CN1030250A - Improve the method for fraction oil reclaim rate of petroleum vacuum distillation - Google Patents
Improve the method for fraction oil reclaim rate of petroleum vacuum distillation Download PDFInfo
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- CN1030250A CN1030250A CN 87101902 CN87101902A CN1030250A CN 1030250 A CN1030250 A CN 1030250A CN 87101902 CN87101902 CN 87101902 CN 87101902 A CN87101902 A CN 87101902A CN 1030250 A CN1030250 A CN 1030250A
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- additive
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Abstract
The invention belongs to the improvement of oil vacuum distillation method.It is with the catalytic cracking that contains aromatic hydrocarbons more than 350 ℃ fraction oil in the vacuum distillation tower charging, add 0.5%～10% as additive by weight, do not changing under the vacuum column operation conditions, can make the yield of decompression fraction oil improve 0.5%～10% (weight).This additive does not need through special processing, and is cheap and easy to get.Method is simple, and factory only need carry out very simple technological transformation and can implement.
Description
The invention belongs to the technological improvement of oil vacuum distillation method.
As everyone knows, improve the method for oil decompression fraction oil yield, can adopt the change vacuum column operation conditions, for example reduce residual voltage, ways such as raising heater outlet temperature reach. occurred again in recent years using the purpose that reaches raising fraction oil yield by the composition of adjusting distillating material.
Russian patent (A.C.NO.791599) (1) uses arene concentrate (density of aromatic hydrocarbon 50～100% weights) as additive, adding by certain weight ratio, can improve decompression fraction oil yield. this additive derives from extraction oil (its aromaticity content is about more than 65%) or other method of three-way lubricating oil selective finishing.
On the other hand, according to Soviet Union's " Fuels And Lubricants chemistry and technology " (" X и м и я И Т e х н о л о г и я Т о п л и в И М а с e л ", 1986, NO.7, C.2～3) (2) report, directly adopt three-way lubricating oil (420～470 ℃) fraction as additive, can receive the effect that increases fraction oil yield equally.
With the additive that employed arene concentrate of document (1) and document (2) use, its effect is significant.But document (1) exists a remarkable shortcoming, is exactly its employed additive, and the extraction plant (or allied equipment) that needs a lubricating oil selective finishing provides arene concentrate.This will bring the difficulty on the Technological Economy to the factory of this explained hereafter device of nothing. and arene concentrate is the important source material of petrochemical complex.And document (2) is when using three-way lube cut, still need to vacuum distillation apparatus technological transformation in addition, can implement. undoubtedly, transform reliever construction more complicated, and its employed lube cut itself is the valuable raw material that is used to produce lubricating oil again.
The present invention can be applicable to all refinerys of catalytic cracking unit. and method is easy, and is less demanding to additive, and the source is wide, cheaply is easy to get, and does not need extension set or carries out plant modification.
The objective of the invention is to overcome the shortcoming of known technology, way is to adopt the two mixture of catalytic cracking recycle oil or catalytic slurry or its as additive, directly joins in atmospheric residue or the residual oil.It can not change increase fraction oil yield under the vacuum distillation tower operational condition.
Use additive of the present invention, it is heavy to make decompression fraction oil yield increase by 0.5%～10%(), its increasing degree is relevant with service temperature and residual voltage, and is relevant with the add-on of additive, also relevant with the composition of raw material.
With boiling spread be generally 350～520 ℃ in the scope catalytic cracking recycle oil or the two mixture of catalytic slurry or they as additive, its add-on is heavy by weight the 0.5%～10%(that is inlet amount), it is heavy to be preferably 1.5%～6%(). when this additive of an amount of adding, the physical and chemical index of resulting decompression fraction oil does not have tangible change.If wish to get more catalytically cracked material, can suitably add, so that replace out more wax oil into additive.
Another advantage of present method is to utilize oil property is relatively poor, commodity value is lower catalytic cracking recycle oil or catalytic slurry or the two mixture as additive, need not handle, only add a pipeline between the process furnace ingress to reducing pressure and corresponding measuring instrument gets final product in catalytic cracking unit.Less investment is implemented simple.
The employed additive of present method, its aromaticity content are that 20%～60%(is heavy).
Present method is applicable to the reduced pressure distillation process process of heavy oil, residual oil.
Embodiment 1
With the defeated commingled crude of pipe (to call the pipe oil transportation in the following text) long residuum (＞350 ℃ of fractions, down together), grand celebration long residuum and central plain oil long residuum are additive with catalytic cracking recycle oil, to investigate the action effect of additive.
It is as follows now only to enumerate typical additive:
Additive is numbered total aromaticity content, heavy %
Ⅰ 36.1
Ⅱ 41.8
Ⅲ 60.9
Working pressure is residual voltage 0.267KPa, and the boiling spread of decompression fraction oil is 350～500 ℃.
Test-results sees Table 1.
Being not difficult to find out from table 1 data, doing additive with catalytic cracking recycle oil, is effectively for improving decompression fraction oil yield.
Embodiment 2
With the Central Plains long residuum is charging, heavy with containing aromatic hydrocarbons 50%～60%() catalytic cracking recycle oil produce as additive.Long residuum character sees Table 2.
The main operational condition of vacuum distillation tower:
Tower top temperature, ℃ 72～94
Wax oil is extracted a mouthful temperature out, and ℃ 204～229
The cat head residual voltage, KPa 5.23～3.23
The 2.17%(that accounts for inlet amount when the amount that adds additive is heavy) time, the decompressed wax oil yield sees Table 3.
Produce resulting decompressed wax oil character by above-mentioned condition, analytical results shows, its density, kinematic viscosity, condensation point, carbon residue, number-average molecular weight and group composition etc., and the person compares with not adding the additive, and is basic identical.
Claims (3)
1, a kind of is the method that additive improves fraction oil reclaim rate of petroleum vacuum distillation to contain aromatic hydrocarbon oil, it is characterized in that this additive is petroleum catalytic cracking recycle stock or catalytic slurry, or the mixture of the two.
2, in accordance with the method for claim 1, it is characterized in that this additive is heavy by the part by weight adding 0.5%～10%(of vacuum distillation tower inlet amount), preferably 1.5%～6%(is heavy).
3, described according to claim 1, the aromaticity content that it is characterized in that this additive is that 20%～60%(is heavy).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN87101902.7A CN1005062B (en) | 1987-03-16 | 1987-03-16 | Method for increasing yield of distillate oil of petroleum vacuum distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN87101902.7A CN1005062B (en) | 1987-03-16 | 1987-03-16 | Method for increasing yield of distillate oil of petroleum vacuum distillation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1030250A true CN1030250A (en) | 1989-01-11 |
| CN1005062B CN1005062B (en) | 1989-08-30 |
Family
ID=4813674
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN87101902.7A Expired CN1005062B (en) | 1987-03-16 | 1987-03-16 | Method for increasing yield of distillate oil of petroleum vacuum distillation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1005062B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1094151C (en) * | 2000-01-04 | 2002-11-13 | 中国石油化工集团公司 | Process for treating catalytically cracked oil slurry |
| CN100348695C (en) * | 2006-05-25 | 2007-11-14 | 上海交通大学 | Method for promoting light oil yield of atmospheric and vacuum distillation of petroleum oil |
| CN102041028A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Composite for strengthening crude oil distillation and application thereof |
| CN104024383A (en) * | 2011-10-31 | 2014-09-03 | 国际壳牌研究有限公司 | Method for upgrading oil, fuel product and hydrocarbon product fraction |
| CN111978976A (en) * | 2019-12-19 | 2020-11-24 | 东营华联石油化工厂有限公司 | Method for improving distillate oil yield of atmospheric and vacuum distillation unit |
-
1987
- 1987-03-16 CN CN87101902.7A patent/CN1005062B/en not_active Expired
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1094151C (en) * | 2000-01-04 | 2002-11-13 | 中国石油化工集团公司 | Process for treating catalytically cracked oil slurry |
| CN100348695C (en) * | 2006-05-25 | 2007-11-14 | 上海交通大学 | Method for promoting light oil yield of atmospheric and vacuum distillation of petroleum oil |
| CN102041028A (en) * | 2009-10-13 | 2011-05-04 | 中国石油化工股份有限公司 | Composite for strengthening crude oil distillation and application thereof |
| CN102041028B (en) * | 2009-10-13 | 2013-08-14 | 中国石油化工股份有限公司 | Composite for strengthening crude oil distillation and application thereof |
| CN104024383A (en) * | 2011-10-31 | 2014-09-03 | 国际壳牌研究有限公司 | Method for upgrading oil, fuel product and hydrocarbon product fraction |
| CN111978976A (en) * | 2019-12-19 | 2020-11-24 | 东营华联石油化工厂有限公司 | Method for improving distillate oil yield of atmospheric and vacuum distillation unit |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1005062B (en) | 1989-08-30 |
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