CN201737903U - Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device - Google Patents
Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device Download PDFInfo
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- CN201737903U CN201737903U CN2010202077274U CN201020207727U CN201737903U CN 201737903 U CN201737903 U CN 201737903U CN 2010202077274 U CN2010202077274 U CN 2010202077274U CN 201020207727 U CN201020207727 U CN 201020207727U CN 201737903 U CN201737903 U CN 201737903U
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Abstract
The utility model relates to the fields of petroleum and chemical industry, in particular to a heat integration system of a distilling device, a reforming device and a gasoline and diesel hydrofining device, which takes diesel oil as a medium, and comprises the gasoline and diesel hydrofining device, the catalytic reforming device and the distilling device; the heat integration system is characterized in that the catalytic reforming device is internally and additionally provided with a heat exchanger unit; the gasoline and diesel hydrofining device is internally and additionally provided with another heat exchanger unit, a control valve and another control valve; and the distilling device is internally and additionally provided with a third heat exchanger unit and a fourth heat exchanger unit. Compared with the prior art, the heat integration system saves the low-pressure steam of a re-boiling heat source at the bottom of a fractionating tower of the catalytic reforming device or the fuel gas of a heating furnace, reduces the oil refining consumption of a reforming combination unit, reduces the oil refining cost, increases the temperature of crude oil electric desalting of the distilling device, and is beneficial to the operation of the distilling device; and when heat integration heat output is carried out, the heat integration system recovers the low-temperature heat, reduces the oil refining consumption of the gasoline and diesel hydrofining device and improves the economic benefit.
Description
[technical field]
The utility model relates to oil, chemical field, a kind of specifically attainable be medium with diesel oil, heat integration system between water distilling apparatus, reformer and the gasoline and diesel hydrogenation refining plant.
[technical background]
At present, the refinery water distilling apparatus take off preceding crude oil, take off back crude oil mostly and this device thermal source of water distilling apparatus carry out heat exchange; The separation column of reformer generally adopts low-pressure steam or process furnace fuel as thermal source; After refined diesel oil at the bottom of the gasoline and diesel hydrogenation refining plant separation column and the separation column charging heat exchange, advance follow-up cooling process.
Usually the taking off preceding crude oil, take off the heat that thermal source provided of back crude oil and insufficient of water distilling apparatus, it is on the low side to cause crude oil to advance the temperature of electric desalting, influences the operation of electric desalting; The separation column column bottom temperature of reformer is not high, adopts the mode heat supply of low-pressure steam or process furnace consume fuel, and the high-quality low usefulness of energy causes energy dissipation; The heat of the refined diesel oil at the bottom of the gasoline and diesel hydrogenation refining plant separation column is not rationally reclaimed and is utilized energy wastage simultaneously.Therefore need a kind of pattern of heat integration of water distilling apparatus, reformer and gasoline and diesel hydrogenation refining plant of practicality badly, rationally utilize the heat of refined diesel oil at the bottom of the gasoline and diesel hydrogenation refining plant separation column, come the cooperate optimization between implement device.
[summary of the invention]
The purpose of this utility model is in order to overcome the deficiencies in the prior art, with can principle, provide the heat integration system of water distilling apparatus, reformer and the hydrofining diesel oil device of heat that a kind of optimization utilizes refined diesel oil at the bottom of the gasoline and diesel hydrogenation refining plant separation column, energy efficient according to the science of " temperature counterpart; cascade utilization ".
For achieving the above object, the utility model has designed the heat integration system of a kind water distilling apparatus, reformer and gasoline and diesel hydrogenation refining plant, comprises the gasoline and diesel hydrogenation refining plant, catalytic reforming unit, water distilling apparatus is characterized in that: newly-increased heat exchanger package in the catalytic reforming unit; Newly-increased another heat exchanger package in the gasoline and diesel hydrogenation refining plant, control valve and another control valve; Newly-increased the 3rd heat exchanger package and the 4th heat exchanger package in the water distilling apparatus;
The shell import of newly-increased heat exchanger package in the pipe layer outlet that the import of described newly-increased control valve and outlet are connected interchanger in the gasoline and diesel hydrogenation refining plant respectively and the catalytic reforming unit, the import of another control valve is connected on the inlet ductwork of control valve, and outlet is connected with the import of air cooler in the gasoline and diesel hydrogenation refining plant; The pipe layer outlet of described another heat exchanger package is connected on the export pipeline of another control valve, the shell outlet of newly-increased the 4th heat exchanger package in pipe layer import and the water distilling apparatus;
The shell outlet of described newly-increased heat exchanger package connects newly-increased the 3rd heat exchanger package shell import in the water distilling apparatus, and the pipe layer upper outlet of newly-increased heat exchanger package is connected with at the bottom of the tower with the right entrance end of catalytic reforming unit separation column respectively with following outlet;
The shell outlet of described newly-increased the 3rd heat exchanger package connects the shell import of newly-increased the 4th heat exchanger package, and the import of pipe layer is connected the outlet of electrical desalter in the water distilling apparatus and the pipe layer import of interchanger respectively with outlet; The pipe layer import of described newly-increased the 4th heat exchanger package is connected the outlet of interchanger in the water distilling apparatus and the import of electrical desalter respectively with outlet.
Described newly-increased heat exchanger package, newly-increased another heat exchanger package, newly-increased the 3rd heat exchanger package, newly-increased the 4th heat exchanger package all have at least an interchanger to form.
The utility model is compared on the existing equipment basis with prior art, set up heat-exchange equipment, saved the fuel gas of boiling hot again source low-pressure steam at the bottom of the catalytic reforming unit separation column or process furnace, the refining energy consumption that reduces the reformation machinery, reduce the oil refining cost, increase economic efficiency; Promote the preceding crude oil of taking off of water distilling apparatus and advanced the temperature of electric desalting, the operation of favourable water distilling apparatus; In the heat integration thermal output, reclaimed low warmly, the refining energy consumption that reduces the gasoline and diesel hydrogenation refining plant reduces the oil refining cost, increases economic efficiency.
[description of drawings]
Fig. 1 is the connection diagram of existing water distilling apparatus, reformer and gasoline and diesel hydrogenation refining plant.
Fig. 2 is a connection diagram of the present utility model.
Referring to Fig. 1 and Fig. 2,1 is gasoline and diesel hydrogenation refined products separation column; 2 is interchanger; 3 is air cooler; 4 is water cooler; 5 is storage tank; 6 is the catalytic reforming unit separation column; 7 is interchanger; 8 is interchanger; 9 is electrical desalter; 10 is interchanger; 11 is heat exchanger package; 12 is the 3rd heat exchanger package; 13 is the 4th heat exchanger package; 14 is another heat exchanger package; 15 is control valve; 16 is another control valve; 17 is separation column; 18 is first branch road; 19 is second branch road; 20 is the 3rd branch road; 21 is the 4th branch road.
[embodiment]
The utility model is described in further detail below in conjunction with accompanying drawing, and the utility model is still more clearly for the people of this professional skill field.
The connection diagram of existing water distilling apparatus, reformer and gasoline and diesel hydrogenation refining plant.
The temperature that gasoline and diesel hydrogenation refined products separation column 1 comes out is T
3Refined diesel oil, through interchanger 2, with temperature be T
1The charging heat exchange of gasoline and diesel hydrogenation refined products separation column 1 to T
4, advance air cooler 3 and be cooled to T
5, water inlet cooler 4 is cooled to 40～60 ℃, goes out device to storage tank 5; Here refined diesel oil is by T
4Directly be cooled to 40～60 ℃, cause the partial heat energy of refined diesel oil to be underutilized.
The catalytic reforming unit processing medium that boils again comes out at the bottom of catalytic reforming unit separation column 6 towers, and temperature is T
6, behind interchanger 7 heat-obtainings, temperature rise is to T
7Return catalytic reforming unit separation column 6; The thermal source of interchanger 7 is low-pressure steam or process furnace fuel normally.
Temperature is T
8Take off before crude oil enter water distilling apparatus from the tank field, be divided into first 18 and second branch road 19, separately with the heat exchange of this device endogenous pyrogen; Crude oil is after interchanger 8 and the heat exchange of this device endogenous pyrogen before the taking off of first branch road 18 wherein, and merges with crude oil before the taking off after 19 heat exchange of second branch road, and taking off preceding crude oil temperature after the merging is T
9, advance electrical desalter 9.From electrical desalter 9 come out take off the back crude oil temperature be T
10, be divided into the 3rd branch road 20 and and the 4th branch road 21, each branch road and the heat exchange of this device endogenous pyrogen; The 3rd branch road 20 wherein take off back crude oil after interchanger 10 and the heat exchange of this device endogenous pyrogen, merge with the back crude oil that takes off after other the 4th branch road 21 heat exchange, taking off preceding crude oil temperature after the merging is T
11, advance separation column 17.
Usually the taking off preceding crude oil, take off the heat that thermal source provided of back crude oil and insufficient of water distilling apparatus, it is on the low side to cause crude oil to advance the temperature of electric desalting, influences the operation of electric desalting 9; Catalytic reforming unit separation column 6 column bottom temperatures are not high, adopt the mode heat supply of low-pressure steam or process furnace consume fuel, and the high-quality low usefulness of energy causes energy dissipation; The heat of the refined diesel oil at the bottom of the gasoline and diesel hydrogenation refining plant separation column is not rationally reclaimed and is utilized energy wastage simultaneously.
Fig. 2 is a connection diagram of the present utility model.
The utility model is increasing heat exchanger package 11 newly in catalytic reforming unit on the prior art; Newly-increased another heat exchanger package 14 in the gasoline and diesel hydrogenation refining plant, control valve 15 and another control valve 16; Newly-increased the 3rd heat exchanger package 12 and the 4th heat exchanger package 13 in the water distilling apparatus.
Increase the shell import of heat exchanger package 11 in the pipe layer outlet that the import of newly-increased control valve 15 and outlet are connected interchanger 2 in the gasoline and diesel hydrogenation refining plant respectively and the catalytic reforming unit newly, the import of another control valve 16 is connected on the inlet ductwork of control valve 15, and outlet is connected with the import of air cooler 3 in the gasoline and diesel hydrogenation refining plant; The pipe layer outlet of another heat exchanger package 14 is connected on the export pipeline of another control valve 16, the shell outlet of newly-increased the 4th heat exchanger package 13 in pipe layer import and the water distilling apparatus.
The shell of newly-increased heat exchanger package 11 exports and connects newly-increased the 3rd heat exchanger package 12 shell imports in the water distilling apparatus, and the pipe layer upper outlet of newly-increased heat exchanger package 11 is connected with at the bottom of the tower with the right entrance end of catalytic reforming unit separation column 6 respectively with exporting down.
The shell outlet of newly-increased the 3rd heat exchanger package 12 connects the shell import of newly-increased the 4th heat exchanger package 13, and the import of pipe layer is connected the outlet of electrical desalter 9 in the water distilling apparatus and the pipe layer import of interchanger 10 respectively with outlet; The pipe layer import of newly-increased the 4th heat exchanger package 13 is connected the outlet of interchanger 8 in the water distilling apparatus and the import of electrical desalter 9 respectively with outlet.
Refined diesel oil temperature T with the gasoline and diesel hydrogenation refining plant
aBe 190 ℃～210 ℃ and cause at the bottom of the interior rectifying tower of reformer column bottom temperature T
6Be 130 ℃～160 ℃, the heat of refined diesel oil substitutes thermal source---low-pressure steam or the process furnace fuel at the bottom of catalytic reforming unit separation column 6 towers.The refined diesel oil temperature drop is to temperature T
cIt is 170 ℃～190 ℃; Again refined diesel oil is caused water distilling apparatus, earlier with take off back crude oil temperature T
10' be 110 ℃～120 ℃ and carry out the heat exchange first time that the refined diesel oil temperature drop is to temperature T
eBe 140 ℃～160 ℃, again with take off before crude oil temperature T
12Be 70 ℃～90 ℃ and carry out heat exchange that the crude oil heat exchange is to temperature T before will taking off
9' be 110 ℃～120 ℃, refined diesel oil self temperature drop is to temperature T
fIt is 120 ℃～140 ℃; Refined diesel oil is returned the gasoline and diesel hydrogenation refining plant, through newly-increased interchanger 14 and low-temperature water heating heat exchange, recovery is low warm again, and temperature drop is to T
4Be 50 ℃～100 ℃ and enter the follow-up air cooling and the process for cooling of water-cooled again, be cooled to 40～60 ℃.Energy is fully used, and has realized heat integration.
Saved the fuel gas of boiling hot again source low-pressure steam at the bottom of catalytic reforming unit fractionation 6 towers or process furnace with crossing this device, the refining energy consumption that reduces the reformation machinery reduces the oil refining cost, increases economic efficiency; Promote the preceding crude oil of taking off of water distilling apparatus and advanced the temperature of electric desalting, the operation of favourable water distilling apparatus; In the heat integration thermal output, reclaimed low warmly, the refining energy consumption that reduces the gasoline and diesel hydrogenation refining plant reduces the oil refining cost, increases economic efficiency.
Claims (2)
1. the heat integration system of a water distilling apparatus, reformer and gasoline and diesel hydrogenation refining plant comprises the gasoline and diesel hydrogenation refining plant, catalytic reforming unit, and water distilling apparatus is characterized in that: newly-increased heat exchanger package (11) in the catalytic reforming unit; Newly-increased another heat exchanger package (14) in the gasoline and diesel hydrogenation refining plant, control valve (15) and another control valve (16); Newly-increased the 3rd heat exchanger package (12) and the 4th heat exchanger package (13) in the water distilling apparatus;
The shell import of newly-increased heat exchanger package (11) in the pipe layer outlet that the import of described newly-increased control valve (15) and outlet are connected interchanger in the gasoline and diesel hydrogenation refining plant (2) respectively and the catalytic reforming unit, the import of another control valve (16) is connected on the inlet ductwork of control valve (15), and outlet is connected with the import of air cooler (3) in the gasoline and diesel hydrogenation refining plant; The pipe layer outlet of described another heat exchanger package (14) is connected on the export pipeline of another control valve (16), the shell outlet of newly-increased the 4th heat exchanger package (13) in pipe layer import and the water distilling apparatus;
The shell outlet of described newly-increased heat exchanger package (11) connects newly-increased the 3rd heat exchanger package (12) shell import in the water distilling apparatus, and the pipe layer upper outlet of newly-increased heat exchanger package (11) is connected with at the bottom of the tower with the right entrance end of catalytic reforming unit separation column (6) respectively with following outlet;
The shell outlet of described newly-increased the 3rd heat exchanger package (12) connects the shell import of newly-increased the 4th heat exchanger package (13), and the import of pipe layer is connected the outlet of electrical desalter in the water distilling apparatus (9) and the pipe layer import of interchanger (10) respectively with outlet; The pipe layer import of described newly-increased the 4th heat exchanger package (13) is connected the outlet of interchanger in the water distilling apparatus (8) and the import of electrical desalter (9) respectively with outlet.
2. the heat integration system of a kind of water distilling apparatus according to claim 1, reformer and gasoline and diesel hydrogenation refining plant is characterized in that: described newly-increased heat exchanger package (11), newly-increased another heat exchanger package (14), newly-increased the 3rd heat exchanger package (12), newly-increased the 4th heat exchanger package (15) all have at least an interchanger to form.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202077274U CN201737903U (en) | 2010-05-27 | 2010-05-27 | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202077274U CN201737903U (en) | 2010-05-27 | 2010-05-27 | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201737903U true CN201737903U (en) | 2011-02-09 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202077274U Expired - Fee Related CN201737903U (en) | 2010-05-27 | 2010-05-27 | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device |
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| CN (1) | CN201737903U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103363295A (en) * | 2012-04-09 | 2013-10-23 | 中国石油化工股份有限公司 | Process product diesel hot feeding method |
| CN103421542A (en) * | 2013-08-08 | 2013-12-04 | 华南理工大学 | Diesel hydrogenation process |
| CN106635155A (en) * | 2016-11-03 | 2017-05-10 | 兰州兰石集团有限公司 | Efficient-residual-heat-utilization system for light-fraction conversion of coal tar and method |
| CN112280589A (en) * | 2020-09-04 | 2021-01-29 | 雷泽永 | Catalysis-atmospheric and vacuum distillation-hydrogenation heat combination device |
| CN112745954A (en) * | 2015-08-24 | 2021-05-04 | 沙特阿拉伯石油公司 | Recovery and reuse of waste energy in industrial plants |
-
2010
- 2010-05-27 CN CN2010202077274U patent/CN201737903U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103363295A (en) * | 2012-04-09 | 2013-10-23 | 中国石油化工股份有限公司 | Process product diesel hot feeding method |
| CN103363295B (en) * | 2012-04-09 | 2015-09-23 | 中国石油化工股份有限公司 | The hot method of feeding of a kind of process product diesel oil |
| CN103421542A (en) * | 2013-08-08 | 2013-12-04 | 华南理工大学 | Diesel hydrogenation process |
| CN112745954A (en) * | 2015-08-24 | 2021-05-04 | 沙特阿拉伯石油公司 | Recovery and reuse of waste energy in industrial plants |
| CN106635155A (en) * | 2016-11-03 | 2017-05-10 | 兰州兰石集团有限公司 | Efficient-residual-heat-utilization system for light-fraction conversion of coal tar and method |
| CN112280589A (en) * | 2020-09-04 | 2021-01-29 | 雷泽永 | Catalysis-atmospheric and vacuum distillation-hydrogenation heat combination device |
| CN112280589B (en) * | 2020-09-04 | 2023-08-04 | 雷泽永 | Catalytic-atmospheric-vacuum-hydrogenation heat combination device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20110209 Termination date: 20150527 |
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| EXPY | Termination of patent right or utility model |