CN201389355Y - Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system - Google Patents
Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system Download PDFInfo
- Publication number
- CN201389355Y CN201389355Y CN200820156670U CN200820156670U CN201389355Y CN 201389355 Y CN201389355 Y CN 201389355Y CN 200820156670 U CN200820156670 U CN 200820156670U CN 200820156670 U CN200820156670 U CN 200820156670U CN 201389355 Y CN201389355 Y CN 201389355Y
- Authority
- CN
- China
- Prior art keywords
- fractionating column
- heat
- heat exchanger
- catalytic reforming
- reforming unit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to the technical field of the chemical engineering heat exchanging network, and in particular to an improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system, which is characterized in that the bottom part of a fractionating tower in a catalysis reforming device is divided into two loops: one loop is connected with a discharging pipe (4) on the bottom part of the fractionating tower, and the other loop is connected with a shell side entrance of a heat exchanger assembly (3), and a shell side outlet of the heat exchanger assembly (3) is connected with a re-boiled object returning tower port; and a shell side inlet of the heat exchanger assembly (3) is connected with a device outlet of a technological logistics conveying pipeline of other devices with corresponding temperature, and the shell side outlet of the heat exchanger assembly (3) is connected with a device inlet of a technological logistics returning pipeline of other devices. Compared with the prior art, the technological logistics heat of the other devices at the temperature of 150 DEG C to 300 DEG C is reasonably utilized, the re-boiling heat source fuel or the low-pressure vapor at the bottom of the fractionating tower of the reforming device can be saved, the oil refining energy consumption of the reforming device can be reduced, the oil refining cost can be reduced, and the economic benefit can be improved.
Description
[technical field]
The utility model relates to the technical field of chemical industry heat-exchange network, and heat-exchange system heavily boils at the bottom of specifically a kind of improved catalytic reforming unit fractionating column.
[technical background]
At present, the fractionating column of catalytic reforming unit generally adopts low-pressure steam or heating furnace as thermal source, and other device has the heat more than needed of temperature counterpart can supply to utilize simultaneously.
Idiographic flow is as follows:
The temperature that in the catalytic reforming unit come out in 1 end of fractionating column is T
1=120 ℃-260 ℃ the processing medium that boils again, from coming from heat power supply device 2, behind the thermal source heat-obtaining as low-pressure steam or heating furnace, temperature rise is to T
2=120 ℃-280 ℃ are returned catalytic reforming fractionating column 1.
Adopt above flow process, the fractionating column column bottom temperature of reformer is not high, adopts the mode heat supply of low-pressure steam or heating furnace, and the high-quality low usefulness of energy causes energy waste; Simultaneously other device has the heat more than needed of potential temperature counterpart rationally not reclaimed and utilizes in the factory, energy dissipation, therefore the fractionation tower weight of needing a kind of novel catalytic reforming unit of practicality badly the flow process of boiling, rationally utilize the heat more than needed of other unit temp counterpart, realize the reasonable utilization of energy, reduce material consumption, energy consumption.
[summary of the invention]
The purpose of this utility model is in order to overcome the deficiencies in the prior art, and catalytic reforming unit logistics and other device are had the heat logistics heat exchange more than needed of temperature counterpart, energy efficient.
For achieving the above object, the heat-exchange system that heavily boils at the bottom of a kind of improved catalytic reforming unit fractionating column is provided, catalytic reforming unit fractionating column 1, other device 4 of catalytic reforming unit fractionating column outside, it is characterized in that: two-way is divided in the bottom of fractionating column 1 in catalytic reforming unit, one the tunnel connects fractionating column bottom discharge pipe 4, and another road connects the shell side inlet of heat exchanger package 3, and the logistics of heavily boiling below the outlet of heat exchanger package 3 shell sides and the fractionating column is returned the tower mouth and is connected; The tube side import of heat exchanger package 3 connect the temperature counterpart other device the process-stream conveyance conduit go out the device mouth, the tube side outlet of heat exchanger package 3 connects the motion device mouth of the process-stream Returning pipe of other device again.
Fractionating column 1 in the described catalytic reforming unit is meant that column bottom temperature is at 120-260 ℃ fractionating column, as tops stripper, C
4/ C
5In fractionating column, depentanizer, the dehexanizer any.
Described other device is gasoline and diesel hydrogenation refining system device or heat-conducting oil system device.
Described heat exchanger package is made up of 1～6 heat exchanger.
Compared with prior art, the utility model is on the existing equipment basis, set up heat transmission equipment, rationally utilized the heat of temperature at the process-stream of other device of 150 ℃-300 ℃, boiling hot again source fuel or low-pressure steam at the bottom of the reformer fractionating column have been saved, reduce the refining energy consumption of reformer, reduce the oil refining cost, increase economic efficiency.
[description of drawings]
Fig. 1 is the boil connection diagram of flow process of the fractionation tower weight of existing catalytic reforming unit.
Fig. 2 is the fractionation tower weight of the catalytic reforming unit of embodiment in the utility model flow process connection diagram of boiling
Appointment Fig. 2 is a Figure of abstract.
Referring to Fig. 1 and Fig. 2,1 is fractionating column, is the fractionating column in the catalytic reforming unit; 2 is heat power supply device, as low-pressure steam heat exchanger or heating furnace; 3 is heat exchanger package; 4 is other device of temperature counterpart; Sto is the fractionating column top discharge; Sin is charging; S1 is for returning the tower logistics; Sbo is the fractionating column bottom discharge; S2 returns the tower logistics for another road; Sot is other device logistics.
[specific embodiment]
Below the utility model is described in further detail, the utility model is still more clearly for the people of this professional skill field.
What follows temperature is respectively: T
1=120 ℃-260 ℃; T
2=120 ℃-280 ℃; T
a=150 ℃-300 ℃; T
b=130 ℃-270 ℃;
The inlet of the shell side of heat exchanger package 3 was connected with 1 end of fractionating column, the logistics of heavily boiling of the outlet of heat exchanger package 3 shell sides and fractionating column 1 tower below is returned the tower mouth and is connected, the tube side import and export of heat exchanger package 3, connect respectively temperature counterpart in the factory other device the process-stream conveyance conduit the outlet that goes out other device, return the inlet of other device; Temperature is T in the catalytic reforming unit
1Fractionating column 1 substrate flow to the shell side of newly-increased heat exchanger package 3, with temperature in the tube side of heat exchanger package 3 be T
aFrom the process-stream heat exchange of other device to T
2After return fractionating column 1; Temperature from other device is T
aProcess-stream then be cooled to T
bAfter return original device; The tube side of heat exchanger package 3 is walked the process-stream of introducing from other device 4;
Device after the improvement, temperature are T
aFrom the process-stream of other device, the heat exchanger package 3 through newly-increased provides heat to the fractionating column in the catalytic reforming unit 1, and the energy of the process-stream of the temperature counterpart of other device 4 obtains rationally, makes full use of; Simultaneously, the flow process of heavily boiling at the bottom of original reformation fractionating column of stopping using is saved low-pressure steam or heating furnace fuel.
Claims (4)
1, the heat-exchange system that heavily boils at the bottom of a kind of improved catalytic reforming unit fractionating column, mainly comprise catalytic reforming unit fractionating column (1), other device (4) of catalytic reforming unit fractionating column outside, it is characterized in that: two-way is divided in the bottom of fractionating column in catalytic reforming unit (1), one the tunnel connects fractionating column bottom discharge pipe (4), another road connects the shell side inlet of heat exchanger package (3), and the logistics of heavily boiling below the outlet of heat exchanger package (3) shell side and the fractionating column is returned the tower mouth and is connected; The tube side import of heat exchanger package (3) connect the temperature counterpart other device the process-stream conveyance conduit go out the device mouth, the tube side outlet of heat exchanger package (3) connects the motion device mouth of the process-stream Returning pipe of other device again.
2, the heat-exchange system that heavily boils at the bottom of a kind of improved catalytic reforming unit fractionating column as claimed in claim 1, it is characterized in that: the fractionating column in the described catalytic reforming unit (1) is meant column bottom temperature at 120-260 ℃ fractionating column, is in tops stripper, C4/C5 fractionating column, depentanizer, the dehexanizer any.
3, the heat-exchange system that heavily boils at the bottom of a kind of improved catalytic reforming unit fractionating column as claimed in claim 1 is characterized in that: described other device is gasoline and diesel hydrogenation refining system device or heat-conducting oil system device.
4, the heat-exchange system that heavily boils at the bottom of a kind of improved catalytic reforming unit fractionating column as claimed in claim 1, it is characterized in that: described heat exchanger package is made up of 1～6 heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200820156670U CN201389355Y (en) | 2008-12-05 | 2008-12-05 | Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200820156670U CN201389355Y (en) | 2008-12-05 | 2008-12-05 | Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201389355Y true CN201389355Y (en) | 2010-01-27 |
Family
ID=41596173
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200820156670U Expired - Lifetime CN201389355Y (en) | 2008-12-05 | 2008-12-05 | Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201389355Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113136241A (en) * | 2020-01-20 | 2021-07-20 | 中国石油天然气股份有限公司 | Reformer and method for producing the same |
-
2008
- 2008-12-05 CN CN200820156670U patent/CN201389355Y/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113136241A (en) * | 2020-01-20 | 2021-07-20 | 中国石油天然气股份有限公司 | Reformer and method for producing the same |
| CN113136241B (en) * | 2020-01-20 | 2023-04-07 | 中国石油天然气股份有限公司 | Reformer and method for producing the same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101424453B (en) | High temperature heat integration system for oil-extraction plant and use thereof | |
| CN102432016B (en) | Optimization recovery system for reduction tail gas heat energy in polycrystalline silicon production | |
| CN108286700A (en) | New heat pipe steam boiler | |
| CN201737903U (en) | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device | |
| CN103528122B (en) | A kind of packaged type phase change heat storage heat supply device | |
| CN102721222B (en) | System for recovering waste heat of process cooling water | |
| CN201110594Y (en) | Coupled type energy-saving heating system special for plateau | |
| CN206372822U (en) | A kind of reactor heat-energy utilizing device | |
| CN201389355Y (en) | Improved catalysis reforming device fractionating tower bottom re-boiling heat-exchanging system | |
| CN202648227U (en) | Waste heat recovery system for process cooling water | |
| CN201795634U (en) | Waste heat recovery energy saving apparatus for cooling | |
| CN201620134U (en) | Novel tower top heat exchange system of fractionating tower of aromatic hydrocarbon device | |
| CN101289631B (en) | Optimizing hydrogenation and heat-exchange system | |
| CN203183716U (en) | Alcohol distillation device with heat recovery device | |
| CN201740358U (en) | Drying tower system | |
| CN109059595B (en) | Fused salt heat accumulation device | |
| CN201173725Y (en) | High-temperature vapour water heat exchanger | |
| CN110566921A (en) | Gas boiler waste heat recycling device and method | |
| CN201517430U (en) | Steam condensation type turbo set residual-heat heating system | |
| CN2876669Y (en) | Heat energy recovering system for beer plant | |
| CN202144482U (en) | Methanol recovery device | |
| CN105371512B (en) | Condensate recycling system | |
| CN210833174U (en) | Air heat energy recovery device | |
| CN221016008U (en) | Solvent condensation reflux type reaction kettle for preparing polyester resin | |
| CN210176809U (en) | Reaction tower waste gas recycling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI YOUHUA SYSTEM INTEGRATION TECHNOLOGY CO., Free format text: FORMER OWNER: SHANGHAI JIUYUAN PETROLEUM CHEMICAL CO., LTD. Effective date: 20101224 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 200120 ROOM 701, SHENGKANG LIAOSHI BUILDING, NO.738, SHANGCHENG ROAD, PUDONG NEW DISTRICT, SHANGHAI TO: 200120 ROOM 703, NO.738, SHANGCHENG ROAD, PUDONG NEW DISTRICT, SHANGHAI |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20101224 Address after: 200120 room 738, 703 Shangcheng Road, Pudong New Area, Shanghai Patentee after: Shanghai Youhua System Integration Technology Co., Ltd. Address before: Sheng Kangliaoshi No. 738 building, 200120 Shanghai Pudong New Area Mall Road, room 701 Patentee before: Shanghai Jiuyuan Petrochemical Co., Ltd. |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100127 |