CN103102946A - Production method for light lubricant base oil and heavy lubricant base oil - Google Patents
Production method for light lubricant base oil and heavy lubricant base oil Download PDFInfo
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Abstract
The invention relates to a production method for light lubricant base oil and heavy lubricant base oil. The production method is characterized by comprising two operation phases, i.e., a first phase of producing the light lubricant base oil meeting quality requirements from raw oil through hydroisomerization and a second phase of producing the heavy lubricant base oil meeting quality indexes with a heavy lubricant base oil fraction obtained in the first phase used as a raw material for hydroisomerization. The pour points and the viscosity indexes of the light and heavy lubricant base oil are allowed to meet product quality indexes by controlling the depth of hydroisomerization in the two phases. Compared with the prior art, the method provided by the invention has the following advantages: high-quality light and heavy lubricant base oil can be obtained, and the production method is simple and consumes a small amount of energy for operation.
Description
Technical field
The present invention relates to a kind of hydrogen production method that adds of base oil of high viscosity index lubricant.Specifically with the wide fraction waxy oil directly as the charging of hydroisomerization dewax, produce the method for light lubricating oil base oil and heavy base oil of high viscosity index lubricant.
Background technology
Traditional lubricant base production is to adopt solvent treatment, solvent dewaxing process.Its main two steps are to adopt solvent treatment to remove the undesirable components such as aromatic hydrocarbons and solvent dewaxing to guarantee the low temperature flowability of base oil.In addition, generally also to carry out carclazyte or hydrofinishing.
The performance that develops rapidly lubricant base of increasingly strict environmental legislation and mechanical industry has proposed more and more higher requirement.Simultaneously, due to worldwide crude oil in poor quality, make the crude oil quantity that is suitable for producing lubricating oil reduce gradually.Therefore, the development of hydrogenation method production Lubricating Oil Technique is very rapid.Hydrogenation method technique refers to adopt the process of hydrocracking process or hydrotreatment-isomerization dewaxing-hydrofining process integration production lubricant base, and its advantage is that feed flexibility is large, base oil yield is high, by-product value is high.
The shortcoming that traditional hydroisomerization dewax process exists is, during as charging, is difficult to make simultaneously light lubricating oil component and heavy grease component to satisfy simultaneously the requirement of pour point and viscosity index when the waxy oil that adopts full cut or wide fraction.Generally, when heavy grease component pour point was qualified, the viscosity index of light lubricating oil component loss was larger, is difficult to the production viscosity index〉120 API III class light lubricating oil base oil product; And when light lubricating oil component viscosity index was qualified, heavy component can not be as qualified lubricating oil component.
For the problems referred to above, at present prior art adopts the waxy oil raw material is carried out prefractionation, then with each narrow fraction respectively as the raw material of hydroisomerization dewax, solve above-mentioned light lubricating oil base oil and the irreconcilable problem of heavy grease base oil quality.US5,580,442 have proposed a kind of method that hydrocracking tail oil is produced base oil of high viscosity index lubricant.At first the prefractionation of hydrocracking tail oil being reduced pressure cuts out 100 ℃ of viscosity and is respectively 3mm
2/ s, 4mm
2/ s, 6 mm
2/ s and 8mm
2Four narrow fractions of/s, these narrow fractions carry out respectively hydroisomerization dewax, production viscosity index〉100 ℃ of viscosity of 130 are respectively 3mm
2/ s, 4mm
2/ s, 6 mm
2/ s and 8mm
2Four kinds of lube base oil productions of/s.
US7,198,710 have proposed a kind of method of being produced base oil of high viscosity index lubricant by Fischer-Tropsch wax.First Fischer-Tropsch wax is carried out fractionation and obtain light constituent and heavy constituent, then carry out respectively hydroisomerization dewax and reduce the raw material pour point, can obtain the light lubricating oil base oil that pour point meets the demands.The hydroisomerization dewax heavy constituent is because pour point is defective, and the method for employing solvent dewaxing further reduces the pour point of heavy constituent, obtains at last the satisfactory heavy grease base oil product of pour point.
Adopt the narrow fraction waxy oil as the feed process of hydroisomerization dewax, can solve the method for production lightweight and heavy base oil of high viscosity index lubricant, but a plurality of head tanks need to be set, two cover water distilling apparatus are set simultaneously, and (the hydroisomerizing product still need distill, because in reaction process, cracking reaction can occur, the lightweight of generation partly needs further distillation) increased the construction investment of device; And to often switch raw material and frequent adjusting process parameter in actual production, greatly increased the device operation easier and produced a large amount of substandard products.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of hydrogen production method that adds of base oil of high viscosity index lubricant, be that waxy feeds oil is without fractionation, direct charging as hydroisomerization dewax, enter the Hydrodewaxing reaction zone, by controlling the isomerization reaction degree of depth of hydroisomerization dewax reaction zone, make the light lubricating oil base oil product all to meet index request with the pour point heavy grease base oil and viscosity index.
The present invention produces the method for light lubricating oil base oil and heavy grease base oil, comprises two operational phases:
(1) light lubricating oil base oil stage of conforming to quality requirements of stock oil hydroisomerizing production: with the hydrotreatment distillate, the frivolous oil of hydrotreatment, one or more waxy oil in Fischer-Tropsch synthetic wax or hydrocracking tail oil are stock oil, stock oil and hydrogen are mixed into the hydroisomerization dewax reaction zone, carry out hygrogenating isomerization reaction, reaction product is carried out fractionation, obtain respectively the light lubricating oil base oil fractions, the heavy grease base oil fractions, control the hydroisomerizing reaction depth, make pour point and the viscosity index of light lubricating oil base oil fractions all meet index request,
(2) obtain the heavy grease base oil fractions as the hydroisomerizing reaction raw materials take the stage (1), production meets the heavy grease base oil stage of quality index: the hydroisomerization dewax reaction zone stops incoming stock oil, charging is the heavy grease base oil fractions that obtains in the stage (1), control the isomerization reaction degree of depth of hydroisomerization dewax reaction zone, make the pour point of heavy grease base oil and viscosity index all meet index request.
In the inventive method, the target viscosity index of light lubricating oil base oil fractions and heavy grease base oil fractions is generally 120～170 all greater than 120.The pour point index of light lubricating oil base oil fractions and heavy grease base oil fractions all requires lower than-10 ℃, preferably lower than-15 ℃.The pour point of light lubricating oil base oil fractions is-10～-30 ℃, is preferably-15～-27 ℃; The pour point of heavy grease base oil fractions is-10～-25 ℃, is preferably-12～-21 ℃.
In the inventive method, stock oil can be one or more in hydrotreatment distillate, the frivolous oil of hydrotreatment, Fischer-Tropsch synthetic wax or hydrocracking tail oil, and the sulphur content of these raw materials requires lower than 30 μ g/g, preferably lower than 15 μ g/g; Nitrogen content requires lower than 5 μ g/g, preferably lower than 2 μ g/g.To reach noble metal catalyst that hydroisomerization dewax uses to the requirement of raw material impurity content.The hydrotreatment of distillate and frivolous oil or hydrocracking are this area ordinary method, and generally using non-precious metal catalyst, main purpose is the impurity such as deep removal sulphur, nitrogen.Any cut of the boiling range of above-mentioned raw materials oil in 280～700 ℃ of scopes, general initial boiling point to the temperature head of final boiling point between 100～400 ℃.
The hydroisomerization dewax catalyzer that the inventive method is used can be selected this area lube oil hydrogenation heterogeneous catalyst commonly used, also can the commodity in use hydroisomerization catalyst, also can prepare by this area general knowledge.The hydroisomerization catalyst carrier is generally the NU-10 molecular sieve of aluminum oxide and TON structure or ZSM-22 molecular sieve etc., and the content of molecular sieve in catalyzer is 30wt% ~ 80wt%, is preferably 40wt% ~ 70wt%, also can add the partial oxygen SiClx in carrier; Active metal component be in Pt, Pd, Ru and Rh one or more, the content in catalyzer is 0.1wt% ~ 5.0wt%.Selectable adjuvant component is one or more in boron, fluorine, chlorine and phosphorus, and the content in catalyzer is 0.1wt% ~ 5.0wt%; The specific surface of hydroisomerization catalyst is 150～500m
2/ g, pore volume are 0.15～0.60ml/g.Before using, catalyzer is reduced processing, make hydrogenation active metals be in reduction-state in reaction process.
The reaction conditions of described stage (1) and stage (2) hydroisomerization dewax reaction zone is: temperature of reaction is 300 ℃～380 ℃, preferred 310 ℃～340 ℃, the hydrogen dividing potential drop is 2.0MPa～18.0MPa, preferred 10.0MPa～15.0MPa, and during feeding liquid, volume space velocity is 0.2 h
-1～6.0h
-1, preferred 0.5 h
-1～1.8h
-1, hydrogen to oil volume ratio is 400:1～1500:1, preferred 600:1～800:1.
In stage (1) and stage (2), the method for controlling the hydroisomerizing reaction depth is mainly to adjust temperature of reaction, and temperature of reaction raises, and the hydroisomerizing reaction depth increases; Temperature of reaction reduces, and the hydroisomerizing reaction depth reduces.Specifically can by those skilled in the art, require to adjust in above-mentioned scope according to quality product.Stage (1) and stage (2) are used same hydroisomerization dewax reaction zone.Two stages can cyclical operation, and can adjust flexibly the switching time of cyclical operation according to situations such as unit scale, market requirement situations.
In the inventive method, it is 450～520 ℃ that temperature (referring to the true boiling point temperature) is cut apart in the distillation of light lubricating oil base oil fractions and heavy grease base oil fractions, boiling point is the light lubricating oil base oil fractions lower than the lubricant base of cut-point, and boiling point is the heavy lubricant base oil fraction higher than the lubricant base oil fraction of cut-point.Described light lubricating oil base oil fractions can be one or more, and described heavy grease base oil fractions can be also one or more, specifically determines according to the character of raw material.According to present quality standard, No. 4 base oils are light lubricating oil base oil fractions of the present invention, and No. 6 base oils and No. 10 base oils are heavy grease base oil fractions of the present invention.
The working method of fractionation and condition are well-known to those skilled in the art, and as the vacuum distillation method that adopts, the vacuum still feeding temperature is 350 ℃～410 ℃, and more suitable feeding temperature is 375 ℃～400 ℃; The vacuum still tower top pressure is 4KPa～10KPa, and more suitable tower top pressure is 5KPa～8KPa; The vacuum still tower top temperature is 110～180 ℃, can obtain some light-end products.The condition of underpressure distillation generally can be adjusted in above-mentioned scope, obtains required product.If it is more that reacted material contains light component, also can first fractionation in atmospheric fractional tower, and then enter vacuum still and carry out fractionation.2～4 side lines of vacuum still operated by rotary motion, corresponding side line obtains light lubricating oil base oil and heavy grease base oil.100 ℃ of viscosity of light lubricating oil base oil are 2.5-4.5mm
2/ s; 100 ℃ of viscosity of heavy grease base oil are 5.5-10.5mm
2/ s.
Also can increase the hydrofinishing reaction zone after the hydroisomerization dewax reaction zone in the inventive method, improve color and the stability of base oil product.The hydrofinishing catalyzer, reduced form Hydrobon catalyst for routine, its reactive metal is that one or both or the reactive metal in Pt, Pd is the nickel catalyzator of reduction-state, in noble metal catalyst, reactive metal is generally 0.05%～1% at the weight content of catalyzer, the reactive metal of the catalyzer of reduced state nickel counts 30%～80% with oxide weight, and support of the catalyst is generally Al
2O
3Or Al
2O
3-SiO
2, can contain the auxiliary agents such as P, Ti, B, Zr.Use procatalyst to carry out conventional reduction, guarantee that hydrogenation active metals is in reduction-state in reaction process.Can select this field general goods catalyzer, or by the preparation of this area usual way.
Described hydrofinishing reaction conditions is: temperature is 200 ℃～300 ℃, and preferred 210 ℃～280 ℃, the hydrogen dividing potential drop is 6.0MPa～18.0MPa, preferred 10.0～15.0MPa, and during liquid, volume space velocity is 0.3h
-1～3.0h
-1, be preferably 0.6h
-1～1.2h
-1, hydrogen to oil volume ratio is 400:1～1500:1, preferred 600:1～800:1.
The inventive method by to the waxy oil hydroisomerization dewax process analysis know, under identical hydroisomerization dewax condition, the isomerization dewaxing degree of depth of weight component is different, for reaching identical pour point requirement, must control the reaction depth of isomerization dewaxing process, make weight component in waxy oil reach respectively the best dewaxing degree of depth, thereby realize reaching optimal balance point between the pour point of light, heavy lubricating oil base oil product and viscosity index.The inventive method is in the stage (1), raw material all carries out hydroisomerizing, but the quality that the control hydroisomerizing degree of depth is the light lubricating oil base oil meets the requirements, the heavy grease base oil fractions can't reach specification of quality, through the stage (2), targetedly the heavy lubricant base oil fraction is carried out hydroisomerization dewax, so the inventive method is suitable to wide fraction raw material production light lubricating oil base oil and heavy grease base oil.
Compared with prior art, the inventive method need not the waxy oil raw material is carried out prefractionation, namely can solve the qualified lightweight of pour point and the method for heavy base oil of high viscosity index lubricant of producing.A heavy grease base oil fractions storage tank is set after separation column.Carry out blocked operation suitable opportunity, this part tail oil as the hydroisomerization dewax charging, is mixed into reaction zone with hydrogen, produce light, heavy grease base oil product, solved the problem of producing the Raw deficiency, thing has used, increases economic benefit.
Embodiment
The present invention adopts semi-batch to produce the method for base oil of high viscosity index lubricant, one or more waxy oil in hydrotreatment distillate, the frivolous oil of hydrotreatment, Fischer-Tropsch wax or the hydrocracking tail oil are as raw material, raw material and hydrogen are mixed into the hydroisomerization dewax reaction zone, carry out hygrogenating isomerization reaction, reaction product is carried out fractionation, obtains respectively light lubricating oil base oil fractions, heavy grease base oil fractions.The heavy grease base oil fractions derives at the bottom of the tower and enters a storage tank, when running up to some amount, is mixed into reaction zone by switch means as hydroisomerization dewax raw material and hydrogen.By parameter adjustment, control the isomerization reaction degree of depth of hydroisomerization dewax reaction zone, make lube base oil production pour point and viscosity index meet index request.
The various catalyzer that the present invention relates to can be selected commercial catalyst by character, also can prepare by this area knowledge.The FIW-1 catalyzer of hydroisomerization dewax catalyzer such as Fushun Petrochemical Research Institute's development and production also can be by the existing patented technology preparation such as CN03133557.8, CN02133128.6.
As press as described in CN02133128.6, the hydroisomerization dewax support of the catalyst is NU-10 molecular sieve or the ZSM-22 molecular sieve of aluminum oxide and TON structure; The content of molecular sieve in catalyzer is 30wt% ~ 80wt%; Active metal component be in Pt, Pd, Ru, Rh and Ni one or more, the content in catalyzer is 0.1wt% ~ 30.0wt%; Its specific surface is 150～500m
2/ g, pore volume are 0.15～0.60ml/g.The FIW-1 catalyzer of recommending Fushun Petrochemical Research Institute to produce.
Particular content and effect below by specific embodiment explanation the inventive method.
Following implementation column will be further described method provided by the invention, but scope not thereby limiting the invention.The feedstock property that the present invention processes sees Table 1, and the physico-chemical property of the hydroisomerization dewax catalyzer of employing sees Table 2.
Table 1 embodiment feedstock property.
| Stock oil | Hydrocracking tail oil | Hydrotreatment VGO | The Fischer-Tropsch synthetic wax |
| Density, kg/m 3 | 846 | 862 | 796 |
| The boiling range scope, ℃ | 322～510 | 345～535 | 290～652 |
| Viscosity (100 ℃), mm 2/s | 6.35 | 8.548 | 12.23 |
| Pour point, ℃ | 32 | 34 | The 105(melt drop temperature) |
| Sulphur, μ g/g | 5.0 | 14.0 | 2.0 |
| Nitrogen, μ g/g | 1.0 | 1.5 | 2.0 |
| Wax content, wt% | 24.8 | 30.1 | 6.71(oleaginousness) |
Table 2 catalyst property.
| Catalyzer | Isomerization dewaxing |
| Chemical constitution, % by weight | ? |
| Platinum (Pt) | 0.2-0.5 |
| Physical properties | ? |
| Physical dimension (φ * L), mm | (1.4-1.6)×(3~8) |
| Pore volume, mL/g | ≥0.30 |
| Specific surface area, m 2/g | ≥180 |
| Tap density, g/cm 3 | 0.65~0.75 |
| Crushing strength, N/cm | ≥100 |
| Shape | Cylindrical bars |
Embodiment 1 ~ 3
Embodiment 1 ~ 3, and stock oil and hydrogen are mixed into the hydroisomerization dewax reaction zone, and reaction product obtains light lubricating oil base oil fractions and heavy grease base oil fractions through fractionation.Raw material is respectively 3 kinds of raw materials listed in table 1, the FIW-1 catalyzer that the catalyzer that hydroisomerization dewax uses is produced as Fushun Petrochemical Research Institute, and its character sees Table 2.The embodiment result specifically sees Table 3.Hydroisomerization catalyst is implemented after reducing according to a conventional method.After fs hydroisomerization dewax reaction, the reaction product vacuum still obtains light lubricating oil base oil fractions (No. 4 base oil fractions), with the heavy grease base oil fractions, the heavy grease base oil fractions runs up to some amount carries out the processing of subordinate phase hydroisomerization dewax, and the reaction product fractionation obtains No. 6 base oil fractions and No. 10 base oil fractions.The cut-point of light lubricating oil base oil fractions and heavy grease base oil fractions is controlled to be 480 ℃.
Comparative Examples 1
Comparative Examples 1 adopts listed hydrocracking tail oil raw material in table 1, adopt a stage hydroisomerization dewax reaction, use hydroisomerization dewax catalyzer in the same manner as in Example 1, the reaction product fractionation obtains No. 4 base oil fractions, No. 6 base oil fractions and No. 10 base oil fractions, the results are shown in Table 3.
Comparative Examples 2
Comparative Examples 2 adopts listed hydrocracking tail oil raw material in table 1, and hydrocracking tail oil is carried out prefractionation, obtains 100 ℃ of viscosity and is respectively 4.2mm
2/ s and 6.3mm
2/ s hydrocracking tail oil narrow fraction, the technological process of then carrying out respectively the hydroisomerization dewax reaction is used hydroisomerization dewax catalyzer in the same manner as in Example 1, the results are shown in Table 3.
Comparative Examples 3
Comparative Examples 3 adopts listed Fischer-Tropsch synthetic wax raw material in table 1, will carry out the Fischer-Tropsch wax prefractionation, obtains 100 ℃ of viscosity and is respectively 4.05mm
2/ s, 6.5mm
2/ s and 8.46mm
2The Fischer-Tropsch wax narrow fraction of/s, the technological process of then carrying out respectively the hydroisomerization dewax reaction is used hydroisomerization dewax catalyzer in the same manner as in Example 1, the results are shown in Table 3.
The comparative data of embodiment and Comparative Examples as can be known, concerning raw material does not carry out the prior art scheme of prefractionation, can not be taken into account the quality index of light lubricating oil base oil fractions and heavy grease base oil fractions from table 3.Carry out for raw material the prior art scheme that prefractionation is processed, although also can get qualified weight lubricant base, process is complicated.
The processing condition of table 3 embodiment and Comparative Examples and result.
| Test number | Embodiment 1 | Comparative Examples 1 | Comparative Examples 2 |
| Stock oil | 1 | 1 | 1 |
| Isomerization dewaxing district processing condition | ? | ? | ? |
| Temperature of reaction/℃ | Fs 305/ subordinate phase 320 | 320 | 305/330* |
| Reaction pressure/MPa | 9.0 | 9.0 | 9.0 |
| Hydrogen to oil volume ratio | 600 | 600 | 800 |
| Volume space velocity/h -1 | Fs 1.2/ subordinate phase 1.5 | 1.0 | 1.2 |
| Base oil character | ? | ? | ? |
| No. 4 base oils | ? | ? | ? |
| Yield, quality % | 23.6 | 14.5 | 23.5 |
| Pour point/℃ | -18 | -36 | -18 |
| Viscosity (100 ℃), mm/s 2 | 4.023 | 4.282 | 4.261 |
| Viscosity index | 123 | 99 | 122 |
| No. 6 base oils | ? | ? | ? |
| Yield, quality % | 19.8 | 17.8 | 19.5 |
| Pour point/℃ | -18 | -24 | -18 |
| Viscosity (100 ℃), mm/s 2 | 6.015 | 6.342 | 6.088 |
| Viscosity index | 126 | 111 | 126 |
| No. 10 base oils | ? | ? | ? |
| Yield, quality % | 34.5 | 36.5 | ** |
| Pour point/℃ | -15 | -9 | ** |
| Viscosity (100 ℃), mm/s 2 | 10.012 | 9.984 | ** |
| Viscosity index | 128 | 124 | ** |
3(is continuous for table) processing condition and the result of embodiment and Comparative Examples.
| Test number | Embodiment 2 | Embodiment 3 | Comparative Examples 3 |
| Stock oil | 2 | 3 | 3 |
| Isomerization dewaxing district processing condition | ? | ? | ? |
| Temperature of reaction/℃ | Fs 308/ subordinate phase 325 | Fs 316/ subordinate phase 345 | 310/320/340* |
| Reaction pressure/MPa | 12.0 | 15.0 | 15.0 |
| Hydrogen to oil volume ratio | 800 | 800 | 800 |
| Volume space velocity/h -1 | Fs 1.2/ subordinate phase 1.5 | Fs 1.2/ subordinate phase 1.5 | 0.7 |
| Base oil character | ? | ? | ? |
| No. 4 base oils | ? | ? | ? |
| Yield, quality % | 18.9 | 27.5 | 27.6 |
| Pour point/℃ | -24 | -21 | -21 |
| Viscosity (100 ℃), mm/s 2 | 4.035 | 4.012 | 4.01 |
| Viscosity index | 121 | 128 | 129 |
| No. 6 base oils | ? | ? | ? |
| Yield, quality % | 29.3 | 15.5 | 16.5 |
| Pour point/℃ | -21 | -18 | -18 |
| Viscosity (100 ℃), mm/s 2 | 6.283 | 6.015 | 6.184 |
| Viscosity index | 124 | 134 | 135 |
| No. 10 base oils | ? | ? | ? |
| Yield, quality % | 25.2 | 33.2 | 32.9 |
| Pour point/℃ | -15 | -15 | -12 |
| Viscosity (100 ℃), mm/s 2 | 5.498 | 8.325 | 8.324 |
| Viscosity index | 129 | 142 | 146 |
* the hydroisomerization dewax temperature of reaction of each narrow fraction, the light ends temperature of reaction is low, and the heavy ends temperature of reaction is high;
The * product can not be as lubricant base.
Claims (13)
1. method of producing light lubricating oil base oil and heavy grease base oil is characterized in that comprising two operational phases:
(1) light lubricating oil base oil stage of conforming to quality requirements of stock oil hydroisomerizing production: with the hydrotreatment distillate, the frivolous oil of hydrotreatment, one or more waxy oil in Fischer-Tropsch synthetic wax or hydrocracking tail oil are stock oil, stock oil and hydrogen are mixed into the hydroisomerization dewax reaction zone, carry out hygrogenating isomerization reaction, reaction product is carried out fractionation, obtain respectively the light lubricating oil base oil fractions, the heavy grease base oil fractions, control the hydroisomerizing reaction depth, make pour point and the viscosity index of light lubricating oil base oil fractions all meet light lubricating oil base oil index request,
(2) obtain the heavy grease base oil fractions as the hydroisomerizing reaction raw materials take the stage (1), production meets the heavy grease base oil stage of quality index: the hydroisomerization dewax reaction zone stops incoming stock oil, charging is the heavy grease base oil fractions that obtains in the stage (1), control the isomerization reaction degree of depth of hydroisomerization dewax reaction zone, make the pour point of heavy grease base oil fractions and viscosity index all meet heavy grease base oil index request.
2. in accordance with the method for claim 1, it is characterized in that: the target viscosity index of light lubricating oil base oil fractions and heavy grease base oil fractions is all greater than 120, and the pour point index of light lubricating oil base oil fractions and heavy grease base oil fractions all requires lower than-10 ℃.
3. in accordance with the method for claim 1, it is characterized in that: the target viscosity index of light lubricating oil base oil fractions and heavy grease base oil fractions is 120～170, the pour point of light lubricating oil base oil fractions is-10～-30 ℃, and the pour point of heavy grease base oil fractions is-10～-25 ℃.
4. in accordance with the method for claim 1, it is characterized in that: the stock oil in stage (1) is one or more in hydrotreatment distillate, the frivolous oil of hydrotreatment, Fischer-Tropsch synthetic wax or hydrocracking tail oil, sulphur content requires lower than 30 μ g/g, and nitrogen content requires lower than 5 μ g/g.
5. according to the described method of claim 1 or 4, it is characterized in that: any cut of the boiling range of the stock oil in stage (1) in 280～700 ℃ of scopes, initial boiling point to the temperature head of final boiling point between 100～400 ℃.
6. in accordance with the method for claim 1, it is characterized in that: the hydroisomerization dewax reaction zone uses the hydroisomerization dewax catalyzer, the hydroisomerization dewax support of the catalyst is NU-10 molecular sieve or the ZSM-22 molecular sieve of aluminum oxide and TON structure, the content of molecular sieve in catalyzer is 30wt% ~ 80wt%, active metal component be in Pt, Pd, Ru and Rh one or more, the content in catalyzer is 0.1wt% ~ 5.0wt%.
7. in accordance with the method for claim 1, it is characterized in that: the reaction conditions of the hydroisomerization dewax reaction zone in stage (1) and stage (2) is: temperature of reaction is 300 ℃～380 ℃, the hydrogen dividing potential drop is 2.0MPa～18.0MPa, and during feeding liquid, volume space velocity is 0.2 h
-1～6.0h
-1, hydrogen to oil volume ratio is 400:1～1500:1.
8. in accordance with the method for claim 7, it is characterized in that: in stage (1) and stage (2), the method for controlling the hydroisomerizing reaction depth is to adjust temperature of reaction, and temperature of reaction raises, and the hydroisomerizing reaction depth increases; Temperature of reaction reduces, and the hydroisomerizing reaction depth reduces.
9. it is characterized in that in accordance with the method for claim 1: stage (1) and stage (2) are used same hydroisomerization dewax reaction zone.
10. it is characterized in that in accordance with the method for claim 1: stage (1) and stage (2) cyclical operation.
11. in accordance with the method for claim 1, it is characterized in that: it is 450～520 ℃ that temperature is cut apart in the distillation of light lubricating oil base oil fractions and heavy grease base oil fractions, boiling point is the light lubricating oil base oil fractions lower than the lubricant base of cut-point, and boiling point is the heavy lubricant base oil fraction higher than the lubricant base oil fraction of cut-point.
12. in accordance with the method for claim 1, it is characterized in that: increase the hydrofinishing reaction zone after the hydroisomerization dewax reaction zone, the hydrofinishing reaction zone uses the reduced form Hydrobon catalyst as routine, its reactive metal is that one or both or the reactive metal in Pt, Pd is the nickel catalyzator of reduction-state, in noble metal catalyst, reactive metal is generally 0.05%～1% at the weight content of catalyzer, and the reactive metal of the catalyzer of reduced state nickel counts 30%～80% with oxide weight.
13. in accordance with the method for claim 12, it is characterized in that: the hydrofinishing reaction conditions is: temperature is 200 ℃～300 ℃, and the hydrogen dividing potential drop is 6.0MPa～18.0MPa, and during liquid, volume space velocity is 0.3h
-1～3.0h
-1, hydrogen to oil volume ratio is 400:1～1500:1.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103289738A (en) * | 2013-06-25 | 2013-09-11 | 中石化南京工程有限公司 | Combination method for producing high-grade lubricant base oil by hydrogenating hydrocracking tail oil |
| CN108031486A (en) * | 2017-11-30 | 2018-05-15 | 西北化工研究院 | The preparation method and application of the waxed standby lube base oil catalyst of Fischer-Tropsch lighter component |
| CN109164075A (en) * | 2018-08-31 | 2019-01-08 | 北方华锦化学工业股份有限公司 | The method of ultraviolet fluorescence method analysis heavy wax oil samples |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103289738A (en) * | 2013-06-25 | 2013-09-11 | 中石化南京工程有限公司 | Combination method for producing high-grade lubricant base oil by hydrogenating hydrocracking tail oil |
| CN103289738B (en) * | 2013-06-25 | 2015-10-28 | 中石化南京工程有限公司 | A kind of hydrocracking tail oil hydrogenation produces the combined method of top-grade lubricating oil base oil |
| CN108031486A (en) * | 2017-11-30 | 2018-05-15 | 西北化工研究院 | The preparation method and application of the waxed standby lube base oil catalyst of Fischer-Tropsch lighter component |
| CN108031486B (en) * | 2017-11-30 | 2020-09-18 | 西北化工研究院 | Preparation method and application of catalyst for preparing lubricating oil base oil from Fischer-Tropsch light component wax |
| CN109164075A (en) * | 2018-08-31 | 2019-01-08 | 北方华锦化学工业股份有限公司 | The method of ultraviolet fluorescence method analysis heavy wax oil samples |
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| CN103102946B (en) | 2015-07-22 |
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