CN1059919C - Method for production of light fuel and lubricating oil with high viscosity index - Google Patents
Method for production of light fuel and lubricating oil with high viscosity index Download PDFInfo
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- CN1059919C CN1059919C CN95106351A CN95106351A CN1059919C CN 1059919 C CN1059919 C CN 1059919C CN 95106351 A CN95106351 A CN 95106351A CN 95106351 A CN95106351 A CN 95106351A CN 1059919 C CN1059919 C CN 1059919C
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- oil
- hydrocracking
- hydrofining
- lubricating oil
- viscosity index
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Abstract
The present invention relates to a method for simultaneously producing fuel and heavy lubricating oil with a high viscosity index. The existing hydro-cracking device is mainly utilized, a proper hydro-fining catalyst is adopted to make parts of hydro-fined generation oil and materials from a hydro-cracking section mixed and then directly enter a separation system to be divided into various kinds of fuel and lubricating oil. The method of the present invention can simultaneously obtain the heavy lubricating oil with the high viscosity index on the premise without influencing the quality of fuel oil. The present invention can also neatly adjust the yield of oil products by controlling the quantity of materials separated from the hydro-fined section.
Description
The invention belongs to the petroleum hydrocarbon complete processing, or rather, be with high boiling petroleum hydrocarbon by hydrotreatment and hydrocracking, produce the method for the heavy grease of the light-weight fuel oil comprise gasoline, kerosene, diesel oil and high viscosity index (HVI) simultaneously.
Hydrocracking process is one of important process in the modern refining of petroleum.Usually be that the flow process of the hydroeracking unit of purpose is an one-stage serial recycle to extinction hydrocracking reaction flow process to produce fuel, it is hydrofining reactor and hydrocracking reactor that system adopts two placed in-line reactors, at first with stock oil with enter hydrofining reactor after hydrogen mixes, the purified material passes through hydrocracking reactor again, the material of hydrocracking obtains required product through fractionation, hydrocracking reactor (" refining of petroleum collected translation " is returned in part unconverted oil (or claiming tail oil) circulation, [10], 1981,1～3).The used Hydrobon catalyst of this flow process is the stronger catalyzer of hydrodenitrification ability, and its effect is that raw material process pre-refining is to reduce nitrogen content in the stock oil; Hydrocracking catalyst adopts the dual-function catalyst with cracking and two kinds of effects of hydrogenation, and its cracking activity is provided by amorphous silicic aluminium or Zeolite support, and hydrogenating function is supplied with by metal components such as W, Mo, Ni.
Hydrocracking is to carry out under high pressure, high temperature, and need consume a large amount of hydrogen, the construction investment and the process cost of device are all very high, so wish can a production part has high value-added product the hydroeracking unit that fuel is purpose to produce from existing, as lubricant base.Nineteen ninety Maoming petrochemical corporation (complex) with the part unconverted oil through benzol-kentone dewaxing and clay-filtered to produce lubricant base (" lubricating oil ", (2), 1990), this method since unconverted oil from the effusive material of hydrocracking reactor, separate and obtain, passed through drastic cracking, therefore doing of it has only 464 ℃, and 50% recovered temperature is 356 ℃, and the back 40 ℃ of kinematic viscosity that dewax are 16.5mm
2/ s is equivalent to neutral oil No. 75, and this kind lighter body modulation lube product not only needs more viscosity additive, and can not modulate the qualified lube product that vaporization losses is had strict demand.
For can be from producing a part of high viscosity index (HVI) heavy grease simultaneously to produce the hydroeracking unit that fuel is purpose, IFP have been announced the method that a kind of maximum ground produces intermediate oil and lubricant base in the 10th World Petroleum Congress (WPC).This method is the material that comes out from refining section, after condensation cools and isolates recycle hydrogen, enter water distilling apparatus and separate products such as fuel and lube stock, unconverted oil is then sent into the further cracking of hydrocracking reactor, lube stock is produced lubricant base again through dewaxing.This method flow process complexity, material is through the laggard refining reaction device that boosts, and step-down enters water distilling apparatus again, and a large amount of then unconverted oil is boosted again and is entered hydrocracking reactor, and because material is through boosting, step-down, boost again, so energy consumption must increase.In addition, with existing be the hydroeracking unit of purpose to produce fuel, it is also bigger to transform difficulty by the method for IFP.
USP 4764266 has introduced the combined hydrogenation technology of a kind of production high-quality intermediate oil and lubricating oil.This method is with hydrocarbon raw material, in the presence of catalyzer, carry out hydrocracking with acid and hydrogenation-dehydrogenation functionality, the logistics that obtains is told petroleum naphtha, intermediate oil through separation column, unconverted oil is sent into to load and is had in the reactor of beta-zeolite catalyst at the bottom of the tower, carrying out hydroisomerization handles, make the alkane in the unconverted oil be converted into the isoparaffin product, and then separation obtain lubricating oil distillate.But when producing heavy grease with this method, hydrocracking must be carried out under the demulcent condition, and the light Fuel oil quality is reduced, and the lube stock color that obtains is very dark, needs further solvent extraction and hydrofining.
The objective of the invention is to overcome the shortcoming of prior art, propose a kind ofly to utilize existing to be the hydroeracking unit of purpose to produce fuel, can to produce the method for light-weight fuel oil and high viscosity index (HVI) heavy grease simultaneously.
Another object of the present invention is to utilize a kind of Hydrobon catalyst that has certain cracking activity, can produce high-viscosity index lubricating oil.
Characteristics of the present invention are raw material hydrofining in the presence of the catalyzer with certain cracking activity, a purified material part enters hydrocracking reactor, another part directly enters separation system with effusive mixing of materials from hydrocracking reactor, separates various light-weight fuel oils and high-viscosity index lubricating oil product.
Concrete steps of the present invention:
(1) stock oil makes its temperature be increased to 250～400 ℃ through heat exchange, enters in the reactor that is filled with certain lytic activity catalyzer after mixing with hydrogen through heating, and hydrofining under certain conditions obtains hydrofining and generates oily;
(2) part with (1) step hydrogenated oil enters and carries out hydrocracking in the reactor that is filled with the stronger catalyzer of cracking activity, obtains the hydrocracking material;
(3) obtain the living olefiant another part of hydrofining by (1) step and obtain entering separation system after the hydrocracking mixing of materials, to fractionate out various light-weight fuel oils, lubricating oil with (2) step.
Common operational condition is adopted in the hydrofining of step of the present invention (1): 360～400 ℃ of temperature, pressure 15～20MPa, air speed 0.5～2.0h
-1, hydrogen-oil ratio 850～1500 (body).
The hydrocracking of step of the present invention (2), adopting common is the operational condition of the hydroeracking unit of purpose to produce fuel: 370～440 ℃ of temperature, pressure 15～20MPa, air speed 0.5～2.0h
-1, hydrogen-oil ratio 1000～1500 (body).
The described hydrofining of step of the present invention (3) is given birth to olefiant amount and can be controlled as required, increases the amount of thick oil if desired, can reduce the hydrofining that enters hydrocracking reactor and give birth to olefiant amount.
Described stock oil is decompressed wax oil, deasphalted oil or its mixing oil of paraffinic base, middle paraffinic base or intermediate base crude oil.
Described Hydrobon catalyst comprises WO
3-NiO/ auxiliary agent, WO
3-MoO
3-NiO metal component, carrier comprises Al
2O
3, Al
2O
3-SiO
2, Al
2O
3-SiO
2-P, Al
2O
3-zeolite; The catalyzer that gets by ZL 85104438 patent systems preferably, this catalyzer contains NiO 1～5%, WO
312～35%, auxiliary agent F 1～9%, carrier are highly purified γ-Al
2O
3, it has higher activity, stability and intensity, particularly has high hydrodenitrogenationactivity activity; Perhaps use the catalyzer that gets by ZL 90102648 patent systems, this catalyzer contains NiO 2.5～6.0%, WO
310～32%, auxiliary agent F 0.5～5.0%, carrier are high-purity γ-Al
2O
3And through the zeolite of cationic exchange, it has higher aromatic hydrogenation activity, lytic activity and hydrofining performance.
Described hydrocracking catalyst is the WO that uses always
3-NiO/SiO
2-Al
2O
3, WO
3The high silicon large pore zeolite+SiO of-NiO/
2-Al
2O
3, MoO
3-NiO/Y zeolite+Al
2O
3(seeing the Hou Xianglin chief editor, " Chinese oil Refining Technologies ",, 514 pages, Sinopec press in 1991).
Below in conjunction with accompanying drawing processing method of the present invention is described.
Accompanying drawing is a schema of the present invention.
Shown in accompanying drawing, raw material makes its temperature be increased to 250～400 ℃ through heat exchange, by pipeline 8 with enter hydrofining reactor 1 after the circulating hydrogen through heating furnace 7 heating by pipeline 12 mixes, hydrofinishing generates oil from pipeline 9 derivation and is divided into two parts: a part enters hydrocracking reactor 2 through pipeline 11, a part is through pipeline 10 and mixing of materials from hydrocracking reactor 2, enter high-pressure separator 3, the hydrogen of separating is drawn from pipeline 12 and is looped back reactor 1 and reactor 2, liquid phase stream then enters low pressure separator 4, tells C1～C
2Enter fractionating column 5 behind the gas, fractionate out again naphtha, diesel oil, lubricated wet goods.
The present invention has following advantage:
1. the present invention generates oil with a part of hydrofinishing to release without hydrocracking reactor, direct air inlet body piece-rate system, therefore can produce full-bodied lube stock, and it is existing to produce fuel as main hydrocracking unit, because refining oil plant all enters hydrocracking reactor, unconverted oil becomes the hydro carbons of molecular weight through cracking, so is difficult to make the higher lubricating oil of viscosity.
2. because the present invention adopts the Hydrobon catalyst with certain cracking function, make the hydrorefined hydro carbons that oil has the more long side-chain structure of few ring that generates, therefore lubricating oil has high viscosity index (VI), and existing hydrocracking unit, the used catalyst of hydrofinishing section does not have the cracking function or the cracking function is very low, therefore generate oil and be cycloalkane structure take many rings as main, viscosity index (VI) is lower.
3. thick oil cut of the present invention mainly obtains from the material of hydrofining reactor, and the hydrocracking reaction operating condition is controlled by the requirement of producing fuel oil fully, so the quality of fuel oil is not affected.
4. method of the present invention is very flexible, can be according to different requirements, and the hydrofinishing that enters hydrocracking reactor by control generates oily amount, can produce simultaneously needed light-weight fuel oil and full-bodied lubricating oil.
5. transforming existing production fuel according to this method is that main hydrocracking unit is easily, only needs the removable parts catalyst and increase the part pipeline to realize.
Further specify characteristics of the present invention below by example.
Example 1
This example is that the selected Hydrobon catalyst of explanation the present invention can obtain the high viscosity index (HVI) heavy grease.
Experiment is to carry out on inlet amount is 0.5 kilogram/hour medium-sized tester, and stock oil is decompressed wax oil, and its character sees Table 1.
Test 1 is by being used Hydrobon catalyst (trade mark 3822) on the existing hydrocracking full scale plant, it consists of: active ingredient NiO-MO
3, carrier γ-Al
2O
3/ SiO
2
The Hydrobon catalyst with certain lytic activity that test 2 is selected for use for the present invention, this catalyzer are that the active ingredient that the method by patent No. ZL 85104438 makes is WO
3-NiO, auxiliary agent are that F, carrier are γ-Al
2O
3
Test 1 and test 2 are to carry out under the identical operations condition, and promptly the hydrofining reaction temperature is 380 ℃, pressure 15MPa, air speed 1.0h
-1, hydrogen-oil ratio 850, hydrorefined generation oil does not enter cracking case, directly enters separation system, tells boiling point and is lower than 370 ℃ of cuts, and the separation column bottom through solvent dewaxing, promptly obtains required lubricating oil greater than 370 ℃ of cuts, and its character sees Table 2.
As shown in Table 2, the Hydrobon catalyst that uses on the catalyzer that the present invention selects for use and the existing hydrocracking full scale plant is compared, and gained oil body index is wanted high 14 units.
Example 2
Another Hydrobon catalyst that this example explanation the present invention selects for use can obtain the high viscosity index (HVI) heavy grease equally.
The selected catalyzer of this example prepares by patent No. ZL 90102648, and its active ingredient is W-Ni, and auxiliary agent is F, and carrier is high-purity γ-Al
2O
3And zeolite.Other condition is with example 1.Resulting lubricating oil property sees Table 3.
Example 3
This example is undertaken by flow process provided by the invention, and used testing apparatus and raw material are with example 1.
It is 3824 that this example is tested the 1 hydrocracking reactor catalyst system therefor trade mark, and its active ingredient is MoO
3-NiO, carrier are Y-zeolite+Al
2O
3Hydrobon catalyst is with the used catalyzer of the test 1 of example 1, test is to adopt existing one-stage serial recycle to extinction flow process, be that hydrofining generation oil all enters hydrocracking reactor, in the separation column fractionation is petroleum naphtha, boat coal, diesel oil and lubricating oil, and operational condition and oil property see Table 3.
This example is tested the used catalyzer of 2 hydrocracking reactors with test 1, Hydrobon catalyst is with the test 2 of example 1, flow process of the present invention is adopted in test, and the refining generation oil content that comes out from hydrofining reactor becomes two portions: 70% enters hydrocracking reactor; The 30%th, enter separation system after the mixing of materials of coming out with hydrocracking reactor, obtain petroleum naphtha, boat coal, diesel oil and lubricating oil from the separation column fractionation, its operational condition and oil property see Table 3.
As shown in Table 3, the lubricating oil viscosity index that adopts flow process of the present invention to obtain is higher than 100, and the lubricated innage that the existing full scale plant of viscosity ratio is produced is a lot, and the quality of lightweight oil and existing full scale plant are approaching.
Table 1 raw material reduced pressure distillate oil properties
| Density, g/cm 3Kinematic viscosity (100 ℃), mm 2/ s carbon residue, m% C 5Insolubles, m% dewaxing back viscosity index | 0.8874 10.4 0.1 0.04 26 |
Table 2 embodiment 1 gained lubricates oil properties
| Project | Test 1 |
| Kinematic viscosity (40 ℃), mm 2/ s (100 ℃) viscosity index zero pour, ℃ | 39.2 40.1 6.12 5.98 76 90 -9 -10 |
Table 3 embodiment 2 gained lubricate oil properties
| Kinematic viscosity, (40 ℃) mm 2/ s (100 ℃) viscosity index zero pour, ℃ | 40.5 6.02 88 -10 |
The test conditions of table 4 embodiment 3 and oil property
| Project | Test 1 | |
| Test conditions: refining section pressure, the MPa air speed, 1/ o'clock temperature, ℃ cracking zone pressure, the MPa air speed, 1/ o'clock temperature, ℃ | 15 1.0 380 15 1.2 385 | 15 1.0 380 15 1.2 385 |
| Main products character: heavy naphtha sulphur content, the ppm nitrogen content, ppm arene underwater content aviation kerosene freezing point, ℃ smoke point, mm diesel oil zero pour, ℃ cetane value＞370 ℃ lubricating oil (dewaxing back) character: viscosity (40 ℃), mm 2/ s viscosity index zero pour, ℃ | ＜1 ＜1 41 -55 30 -5 70 28 125 -10 | ＜1 ＜1 40 -57 32 -6 74 54 106 -12 |
Claims (4)
1. method of producing light Fuel and high viscosity index (HVI) heavy grease is characterized in that the concrete operations step is as follows:
(1) stock oil makes its temperature be increased to 250～400 ℃ through heat exchange, enters after mixing in the reactor of filling Hydrobon catalyst with hydrogen through heating and carries out hydrofining, obtains hydrofining and generates oily;
(2) the living olefiant part of hydrofining that (1) step is obtained enters in the reactor that loads hydrocracking catalyst carries out hydrocracking, obtains the hydrocracking material;
(3) enter separation system after (1) hydrofining of obtaining of step being given birth to the hydrocracking mixing of materials that olefiant remainder and (2) step obtain, fractionate out unconverted oil at the bottom of various light Fuels, lubricating oil and the tower.
2. in accordance with the method for claim 1, it is characterized in that described stock oil is decompressed wax oil or deasphalted oil, or its mixing oil.
3. in accordance with the method for claim 1, its feature comprises WO at described Hydrobon catalyst metal component
3-NiO/ auxiliary agent, WO
3-MoO
3-NiO, carrier comprises Al
2O
3, Al
2O
3-SiO
2, Al
2O
3-zeolite, Al
2O
3-SiO
2-P.
4. in accordance with the method for claim 1, it is characterized in that described Hydrobon catalyst metal component is WO
3-NiO/F, carrier γ-Al
2O
3Or γ-Al
2O
3-zeolite.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95106351A CN1059919C (en) | 1995-06-14 | 1995-06-14 | Method for production of light fuel and lubricating oil with high viscosity index |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95106351A CN1059919C (en) | 1995-06-14 | 1995-06-14 | Method for production of light fuel and lubricating oil with high viscosity index |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1138083A CN1138083A (en) | 1996-12-18 |
| CN1059919C true CN1059919C (en) | 2000-12-27 |
Family
ID=5075888
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95106351A Expired - Fee Related CN1059919C (en) | 1995-06-14 | 1995-06-14 | Method for production of light fuel and lubricating oil with high viscosity index |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1059919C (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1074039C (en) * | 1997-03-24 | 2001-10-31 | 荆门石油化工研究院 | Producing technology for refined jet fuel |
| CN101210195B (en) * | 2006-12-27 | 2012-05-30 | 中国石油化工股份有限公司 | Hydrocracking method for more producing chemical industry light oil from poor heavy raw material |
| CN103102956B (en) * | 2011-11-10 | 2015-02-18 | 中国石油化工股份有限公司 | Hydrogenation production method for high-viscosity index lubricant base oil |
| CN103102947B (en) * | 2011-11-10 | 2016-01-20 | 中国石油化工股份有限公司 | The producing and manufacturing technique of base oil of high viscosity index lubricant |
| CN104611019B (en) * | 2013-11-05 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of low energy consumption method for hydrogen cracking producing high-quality jet fuel |
| CN105001909B (en) * | 2014-04-23 | 2017-02-01 | 中国石油化工股份有限公司 | Two-stage hydrocracking method for low energy consumption production of high-quality jet fuels |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4764266A (en) * | 1987-02-26 | 1988-08-16 | Mobil Oil Corporation | Integrated hydroprocessing scheme for production of premium quality distillates and lubricants |
| EP0590672A1 (en) * | 1992-10-02 | 1994-04-06 | Mitsubishi Oil Company, Limited | Process for producing low viscosity lubricating base oil having high viscosity index |
| EP0590673A1 (en) * | 1992-10-02 | 1994-04-06 | Mitsubishi Oil Company, Limited | Process for producing low viscosity lubricating base oil having high viscosity index |
-
1995
- 1995-06-14 CN CN95106351A patent/CN1059919C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4764266A (en) * | 1987-02-26 | 1988-08-16 | Mobil Oil Corporation | Integrated hydroprocessing scheme for production of premium quality distillates and lubricants |
| EP0590672A1 (en) * | 1992-10-02 | 1994-04-06 | Mitsubishi Oil Company, Limited | Process for producing low viscosity lubricating base oil having high viscosity index |
| EP0590673A1 (en) * | 1992-10-02 | 1994-04-06 | Mitsubishi Oil Company, Limited | Process for producing low viscosity lubricating base oil having high viscosity index |
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| Publication number | Publication date |
|---|---|
| CN1138083A (en) | 1996-12-18 |
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