CN102661673B - Stripping water heat exchanger and process for aromatic device - Google Patents
Stripping water heat exchanger and process for aromatic device Download PDFInfo
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- CN102661673B CN102661673B CN201210163606.8A CN201210163606A CN102661673B CN 102661673 B CN102661673 B CN 102661673B CN 201210163606 A CN201210163606 A CN 201210163606A CN 102661673 B CN102661673 B CN 102661673B
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Abstract
The invention relates to the technical field of chemical industry, in particular to a stripping water heat exchanger and a process for an aromatic device. The stripping water heat exchanger is characterized in that a hot material feeding heat exchanger control mechanism which comprises a first tube section and a second tube section is arranged on the heat exchanger, so that heat exchange amount in the heat exchanger can be controlled, and the superheat degree of the stripping water at an outlet of the heat exchanger is reduced; meanwhile, if the heat exchanger fails, the heat exchanger can be isolated, and the whole extraction device is prevented from being shut down. By the process, the problem of leakage and thinning of tube bundles in the production process can be solved, the treatment capacity and consumption of the device are reduced, and an excellent heat exchange effect is achieved.
Description
technical field
The present invention relates to chemical technology field, specifically relate to aromatic device water stripping heat exchanger and technique thereof.
Background technology
It is more ripe that extraction process wraps in domestic generally application, although more domestic large-scale extractor meet the requirements according to design accounting, in application, equipment may produce the stress larger than design accounting and cause device damage.In overhaul of the equipments in the past, find that from pressure testing process leakage situation often appears in tube bank top, thereby have pit, fracture port phenomenon at tube side, cause extraction device to stop work.In addition, shell side middle and upper part can form evaporating space, forms moisture balance position and can be considered in evaporation interface.Enter at the bottom of shell side by flow process water, the generating steam that is finally heated is discharged shell side., there is phase transition process in the water generation steam bubble that is progressively heated.Steam bubble is further heated until evaporation interface breaks at uphill process, produces cavitation and steam and agitates and make to restrain single tube frequency vibration and rub and cause tube bank attenuate with deflection plate.Above problem all can affect heat-exchanger rig effect, and not only unit capacity and energy consumption increase but also maintenance cost significantly increases.
summary of the invention
The present invention is in order to make up above-mentioned technological deficiency, aromatic device water stripping heat exchanger and technique thereof are provided, this heat exchanger can be avoided tube bank leakage, attenuate problem in production process, and unit capacity and consumption are reduced, and realizes more excellent heat transfer effect.
Technical scheme of the present invention is: aromatic device water stripping heat exchanger and technique thereof, it is characterized in that aromatic device water stripping heat exchanger, it is characterized in that comprising: heat exchanger body, control valve control bypass, tube side inlet pipe line, tube side inlet valve, tube side outlet valve, tube side go out pipeline, shell side inlet valve, shell side outlet valve, recovery tower and non-aromatics tower bottom reboiler; Control valve control bypass connects water stripping heat exchanger tube pass inlet pipe line and tube side goes out pipeline, goes out on pipeline to be respectively equipped with tube side inlet valve and tube side outlet valve at tube side inlet pipe line and tube side, is provided with the second pipeline section simultaneously; Be provided with shell side inlet valve and shell side outlet valve at the heat exchanger body other end, tube side outlet valve is connected with recovery tower.
Described control valve control bypass is divided into the first pipeline section and the second pipeline section.
Its innovative point is: increased thermal material and entered heat exchanger controlling organization: the first pipeline section and the second pipeline section, can control the heat exchange amount in heat exchanger, and reduce the heat exchanger exit water stripping degree of superheat., if other problems fault appears in heat exchanger, heat exchanger can be isolated meanwhile, avoid the shut-down of whole extraction device.
Aromatic device water stripping heat exchanger, its process system and flow process are as follows:
Tube side flow process: lean solvent is provided after thermal source for non-aromatic tower by non-aromatics tower bottom reboiler, and the tube side inlet pipe line of flowing through enters heat exchanger body and water stripping is carried out heat exchange, lean solvent continues to enter extracting feed exchanger afterwards provides thermal source for extracting raw material.
Shell side flow process: water stripping is by non-aromatics destilling tower return tank water bag, recovery tower return tank water bag and newly fill into turbine water 1687Kg/h through the supercharging of stripping water pump, enters afterwards heat exchanger body and lean solvent heat exchange, at the bottom of stripped vapor enters recovery tower tower after heat exchange.
Described tube side inlet temperature is 152 ℃ of left and right, 129 ℃ of outlet temperatures.
Described shell side inlet temperature 30-35 ℃, 104 ℃ of outlet temperatures; The analysis of lean solvent pH value is 8.0 left and right, and the analysis of cold conditions water stripping pH value is 9.0-10.0.
Beneficial effect of the present invention is: aromatic device water stripping heat exchanger and technique thereof, this heat exchanger can be avoided tube bank leakage, attenuate problem in production process, and unit capacity and consumption are reduced, and realizes more excellent heat transfer effect.Can isolate online maintenance, the device of having avoided device local devices fault to cause stops simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of heat exchanger.
In figure, 1, heat exchanger body, 2, control valve control bypass, 3, tube side inlet pipe line, 4, tube side inlet valve, 5, tube side outlet valve, 6, tube side goes out pipeline, 7, shell side inlet valve, 8, shell side outlet valve, 9, recovery tower, 10, the first pipeline section, 11, the second pipeline section, 12, non-aromatics tower bottom reboiler.
The specific embodiment
Fig. 1 shows aromatic device water stripping heat exchanger schematic diagram, and its process system and flow process are as follows:
Tube side flow process: lean solvent is provided after thermal source for non-aromatic tower by non-aromatics tower bottom reboiler 12, the tube side inlet pipe line 3 of flowing through enters heat exchanger body 1 and carries out heat exchange with water stripping, and lean solvent continues to enter extracting feed exchanger afterwards provides thermal source for extracting raw material.
Shell side flow process: water stripping is by non-aromatics destilling tower return tank water bag, recovery tower return tank water bag and newly fill into turbine water 1687Kg/h through the supercharging of stripping water pump, enter afterwards heat exchanger body 1 and lean solvent heat exchange, at the bottom of stripped vapor enters recovery tower 9 towers after heat exchange.
Described tube side inlet temperature is 152 ℃ of left and right, 129 ℃ of outlet temperatures.
Described shell side inlet temperature 30-35 ℃, 104 ℃ of outlet temperatures; The analysis of lean solvent pH value is 8.0 left and right, and the analysis of cold conditions water stripping pH value is 9.0-10.0.
Claims (1)
1. aromatic device water stripping heat-exchanging process, it is characterized in that equipment aromatic device water stripping heat exchanger used, comprising: heat exchanger body, control valve control bypass, tube side inlet pipe line, tube side inlet valve, tube side outlet valve, tube side go out pipeline, shell side inlet valve, shell side outlet valve, recovery tower and non-aromatics tower bottom reboiler; Control valve control bypass connects water stripping heat exchanger tube pass inlet pipe line and tube side goes out pipeline, goes out on pipeline to be respectively equipped with tube side inlet valve and tube side outlet valve at tube side inlet pipe line and tube side, is provided with the second pipeline section simultaneously; Be provided with shell side inlet valve and shell side outlet valve at the heat exchanger body other end, shell side outlet valve is connected with recovery tower, meanwhile, goes out between pipeline, to be provided with the first pipeline section at shell side inlet pipe line and shell side; Process system and flow process are: tube side flow process: lean solvent is provided after thermal source for non-aromatic tower by non-aromatics tower bottom reboiler, the tube side inlet pipe line of flowing through enters heat exchanger body and water stripping is carried out heat exchange, and lean solvent continues to enter extracting feed exchanger afterwards provides thermal source for extracting raw material; Shell side flow process: water stripping is by non-aromatics destilling tower return tank water bag, recovery tower return tank water bag and newly fill into turbine water 1687Kg/h through the supercharging of stripping water pump, enters afterwards heat exchanger body and lean solvent heat exchange, at the bottom of stripped vapor enters recovery tower tower after heat exchange; Tube side inlet temperature is 152 ℃, 129 ℃ of outlet temperatures; Shell side inlet temperature 30-35 ℃, 104 ℃ of outlet temperatures; The analysis of lean solvent pH value is 8.0 left and right, and the analysis of cold conditions water stripping pH value is 9.0-10.0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210163606.8A CN102661673B (en) | 2012-05-24 | 2012-05-24 | Stripping water heat exchanger and process for aromatic device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210163606.8A CN102661673B (en) | 2012-05-24 | 2012-05-24 | Stripping water heat exchanger and process for aromatic device |
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| Publication Number | Publication Date |
|---|---|
| CN102661673A CN102661673A (en) | 2012-09-12 |
| CN102661673B true CN102661673B (en) | 2014-05-28 |
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| CN201210163606.8A Active CN102661673B (en) | 2012-05-24 | 2012-05-24 | Stripping water heat exchanger and process for aromatic device |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105240063B (en) * | 2015-10-24 | 2016-11-30 | 大连福佳·大化石油化工有限公司 | Dead steam recovery system |
| CN109458860A (en) * | 2018-12-08 | 2019-03-12 | 大连福佳·大化石油化工有限公司 | Extraction device heat exchanger improves structure |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101629791A (en) * | 2008-09-27 | 2010-01-20 | 何巨堂 | Shell-and-tube exchanger provided with shell-side short circuit inlet |
| CN201620134U (en) * | 2009-12-29 | 2010-11-03 | 上海九元石油化工有限公司 | Novel tower top heat exchange system of fractionating tower of aromatic hydrocarbon device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8008534B2 (en) * | 2008-06-30 | 2011-08-30 | Uop Llc | Liquid phase hydroprocessing with temperature management |
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- 2012-05-24 CN CN201210163606.8A patent/CN102661673B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101629791A (en) * | 2008-09-27 | 2010-01-20 | 何巨堂 | Shell-and-tube exchanger provided with shell-side short circuit inlet |
| CN201620134U (en) * | 2009-12-29 | 2010-11-03 | 上海九元石油化工有限公司 | Novel tower top heat exchange system of fractionating tower of aromatic hydrocarbon device |
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| CN102661673A (en) | 2012-09-12 |
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