model that xylene unit unit consumption of energy can be made to reduce by 15 kg. mark oil/(t.PX) by calculating.
Accompanying drawing explanation
Fig. 1 is the utility model xylene production system schematic.
Embodiment
As shown in Figure 1, the utility model provides a kind of xylene production system, and described xylene production system comprises benzenol hydrorefining 21, adsorption tower 10, Extract tower 12, raffinate column 18, finishing column 14, isomerization reactor 1, process furnace 6, deheptanizer 19, the tower top outlet of described dimethylbenzene 21 tower is successively through finishing column reboiler 16, be connected with adsorption tower 10 after fractionation by adsorption feed exchanger 7, the Extract mouth of adsorption tower 10 is connected with Extract tower 12 through pipeline, the raffinate mouth of adsorption tower 10 is connected with raffinate column 18 through pipeline, the upper outlet of described Extract tower 12 is connected with finishing column 14 through pipeline, Extract tower 12 is connected with adsorption tower 10 through finishing column reboiler 15 with the tower bottom outlet of raffinate column 18, the upper outlet of raffinate column 18 is successively through reaction feed interchanger 5, input and output material interchanger 2, be connected with the entrance of isomerization reactor 1 after process furnace 6, the outlet of isomerization reactor 1 is connected with hot high score tank 10 through input and output material interchanger 2, the upper outlet of hot high score tank 20 is through air cooler 23, be connected with the entrance of cold high score tank 3 after water cooler 24, the upper outlet of cold high score tank 3 divides two-way, wherein a road is connected with input and output material interchanger 2 through compressor 4, arrange outside another road, through reaction feed interchanger 5 after the outlet at bottom of hot high score tank 20 and cold high score tank 3 converges, fractionation by adsorption feed exchanger 7, deheptanizer input and output material interchanger 8 is connected with deheptanizer 19, the tower bottom outlet of deheptanizer 19 is connected with benzenol hydrorefining 21 entrance through deheptanizer input and output material interchanger 8.
Composition graphs 1, further illustrates the utility model technical process.Input and output material interchanger 2 and reaction feed heat exchange is entered from isomerization reactor 1 reaction product out, reaction product after heat exchange enters hot high score tank 20 and carries out gas-liquid separation, isolated gas phase enters cold high score tank 3 and carries out gas-liquid separation after air cooling, water-cooled, isolated gas phase portion is arranged outward, and part is compressed Posterior circle through circulating hydrogen compressor 4 and used; First through reaction feed interchanger 5 and reaction feed heat exchange after hot high score tank 20 and the isolated liquid-phase mixing of cold high score tank 3, then by fractionation by adsorption feed exchanger 7 and fractionation by adsorption charging 9 heat exchange, deheptanizer 19 is entered finally by after discharging heat exchange at the bottom of deheptanizer input and output material interchanger 8 and deheptanizer tower; Discharging at the bottom of deheptanizer tower and the C from reformer unit
8 +enter benzenol hydrorefining 21 as charging 22 after mixing to be separated, the C that tower top obtains
8mixture 9 as fractionation by adsorption charging first as the thermal source of finishing column reboiler 16, and then adsorption tower 10 is entered after fractionation by adsorption feed exchanger 7 with deheptanizer charging heat exchange, enter Extract tower 12 by adsorption tower Extract 11 to be out separated, overhead product 13 enters finishing column 14; Enter raffinate column 18 by adsorption tower raffinate 17 to be out separated, overhead product is isomerization reaction charging, first as the thermal source of the tower bottom reboiler 15 of finishing column 14 after the bottom product of raffinate column 18 and Extract tower 12 converges, return adsorption tower 10 more afterwards.
Claims (10)
1. an xylene production system, described system comprises benzenol hydrorefining, adsorption tower, Extract tower, raffinate column, finishing column, isomerization reactor, process furnace, deheptanizer, the tower top outlet of described benzenol hydrorefining is successively through finishing column reboiler, be connected with adsorption tower after fractionation by adsorption feed exchanger, the Extract mouth of adsorption tower is connected with Extract tower through pipeline, the raffinate mouth of adsorption tower is connected with raffinate column through pipeline, the upper outlet of described Extract tower is connected with finishing column through pipeline, Extract tower is connected with adsorption tower through finishing column reboiler with the tower bottom outlet of raffinate column, the upper outlet of raffinate column is successively through reaction feed interchanger, input and output material interchanger, be connected with the entrance of isomerization reactor after process furnace, the outlet of isomerization reactor is connected with hot high score tank through input and output material interchanger, the upper outlet of hot high score tank is through air cooler, be connected with the entrance of cold high score tank after water cooler, the upper outlet of cold high score tank divides two-way, wherein a road is connected with input and output material interchanger through compressor, arrange outside another road, through reaction feed interchanger after the outlet at bottom of hot high score tank and cold high score tank converges, fractionation by adsorption feed exchanger, deheptanizer input and output material interchanger is connected with deheptanizer, the tower bottom outlet of deheptanizer is connected with benzenol hydrorefining entrance through deheptanizer input and output material interchanger.
2. according to system according to claim 1, it is characterized in that: described compressor is screw or reciprocation compressor.
3. according to the system described in claim 1 or 2, it is characterized in that: described compressor is screw-type compressor.
4. according to system according to claim 1, it is characterized in that: described input and output material interchanger is around tubular type, shell and tube or shell-and-plate(heat)exchanger.
5. according to the system described in claim 1 or 4, it is characterized in that: described input and output material interchanger is shell-and-plate(heat)exchanger.
6. according to system according to claim 1, it is characterized in that: described benzenol hydrorefining is tray column, stage number is 150 ~ 200.
7. according to system according to claim 1, it is characterized in that: described deheptanizer is tray column, stage number is 20 ~ 50.
8. according to system according to claim 1, it is characterized in that: described Extract tower, raffinate column, finishing column are tray column.
9. according to system according to claim 8, it is characterized in that: described Extract tower, raffinate column, finishing column stage number 30 ~ 70.
10. according to system according to claim 1, it is characterized in that: described adsorption tower inside filling has the sorbent material of highly selective to p-Xylol.
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| CN201420633375.7U CN204162631U (en) | 2014-10-30 | 2014-10-30 | A kind of xylene production system |
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| CN201420633375.7U CN204162631U (en) | 2014-10-30 | 2014-10-30 | A kind of xylene production system |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105498269A (en) * | 2015-12-10 | 2016-04-20 | 上海优华系统集成技术股份有限公司 | Xylene disproportionation reaction product separation system based on thermal high-pressure separation process and separation method of the xylene disproportionation reaction product separation system |
| CN105566051A (en) * | 2016-02-24 | 2016-05-11 | 上海优华系统集成技术股份有限公司 | Disproportionated reaction product separation and heat exchange system and processing method thereof |
| 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 |
| CN109336731A (en) * | 2018-12-08 | 2019-02-15 | 大连福佳·大化石油化工有限公司 | Improved crude benzol production system |
| CN109370636A (en) * | 2018-12-08 | 2019-02-22 | 大连福佳·大化石油化工有限公司 | Aromatics isomerization process system |
| CN110937974A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
| CN112194549A (en) * | 2019-07-08 | 2021-01-08 | 中国石油化工股份有限公司 | Device and process for producing aromatic hydrocarbon product |
| CN112441870A (en) * | 2019-08-27 | 2021-03-05 | 中国石油化工股份有限公司 | Production device and process of aromatic hydrocarbon product |
| CN113307718A (en) * | 2021-07-14 | 2021-08-27 | 安庆亿成化工科技有限公司 | Device and method for generating durene from durene and durene |
| CN113461472A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Production device and production process of p-xylene |
| CN113461471A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Production device and production process of p-xylene |
-
2014
- 2014-10-30 CN CN201420633375.7U patent/CN204162631U/en active Active
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105498269A (en) * | 2015-12-10 | 2016-04-20 | 上海优华系统集成技术股份有限公司 | Xylene disproportionation reaction product separation system based on thermal high-pressure separation process and separation method of the xylene disproportionation reaction product separation system |
| CN105566051A (en) * | 2016-02-24 | 2016-05-11 | 上海优华系统集成技术股份有限公司 | Disproportionated reaction product separation and heat exchange system and processing method thereof |
| CN105566051B (en) * | 2016-02-24 | 2018-02-27 | 上海优华系统集成技术股份有限公司 | A kind of disproportionated reaction product separation and heat-exchange system and its processing method |
| 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 |
| CN110937974A (en) * | 2018-09-25 | 2020-03-31 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
| CN110937974B (en) * | 2018-09-25 | 2022-09-09 | 中国石油化工股份有限公司 | Production device and process of p-xylene |
| CN109336731A (en) * | 2018-12-08 | 2019-02-15 | 大连福佳·大化石油化工有限公司 | Improved crude benzol production system |
| CN109370636A (en) * | 2018-12-08 | 2019-02-22 | 大连福佳·大化石油化工有限公司 | Aromatics isomerization process system |
| CN112194549A (en) * | 2019-07-08 | 2021-01-08 | 中国石油化工股份有限公司 | Device and process for producing aromatic hydrocarbon product |
| CN112194549B (en) * | 2019-07-08 | 2023-01-10 | 中国石油化工股份有限公司 | Device and process for producing aromatic hydrocarbon product |
| CN112441870A (en) * | 2019-08-27 | 2021-03-05 | 中国石油化工股份有限公司 | Production device and process of aromatic hydrocarbon product |
| CN112441870B (en) * | 2019-08-27 | 2023-03-24 | 中国石油化工股份有限公司 | Production device and process of aromatic hydrocarbon product |
| CN113461472A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Production device and production process of p-xylene |
| CN113461471A (en) * | 2020-03-30 | 2021-10-01 | 中国石油化工股份有限公司 | Production device and production process of p-xylene |
| CN113461472B (en) * | 2020-03-30 | 2023-10-10 | 中国石油化工股份有限公司 | Production device and production process of paraxylene |
| CN113461471B (en) * | 2020-03-30 | 2023-10-10 | 中国石油化工股份有限公司 | Production device and production process of paraxylene |
| CN113307718A (en) * | 2021-07-14 | 2021-08-27 | 安庆亿成化工科技有限公司 | Device and method for generating durene from durene and durene |
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