CN205528608U - White oil initial boiling point lift system - Google Patents
White oil initial boiling point lift system Download PDFInfo
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- CN205528608U CN205528608U CN201620139405.8U CN201620139405U CN205528608U CN 205528608 U CN205528608 U CN 205528608U CN 201620139405 U CN201620139405 U CN 201620139405U CN 205528608 U CN205528608 U CN 205528608U
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- white oil
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- initial boiling
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Abstract
The utility model discloses a white oil initial boiling point lift system, including fractionating tower and strip tower, the middle section of fractionating tower is equipped with backflow pipeline, last backwash pump and the heat exchanger of being equipped with in proper order of backflow pipeline, the fractionating tower through white oil output pipeline with the strip tower is linked together, backflow pipeline is divided into two way backflow pipeline behind the backwash pump, wherein backflow pipeline connects back the fractionating tower along former backflow pipeline through heat exchanger all the way, and another way backflow pipeline inserts white oil output pipeline. This system can effectively promote the initial boiling point of white oil, and the gained white oil does not have kerosene flavor, is worth higherly relatively.
Description
Technical field
This utility model belongs to hydrocracking technology field, is specifically related to a kind of white oil initial boiling point and promotes system.
Background technology
As shown in fig. 1, in prior art after hydrocracking unit product out is fractionated into tower 1 fractional distillation, 5# technical white oil is extracted out from n-th layer tower tray, go to diesel oil side stripper 2, stage casing backflow is extracted out from the n-th+2 layers tower tray of fractionating column 1, after reflux pump 4 and heat exchanger 5 heat exchange, (n-1)th layer of tower tray of fractionating column 1 it is back to by reflux line 3, so design, owing to being affected by fractionating column fractional distillation precision, the initial boiling point of the 5# white oil material of test manufacture can only achieve about 208 DEG C, and have kerosene taste, the initial boiling point required from high quality white oil plant and technical white oil has bigger gap, only as ordinary diesel oil or white oil material use at a low price.
Utility model content
The purpose of this utility model is to provide a kind of white oil initial boiling point to promote system, and this system can effectively promote the initial boiling point of white oil, and gained white oil is without kerosene taste, is worth of a relatively high.
Above-mentioned purpose of the present utility model is achieved through the following technical solutions: a kind of white oil initial boiling point promotes system, including fractionating column and stripper, the stage casing of described fractionating column is provided with reflux line, reflux pump and heat exchanger it is sequentially provided with on described reflux line, described fractionating column is connected with described stripper by white oil output channel, described reflux line is divided into two-way reflux line after reflux pump, wherein a road reflux line takes back fractionating column along former reflux line through heat exchanger, and another road reflux line accesses white oil output channel.
Further, described white oil output channel includes white oil output main pipeline and the white oil output bypass line separated from white oil output main pipeline, the two ends of described white oil output bypass line are connected with described white oil output main pipeline, described white oil output bypass line is provided with multiple stop valve, described white oil output main pipeline is provided with charging regulation valve, and described charging regulation valve is positioned on the white oil output main pipeline corresponding with described white oil output bypass line.
Another road reflux line described and the access point of described white oil output channel are on the white oil output main pipeline corresponding with described white oil output bypass line, and before being positioned at described charging regulation valve.
Wherein a road reflux line accesses the entrance of described fractionating column the (n-1)th floor tower tray successively along former reflux line from the outlet of described fractionating column the n-th+2 floor tower tray through reflux pump and heat exchanger.
So design reflux line, vapour in tower, liquid phase load can be made to be evenly distributed, take out reflux heat from bottom high temperature position simultaneously, can more reasonably utilize backflow heat.
Described fractionating column n-th layer tower tray is distillated mouth and is connected by the charging aperture of white oil output channel with described stripper.
When reflux line is divided into two-way after reflux pump, need to close stop valve, so that the white oil at fractionating column n-th layer column plate cannot be delivered in stripper, open charging regulation valve simultaneously, make the part white oil in the backflow of stage casing flow in stripper charging aperture via reflux pump and another road reflux line, thus promote the initial boiling point of white oil.
This utility model has the advantage that this system is by before reflux pump adapter line to stripper charging regulation valve, stripper is introduced in part stage casing backflow (260 DEG C), improve the end temperature of stripper, improve 5# white oil material initial boiling point to more than 250 DEG C, and gained white oil is without kerosene taste, it is worth of a relatively high.
Accompanying drawing explanation
Fig. 1 is white oil output system schematic in prior art；
Fig. 2 is that in detailed description of the invention, white oil initial boiling point promotes system schematic.
Detailed description of the invention
Embodiment
1
As shown in Figure 2, a kind of white oil initial boiling point promotes system, including fractionating column 1 and stripper 2, the stage casing of fractionating column 1 is provided with reflux line 3, being sequentially provided with reflux pump 4 and heat exchanger 5 on reflux line 3, fractionating column 1 is connected with stripper 2 by white oil output channel 6, and reflux line 3 is divided into two-way reflux line after reflux pump 4, wherein a road reflux line 31 takes back fractionating column 1 along former reflux line through heat exchanger 5, and another road reflux line 32 accesses white oil output channel 6.
White oil output channel 6 includes white oil output main pipeline 61 and the white oil output bypass line 62 separated from white oil output main pipeline 61, the two ends of white oil output bypass line 62 are connected with white oil output main pipeline 61, white oil output bypass line is provided with multiple stop valve 63, white oil output main pipeline is provided with charging regulation valve 64, and charging regulation valve 64 is positioned on the white oil output main pipeline 61 corresponding with white oil output bypass line 62.
Another road reflux line 32 and the access point of white oil output channel 6 are on the white oil output main pipeline 61 corresponding with white oil output bypass line 62, and before being positioned at charging regulation valve 64.
Wherein a road reflux line 31 accesses the entrance of fractionating column 1 (n-1)th floor tower tray successively along former reflux line from the outlet of fractionating column 1 n-th+2 floor tower tray through reflux pump 4 and heat exchanger 5.
Fractionating column 1 n-th layer tower tray is distillated mouth and is connected by the charging aperture of white oil output channel 6 with stripper 2.
Before transformation, 5# white oil material is because there being kerosene taste, and owing to being affected by fractionating column fractional distillation precision, the initial boiling point of the 5# white oil material of test manufacture can only achieve about 208 DEG C, initial boiling point from high quality white oil plant and technical white oil requirement is not less than 260 DEG C bigger gap, can only do ordinary diesel oil or low price white oil material.
In order to promote the initial boiling point of white oil, this utility model is by above-mentioned improvement, originally evaporated the stop valve 63 exporting to stripper from the n-th layer tower tray of fractionating column 1 by closedown, reflux line 3 is divided into two-way after reflux pump 4, wherein a former reflux line of curb takes back fractionating column 1 through heat exchanger 5, and white oil output channel 6 is accessed on another road, and stripper 2 is introduced in part stage casing backflow (260 DEG C), improve the end temperature of stripper 2, white oil initial boiling point can be improved to more than 250 DEG C.
Improved 5# technical white oil is 1450 yuan/ton with the price difference of ordinary diesel oil, can produce 5# white oil material 17t/h, the highest profit that increases: 1450 × 17 × 24 × 30/10000=1774.8 ten thousand yuan after transformation.
Therefore, by the lifting system in applying this reality new, 2# adds the 5# technical white oil initial boiling point that cracking produces and improves to 250 DEG C, and kerosene taste significantly reduces, and has reached the standard of qualified 5# technical white oil.Add profit simultaneously.
Finally it should be noted that; above content is only a kind of detailed description of the invention of the present utility model; should not become the restriction to this utility model protection domain; those of ordinary skill in the art is in the case of without departing from the essence of technical solutions of the utility model; to the various simple deformation done by this utility model or equivalent, all should fall in protection domain of the present utility model.
Claims (5)
1. a white oil initial boiling point promotes system, including fractionating column and stripper, the stage casing of described fractionating column is provided with reflux line, reflux pump and heat exchanger it is sequentially provided with on described reflux line, described fractionating column is connected with described stripper by white oil output channel, it is characterized in that: described reflux line is divided into two-way reflux line after reflux pump, and wherein a road reflux line takes back fractionating column along former reflux line through heat exchanger, another road reflux line accesses white oil output channel.
White oil initial boiling point the most according to claim 1 promotes system, it is characterized in that: described white oil output channel includes white oil output main pipeline and the white oil output bypass line separated from white oil output main pipeline, the two ends of described white oil output bypass line are connected with described white oil output main pipeline, described white oil output bypass line is provided with multiple stop valve, described white oil output main pipeline is provided with charging regulation valve, and described charging regulation valve is positioned on the white oil output main pipeline corresponding with described white oil output bypass line.
White oil initial boiling point the most according to claim 2 promotes system, it is characterized in that: another road reflux line described and the access point of described white oil output channel are on the white oil output main pipeline corresponding with described white oil output bypass line, and before being positioned at described charging regulation valve.
4. promote system according to the white oil initial boiling point described in any one of claim 1-3, it is characterized in that: wherein a road reflux line accesses the entrance of described fractionating column the (n-1)th floor tower tray successively along former reflux line from the outlet of described fractionating column the n-th+2 floor tower tray through reflux pump and heat exchanger.
White oil initial boiling point the most according to claim 4 promotes system, it is characterized in that: described fractionating column n-th layer tower tray is distillated mouth and is connected by the charging aperture of white oil output channel with described stripper.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620139405.8U CN205528608U (en) | 2016-02-25 | 2016-02-25 | White oil initial boiling point lift system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620139405.8U CN205528608U (en) | 2016-02-25 | 2016-02-25 | White oil initial boiling point lift system |
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| Publication Number | Publication Date |
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| CN205528608U true CN205528608U (en) | 2016-08-31 |
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| CN201620139405.8U Active CN205528608U (en) | 2016-02-25 | 2016-02-25 | White oil initial boiling point lift system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108913203A (en) * | 2018-06-15 | 2018-11-30 | 中国石油化工股份有限公司 | A kind of production technology of-No. 10 military diesels and 5# technical white oil |
-
2016
- 2016-02-25 CN CN201620139405.8U patent/CN205528608U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108913203A (en) * | 2018-06-15 | 2018-11-30 | 中国石油化工股份有限公司 | A kind of production technology of-No. 10 military diesels and 5# technical white oil |
| CN108913203B (en) * | 2018-06-15 | 2022-07-26 | 中国石油化工股份有限公司 | Production process of No. 10 military diesel oil and No. 5 industrial white oil |
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