CN105709817A - Isomerization dewaxing catalyst and preparation method thereof - Google Patents
Isomerization dewaxing catalyst and preparation method thereof Download PDFInfo
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Abstract
The invention discloses an isomerization dewaxing catalyst, and a preparation method thereof. According to the preparation method, MTT-type molecular sieve loaded with a hydrogenation active ingredient is coated with an organic matter, an obtained product is uniformly mixed with a precursor of a high temperature resistant indifferent oxide, and an obtained mixture is subjected to moulding, drying, and roasting so as to obtain the isomerization dewaxing catalyst. The isomerization dewaxing catalyst is especially suitable for isomerization dewaxing of lubricating oil cut fractions. Compared with the prior art, the isomerization dewaxing catalyst possesses following advantages: molecular sieve using amount of the isomerization dewaxing catalyst is reduced greatly, so that catalyst production cost is reduced greatly, and discharge of wastewater difficult to process in molecular sieve synthesis process is avoided; target product yield is high; and pour point is low.
Description
Technical field
The present invention relates to a kind of isomerization dewaxing catalyst and preparation method thereof.This isomerization dewaxing catalyst is for, in waxy feeds oil isomerization dewaxing process, being particularly suitable for producing the process of top-grade lubricating oil base oil.
Background technology
Heretofore described waxy feeds oil mainly includes diesel oil, AGO, VGO, white oil, hydrocracking tail oil and lube cut etc..Waxy feeds oil, it is especially originating from the heavy distillate of paraffinic base crude oil containing more wax, condensation point is higher, low temperature flow is poor, storing, transporting and in use procedure, oil retrogradation can be made with the reduction of ambient temperature, even solidify, thus the fuel feeding blocking petroleum pipeline and interruption electromotor makes engine breakdown.The method solving the various problems that content of wax heavy distillate causes because of solidification at present is a lot, and wherein main means are dewaxings, including solvent dewaxing, catalytic dewaxing and isomerization dewaxing.
Solvent dewaxing is exactly utilize wax solubility property in a solvent to remove, the shortcoming of this method be solvent select difficulty, waste substantial amounts of organic solvent, harmful and contaminated environment, equipment investment and operating cost is high and product quality is limited by raw material.Catalytic dewaxing is exactly use to have the catalyst selecting shape cracking function, make the wax component generation selective catalytic cracking in fraction, generate more micromolecular hydro carbons, P.4247388, such as US Patent No. is exactly that the method using catalytic dewaxing removes the wax in lubricating oil with USP.4659311, the shortcoming of this method is the small-molecule substance owing to the macromolecular compound of substantial amounts of high value being converted into low value, makes that base oil yield is low, viscosity index (VI) loss is big, by-product is worth low.Compared with first two process for dewaxing, isomerization dewaxing is to make macromole wax generation isomerization reaction generate isoparaffin, and the wax phase ratio of isoparaffin and same molecular amount has less condensation point and pour point and higher viscosity index (VI), and remain in heavy distillate, so that distillate yield is greatly enhanced.
The purpose of isomerization dewaxing is exactly make high melting-point wax be converted into the isoparaffin that fusing point is relatively low, but the alkane fusing point that isomerisation degree is high is higher on the contrary, so being necessary for controlling the isomerisation degree of wax molecule, the Acidity of acidic components and pore structure and hydrogenation component are just proposed strict requirement by this.Acidic components to have moderate strength, acid amount more and have the pore structure of space restriction effect in general, and active metal component has quick hydrogenation/dehydrogenation activity, it is prevented that the further isomery of tertiary carbonium ion or even cracking.
It is a lot of about the report of isomerization dewaxing catalyst at present, for instance, US Patent No. 5990371, US5833837, US5817907, US5149421, US5135638, US5110445, US4919788, US4419420, US4601993, US4599162, US4518485 etc. all relate to Isodewaxing Technology, and the acidic components wherein used mainly have modenite, SAPO-11, SAPO-31, SAPO-41, ZSM-23, SSZ-32, ZSM-22 molecular sieve etc., although the acid centre that these materials above-mentioned have moderate strength and the pore structure matched with wax molecule, obvious space is had to limit highly-branched chain isomerous body, paraffin hydrocarbon generation isomerization reaction can both be made to a certain extent, but due in catalyst preparation process, most acid centre can be made to be capped, the acidity of catalyst obtained is more weak, activity and selectivity is relatively low, it addition, the stability of catalyst is closely related with its acidity, acid stronger catalyst resistant to sulfur nitrogen poisoning capability is strong, good stability, but it is also easier to the side reactions such as cracking.
CN103031144A discloses a kind of method using metal-modified small crystallite MTT molecular sieve to prepare base oil, this catalyst comprises: has MTT matrix topology and has the molecular sieve of crystal grain diameter of about 200 ~ 400 nanometers in the longest direction, at least one selected from Ca, Cr, Mg, La, Na, Pr, Sr, the metal of K and Nd and at least one group VIII metal.The method is to adopt conventional hydrothermal crystallizing method synthesis of molecular sieve, adopts conventional infusion process carried metal component.Adopting the method, the effective rate of utilization of molecular sieve reduces, and activity and diffusion are deteriorated, and affect selectivity of catalyst and stability.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of isomerization dewaxing catalyst and preparation method thereof.The method can make the more active center distribution of catalyst in pore passage structure, the acid centre that not only can avoid catalyst is capped, but also enable acid centre and hydrogenation sites better to coordinate, improve the activity of catalyst and isomerisation selectivity and stability, and reduce the generation of side reaction.
The preparation method of the isomerization dewaxing catalyst of the present invention, including:
(1) hydrogenation active component is loaded on MTT type molecular sieve, obtain the molecular sieve of load hydrogenation active component；
(2) molecular sieve that step (1) obtains is embedded in Organic substance, obtains the molecular sieve of Organic substance embedding；
(3) molecular sieve of Organic substance embedding step (2) obtained is mixed homogeneously with the precursor of high temperature resistant indifferent oxide, through molding, and dry and roasting, obtain the isomerization dewaxing catalyst of the present invention.
Step (1) described molecular sieve is topological structure is MTT type small crystal grain molecular sieve, and average grain diameter is 0.1 ~ 1.0 micron, it is preferred to 0.2 ~ 0.8 micron, SiO2/Al2O3Mol ratio is 10 ~ 50, it is preferred to 20 ~ 40.Described MTT type molecular sieve can be selected from various MTT structure molecular screens in prior art, including one or more in ZSM-23, ISI-4, KZ-1 and SSZ-32, it is preferred to one or more in ZSM-23 and SSZ-32 molecular sieve.Described MTT type molecular sieve mass content in the catalyst is 1.0% ~ 20.0%, it is preferred to 2.0% ~ 15.0%, more preferably 2.0% ~ 10.0%.Described hydrogenation active component is at least one in the VIIIth race's element in the periodic table of elements, it is preferred to platinum is or/and palladium, and described hydrogenation active component mass content in the catalyst is calculated as 0.01% ~ 0.30% with metal, it is preferred to 0.05% ~ 0.10%.Described high temperature resistant indifferent oxide can be selected from one or more in aluminium oxide, silicon oxide, calcium oxide, zinc oxide, magnesium oxide etc., it is preferred to aluminium oxide is or/and silicon oxide.The precursor of described high temperature resistant indifferent oxide refers to the hydroxide that this oxide is corresponding.
Step (1) described carrying method can be selected from one or more in infusion process, kneading method and cladding process, it is preferably infusion process, it is more preferably supersaturation infusion process, namely it is sufficiently mixed with molecular sieve with the solution containing hydrogenation metal component more than institute's impregnated zeolite saturated extent of adsorption, is then passed through the dry molecular sieve obtaining load hydrogenation active component with calcination process.
Organic species described in step (2) can be selected from one or more in starch and polyvinyl alcohol, and the degree of polymerization of described polyvinyl alcohol is 1500 ~ 2500, and alcoholysis degree is more than 85%, it is preferred to 90% ~ 99%.Described starch is water soluble starch, and its molecular weight is 20000 ~ 100000, and described starch sedimentation is one or more in corn starch, tapioca and potato starch, it is preferred to corn starch.The process that step (2) can adopt by the method for Organic substance embedding molecular sieve is as follows: mixed with water by Organic substance, the molecular sieve of load hydrogenation active component step (1) prepared is suspended in wherein, then pelletize is carried out, the molecular sieve making load hydrogenation active component is embedded in Organic substance, wherein prilling process can be vacuum spray drying method, boiling granulation method, centrifugal granulation or extrusion-spherozation etc., it is preferred to vacuum spray drying method.In vacuum spray drying method, vacuum is generally 0.01 ~ 0.05MPa, and baking temperature is 50 ~ 150 DEG C, and drying time is 1 ~ 24 hour, carries out vacuum spray drying by suspension obtained above, forms small dry granule.In the molecular sieve of the Organic substance embedding of step (2) gained, the mass ratio of Organic substance and molecular sieve is 20:1 ~ 1:1, it is preferred to 10:1 ~ 5:1.The particle diameter of the molecular sieve of the Organic substance embedding of step (2) gained is 10 ~ 100 microns.
Molding described in step (3), it is possible to select according to practical application, such as spherical, strip or other abnormity granules, it is preferred to strip.Drying condition described in step (3) is: baking temperature 80 ~ 150 DEG C, 5 ~ 20 hours drying times, and described roasting is to carry out in oxygenous atmosphere, and the condition of roasting is: sintering temperature 400 ~ 650 DEG C, roasting time 5 ~ 20 hours.Purpose is by Organic substance at high temperature oxidation removal, while discharging duct and the reaction channel of needs, is anchored on the inwall of molecular sieve pore passage by active metal component.
The isomerization dewaxing catalyst of the present invention needs to carry out pretreatment before use, is converted into simple substance by hydrogenation active metals component, it is possible to adopt wet reducing or dry reduction, it is preferred to dry reduction.Described dry reduction can adopt pure hydrogen, it is also possible to is the hydrogen containing noble gas, and wherein hydrogen volume content is 5% ~ 100%, it is preferred to 50% ~ 100%；Reducing condition is as follows: pressure is normal pressure ~ 10MPa, it is preferred to 2MPa ~ 8MPa；Temperature is 200 DEG C ~ 500 DEG C, it is preferred to 250 DEG C ~ 400 DEG C；Time is 0.5 hour ~ 24 hours, it is preferred to 1 hour ~ 12 hours, more preferably 2 hours ~ 8 hours, and gas agent volume ratio (i.e. the volume ratio of hydrogen and catalyst) is 500 ~ 1500, it is preferred to 800 ~ 1200.
Isomerization dewaxing catalyst of the present invention can be used for the isomerization dewaxing process of lube cut, and reaction condition is as follows: volume space velocity 0.5h during liquid-1~4.0h-1, reaction temperature is 260 DEG C ~ 400 DEG C, and reaction pressure is 2MPa ~ 20MPa, and hydrogen to oil volume ratio is 800 ~ 1200.
The isomerization dewaxing catalyst of the present invention is to adopt first to be embedded by the molecular sieve Organic substance being loaded with hydrogenation active metals component, then it is mixed with catalyst with high temperature resistant inert inorganic oxide again, so can make the more active center distribution of catalyst in pore passage structure, the acid centre that not only can avoid catalyst is capped, but also enable acid centre and hydrogenation sites better to coordinate, when reactant is by catalyst duct, directly contact with the catalytic active species in its duct and react efficiently, again owing to active particle is little, orifice throat length is short, isomerization product can quickly diffuse out, avoid deep reaction, improve the selectivity of isomerization reaction.Compared with prior art, the inventive method is for the isomerization dewaxing process of lube cut, owing to molecular sieve makes consumption be greatly lowered, not only Catalyst Production cost significantly declines, also avoid the discharge of intractable waste water in sieve synthesis procedure, and have the advantages that purpose product yield is high and pour point is low.
Detailed description of the invention
By the examples below the technology of the present invention is described further, but should not be construed as being limited to this scope.In the present invention, wt% is mass fraction.
In the present invention, the grain size of molecular sieve adopts SEM(scanning electron microscope) mode measure, silica alumina ratio is to adopt chemical analysis to record.
Evaluate used feedstock property in Table 1.The fine grain ZSM-5-23 used is that the method with reference to Chinese patent CN101214971A is synthetically derived, and its average grain diameter is 0.5 micron.
Table 1 raw oil main character
| Project | Raw material 1 |
| Viscosity (50 DEG C)/mm2.s-1 | 15.14 |
| Viscosity (100 DEG C)/mm2.s-1 | 4.365 |
| Pour point/DEG C | 35 |
| Sulfur/μ g.g-1 | 8.0 |
| Nitrogen/μ g.g-1 | 1.0 |
| Wax content, % | 28.5 |
| Boiling range/DEG C | |
| IBP/10% | 378/390 |
| 30%/50% | 407/423 |
| 70%/90% | 444/483 |
| 95%/EBP | 503/520 |
Embodiment 1
Catalyst one preparation process of the present invention is as follows:
(1) being dissolved in by the chloroplatinic acid containing 1 gram of platinum in 14 grams of water, by 19 grams of ZSM-23 molecular screens, (particle diameter is 0.5 micron, SiO2/Al2O3Mol ratio is 35) it is sufficiently mixed with above-mentioned solution, mixture, through 120 DEG C of dry 16 hours and 480 DEG C of roastings 4 hours, obtains the ZSM-23 molecular screen of Supported Pt Nanoparticles；
(2) 90 grams of water solublity corn starchs (molecular weight is 35000) are dissolved in 300 grams of water, then the molecular sieve that 10 grams of steps (1) obtain is added under room temperature, it is sufficiently stirred for uniformly suspension, through vacuum spray drying (vacuum 0.03MPa, baking temperature is 60 DEG C, drying time is 5h), obtain the catalytic active species of the starch embedding that average particulate diameter is 80 microns.
(3) take the molecular sieve of starch embedding prepared by 25 grams of steps (2) and 118 grams of (butt 76%) aluminium hydroxide and SB powder is sufficiently mixed, it is subsequently adding the salpeter solution that 85mL concentration is 0.1mol/L, abundant kneading, make paste plastic, on banded extruder, forming diameter is the cylindrical bars of 1.5mm, this cylindrical bars dries 16 hours at 100 DEG C, and then in air atmosphere, 550 DEG C of roastings obtain catalyst of the present invention in 4 hours.Catalyst forms, in mass fraction, Pt:0.05%, ZSM-23:2.5%, aluminium oxide: surplus.
Take 10mL catalyst, be packed in the miniature flow reactor of fixing bed after diluting with 10mL quartz sand and carry out catalytically active assessment.At pressure 1MPa, when temperature 200 DEG C, passing into pure hydrogen with the speed of gas agent volume ratio (entering the volume of gas and the admission space ratio of catalyst) 800, improve temperature to 320 DEG C, the retention time is carry out activation of catalyst in 4 hours；Then constant at pressure and temperature, hydrogen to oil volume ratio is adjusted to 900, and during with liquid, volume space velocity is 1.0h-1Entering raw material shown in table 1, carry out catalyst activity evaluation, negate and answer the product of 4 hours to be analyzed, evaluation result is in Table 2.
Embodiment 2
Catalyst one embodiment of the present invention is with embodiment 1, and being different in that in each step, content of material has adjusted, and SSZ-32(particle diameter is 0.7 micron, SiO2/Al2O3Mol ratio is 25) replace ZSM-23 molecular screen, obtain catalyst and consist of Pt:0.02%, SSZ-32:4.0%, aluminium oxide: surplus.Evaluation result is in Table 2.
Embodiment 3
Catalyst one embodiment of the present invention is with embodiment 1, and being different in that in each step, content of material has adjusted, and the mass ratio of starch and molecular sieve is 5:1, is prepared into the molecular sieve of the starch embedding that average particulate diameter is 50 microns.Obtain catalyst and consist of Pt:0.1%, ZSM-23:8%, aluminium oxide: surplus.Evaluation result is in Table 2.
Embodiment 4
Catalyst one embodiment of the present invention is with embodiment 1, it is different in that in step (1) and replaces chloroplatinic acid with Palladous chloride., and content of material has adjusted in each step, the mass ratio of starch and molecular sieve is 10:1, it is prepared into the molecular sieve of the starch embedding that average particulate diameter is 100 microns, obtain catalyst composition, in mass fraction, Pd:0.4%, ZSM-23:5.5%, aluminium oxide: surplus.Evaluation result is in Table 2.
Embodiment 5
Catalyst one embodiment of the present invention is with embodiment 1, it is different in that in step (1) and is additionally added Palladous chloride., and content of material has adjusted in each step, the mass ratio of starch and molecular sieve is 2:1, it is prepared into the molecular sieve of the starch embedding that average particulate diameter is 70 microns, obtain catalyst composition, in mass fraction, Pt:0.07%, Pd:0.15%, ZSM-23:4.5%, aluminium oxide: surplus.Evaluation result is in Table 2.
Embodiment 6
Catalyst one embodiment of the present invention is with embodiment 1, it is different in that (degree of polymerization is 1800 to step (2) middle polyvinyl alcohol, alcoholysis degree is 92%) replace water soluble starch, in each step, content of material has adjusted, the mass ratio of polyvinyl alcohol and molecular sieve is 5:1, is prepared into the molecular sieve of the polyvinyl alcohol embedding that average particulate diameter is 50 microns, obtains catalyst composition, in mass fraction, Pt:0.3%, ZSM-23:8%, aluminium oxide: surplus.Evaluation result is in Table 2.
Embodiment 7
Catalyst one embodiment of the present invention is with embodiment 1, it is different in that in step (3) and replaces aluminium hydroxide with silica gel, in each step, content of material has adjusted, the mass ratio of starch and molecular sieve is 8:1, it is prepared into the molecular sieve of the starch embedding that average particulate diameter is 80 microns, obtain catalyst to form in mass fraction, Pt:0.03%, ZSM-23:1.0%, silicon oxide: surplus.Evaluation result is in Table 2.
Comparative example 1
Aluminium hydroxide and SB, ZSM-23 molecular screen and sesbania powder are sufficiently mixed, it is subsequently adding the salpeter solution that appropriate concentration is 0.1mol/L, abundant kneading, make paste plastic, extruding diameter on banded extruder is the cylindrical bars of 1.5mm, cylindrical bars dries 16 hours at 100 DEG C, and then in air atmosphere, 550 DEG C of roastings obtain catalyst carrier in 4 hours.With containing H2PtCl6The saturated dipping said catalyst carrier of solution, then again 100 DEG C dry 8 hours, 500 DEG C of roasting 3h in air atmosphere, prepared catalyst consists of Pt:0.05%, ZSM-23:55%, aluminium oxide: surplus.Appreciation condition is with embodiment 1, and evaluation result is in Table 2.
Comparative example 2
A kind of preparation method of comparative example catalyst with comparative example 1, be different in that obtained catalyst form with embodiment 1, namely Pt:0.05%, ZSM-23:3.0%, aluminium oxide: surplus.The same embodiment of appreciation condition
Comparative example 3
The preparation method of a kind of comparative example catalyst, with comparative example 1, is different in that obtained catalyst forms with embodiment 2, in mass fraction, Pt:0.02%, SSZ-32:4.0%, aluminium oxide: surplus.Appreciation condition is with embodiment 1, and evaluation result is in Table 2.
Table 2 evaluation result
| Embodiment is numbered | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| C5 +Liquid is received, wt% | 94.5 | 94.8 | 95.0 | 95.2 | 95.1 |
| Base oil yield, wt% | 81.5 | 81.8 | 82.4 | 82.3 | 81.8 |
| Viscosity index (VI) | 119 | 118 | 120 | 121 | 120 |
| Pour point, DEG C | -22 | -21 | -22 | -22 | -22 |
Continued 2
| Embodiment is numbered | Embodiment 6 | Embodiment 7 | Comparative example 1 | Comparative example 2 | Comparative example 3 |
| C5 +Liquid is received, wt% | 95.3 | 94.8 | 91.5 | 96.2 | 93.7 |
| Base oil yield, wt% | 82.1 | 81.7 | 76.0 | 85.1 | 82.2 |
| Viscosity index (VI) | 120 | 121 | 115 | 108 | 110 |
| Pour point, DEG C | -20 | -21 | -20 | 15 | 17 |
The evaluation result of table 2 shows, compared with comparative catalyst, adopts catalyst provided by the invention, for processing in the hydroprocessing processes of the higher lube cut of wax content, when lube base oil pour point is close, and C5 +Liquid is received and is improved more than 3%, and lube base oil yield improves about 7wt%, the viscosity index (VI) of product improve 5 units, and molecular sieve content reduce by more than 80%, illustrates that catalyst of the present invention is in process crude lube stock process, effect has and significantly improves.
Claims (18)
1. a preparation method for isomerization dewaxing catalyst, including:
(1) hydrogenation active component is loaded on MTT type molecular sieve, obtain the molecular sieve of load hydrogenation active component；
(2) molecular sieve that step (1) obtains is embedded in Organic substance, obtains the molecular sieve of Organic substance embedding；
(3) molecular sieve of Organic substance embedding step (2) obtained is mixed homogeneously with the precursor of high temperature resistant indifferent oxide, through molding, and dry and roasting, obtain isomerization dewaxing catalyst.
2. in accordance with the method for claim 1, it is characterised in that described MTT type molecular sieve adopts small crystallite MTT type molecular sieve, and average grain diameter is 0.1 ~ 1.0 micron, it is preferred to 0.2 ~ 0.8 micron.
3. the method described in claim 1 or 2, it is characterised in that the SiO of described MTT type molecular sieve2/Al2O3Mol ratio is 10 ~ 50, it is preferred to 20 ~ 40.
4. the method described in claim 1 or 2, it is characterised in that one or more in ZSM-23, ISI-4, KZ-1 and SSZ-32 of described MTT type molecular screening, it is preferred to one or more in ZSM-23 and SSZ-32.
5. in accordance with the method for claim 1, it is characterised in that described MTT type molecular sieve mass content in the catalyst is 1.0% ~ 20.0%, it is preferred to 2.0% ~ 15.0%.
6. in accordance with the method for claim 1, it is characterised in that described hydrogenation active component is selected from platinum or/and palladium, and described hydrogenation active component mass content in the catalyst is calculated as 0.01% ~ 0.30% with metal.
7. in accordance with the method for claim 1, it is characterised in that described high temperature resistant indifferent oxide selected from aluminium oxide or/and silicon oxide.
8. in accordance with the method for claim 1, it is characterized in that one or more in starch and polyvinyl alcohol of Organic substance described in step (2), the degree of polymerization of described polyvinyl alcohol is 1500 ~ 2500, alcoholysis degree is more than 85%, described starch is water soluble starch, and its molecular weight is 20000 ~ 100000.
9. in accordance with the method for claim 8, it is characterised in that described starch is one or more in corn starch, tapioca and potato starch.
10. in accordance with the method for claim 1, it is characterized in that the process that the method for step (2) Organic substance embedding molecular sieve adopts is as follows: mixed with water by Organic substance, the molecular sieve of load hydrogenation active component step (1) prepared is suspended in wherein, then pelletize is carried out, the molecular sieve making load hydrogenation active component is embedded in Organic substance, and wherein prilling process is vacuum spray drying method, boiling granulation method, centrifugal granulation or extrusion-spherozation.
11. in accordance with the method for claim 10, it is characterised in that step (2) prilling process is vacuum spray drying method, vacuum is 0.01 ~ 0.05MPa, baking temperature is 50 ~ 150 DEG C, and drying time is 1 ~ 24 hour.
12. the method described in claim 1 or 10, it is characterised in that in the molecular sieve of the Organic substance embedding of step (2) gained, the mass ratio of Organic substance and molecular sieve is 20:1 ~ 1:1, it is preferred to 10:1 ~ 5:1.
13. the method described in claim 1 or 10, it is characterised in that the particle diameter of the molecular sieve of the Organic substance embedding of step (2) gained is 10 ~ 100 microns.
14. in accordance with the method for claim 1, it is characterized in that the drying condition described in step (3) is: baking temperature 80 ~ 150 DEG C, 5 ~ 20 hours drying times, described roasting is to carry out in oxygenous atmosphere, the condition of roasting is: sintering temperature 400 ~ 650 DEG C, roasting time 5 ~ 20 hours.
15. an isomerization dewaxing catalyst, it is characterised in that adopt the arbitrary described method of claim 1 ~ 14 to prepare.
16. the isomerization dewaxing method of a waxy feeds, it is characterised in that adopt the catalyst described in claim 15.
17. in accordance with the method for claim 16, it is characterised in that described isomerization dewaxing catalyst needs to reduce before use, adopt dry reduction, described dry reduction to adopt pure hydrogen or the hydrogen containing noble gas；Reducing condition is as follows: pressure is normal pressure ~ 10MPa, and temperature is 200 DEG C ~ 500 DEG C, and the time is 0.5 hour ~ 24 hours, and gas agent volume ratio is 500 ~ 1500.
18. the method described in claim 16 or 17, it is characterised in that described isomerization dewaxing catalyst is for the isomerization dewaxing process of lube cut, and reaction condition is as follows: volume space velocity 0.5h during liquid-1~4.0h-1, reaction temperature is 260 DEG C ~ 400 DEG C, and reaction pressure is 2MPa ~ 20MPa, and hydrogen to oil volume ratio is 800 ~ 1200.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5246566A (en) * | 1989-02-17 | 1993-09-21 | Chevron Research And Technology Company | Wax isomerization using catalyst of specific pore geometry |
| CN1204683A (en) * | 1997-03-05 | 1999-01-13 | 法国石油公司 | Process for selective hydroisomerisation of alkane hydrocarbon |
| CN103657713A (en) * | 2012-08-29 | 2014-03-26 | 中国石油化工股份有限公司 | Catalyst with hydrogenation catalysis effect, preparation method and application of catalyst and hydroisomerization method |
| CN103801385A (en) * | 2012-11-13 | 2014-05-21 | 中国石油化工股份有限公司 | Hydrogenation catalyst composition |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5246566A (en) * | 1989-02-17 | 1993-09-21 | Chevron Research And Technology Company | Wax isomerization using catalyst of specific pore geometry |
| CN1204683A (en) * | 1997-03-05 | 1999-01-13 | 法国石油公司 | Process for selective hydroisomerisation of alkane hydrocarbon |
| CN103657713A (en) * | 2012-08-29 | 2014-03-26 | 中国石油化工股份有限公司 | Catalyst with hydrogenation catalysis effect, preparation method and application of catalyst and hydroisomerization method |
| CN103801385A (en) * | 2012-11-13 | 2014-05-21 | 中国石油化工股份有限公司 | Hydrogenation catalyst composition |
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