CN203360389U - Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil - Google Patents
Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil Download PDFInfo
- Publication number
- CN203360389U CN203360389U CN 201320373631 CN201320373631U CN203360389U CN 203360389 U CN203360389 U CN 203360389U CN 201320373631 CN201320373631 CN 201320373631 CN 201320373631 U CN201320373631 U CN 201320373631U CN 203360389 U CN203360389 U CN 203360389U
- Authority
- CN
- China
- Prior art keywords
- reactor
- oil
- separation tank
- separating tank
- cold
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model provides a device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil. The device comprises a pressure reduction prefractionator, an isodewaxing reactor, a supplemental refining reactor, a cold high pressure separation tank, a cold low pressure separation tank, a normal pressure fractionating tower and a pressure reduction fractionating tower, wherein the pressure reduction fractionating tower, the isodewaxing reactor and the supplemental refining reactor are connected in series; the bottom of the supplemental refining reactor is connected with the cold high pressure separation tank; the bottom of the cold high pressure separation tank is connected with the cold low pressure separation tank; the top of the cold high pressure separation tank is connected with a recycle hydrogen devulcanizer; the recycle hydrogen devulcanizer is communicated with the inlet in the top of the isodewaxing reactor through a pipeline; the bottom of the cold low pressure separation tank is connected with the normal pressure fractionating tower; the bottom of the normal pressure fractionating tower is communicated with the pressure reduction fractionating tower. According to the device, the method of switchover feeding together with mixed feeding is adopted, and three kinds of work conditions can be simultaneously satisfied to produce the high grade lubricating oil base oil, so that the selectivity of raw materials and flexibility of production are improved.
Description
Technical field
the utility model belongs to petrochemical industry, is specifically related to the equipment that a kind of hydrocracking tail oil hydrogenation is produced the top-grade lubricating oil base oil.
Background technology
The content of lubricant base in finished lube is generally 70%～99%, and the quality of base oil directly affects the quality of lubricating oil.The most important thing is I. C. engine oil in Chinese Lubricating Oil Market, be divided in quality high, medium and low third gear, their shared market shares are respectively 10%, 30%, 60%.The production status of current China lubricating oil is that low grade products output is excessive, and the medium and high-grade goods ratio is less than normal, and the high-end product breach is larger, and, with world level, larger gap is arranged aspect quality.Major cause is that to produce the base oil proportion of top-grade lubricating oil on the low side, develops the required low viscosity of some top-grade lubricating oil product, low solidifying, high viscosity index (HVI) or superhigh viscosity index base oil and still can not produce.Therefore, for the development of meeting the market requirement and industrial technology, need a kind of novel process equipment to produce the high quality lubricant base to meet the demand of top-grade lubricating oil.
Summary of the invention
The purpose of this utility model is to overcome the lower defect of top-grade lubricating oil base oil yield existed in prior art, provide a kind of and take hydrocracking tail oil as raw material, by hydrocracking tail oil is produced to the device of API II class and III class lubricating oil base oil through decompression prefractionation, the mode of taking into account parallel feeding.
The technical solution of the utility model is as follows:
A kind of hydrocracking tail oil hydrogenation is produced the device of top-grade lubricating oil base oil, this device comprises the decompression preliminary fractionator, the isomerization dewaxing reactor, the post-refining reactor, the cold anticyclone separating tank, the cold low separating tank, atmospheric fractional tower and vacuum fractionation tower, wherein said decompression preliminary fractionator, the isomerization dewaxing reactor is connected with the post-refining reactors in series, the bottom of described post-refining reactor connects described cold anticyclone separating tank, the bottom of described cold anticyclone separating tank connects described cold low separating tank, the top of described cold anticyclone separating tank is connected with the desulphurization of recycle hydrogen tank, described desulphurization of recycle hydrogen tank communicates with the top entrance of described isomerization dewaxing reactor by pipeline, the bottom of described cold low separating tank is connected with described atmospheric fractional tower, and the bottom of described atmospheric fractional tower is connected with described vacuum fractionation tower.
This device further comprises circulating hydrogen compressor, this circulating hydrogen compressor is located on the pipeline between desulphurization of recycle hydrogen tank and isomerization dewaxing reactor head entrance, wherein the entrance of circulating hydrogen compressor is connected with the outlet of desulphurization of recycle hydrogen tank, and the outlet of circulating hydrogen compressor is connected with isomerization dewaxing reactor head entrance.
The beneficial effects of the utility model: adopt feed switched to take into account the method for parallel feeding, can meet three kinds of operating modes simultaneously and produce the top-grade lubricating oil base oil, improved the selectivity of raw material and the handiness of production.The top-grade lubricating oil base oil that kind, grade and the yield that adopts the top-grade lubricating oil base oil that feed switched produces produced during all higher than full cut charging, so the user can select suitable production technique according to raw material sources and the market requirement.
The accompanying drawing explanation
Fig. 1 is a kind of structural representation of the present utility model.
Wherein 1 is hydrocracking tail oil, 2 is the decompression preliminary fractionator, 3 is No. 4 oil base stock, and 4 is No. 6 oil base stock, and 5 is new hydrogen, 6 is circulating hydrogen compressor, 7 is the isomerization dewaxing reactor, and 8 is the post-refining reactor, and 9 is the cold anticyclone separating tank, 10 is the desulphurization of recycle hydrogen tank, 11 is the cold low separating tank, and 12 is fuel gas, and 13 is atmospheric fractional tower, 14 is the low fragrant solvent oil of gasoline-type, 15 is the low fragrant solvent oil of kerosene type, and 16 is the 3# industrial white oil, and 17 is the vacuum fractionation tower, 18 is No. 2 base oils of API II class, and 19 is the API II
+no. 4 base oils of class, 20 is No. 6 base oils of API III class, 21 is No. 8, API III class or No. 4 base oils of API III class.
Embodiment
Below in conjunction with accompanying drawing, this device and technological process thereof are described further.
As shown in Figure 1, production equipment comprises decompression preliminary fractionator 2, circulating hydrogen compressor 6, isomerization dewaxing reactor 7, post-refining reactor 8, cold anticyclone separating tank 9, cold low separating tank 11, atmospheric fractional tower 13 and vacuum fractionation tower 17, wherein said decompression preliminary fractionator 2, isomerization dewaxing reactor 7 and post-refining reactor 8 are connected in series, the bottom of described post-refining reactor 8 connects described cold anticyclone separating tank 9, the bottom of described cold anticyclone separating tank 9 connects described cold low separating tank 11, the top of described cold anticyclone separating tank 9 is connected with desulphurization of recycle hydrogen tank 10, described desulphurization of recycle hydrogen tank 10 is connected with described circulating hydrogen compressor 6 by pipeline, described circulating hydrogen compressor 6 communicates with the top entrance of described isomerization dewaxing reactor 7, the bottom of described cold low separating tank 11 is connected with described atmospheric fractional tower 13, and the bottom of described atmospheric fractional tower 13 is connected with described vacuum fractionation tower 17.
In production process, hydrocracking tail oil fractionates out No. 6 oil base stock of No. 4 oil base stock of final boiling point≤430 ℃ and initial boiling point>430 ℃ in preliminary fractionator 2 in decompression, they adopt the mode of feed switched to enter isomerization dewaxing-post-refining reactive system, (No. 4 material operations switching in 31 days, No. 6 material operations switching in 25 days).Oil base stock is mixed with new hydrogen 5 and the recycle hydrogen after circulating hydrogen compressor 6 compressions, enter successively isomerization dewaxing reactor 7 and post-refining reactor 8, reaction effluent carries out gas-liquid separation in high pressure separating tank 9, gas phase enters circulating hydrogen compressor 6 and boosts and use as recycle hydrogen after digester 10 desulfurization, liquid phase enters cold low separating tank 11 and further carries out gas-liquid separation, the gas phase gas 12 that acts as a fuel is incorporated to the fuel gas pipe network, low minute oil enters atmospheric fractional tower 13 and carries out fractionation, overhead condensation liquid is partly extracted out as low fragrant solvent oil 14 carrying devices of gasoline-type, a normal line is extracted the low fragrant solvent oil 15 of kerosene type out, normal two wires is extracted No. 3 industrial white oils 16 out, at the bottom of the atmospheric fractional tower tower, oil enters vacuum fractionation tower 17.When No. 4 material operations, overhead condensation liquid is partly extracted No. 2 base oils 18 of API II class out, goes out No. 4 base oils 21 of API III class at the bottom of tower; When No. 6 material operations, the tower top liquid phase part is extracted No. 2 base oils 18 of API II class out, and vacuum 1st side cut is extracted the API II out
+no. 4 base oils 19 of class, second line of distillation is extracted No. 6 base oils 20 of API III class out, and VACUUM TOWER BOTTOM is extracted No. 8 base oils 21 of API III class out.Simultaneously, if hydrocracking tail oil is without decompression preliminary fractionator 2, and with enter successively isomerization dewaxing reactor 7 and post-refining reactor 8 and follow-up fractionating system after new hydrogen 5 and recycle hydrogen mix, experience reaction mechanism same as described above, can produce equally satisfactory top-grade lubricating oil base oil.
Claims (2)
1. a hydrocracking tail oil hydrogenation is produced the device of top-grade lubricating oil base oil, it is characterized in that this device comprises the decompression preliminary fractionator, the isomerization dewaxing reactor, the post-refining reactor, the cold anticyclone separating tank, the cold low separating tank, atmospheric fractional tower and vacuum fractionation tower, wherein said decompression preliminary fractionator, the isomerization dewaxing reactor is connected with the post-refining reactors in series, the bottom of described post-refining reactor connects described cold anticyclone separating tank, the bottom of described cold anticyclone separating tank connects described cold low separating tank, the top of described cold anticyclone separating tank is connected with the desulphurization of recycle hydrogen tank, described desulphurization of recycle hydrogen tank communicates with the top entrance of described isomerization dewaxing reactor by pipeline, the bottom of described cold low separating tank is connected with described atmospheric fractional tower, and the bottom of described atmospheric fractional tower is connected with described vacuum fractionation tower.
2. device according to claim 1, it is characterized in that this device also comprises circulating hydrogen compressor, this circulating hydrogen compressor is located on the pipeline between desulphurization of recycle hydrogen tank and isomerization dewaxing reactor head entrance, wherein the entrance of circulating hydrogen compressor is connected with the outlet of desulphurization of recycle hydrogen tank, and the outlet of circulating hydrogen compressor is connected with isomerization dewaxing reactor head entrance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320373631 CN203360389U (en) | 2013-06-25 | 2013-06-25 | Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320373631 CN203360389U (en) | 2013-06-25 | 2013-06-25 | Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203360389U true CN203360389U (en) | 2013-12-25 |
Family
ID=49808181
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320373631 Expired - Fee Related CN203360389U (en) | 2013-06-25 | 2013-06-25 | Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203360389U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305267A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Method for producing high-grade lubricant base oil through hydrogenating of hydrocracking tail oil |
-
2013
- 2013-06-25 CN CN 201320373631 patent/CN203360389U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103305267A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Method for producing high-grade lubricant base oil through hydrogenating of hydrocracking tail oil |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103305267B (en) | A kind of hydrocracking tail oil hydrogenation produces the method for top-grade lubricating oil base oil | |
| CN103289738B (en) | A kind of hydrocracking tail oil hydrogenation produces the combined method of top-grade lubricating oil base oil | |
| CN203878113U (en) | Reforming reaction liquid-phase product hydrogenation system | |
| CN104611059A (en) | Method for preparing liquid paraffin, paraffin precursor and lubricant base oil precursor from Fischer-Tropsch synthesis products | |
| CN105602619B (en) | A kind of liquid-phase hydrogenatin heterogeneous system and its technique and application | |
| CN103146426B (en) | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN104962307B (en) | Method for producing light oil through coal liquefaction | |
| CN102041029A (en) | Comprehensive utilization method of hydrocracking tail oil | |
| CN111518589A (en) | Production process of food-grade white oil | |
| CN103396833B (en) | A kind of synthetic naphtha produces the method for motor spirit | |
| CN103205274B (en) | Method for converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN104862006B (en) | Anti-evolving-gas additive of transformer oil and preparation method thereof | |
| CN203360389U (en) | Device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil | |
| CN103059946B (en) | Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method | |
| CN105085154A (en) | Method for increase production of aromatic hydrocarbon raw material by use of inferior heavy aromatics | |
| CN105085135A (en) | Method for direct production of benzene and xylene from inferior heavy aromatics | |
| CN203360388U (en) | Combined device for producing high grade lubricating oil base oil by adding hydrogen into hydrocracking tail oil | |
| CN205549690U (en) | A device for separating sour hydrocarbon mixture | |
| CN210765173U (en) | Aromatic extraction combination device | |
| CN103614160B (en) | A kind of Heavy lubricant base oil production system and production method | |
| CN103146424B (en) | The method of full cut preparing fuel oil by coal tar hydrogenation and lubricant base | |
| CN210595940U (en) | Heat conduction oil processing device | |
| CN103242886B (en) | Deep reduced pressure flash tank and reduced pressure deep distillation method | |
| CN102268292A (en) | Combined hydrogenation method | |
| JP2018510935A (en) | Hydrorefining method for low-temperature Fischer-Tropsch synthesized whole distillates of high yield middle distillates |
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: 20131225 Termination date: 20210625 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |