CN205170706U - Alkanisation result separator - Google Patents
Alkanisation result separator Download PDFInfo
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- CN205170706U CN205170706U CN201520638576.0U CN201520638576U CN205170706U CN 205170706 U CN205170706 U CN 205170706U CN 201520638576 U CN201520638576 U CN 201520638576U CN 205170706 U CN205170706 U CN 205170706U
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Abstract
The utility model discloses an alkanisation result separator, including the debutanizing tower, the butane splitter, first top of the tower oil production port, oil production port at the bottom of the first tower, oil production port at the bottom of second top of the tower oil production port and the second tower, a serial communication port, still include alkylate oil production port, butane oil production port with take out the light oil mouth, through oil production port discharge heavy oil impurity at the bottom of the first tower and adjust alkylate oil production port and the position and the extraction volume of taking out the light oil mouth, control access to normal butane content among the mixtures of butane splitter feed inlet, reduce the operation load of butane splitter, oil production port obtains isobutane and normal butane product respectively at the bottom of second top of the tower oil production port and second tower. The utility model discloses beneficial effect does: in the operation that by a wide margin reduces butane splitter load and separation cost, obtain purity and be greater than the isobutane product that 97% normal butane and purity are greater than 87% to reach the alkylate that the octane number is greater than 93.
Description
Technical field
The utility model relates to alkylate oil and generates equipment de-sign field, particularly relates to a kind of alkylate oil tripping device comprising debutanizing tower and butane splitter.
Background technology
At present, the production technique of domestic alkylate oil based on liquid acid Catalytic processes, mainly sulphuric acid catalysis Technology.The alkylated reaction raw material of low-carbon alkene and Trimethylmethane mostly is C4 mixture, mainly comprise 1-butylene, 2-butylene, normal butane and Trimethylmethane, raw material and concentrated sulfuric acid catalyst are through to react and after deacidification system, except containing except alkylate oil product in the alkylate obtained, also comprise a large amount of normal butanes and Trimethylmethane, alkylate need be processed through debutanizing tower and butane splitter, alkylate oil product is obtained after being separated, be separated simultaneously and obtain normal butane and Trimethylmethane, Trimethylmethane can directly use as reaction raw materials, the concentration of recycle isobutane in reactive system can be improved, avoid the accumulation of normal butane in reactive system simultaneously.
In prior art, debutanizing tower only has two extraction mouths usually, obtains alkylate oil product at the bottom of tower, tower top isolates the mixture of normal butane and Trimethylmethane, again normal butane and Trimethylmethane are delivered to butane splitter to be separated, tower top obtains Trimethylmethane product, obtains normal butane product at the bottom of tower.
Because octane-iso has higher octane value, in alkylate oil product, C8 component concentration is higher, the octane value of alkylate oil product is higher, but occur owing to being attended by the side reaction such as disproportionation, polymerization in alkylation process simultaneously, can produce a small amount of containing the light oil of C6, C7 component and be greater than the heavy oil of C8 component, the content of light oil and heavy oil too much will have a strong impact on the octane value of alkylate oil product.
Enter the normal butane in butane splitter and Trimethylmethane mixture simultaneously, because Trimethylmethane content is higher, want separation and obtain high purity normal butane product, the operational load of butane splitter is larger, required theoretical plate number is more, causes product separation cost higher.
Utility model content
In order to effectively solve the problems of the technologies described above, the utility model provides a kind of alkylate tripping device, while obtaining high-octane alkylation products, also reduces separation costs.
For providing above-mentioned functions, the alkylate tripping device that the utility model provides, comprise debutanizing tower and butane splitter, described debutanizing tower is provided with extraction mouth at the bottom of the first overhead extraction mouth and the first tower, described butane splitter is provided with extraction mouth at the bottom of the second overhead extraction mouth and the second tower, wherein: described debutanizing tower is also provided with multiple side take-off mouth, described side take-off mouth comprises alkylate oil extraction mouth, take out light oil mouth and butane extraction mouth, described butane splitter is provided with butane splitter opening for feed, described butane extraction mouth is connected with butane splitter opening for feed.
Above-mentioned first overhead extraction mouth is used for extraction Trimethylmethane product, and extraction mouth at the bottom of the first tower is for discharging heavy oil impurity;
Normal butane and the Trimethylmethane mixture of the extraction of butane extraction mouth are delivered to butane splitter by butane splitter opening for feed;
Second overhead extraction mouth is used for extraction Trimethylmethane product, and extraction mouth at the bottom of the second tower is used for extraction normal butane product.
As the preferred implementation of alkylate tripping device described in the utility model, described alkylate oil extraction mouth is one or more.
As the preferred implementation of alkylate tripping device described in the utility model, described in take out light oil mouth be one or more.
As the preferred implementation of alkylate tripping device described in the utility model, described butane extraction mouth is one or more.
As the preferred implementation of alkylate tripping device described in the utility model, described alkylate oil extraction mouth is positioned at side line bottom debutanizing tower, takes out light oil mouth and is positioned at side line in the middle part of debutanizing tower, and butane extraction mouth is positioned at debutanizing tower top side line.
As the preferred implementation of alkylate tripping device described in the utility model, described debutanizing tower and butane splitter all have 100 layers of tower tray, described alkylate oil extraction mouth is positioned at 83,95,99 layers of tower tray, described light oil mouth of taking out is positioned at 49,52 layers of tower tray, and described butane extraction mouth is positioned at 33,39 layers of tower tray.
Outlet position adopted by the alkylate oil of adjustable debutanizing tower, obtains the alkylation products with higher octane.
Discharged in time by the heavy oil taken out the light oil containing C6, C7 component that side reaction generates by extraction mouth at the bottom of light oil mouth and the first tower and be greater than C8 component of debutanizing tower, improve the octane value of alkylate oil product further.
Trimethylmethane product can be used as reaction raw materials and recycles, the recycle isobutane concentration in augmenting response system, effectively prevent the accumulation of normal butane in reactive system.
Alkylate tripping device disclosed in the utility model, by the butane side take-off mouth extraction normal butane of debutanizing tower and the mixture of Trimethylmethane, adjustment butane adopts outlet position, the mixture controlling extraction is a large amount of normal butanes and a small amount of Trimethylmethane, again normal butane is delivered to butane splitter with the mixture of Trimethylmethane to be separated, significantly can reduce the operational load of butane splitter, obtain normal butane and the purity Trimethylmethane product that is greater than 87% that purity is greater than 97% simultaneously, in addition, alkylate oil octane value is greater than 93.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of alkylate tripping device of the utility model.
In figure: 1-debutanizing tower; 2-butane splitter; 3-first overhead extraction mouth; Extraction mouth at the bottom of 4-first tower; 5-alkylate oil extraction mouth; 6-takes out light oil mouth; 7-butane extraction mouth; 8-butane splitter opening for feed; 9-second overhead extraction mouth; Extraction mouth at the bottom of 10-second tower.
Embodiment
Embodiment of the present utility model is further illustrated below in conjunction with accompanying drawing.
As shown in Figure 1, it is the structural representation of a kind of alkylate tripping device of the utility model, comprise debutanizing tower (1) and butane splitter (2), debutanizing tower (1) is provided with extraction mouth (4) at the bottom of the first overhead extraction mouth (3) and the first tower, butane splitter (2) is provided with extraction mouth (10) at the bottom of the second overhead extraction mouth (9) and the second tower, wherein: debutanizing tower (1) is also provided with alkylate oil extraction mouth (5), take out light oil mouth (6) and butane extraction mouth (7), butane splitter (2) is provided with butane splitter opening for feed (8), butane extraction mouth (7) is connected with butane splitter opening for feed (8).
First overhead extraction mouth (3) is for extraction Trimethylmethane product, and extraction mouth (4) at the bottom of the first tower is for discharging heavy oil impurity;
The normal butane of butane extraction mouth (7) extraction and Trimethylmethane mixture are delivered to butane splitter (2) by butane splitter opening for feed (8);
Second overhead extraction mouth (9) is for extraction Trimethylmethane product, and extraction mouth (10) at the bottom of the second tower is for extraction normal butane product.
Alkylate oil extraction mouth (5) is positioned at debutanizing tower (1) bottom side line, take out light oil mouth (6) and be positioned at debutanizing tower (1) middle part side line, butane extraction mouth (7) is positioned at debutanizing tower (1) top side line.
Alkylate is after tripping device is separated, and the Trimethylmethane product purity obtained is greater than 87%, and normal butane product purity is greater than 97%, and alkylate oil octane value is greater than 93.
Embodiment 1
A kind of alkylate tripping device, debutanizing tower (1) and butane splitter (2) all have 100 layers of tower tray, first overhead extraction mouth (3) extraction Trimethylmethane product, extraction mouth (4) at the bottom of first tower discharges heavy oil impurity, alkylate oil extraction mouth (5) is positioned at 83 layers of tower tray, butane is adopted mouth (7) and is positioned at 33 layers of tower tray, take out light oil mouth (6) and be positioned at 49 layers of tower tray, the normal butane of butane extraction mouth (7) extraction and Trimethylmethane mixture are delivered to butane splitter (2) be separated, second overhead extraction mouth (9) extraction Trimethylmethane product, extraction mouth (10) extraction normal butane product at the bottom of second tower, final isolated Trimethylmethane product purity is 89%, normal butane product purity is 97.3%, alkylate oil octane value is 94.
Embodiment 2
A kind of alkylate tripping device, debutanizing tower (1) and butane splitter (2) all have 100 layers of tower tray, first overhead extraction mouth (3) extraction Trimethylmethane product, extraction mouth (4) at the bottom of first tower discharges heavy oil impurity, alkylate oil extraction mouth (5) is positioned at 95 layers of tower tray, butane is adopted mouth (7) and is positioned at 39 layers of tower tray, take out light oil mouth (6) and be positioned at 52 layers of tower tray, the Trimethylmethane product purity that final separation obtains is 91%, normal butane product purity is 98%, and alkylate oil octane value is 97.
Above disclosedly be only a kind of preferred embodiment of the utility model, certainly can not limit the interest field of the utility model with this, therefore according to the equivalent variations that the utility model claim is done, still belong to the scope that the utility model is contained.
Claims (6)
1. an alkylate tripping device, comprise debutanizing tower (1) and butane splitter (2), described debutanizing tower (1) is provided with extraction mouth (4) at the bottom of the first overhead extraction mouth (3) and the first tower, described butane splitter (2) is provided with extraction mouth (10) at the bottom of the second overhead extraction mouth (9) and the second tower, it is characterized in that: described debutanizing tower (1) is also provided with multiple side take-off mouth, described side take-off mouth comprises alkylate oil extraction mouth (5), take out light oil mouth (6) and butane extraction mouth (7), described butane splitter (2) is provided with butane splitter opening for feed (8), described butane extraction mouth (7) is connected with butane splitter opening for feed (8).
2. alkylate tripping device as claimed in claim 1, it is characterized in that, described alkylate oil extraction mouth (5) is for one or more.
3. alkylate tripping device as claimed in claim 1, is characterized in that, described in take out light oil mouth (6) for one or more.
4. alkylate tripping device as claimed in claim 1, it is characterized in that, described butane extraction mouth (7) is for one or more.
5. alkylate tripping device as claimed in claim 1, it is characterized in that, described alkylate oil extraction mouth (5) is positioned at debutanizing tower (1) bottom side line, take out light oil mouth (6) and be positioned at debutanizing tower (1) middle part side line, butane extraction mouth (7) is positioned at debutanizing tower (1) top side line.
6. alkylate tripping device as claimed in claim 5, it is characterized in that, described debutanizing tower (1) and butane splitter (2) all have 100 layers of tower tray, described alkylate oil extraction mouth (5) is positioned at 83,95,99 layers of tower tray, described light oil mouth (6) of taking out is positioned at 49,52 layers of tower tray, and described butane extraction mouth (7) is positioned at 33,39 layers of tower tray.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520638576.0U CN205170706U (en) | 2015-08-21 | 2015-08-21 | Alkanisation result separator |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520638576.0U CN205170706U (en) | 2015-08-21 | 2015-08-21 | Alkanisation result separator |
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| CN205170706U true CN205170706U (en) | 2016-04-20 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108211405A (en) * | 2016-12-21 | 2018-06-29 | 中国石油化工股份有限公司 | Alkylated reaction device and alkylated reaction separation method |
| CN113563917A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for sulfuric acid alkylation reaction product |
| CN113563916A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for alkylation reaction product |
| CN115317945A (en) * | 2021-08-23 | 2022-11-11 | 中国石油化工股份有限公司 | Alkylation reaction product two-tower thermal coupling and heat pump combined separation process and separation device |
-
2015
- 2015-08-21 CN CN201520638576.0U patent/CN205170706U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108211405A (en) * | 2016-12-21 | 2018-06-29 | 中国石油化工股份有限公司 | Alkylated reaction device and alkylated reaction separation method |
| CN108211405B (en) * | 2016-12-21 | 2024-03-12 | 中国石油化工股份有限公司 | Alkylation reaction device and alkylation reaction separation method |
| CN113563917A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for sulfuric acid alkylation reaction product |
| CN113563916A (en) * | 2021-08-23 | 2021-10-29 | 中国石油化工股份有限公司 | Separation process and separation device for alkylation reaction product |
| CN115317945A (en) * | 2021-08-23 | 2022-11-11 | 中国石油化工股份有限公司 | Alkylation reaction product two-tower thermal coupling and heat pump combined separation process and separation device |
| CN115317945B (en) * | 2021-08-23 | 2024-04-19 | 中国石油化工股份有限公司 | Two-tower thermal coupling and heat pump combined separation process and separation device for alkylation reaction product |
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