CN103102948A - Production process for lubricant base oil through hydrogenation - Google Patents
Production process for lubricant base oil through hydrogenation Download PDFInfo
- Publication number
- CN103102948A CN103102948A CN2011103534717A CN201110353471A CN103102948A CN 103102948 A CN103102948 A CN 103102948A CN 2011103534717 A CN2011103534717 A CN 2011103534717A CN 201110353471 A CN201110353471 A CN 201110353471A CN 103102948 A CN103102948 A CN 103102948A
- Authority
- CN
- China
- Prior art keywords
- reaction
- base oil
- hydrofinishing
- oil
- hydrogenation
- 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.)
- Granted
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a production process for lubricant base oil through hydrogenation. The process provided by the invention employs inverted-sequence procedures consisting of hydrofinishing, hydrogenation isodewaxing and post hydrogenation refining for production of the lubricant base oil. Raw materials enters into a hydrogenation isodewaxing reactor at first and then undergoes fractionation to obtain light lubricant base oil with a qualified pour point, a high viscosity index and low content of aromatic hydrocarbon. A heavy lubricant base oil part is recycled to a hydrofinishing reactor for in-depth removal of aromatic hydrocarbon in the raw materials so as to improve the color and stability of the heavy lubricant base oil, and the heavy lubricant base oil part and the raw materials enter into the hydrogenation isodewaxing reactor together for further reduction of a condensation point. According to the invention, through reasonable sequencing of the procedures, reasonable matching of reaction temperatures in the processes of hydrofinishing and hydrogenation isodewaxing is realized, the purpose of safe, flexible and effective adjusting of reaction temperature of hydrorefining is realized, activity of a hydrorefining catalyst is allowed to be better performed, and a lubricant base oil product has better properties.
Description
Technical field
The present invention relates to a kind of hydrogenation and produce the processing method of lubricant base.The processing method that adopts the inverted sequence technological process production lubricant base made from extra care after hydrofinishing-hydroisomerization dewax-hydrogenation specifically.
Background technology
Traditional lubricant base production is to adopt solvent treatment technique, and 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.
Hydrogenation method is produced Lubricating Oil Technique and is all adopted first hydroisomerization dewax or Hydrodewaxing both at home and abroad at present, carry out again the process of hydrofining or post-refining, as US 6,569,313, US 6,264,826, US 6,337, the disclosed Lubricating oil base oil producing method such as 010, all take hydrotreatment oil as raw material, adopt hydroisomerization dewax-hydrofining technology flow process to produce lubricant base.
When adopting hydroisomerization dewax-hydrofining technology flow process, the temperature of reaction of hydroisomerization dewax is higher, the temperature of reaction of hydrofining technology is lower, in order to realize both Temperature Matchings, generally hydroisomerization dewax reaction effluent and raw material are carried out the heat exchange cooling, then enter hydrofining reactor.When adopting interchanger that material is lowered the temperature, insensitive to the control of temperature of charge, cause the problem of the more difficult adjusting of hydrofining reaction temperature, affected the performance of Hydrobon catalyst activity, the handiness of device operation is restricted.Simultaneously, in order to adjust heat-exchange temperature, also need to be set up in parallel cross-line with interchanger, interchanger is often processed the adjustment state, can not be in desirable design effort state, and the heat exchanging effectiveness affects is obvious, and capacity usage ratio reduces.
Summary of the invention
For the deficiencies in the prior art, the invention provides the method for the inverted sequence technological process production lubricant base made from extra care after a kind of hydrofinishing-hydroisomerization dewax-hydrogenation.
the processing method that hydrogenation of the present invention is produced lubricant base specifically comprises following content: with the hydrotreatment distillate, one or more in the frivolous oil of hydrotreatment or hydrocracking tail oil are stock oil, stock oil mixes with hydrofinishing reaction zone reaction effluent, through after being heated to the hydroisomerizing temperature of reaction, enter the hydroisomerizing reaction zone and carry out the hydroisomerizing reaction, the hydroisomerizing reaction zone sets gradually hydroisomerization catalyst and rare hydrocarbon saturation catalyst by the mobile direction of reaction mass, hydroisomerizing reaction zone reaction effluent enters separation system, obtain light lubricating oil base oil and heavy grease base oil, the heavy grease base oil is partly discharged as product, remainder enters the hydrofinishing reaction zone, carry out the hydrofinishing reaction under hydrogen and the existence of hydrofinishing catalyzer.
In the inventive method, the new hydrogen that replenishes can enter the hydroisomerizing reaction zone, also can enter the hydrofinishing reaction zone.
In the inventive method, the heavy grease base oil that enters the hydrofinishing reaction zone is 0.2:1～5:1 with the mass ratio (abbreviation recycle ratio) of discharging as the heavy grease base oil of product, is preferably 0.5:1～2:1.
In the inventive method, separation system generally comprises high-pressure separator, light pressure separator and separation column.The cut-point temperature of light lubricating oil base oil fractions and heavy grease base oil fractions is 450～520 ℃, be in vacuum still, 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, boiling point partly enters the hydrofinishing reaction zone higher than the heavy grease base oil fractions of cut-point, and remainder is discharged as product.
In the inventive method, sulphur content and the nitrogen content of stock oil (one or more in hydrotreatment distillate, the frivolous oil of hydrotreatment or hydrocracking tail oil etc.) all require lower than 20 μ g/g, preferably lower than 10 μ g/g, with the requirement to raw material impurity content of the noble metal catalyst that reaches hydrofinishing, hydroisomerizing and rear refining use or reduced state nickel catalyzer.Hydrotreatment or hydrocracking are this area ordinary method, generally use non-precious metal catalyst, and main purpose is the impurity such as deep removal sulphur, nitrogen.
Catalyst for refining after the hydrofinishing catalyzer that the inventive method is used and hydrogenation, reduced form Hydrobon catalyst for routine, its reactive metal is that one or both or the reactive metal in Pt, Pd is the reduced state nickel catalyzer, in noble metal catalyst, reactive metal is generally 0.05%～1% at the weight content of catalyzer, the reactive metal of reduced state nickel catalyzer 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.After hydrofinishing catalyzer and hydrogenation, catalyst for refining can be identical, also can be different, be preferably identical catalyzer.
The hydroisomerization dewax catalyzer that the inventive method is used can anthology field lube oil hydrogenation heterogeneous catalyst commonly used, 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 hydroisomerization dewax is: temperature is 260 ℃～380 ℃, and preferred 280 ℃～350 ℃, the hydrogen dividing potential drop is 4.0MPa～18.0MPa, and preferred 10.0～15.0MPa, volume space velocity are 0.6 h
-1～2.0h
-1, preferred 0.8 h
-1～1.5h
-1, hydrogen to oil volume ratio 400:1～1500:1, preferred 600:1～800:1.
Described hydrofinishing reaction conditions is: temperature is 200 ℃～320 ℃, and preferred 220 ℃～280 ℃, the hydrogen dividing potential drop is 8.0MPa～18.0MPa, and preferred 10.0～15.0MPa, volume space velocity are 0.4 h
-1～6.0h
-1, preferred 0.8 h
-1～1.5h
-1, hydrogen to oil volume ratio 400:1～1500:1, preferred 600:1～800:1.
After described hydrogenation, the refining reaction condition is: temperature is 300 ℃～380 ℃, and preferred 320 ℃～350 ℃, the hydrogen dividing potential drop is 8.0MPa～18.0MPa, and preferred 10.0～15.0MPa, volume space velocity are 3.0h
-1～15.0h
-1, be preferably 5.0h
-1～10.0h
-1, hydrogen to oil volume ratio 400:1～1500:1, preferred 600:1～800:1.
Refining noble metal catalyst or the reduced state nickel catalyzer of using after hydrofinishing, hydroisomerization dewax and hydrogenation, the hydroisomerization dewax temperature of reaction is higher 50～180 ℃ than hydrofinishing temperature of reaction, and is preferred high 80～140 ℃; After hydrogenation during refining liquid volume space velocity be 3～15 times of hydroisomerization dewax volume space velocity, be preferably 5～10 times.
Reaction pressure refining after hydroisomerization dewax, hydrofinishing and hydrogenation is the uniform pressure grade, and the hydroisomerization dewax reaction product is directly carried out the hydrofinishing reaction, need not carry out the temperature adjustment.
In the inventive method, in " refining after hydrofinishing-hydroisomerization dewax-hydrogenation " inverted sequence technical process, total scale (being total catalyst for refining consumption) refining after hydrofinishing and hydrogenation lacks nearly 40% than the hydrofinishing scale of prior art " hydroisomerization dewax-hydrofinishing ", and the post-refining reactor of this technique is less than the post-refining reactor of positive sequence, and cost is lower.
In the inventive method, well heater can be steam heater or thermal fluid heater etc., with the convenient hydrofining reaction temperature of adjusting.In the inventive method, hydrofinishing is arranged in a reactor, refining being arranged in a reactor after hydroisomerization dewax and hydrogenation.Quantity and the prior art of reactor remain unchanged.
In the inventive method; the heavy grease base oil fractions is carried out hydrofinishing; be conducive to improve heavy grease base oil product quality; reaction effluent after hydrofinishing carries out hydroisomerizing again; be conducive to reduce the pour point of heavy grease base oil, simultaneously the higher viscosity index of protection.The light lubricating oil base oil that the inventive method obtains and heavy grease base oil all have lower pour point and higher viscosity index simultaneously.
according to this area general knowledge and prior art, adopt the operation of hydroisomerization dewax-hydrofinishing to produce lubricant base, due to the temperature of reaction of the hydroisomerization dewax general high 100 ℃ of left and right of temperature of reaction than hydrofinishing, the reaction product of hydroisomerization dewax is after heat exchange reaches suitable temperature, just can enter hydrofinishing reaction zone device, because the heat interchanging area of this interchanger can't change, generally by adding the cross-line bypass for this interchanger, the flow of the reaction product heat exchange logistics of change and hydroisomerization dewax, realize regulating the temperature of reaction of hydrofinishing.Having a plurality of valves in bypass due to high pressure heat exchanger, is the major hidden danger of whole high-pressure hydrogenation security of system operation.The present invention analyses in depth by the technological process of hydrogenation method being produced lubricant base and learns, by exchange hydroisomerization dewax and the order of hydrofinishing in technological process, and Hydrobon catalyst is in the suitable distribution in hydroisomerization dewax front and back, hydroisomerization dewax and hydrorefined temperature of reaction are reasonably mated, by with the heat exchange of hydroisomerization dewax product and steam or thermal barrier heating, realize the flexible of hydrofining reaction temperature.Because the hydroisomerization dewax process will produce a small amount of alkene, the present invention's employing catalyst for refining after a small amount of hydrogenation of hydroisomerization dewax reactor lower part filling reaches olefin saturated, due to the hydrofinishing of temperature of reaction higher than routine, therefore speed of response is fast, only need a small amount of hydrofinishing catalyzer, can improve the stability of lubricant base.The advantages such as it is simple that the present invention has technical process, and the high-pressure hydrogenation security of system is reliable, and the hydrofining reaction temperature regulation is flexible, is conducive to the Hydrobon catalyst activity and brings into play better, and the lubricant base product property is better.
Description of drawings
Fig. 1 is the inventive method process flow diagram.
Wherein: 1-stock oil, the new hydrogen of 2-, 3-recycle hydrogen, 4-hydrofinishing reactor, 5-hydroisomerization reactor, 6-high-pressure separator, 7-light pressure separator, 8-separation column, 9-light lubricating oil base oil fractions, 10-heavy grease base oil fractions.
Embodiment
In the inventive method, the heavy grease base oil that aromaticity content is high partly is circulated to the hydrofinishing reactor and carries out the reaction of degree of depth aromatic saturation, improve color and the stability of heavy basestock, then enter together the hydroisomerization dewax reactor with raw material and further reduce condensation point, obtain the qualified heavy grease base oil product of pour point after fractionation, part heavy grease base oil continues circulation, until whole flow process reaches balance.
The present invention produces the method for lubricant base and specifically sees Fig. 1: at first raw material enters the hydroisomerization dewax reactor, control the isomery degree of depth, reduce pour point, then the alkene that the saturation isomerism process produces carry out fractionation and obtain the light lubricating oil base oil that pour point is qualified, viscosity index is high, aromaticity content is low.The heavy grease base oil partly is circulated to the aromatic hydrocarbons in hydrofinishing reactor deep removal raw material, improve color, improve stability, then enter together the hydroisomerization dewax reactor with raw material and further reduce condensation point, obtain the qualified heavy grease base oil product of pour point after fractionation, part heavy grease base oil continues circulation, until whole flow process reaches balance.
The various catalyzer that the present invention relates to can be selected commercial catalyst by character, also can prepare by this area knowledge.After hydrofinishing and hydrogenation, catalyst for refining adopts conventional Hydrobon catalyst such as the FHDA-1 catalyzer of Fushun Petrochemical Research Institute's development and production, also can be by the reduced form Hydrobon catalyst of the described preparation of CN00123149.9.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 CN00123149.9, take aluminum oxide as carrier, preparation contains molybdenum oxide 2%～9% by weight, and the catalyzer of nickel oxide 5%～40%, specific surface area of catalyst are 100～250m
2/ g, pore volume are 0.20～0.35ml/g.
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.
It is simple that the present invention has technical process, and the high-pressure hydrogenation security of system is reliable, and hydrofinishing temperature of reaction flexible adjustment can obtain pour point and viscosity index qualified light, the basic wet goods characteristics of heavy grease simultaneously.
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 hydrofining of employing and hydroisomerization dewax catalyzer sees Table 2.
Table 1 embodiment feedstock property.
| Stock oil | 1 | 2 | 3 |
| Density, kg/m 3 | 844.3 | 855.6 | 865.9 |
| The boiling range scope, ℃ | 322～450 | 345～555 | 352～585(78 quality %) |
| Viscosity (100 ℃), mm 2/s? | 5.35 | 8.336 | 12.23 |
| Pour point, |
10 | 34 | 52 |
| Flash-point (opening), ℃ | 156 | 245 | 254 |
| Sulphur, μ g/g | 4.0 | 12 | 8.8 |
| Nitrogen, μ g/g | 1.2 | 1.8 | 1.6 |
| Wax content, wt% | 4.8 | 34.1 | 51.1 |
Table 2 catalyst property.
| Catalyzer | Isomerization dewaxing | Refining after hydrofinishing and hydrogenation |
| Chemical constitution, % by weight | ? | ? |
| Platinum (Pt) | 0.3 | 0.2 |
| Palladium (Pd) | --- | 0.3 |
| Physical properties | ? | ? |
| Physical dimension (diameter * length), mm | (1.4-1.6)×(3~8) | (1.4-1.6)×(3~8) |
| Pore volume, mL/g | ≥0.30 | ≥0.40 |
| Specific surface area, m 2/g | ≥180 | ≥180 |
| Tap density, g/cm 3 | 0.65~0.75 | 0.60~0.75 |
| Crushing strength, N/cm | ≥100 | >70 |
| Shape | Cylindrical bars | Bar shaped |
Embodiment 1 ~ 3
Embodiment 1 ~ 3 adopts the inverted sequence technological process made from extra care after hydrofinishing-hydroisomerization dewax-hydrogenation, listed 3 kinds of raw materials in processing list 1, wherein make with extra care after hydroisomerization dewax, hydrofinishing and hydrogenation and use respectively listed catalyzer in table 2, obtain result and specifically see Table 3.Hydroisomerizing and Hydrobon catalyst are implemented after reducing according to a conventional method.No. 4 base oils and No. 6 base oils are the light lubricating oil base oil fractions, and No. 10 base oils are the heavy lubricant base oil fraction.
Comparative Examples 1 ~ 3
Comparative Examples adopts hydroisomerization dewax-hydrogenation post-refining process process, use with embodiment 1 ~ 3 in corresponding raw material and identical hydrofining and hydroisomerization dewax catalyzer, the results are shown in Table 3.
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 | 2 | 2 |
| The hydroisomerization dewax processing condition | ? | ? | ? | ? |
| Temperature of reaction/℃ | 320 | 320 | 330 | 330 |
| Reaction pressure/MPa | 10.0 | 10.0 | 12.0 | 12.0 |
| Hydrogen to oil volume ratio | 600 | 600 | 800 | 800 |
| Volume space velocity/h -1 | 1.2 | 1.2 | 1.0 | 1.0 |
| Process for refining condition after hydrogenation | ? | ? | ? | ? |
| Temperature of reaction/℃ | 320 | / | 330 | / |
| Reaction pressure/MPa | 10.0 | / | 12.0 | / |
| Hydrogen to oil volume ratio | 600 | / | 800 | / |
| Volume space velocity/h -1 | 6.0 | / | 6.0 | / |
| The hydrogenation post-refining process condition | ? | ? | ? | ? |
| No. 10 base oil recycle ratios | 1：1 | / | 0.8：1 | / |
| Temperature of reaction/℃ | 220 | 200 | 235 | 210 |
| Reaction pressure/MPa | 10.0 | 10.0 | 12.0 | 12.0 |
| Hydrogen to oil volume ratio | 600 | 600 | 800 | 800 |
| Volume space velocity/h -1 | 1.2 | 1.0 | 1.0 | 0.86 |
| 350 ℃ of lube base oil natures | ? | ? | ? | ? |
| Yield, quality % | 82.37 | 82.31 | 79.35 | 79.29 |
| Pour point/℃ | -33 | -33 | -24 | -24 |
| Viscosity (40 ℃), mm/s 2 | 22.15 | 22.10 | 31.54 | 31.59 |
| Viscosity (100 ℃), mm/s 2 | 4.398 | 4.382 | 5.561 | 5.583 |
| Viscosity index | 107 | 106 | 115 | 114 |
| Color (Sai Shi)/number | >+30 | +22 | >+30 | +30 |
| Sulfuric acid color test | By | Do not pass through | By | Do not pass through |
| Oxidation stability, 150 ℃/min | >300 | 220 | >300 | 284 |
| No. 4 base oils | ? | ? | ? | ? |
| Pour point/℃ | -39 | -39 | -30 | -30 |
| Viscosity index | 105 | 103 | 112 | 110 |
| No. 6 base oils | ? | ? | ? | ? |
| Pour point/℃ | -33 | -33 | -24 | -24 |
| Viscosity index | 111 | 110 | 118 | 116 |
| No. 10 base oils | ? | ? | ? | ? |
| Pour point/℃ | -27 | -27 | -21 | -21 |
| Viscosity index | 115 | 114 | 121 | 119 |
3(is continuous for table) processing condition and the result of embodiment and Comparative Examples.
| | Embodiment | 3 | Comparative Examples 3 |
| |
3 | 3 | |
| The hydroisomerization dewax processing condition | ? | ? | |
| Temperature of reaction/℃ | 345 | 345 | |
| Reaction pressure/MPa | 15.0 | 15.0 | |
| Hydrogen to oil volume ratio | 800 | 800 | |
| Volume space velocity/h -1 | 0.6 | 0.6 | |
| Process for refining condition after hydrogenation | ? | ? | |
| Temperature of reaction/℃ | 345 | / | |
| Reaction pressure/MPa | 15.0 | / | |
| Hydrogen to oil volume ratio | 800 | / | |
| Volume space velocity/h -1 | 5.0 | / | |
| The hydrogenation post-refining process condition | ? | ? | |
| No. 10 base oil recycle ratios | 0.5：1 | / | |
| Temperature of reaction/℃ | 250 | 225 | |
| Reaction pressure/MPa | 15.0 | 15.0 | |
| Hydrogen to oil volume ratio | 800 | 800 | |
| Volume space velocity/h -1 | 0.8 | 0.69 | |
| 350 ℃ of lube base oil natures | ? | ? | |
| Yield, quality % | 75.52 | 75.42 | |
| Pour point/℃ | -24 | -24 | |
| Viscosity (40 ℃), mm/s 2 | 42.12 | 42.16 | |
| Viscosity (100 ℃), mm/s 2 | 6.910 | 6.884 | |
| Viscosity index | 122 | 121 | |
| Color (Sai Shi)/number | >+30 | >+30 | |
| Sulfuric acid color test | By | By | |
| Oxidation stability, 150 ℃/min | >300 | 300 | |
| No. 4 base oils | ? | ? | |
| Pour point/℃ | -30 | -30 | |
| Viscosity index | 115 | 113 | |
| No. 6 base oils | ? | ? | |
| Pour point/℃ | -24 | -24 | |
| Viscosity index | 123 | 121 | |
| No. 10 base oils | ? | ? | |
| Pour point/℃ | -21 | -21 | |
| Viscosity index | 127 | 126 |
The comparative data of embodiment and Comparative Examples as can be known from table 3, process of the present invention compared with prior art, when processing different material, hydrofinishing temperature of reaction flexible adjustment, do not rely on the temperature of reaction of hydroisomerization dewax, the activity of Hydrobon catalyst can be more given full play to, pour point and viscosity index qualified light, heavy grease base oil can be obtained simultaneously.
Claims (12)
1. a hydrogenation is produced the processing method of lubricant base, with the hydrotreatment distillate, one or more in the frivolous oil of hydrotreatment or hydrocracking tail oil are stock oil, it is characterized in that: stock oil mixes with hydrofinishing reaction zone reaction effluent, through after being heated to the hydroisomerizing temperature of reaction, enter the hydroisomerizing reaction zone and carry out the hydroisomerizing reaction, the hydroisomerizing reaction zone sets gradually hydroisomerization catalyst and rare hydrocarbon saturation catalyst by the mobile direction of reaction mass, hydroisomerizing reaction zone reaction effluent enters separation system, obtain light lubricating oil base oil and heavy grease base oil, the heavy grease base oil is partly discharged as product, remainder enters the hydrofinishing reaction zone, carry out the hydrofinishing reaction under hydrogen and the existence of hydrofinishing catalyzer.
2. it is characterized in that in accordance with the method for claim 1: the heavy grease base oil that enters the hydrofinishing reaction zone is 0.2:1～5:1 with the mass ratio of discharging as the heavy grease base oil of product.
3. it is characterized in that in accordance with the method for claim 1: the heavy grease base oil that enters the hydrofinishing reaction zone is 0.5:1～2:1 with the mass ratio of discharging as the heavy grease base oil of product.
4. in accordance with the method for claim 1, it is characterized in that: the cut-point temperature of light lubricating oil base oil fractions and heavy grease base oil fractions is 450～520 ℃, 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 cut-point.
5. it is characterized in that in accordance with the method for claim 1: the sulphur content of stock oil and nitrogen content all require lower than 20 μ g/g.
6. in accordance with the method for claim 1, it is characterized in that: after hydrofinishing catalyzer and hydrogenation, catalyst for refining is conventional reduced form Hydrobon catalyst, its reactive metal is that one or both or the reactive metal in Pt, Pd is the reduced state nickel catalyzer, in noble metal catalyst, reactive metal is 0.05%～1% at the weight content of catalyzer, the reactive metal of reduced state nickel catalyzer counts 30%～80% with oxide weight, and support of the catalyst is Al
2O
3Or Al
2O
3-SiO
2
7. in accordance with the method for claim 1, it is characterized in that: 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%.
8. in accordance with the method for claim 1, it is characterized in that: the reaction conditions of hydroisomerization dewax is: temperature is 260 ℃～380 ℃, and the hydrogen dividing potential drop is 4.0MPa～18.0MPa, and volume space velocity is 0.6 h
-1～2.0h
-1, hydrogen to oil volume ratio 400:1～1500:1; The hydrofinishing reaction conditions is: temperature is 200 ℃～320 ℃, and the hydrogen dividing potential drop is 8.0MPa～18.0MPa, and volume space velocity is 0.4 h
-1～6.0h
-1, hydrogen to oil volume ratio is 400:1～1500:1.
9. in accordance with the method for claim 1, it is characterized in that: the reaction conditions of hydroisomerization dewax is: temperature is 280 ℃～350 ℃, and the hydrogen dividing potential drop is 10.0～15.0MPa, and volume space velocity is 0.8 h
-1～1.5h
-1, hydrogen to oil volume ratio 600:1～800:1; The hydrofinishing reaction conditions is: temperature is 220 ℃～280 ℃, and the hydrogen dividing potential drop is 10.0～15.0MPa, and volume space velocity is 0.8 h
-1～1.5h
-1, hydrogen to oil volume ratio is 600:1～800:1.
10. in accordance with the method for claim 1, it is characterized in that: after hydrogenation, the refining reaction temperature is 300 ℃～380 ℃, and the hydrogen dividing potential drop is 8.0MPa～18.0MPa, and volume space velocity is 3.0h
-1～15.0h
-1, hydrogen to oil volume ratio 400:1～1500:1.
11. according to claim 1,8 or 10 described methods, it is characterized in that: the hydroisomerization dewax temperature of reaction is higher 50～180 ℃ than hydrofinishing temperature of reaction, after hydrogenation during refining liquid volume space velocity be 3～15 times of hydroisomerization dewax volume space velocity.
12. in accordance with the method for claim 11, it is characterized in that: the hydroisomerization dewax temperature of reaction is higher 80～140 ℃ than hydrofinishing temperature of reaction, after hydrogenation during refining liquid volume space velocity be 5～10 times of hydroisomerization dewax volume space velocity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110353471.7A CN103102948B (en) | 2011-11-10 | 2011-11-10 | Production process for lubricant base oil through hydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110353471.7A CN103102948B (en) | 2011-11-10 | 2011-11-10 | Production process for lubricant base oil through hydrogenation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103102948A true CN103102948A (en) | 2013-05-15 |
| CN103102948B CN103102948B (en) | 2014-12-31 |
Family
ID=48311154
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110353471.7A Active CN103102948B (en) | 2011-11-10 | 2011-11-10 | Production process for lubricant base oil through hydrogenation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103102948B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103614160A (en) * | 2013-12-13 | 2014-03-05 | 海南汉地阳光石油化工有限公司 | Heavy lubricant base oil production system and production method |
| CN107987883A (en) * | 2017-11-23 | 2018-05-04 | 海南汉地阳光石油化工有限公司 | A kind of shape-selective isomery-supplementing refining method of WSI high-pressure hydrogenations |
| CN109266381A (en) * | 2018-11-30 | 2019-01-25 | 山东齐胜工贸股份有限公司 | A kind of high-sulfur light distillate and organic heat carrier feedstock oil hybrid process technique |
| CN114686260A (en) * | 2020-12-31 | 2022-07-01 | 中国石油化工股份有限公司 | Method for producing naphthenic base rubber filling oil through hydrogenation |
| CN116410785A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Production method of refrigerator oil base oil |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5855767A (en) * | 1994-09-26 | 1999-01-05 | Star Enterprise | Hydrorefining process for production of base oils |
| US20040222129A1 (en) * | 2003-04-23 | 2004-11-11 | Aldous Keith K. | Process for producing lubricant base oils |
| CN102041029A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Comprehensive utilization method of hydrocracking tail oil |
-
2011
- 2011-11-10 CN CN201110353471.7A patent/CN103102948B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5855767A (en) * | 1994-09-26 | 1999-01-05 | Star Enterprise | Hydrorefining process for production of base oils |
| US20040222129A1 (en) * | 2003-04-23 | 2004-11-11 | Aldous Keith K. | Process for producing lubricant base oils |
| CN102041029A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Comprehensive utilization method of hydrocracking tail oil |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103614160A (en) * | 2013-12-13 | 2014-03-05 | 海南汉地阳光石油化工有限公司 | Heavy lubricant base oil production system and production method |
| CN103614160B (en) * | 2013-12-13 | 2016-06-08 | 海南汉地阳光石油化工有限公司 | A kind of Heavy lubricant base oil production system and production method |
| CN107987883A (en) * | 2017-11-23 | 2018-05-04 | 海南汉地阳光石油化工有限公司 | A kind of shape-selective isomery-supplementing refining method of WSI high-pressure hydrogenations |
| CN107987883B (en) * | 2017-11-23 | 2020-06-19 | 海南汉地阳光石油化工有限公司 | WSI high-pressure hydrogenation shape-selective isomerization-supplement refining method |
| CN109266381A (en) * | 2018-11-30 | 2019-01-25 | 山东齐胜工贸股份有限公司 | A kind of high-sulfur light distillate and organic heat carrier feedstock oil hybrid process technique |
| CN114686260A (en) * | 2020-12-31 | 2022-07-01 | 中国石油化工股份有限公司 | Method for producing naphthenic base rubber filling oil through hydrogenation |
| CN114686260B (en) * | 2020-12-31 | 2023-07-28 | 中国石油化工股份有限公司 | Method for producing naphthenic base rubber filling oil through hydrogenation |
| CN116410785A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Production method of refrigerator oil base oil |
| CN116410785B (en) * | 2021-12-31 | 2024-05-07 | 中国石油天然气股份有限公司 | Production method of refrigerator oil base oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103102948B (en) | 2014-12-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102911720B (en) | Hydrogenation method for producing lubricating base oil | |
| CN101333460B (en) | Combined technological process for producing lube oil base stock | |
| CN105586083B (en) | Handle method and lube base oil of Fischer-Tropsch wax and preparation method thereof | |
| CN103102956B (en) | Hydrogenation production method for high-viscosity index lubricant base oil | |
| CN102041029B (en) | Comprehensive utilization method of hydrocracking tail oil | |
| CN103102948B (en) | Production process for lubricant base oil through hydrogenation | |
| CN103773476B (en) | Method for producing high-viscosity-index lubricant base oil by hydrocracking-isodewaxing combination | |
| CN105802665B (en) | A kind of method for hydrogen cracking and reaction unit of maximum volume production heavy naphtha | |
| CN103773466B (en) | Method for producing lubricant base oil by hydrocracking-isodewaxing combination | |
| CN103773467B (en) | A kind of hydroisomerization dewax produces the method for lubricant base | |
| CN101921621B (en) | Method for manufacturing isoparaffin solvent oil | |
| CN102041081A (en) | Combined method of hydrocracking and producing lubricant oil base oil | |
| CN102911726B (en) | Production method for base oil of high velocity index lubricating oil | |
| CN103773413B (en) | A kind of method of producing lubricant base | |
| CN103773465B (en) | Method for production of high viscosity index lubricant base oil by combination technology | |
| CN102465024B (en) | Hydrocracking method for producing lube base oil | |
| CN102465011B (en) | Hydrotreatment method of heavy distillate oil | |
| CN103102947B (en) | The producing and manufacturing technique of base oil of high viscosity index lubricant | |
| CN103773485B (en) | A kind of production method of base oil of high viscosity index lubricant | |
| CN103695028B (en) | The production method of white oil | |
| CN107686746B (en) | Hydrofining system and method thereof | |
| CN103102954A (en) | Production method for high-viscosity index lubricant base oil | |
| CN103102946A (en) | Production method for light lubricant base oil and heavy lubricant base oil | |
| CN103773484B (en) | A kind of combination process produces the method for lubricant base | |
| CN203820722U (en) | Hydroreforming system for full-range coal liquefied oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |