CN105647574B - A kind of method that high-content wax raw material produces lube base oil - Google Patents
A kind of method that high-content wax raw material produces lube base oil Download PDFInfo
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- CN105647574B CN105647574B CN201410732111.1A CN201410732111A CN105647574B CN 105647574 B CN105647574 B CN 105647574B CN 201410732111 A CN201410732111 A CN 201410732111A CN 105647574 B CN105647574 B CN 105647574B
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Abstract
The present invention relates to a kind of method of high-content wax starting isomeric dewaxing production lube base oil, methods described is first pre-processed preprocessing solution with isomerization dewaxing catalyst mixing, isomerization dewaxing catalyst after being pre-processed, then isomerization dewaxing catalyst after obtained pretreatment is loaded into reactor and carries out hydrogen activation, finally feedstock oil and hydrogen are contacted with the isomerization dewaxing catalyst after activation, isomerization dewaxing reaction is carried out under finite concentration vulcanization hydrogen atmosphere.The inventive method by suppress isomerization dewaxing catalyst hydrogen activation after initial reaction stage cracking activity, improve isomerization dewaxing catalyst stereoselectivity, improve lube base oil yield.
Description
Technical field
The present invention relates to a kind of method for producing lube base oil, urged especially with the isomerization dewaxing by pretreatment
Agent produces lube base oil method.
Background technology
Increasingly the developing rapidly of strict environmental legislation and mechanical industry proposes more next to the performance of lube base oil
Higher requirement.Simultaneously as worldwide crude oil in poor quality so that the crude oil quantity for being suitable for producing lubricating oil gradually subtracts
It is few.Therefore, the development of hydrogenation method production Lubricating Oil Technique is very rapid.Hydrogenation method technique refers to use hydrocracking process or hydrogenation
Processing~isomerization dewaxing~hydrofinishing process integration produces the process of lube base oil, its advantage be feed flexibility it is big,
Base oil yield height, by-product value height etc..
In view of the above-mentioned problems, CN200380101175.1 and US7220350 are proposed using oxygenatedchemicals to isomery
The method that dewaxing catalyst is pre-processed improves the selectivity of catalyst, produces the side of base oil of high viscosity index lubricant
Method.Because the pretreatment temperature of oxygenatedchemicals is carried out at 120 DEG C~400 DEG C, equivalent to isomerization dewaxing catalyst molecule
A kind of hydrothermal modification treatment of sieve, although improve the selectivity of heterogeneous catalyst, but due to the radical change of acidic zeolite,
The loss of activity of catalyst is larger.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of high-content wax starting isomeric dewaxing production lube base oil
Method.The inventive method can suppress isomerization dewaxing catalyst in hydrogen by using the isomerization dewaxing catalyst by pretreatment
The cracking activity of initial reaction stage after activation, and the stereoselectivity of isomerization dewaxing catalyst is improved, improve lube base oil
Yield.
The method of high-content wax starting isomeric dewaxing production lube base oil of the present invention, including following content：
（1）Pre-processed after preprocessing solution is mixed with isomerization dewaxing catalyst, isomerization dewaxing after being pre-processed
Catalyst；
（2）By step（1）Isomerization dewaxing catalyst loads reactor after obtained pretreatment, carries out hydrogen activation；
（3）By feedstock oil and hydrogen and step（2）Isomerization dewaxing catalyst contact after activation, isomerization dewaxing reaction controlling
Carried out under finite concentration vulcanization hydrogen atmosphere, i.e., hydrogen sulfide content is 10~500 μ L/L, preferably 20~200 μ L/ in recycle hydrogen
L。
In the inventive method, step（1）Described in preprocessing solution include sulfide, nitride and organic solvent；Its
Described in sulfide be elementary sulfur and sulfur-containing compound, the sulfur-containing compound can be the double two thio ammonia of 2,2- dimethylenes
The ammonia salt of base formic acid two, two coloured glaze base diamino thiophenes, the thio thing of diethanol two, DMDS carbonic acid diformazan ammonia and sub- disulfide group second
One kind in acid, dimethylsulphide, dimethyl disulphide, two tertiary nonylpolysulfides, mercaptide and carbon disulfide etc.
Or it is several；Sulfide consumption is 0.1~50%, preferably the 0.2~10% of catalyst weight.The nitride is carbon number 5~20
Nitrogen-containing compound, be specifically as follows one kind in pyridine, quinoline, acridine, benzacridine, aniline, pyrroles, indoles, carbazole or
It is several, preferably aniline, pyridine and quinoline；The consumption of nitride is 0.1~30%, preferably the 0.2~5% of catalyst weight.
The organic solvent is the one or more in catalytically cracked gasoline, catalytic cracking diesel oil, coker gasoline and coker gas oil, organic
Solvent load is the 5%~15% of catalyst weight.
In the inventive method, step（1）Described in isomerization dewaxing catalyst and the pretreatment of preprocessing solution be in sky
Carried out under the atmosphere of gas and water steam or inert gas, the condition of pretreatment operation is：100~280 DEG C of temperature, preferably 120~
180 DEG C, preferably 1~20h of processing time, 2~10h.
In the inventive method, step（2）Described in hydrogen activation condition be：0.1~20.0MPa of pressure, preferably 5.0~
15.0MPa；The volume ratio 100~2000 of hydrogen and catalyst, preferably 500~1000；150~450 DEG C of Hydrogen activation temperature, it is excellent
Select 250~400 DEG C；1~20 DEG C/h of programming rate of Hydrogen activation process, 8~32h of Hydrogen activation time.
In the inventive method, step（3）Described isomerization dewaxing reaction condition is：250~380 DEG C of reaction temperature, preferably
290~350 DEG C, 1.0~18.0MPa of hydrogen dividing potential drop, preferably 10.0~15.0MPa, 0.1~6.0h of volume space velocity during raw material fluid-1,
It is preferred that 0.2~1.0h-1, hydrogen to oil volume ratio 400:1~1500:1, preferably 600:1~1000:1.
The hydroisomerizing dewaxing catalyst that the inventive method is used is lube oil hydrogenation heterogeneous catalyst commonly used in the art,
It can also can be prepared with commodity in use hydroisomerization catalyst by this area general knowledge.Hydroisomerizing dewaxing catalyst carrier
Molecular sieve of the molecular sieve of the generally NU of aluminum oxide and TON structures~10 or ZSM~22 etc., the content of molecular sieve in the catalyst is
Also partial oxidation silicon can be added in 30wt% ~ 80wt%, preferably 40wt% ~ 70wt%, carrier；Active metal component is Pt, Pd, Ru
With one or more in Rh, content in the catalyst is 0.1wt% ~ 5.0wt%.Selectable adjuvant component be boron, fluorine, chlorine and
One or more in phosphorus, content in the catalyst is 0.1wt% ~ 5.0wt%；The ratio surface of hydroisomerization catalyst is 150
~500m2/ g, pore volume is 0.15~0.60ml/g.
In the inventive method, the feedstock oil can be one kind in Fischer Tropsch waxes, sweat oil, slack wax and pertroleum wax or
It is several.
Compared with prior art, the inventive method has the following advantages that：
1st, the isomerization dewaxing catalyst that the inventive method is used is in preparation due to being pre-loaded into sulfide and nitride,
It is sulphur by sulfide hydro-conversion in the presence of hydrogen and active metal during isomerization dewaxing catalyst Hydrogen activation
Change hydrogen, hydrogen sulfide can be introduced to system, hydrogen sulfide is further adsorbed by noble metal active center quickly, reduce isomerization dewaxing
The heterogeneous activity of catalyst, so that the cracking for reducing isomerization dewaxing catalyst for a large amount of n-alkanes in high-content wax raw material is lived
Property, improve the yield of isomerization dewaxing process lube base oil；Nitrogen-containing compound during isomerization dewaxing Hydrogen activation,
In the presence of hydrogen and active metal hydro-conversion be hydro carbons and ammonia, in alkalescence ammonia can be in isomerization dewaxing catalyst
The acid centre of molecular sieve is suppressed.Because isomerization dewaxing catalyst has preloaded sulfide and nitride, in sulfide and nitrogen
Under the synergy of compound, the higher lytic activity of the initial reaction stage after the activation of isomerization dewaxing catalyst hydrogen is reduced, is improved different
Selectivity, liquid yield and the purpose product base oil yield of structure dewaxing catalyst.Existing hydroisomerizing dewaxing is solved to urge
Initial reaction stage of the agent after hydrogen activation, activity is very high, and reaction is violent, and thermal discharge is big, and side reaction is more, liquid yield and purpose production
The problem of product yield is low.
2nd, the inventive method by hydrogen sulfide in initial reaction stage by introducing system, and maintains isomerization dewaxing to circulate in hydrogen system
Suitable concentration of hydrogen sulfide, reaches the purpose of the long-term maintenance higher stereoselectivity of isomerization dewaxing catalyst.
Embodiment
Isomerization dewaxing catalyst of the present invention can select commercial catalyst by property, can also be by ability domain knowledge
Prepare.FIW-1 the and FIW-12 catalyst of hydroisomerizing dewaxing catalyst such as Fushun Petrochemical Research Institute's development and production, also may be used
To be prepared by the existing patented technology such as CN03133557.8, CN02133128.6.As described in CN02133128.6, hydroisomerizing
Dewaxing catalyst carrier is the NU-10 molecular sieves or ZSM-22 molecular sieves of aluminum oxide and TON structures；Molecular sieve is in the catalyst
Content is 30wt% ~ 80wt%；Active metal component is one or more, content in the catalyst in Pt, Pd, Ru, Rh and Ni
For 0.1wt% ~ 30.0wt%；It is 150~500m than surface2/ g, pore volume is 0.15~0.60ml/g.
Illustrate the particular content and effect of the inventive method below by specific embodiment.
Following implementation row will be further described to the method that the present invention is provided, but therefore not limit this hair
Bright scope.The feedstock property that the present invention is handled is shown in Table 1, and the physicochemical property of the hydroisomerizing dewaxing catalyst of use is shown in Table 2.
The embodiment feedstock property of table 1
| Feedstock oil | Fischer Tropsch waxes | No. 58 paraffin | The line slack wax that subtracts four |
| Density, kg/m3 | 815 | 801 | 830 |
| Boiling range scope, DEG C | 325~580 | 370~490 | 401~535 |
| Viscosity（100℃）, mm2/s | 9.75 | 6.56 | 10.45 |
| Fusing point, DEG C | 100.3（Melt drop temperature） | 59.0 | 50.2 |
| Sulphur, μ g/g | 1.0 | 15.0 | 26.0 |
| Nitrogen, μ g/g | 1.0 | 2.0 | 3.5 |
| Oil content, wt% | 10.1 | 5.1 | 30.2 |
The catalyst property of table 2
| Catalyst | Isomerization dewaxing |
| Chemical composition, weight % | |
| Platinum (Pt) | 0.2-0.5 |
| Physical property | |
| Appearance and size (φ × L)/mm | (1.4-1.6)×(3~8) |
| Pore volume, mL/g | ≥0.30 |
| Specific surface area, m2/g | ≥180 |
| Bulk density ,/g/cm | 0.65~0.75 |
| Crushing strength, N/cm | ≥100 |
| Shape | Cylindrical bars |
Embodiment 1~3
The raw material of embodiment 1~3 is respectively listed 3 kinds of raw materials in table 1, and isomerization dewaxing catalyst is urged using listed in table 2
Agent.Isomerization dewaxing catalyst is pre-processed using sulfide and nitride, in the preprocessing solution, sulfide used
For the sulphur of diethanol two（50wt%）And dimethyl disulphide（50wt%）Mixture, consumption be catalyst weight 1.0%；Institute
It is aniline with nitride（50wt%）With（50wt%）The mixture of pyridine, consumption is the 0.8% of catalyst weight；Organic solvent is
Catalytically cracked gasoline, consumption of organic solvent is the 10% of catalyst weight.Pre-processed under the atmosphere of air, pretreatment temperature
Spend for 160 DEG C, pretreatment time is 5h.By pretreated catalyst in 10.0MPa, the volume ratio 800 of hydrogen and catalyst,
At 320 DEG C of activation temperature, soak time 16 hours.After hydrogen activation, listed feedstock oil is introduced into table, hydroisomerizing dewaxing is carried out anti-
Should, as a result specifically it is shown in Table 3.
Comparative example 1
Comparative example 1 uses F- T synthesis wax stock, and isomerization dewaxing catalyst uses listed catalyst in table 2.Isomerization dewaxing
Catalyst is pre-processed only with nitride, and nitride used is aniline in the preprocessing solution（50wt%）With
（50wt%）The mixture of pyridine, consumption is the 0.8% of catalyst weight；The organic solvent used is catalytically cracked gasoline, organic
Solvent load is the 10% of catalyst weight.Pre-processed under the atmosphere of air, pretreatment temperature is 160 DEG C, during pretreatment
Between be 5h.By pretreated catalyst in 10.0MPa, the volume ratio 800 of hydrogen and catalyst is living at 320 DEG C of activation temperature
16 hours change time.After hydrogen activation, Fischer Tropsch waxes listed in table 1 are introduced into, hydroisomerizing dewaxing reaction are carried out, as a result specifically
It is shown in Table 4.
Comparative example 2
Comparative example 2 is using F- T synthesis wax stock listed in table 1, and isomerization dewaxing catalyst uses listed in table 2 be catalyzed
Agent.Isomerization dewaxing catalyst is pre-processed only with sulfide, and sulfide used is diethanol in the preprocessing solution
Two sulphur（50wt%）And dimethyl disulphide（50wt%）Mixture, consumption be catalyst weight 1.0%；What is used is organic
Solvent is catalytically cracked gasoline, and consumption of organic solvent is the 10% of catalyst weight.Pre-processed under the atmosphere of air, in advance
Treatment temperature is 160 DEG C, and pretreatment time is 5h.By pretreated catalyst in 10.0MPa, the volume of hydrogen and catalyst
Than 800, at 320 DEG C of activation temperature, soak time 16 hours.After hydrogen activation, Fischer Tropsch waxes listed in table 1 are introduced into, are carried out
Hydroisomerizing dewaxing reaction, is as a result specifically shown in Table 4.
Comparative example 3
Comparative example 2 is using F- T synthesis wax stock listed in table 1, and isomerization dewaxing catalyst uses listed in table 2 be catalyzed
Agent.Isomerization dewaxing catalyst is without pretreatment, directly in 10.0MPa, the volume ratio 800 of hydrogen and catalyst, activation temperature
Under the conditions of 320 DEG C of grades, 16 hours hydrogen Activation Activation time is carried out.Then Fischer Tropsch waxes listed in table 1 are introduced into, are hydrogenated with
Isomerization dewaxing reacts, and is as a result specifically shown in Table 4.
The process conditions and result of the embodiment of table 3
| Test number | Embodiment 1 | Embodiment 2 | Embodiment 3 |
| Feedstock oil | Fischer Tropsch waxes | No. 58 paraffin | The line slack wax that subtracts four |
| The duration of runs/hour | 24 | 24 | 24 |
| Reaction temperature/DEG C | 285 | 290 | 310 |
| Reaction pressure/MPa | 10.0 | 12.0 | 15.0 |
| Hydrogen to oil volume ratio | 800 | 1000 | 1000 |
| Volume space velocity/h-1 | 0.5 | 0.5 | 1.0 |
| Liquid yield, % | 95.6 | 96.8 | 97.6 |
| Purpose product base oil yield, % | 55.0 | 64.2 | 83.9 |
| Base oil viscosity index | 157 | 150 | 138 |
| Base oil pour point/DEG C | -21 | -24 | -24 |
| The duration of runs/hour | 1200 | 800 | 1000 |
| Reaction temperature/DEG C | 288 | 295 | 315 |
| Reaction pressure/MPa | 10.0 | 12.0 | 15.0 |
| Hydrogen to oil volume ratio | 800 | 1000 | 1000 |
| Volume space velocity/h-1 | 0.5 | 0.5 | 1.0 |
| Liquid yield, % | 95.8 | 97.0 | 97.7 |
| Purpose product base oil yield, % | 55.5 | 64.3 | 84.0 |
| Base oil viscosity index | 158 | 151 | 138 |
| Base oil pour point/DEG C | -21 | -24 | -24 |
The process conditions and result of the comparative example of table 4
| Test number | Embodiment 1 | Comparative example 1 | Comparative example 2 | Comparative example 3 |
| The duration of runs/hour | 24 | 24 | 24 | 24 |
| Reaction temperature/DEG C | 285 | 278 | 280 | 270 |
| Reaction pressure/MPa | 10.0 | 10.0 | 10.0 | 10.0 |
| Hydrogen to oil volume ratio | 800 | 800 | 800 | 800 |
| Volume space velocity/h-1 | 0.5 | 0.5 | 0.5 | 0.5 |
| Liquid yield, % | 95.6 | 92.5 | 92.2 | 89.5 |
| Purpose product base oil yield, % | 55.0 | 48.1 | 49.6 | 44.3 |
| Base oil viscosity index | 157 | 147 | 148 | 140 |
| Base oil pour point/DEG C | -21 | -24 | -21 | -18 |
| The duration of runs/hour | 1200 | 1200 | 1200 | 1200 |
| Reaction temperature/DEG C | 288 | 290 | 294 | 297 |
| Reaction pressure/MPa | 10.0 | 10.0 | 10.0 | 10.0 |
| Hydrogen to oil volume ratio | 800 | 800 | 800 | 800 |
| Volume space velocity/h-1 | 0.5 | 0.5 | 0.5 | 0.5 |
| Liquid yield, % | 95.8 | 94.3 | 92.0 | 90.9 |
| Purpose product base oil yield, % | 55.5 | 50.5 | 49.3 | 45.2 |
| Base oil viscosity index | 158 | 151 | 148 | 144 |
| Base oil pour point/DEG C | -21 | -21 | -24 | -21 |
It was found from each data compare in embodiment 1 and comparative example 1~3 from table 4, by the way that isomerization dewaxing catalyst is carried in advance
Enter sulfide and nitride, under the synergy of sulfide and nitride, greatly reduce the activation of isomerization dewaxing catalyst hydrogen
The higher lytic activity of rear initial reaction stage, improves the selectivity of isomerization dewaxing catalyst, so as to improve the liquid of process
Yield and purpose product base oil yield.
Claims (20)
1. a kind of method of high-content wax starting isomeric dewaxing production lube base oil, including following content：
（1）Pre-processed after preprocessing solution is mixed with isomerization dewaxing catalyst, isomerization dewaxing is catalyzed after being pre-processed
Agent；
（2）By step（1）Isomerization dewaxing catalyst loads reactor after obtained pretreatment, carries out hydrogen activation；（3）By feedstock oil
With hydrogen and step（2）Isomerization dewaxing catalyst contact after activation, isomerization dewaxing reaction controlling is in finite concentration hydrogen sulfide atmosphere
Lower progress is enclosed, i.e., hydrogen sulfide content is 10~500 μ L/L in recycle hydrogen；
Wherein, step（1）Described in preprocessing solution include sulfide, nitride and organic solvent.
2. in accordance with the method for claim 1, it is characterised in that：The sulfide is elementary sulfur and sulfur-containing compound.
3. in accordance with the method for claim 2, it is characterised in that：The sulfur-containing compound is double two sulphur of 2,2- dimethylenes
For the ammonia salt of carbamic acid two, two coloured glaze base diamino thiophenes, the thio thing of diethanol two, DMDS carbonic acid diformazan ammonia and sub- two sulphur
One in guanidine-acetic acid, dimethylsulphide, dimethyl disulphide, two tertiary nonylpolysulfides, mercaptide and carbon disulfide
Plant or several.
4. in accordance with the method for claim 1, it is characterised in that：Sulfide consumption is the 0.1~50% of catalyst weight.
5. in accordance with the method for claim 4, it is characterised in that：Sulfide consumption is the 0.2~10% of catalyst weight.
6. in accordance with the method for claim 1, it is characterised in that：The nitride is the nitrogen-containing compound of carbon number 5~20.
7. in accordance with the method for claim 6, it is characterised in that：The nitride is pyridine, quinoline, acridine, benzo a word used for translation
One or more in pyridine, aniline, pyrroles, indoles, carbazole.
8. in accordance with the method for claim 7, it is characterised in that：The nitride is one kind in aniline, pyridine and quinoline
Or it is several.
9. in accordance with the method for claim 1, it is characterised in that：The consumption of the nitride for catalyst weight 0.1~
30%。
10. in accordance with the method for claim 9, it is characterised in that：The consumption of the nitride for catalyst weight 0.2~
5%。
11. in accordance with the method for claim 1, it is characterised in that：The organic solvent is catalytically cracked gasoline, catalytic cracking
One or more in diesel oil, coker gasoline and coker gas oil.
12. in accordance with the method for claim 1, it is characterised in that：Consumption of organic solvent is the 5%~15% of catalyst weight.
13. in accordance with the method for claim 1, it is characterised in that：Step（1）Described in isomerization dewaxing catalyst and pre- place
The pretreatment of reason solution is carried out under the atmosphere of air, vapor or inert gas, and the condition of pretreatment operation is：Temperature
100~280 DEG C, 1~20h of processing time.
14. in accordance with the method for claim 13, it is characterised in that：The condition of pretreatment operation is：120~180 DEG C of temperature,
2~10h of processing time.
15. in accordance with the method for claim 1, it is characterised in that：Step（2）Described in hydrogen activation condition be：Pressure 0.1
The volume ratio 100~2000 of~20.0MPa, hydrogen and catalyst, 150~450 DEG C of Hydrogen activation temperature, Hydrogen activation process
1~20 DEG C/h of programming rate, 8~32h of Hydrogen activation time.
16. in accordance with the method for claim 15, it is characterised in that：Step（2）Described in hydrogen activation condition be：Pressure
5.0~15.0MPa；The volume ratio 500~1000 of hydrogen and catalyst；250~400 DEG C of Hydrogen activation temperature.
17. in accordance with the method for claim 1, it is characterised in that：Step（3）Described isomerization dewaxing reaction condition is：Instead
Answer 250~380 DEG C of temperature, 1.0~18.0MPa of hydrogen dividing potential drop, 0.1~6.0h of volume space velocity during raw material fluid-1, hydrogen to oil volume ratio
400:1~1500:1.
18. in accordance with the method for claim 17, it is characterised in that：Step（3）Described isomerization dewaxing reaction condition is：Instead
Answer 290~350 DEG C of temperature, 10.0~15.0MPa of hydrogen dividing potential drop, 0.2~1.0h of volume space velocity during raw material fluid-1, hydrogen to oil volume ratio
600:1~1000:1.
19. in accordance with the method for claim 1, it is characterised in that：Step（3）In middle recycle hydrogen hydrogen sulfide content be 20~
200μL/L。
20. in accordance with the method for claim 1, it is characterised in that：The feedstock oil is Fischer Tropsch waxes, sweat oil, slack wax
With the one or more in pertroleum wax.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2141733A (en) * | 1983-06-06 | 1985-01-03 | Mobil Oil Corp | Improved catalytic hydrodewaxing process |
| CN1703276A (en) * | 2002-10-08 | 2005-11-30 | 埃克森美孚研究工程公司 | Wax isomerate yield enhancement by oxygenate pretreatment of catalyst |
| CN1703273A (en) * | 2002-10-08 | 2005-11-30 | 埃克森美孚研究工程公司 | Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product |
| CN1861257A (en) * | 2005-05-12 | 2006-11-15 | 中国石油化工股份有限公司 | Treatment method before application of hydrogenation catalyst |
| US7297252B2 (en) * | 2003-01-13 | 2007-11-20 | Exxonmobil Research And Engineering Company | Catalyst activation in the presence of olefinic hydrocarbon for selective naphtha hydrodesulfurization |
-
2014
- 2014-12-06 CN CN201410732111.1A patent/CN105647574B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2141733A (en) * | 1983-06-06 | 1985-01-03 | Mobil Oil Corp | Improved catalytic hydrodewaxing process |
| CN1703276A (en) * | 2002-10-08 | 2005-11-30 | 埃克森美孚研究工程公司 | Wax isomerate yield enhancement by oxygenate pretreatment of catalyst |
| CN1703273A (en) * | 2002-10-08 | 2005-11-30 | 埃克森美孚研究工程公司 | Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product |
| US7297252B2 (en) * | 2003-01-13 | 2007-11-20 | Exxonmobil Research And Engineering Company | Catalyst activation in the presence of olefinic hydrocarbon for selective naphtha hydrodesulfurization |
| CN1861257A (en) * | 2005-05-12 | 2006-11-15 | 中国石油化工股份有限公司 | Treatment method before application of hydrogenation catalyst |
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