CN105214717B - A kind of preparation method of lube base oil isomerization dewaxing catalyst - Google Patents
A kind of preparation method of lube base oil isomerization dewaxing catalyst Download PDFInfo
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Abstract
The invention discloses a kind of preparation method of lube base oil isomerization dewaxing catalyst, this method, which is included in sieve synthesis procedure, adds the molecular sieve with TON and MTT topological structures that alkaline-earth metal prepares the modification of the alkaline-earth metal isomorphous；It will be calcined again after molecular sieve and activated alumina extruded moulding, carrier after roasting is subjected to ammonia and exchanges modification, it is then placed in alkanolamine solution and soaks 5min~1 hour in room temperature~70 DEG C, modified support is obtained with after drying, modified carrier is finally used into infusion process or ion-exchange supported active metals, catalyst is obtained by drying, roasting.The catalyst that the inventive method is prepared is used for the isomerization dewaxing of lube cut, production low pour point, base oil of high viscosity index lubricant, with catalyst strong acid and weak acid ratio is low, isomerization dewaxing reactivity and selectivity height；Lube base oil pour point is low, high income the characteristics of.
Description
Technical field
The present invention relates to a kind of preparation method of isomerization dewaxing catalyst, the isomery for particularly producing lube base oil takes off
Wax catalyst and preparation method thereof.
Background technology
Lubricating oil, is one of big product of petroleum industry four, very important effect is played in the development of modern industry.It is high
OIL IN LUBRICATING OIL PRODUCTION production technology main at present in end has the processes such as catalytic dewaxing and isomerization dewaxing.Wherein Isodewaxing Technology is state
Emerging advanced lubricating oil processing technology on border, it can process the higher raw material of the content of wax, by that will have very high viscosity
The wax component of index and higher condensation point is isomerized to the lubricating oil component with viscosity higher index and low condensation point, rather than by its
Cracking is low boiling component, therefore improves the yield of base oil, remains viscosity index (VI).Isodewaxing Technology not only has very
High product yield, and the lube base oil of high-quality can be obtained, with very high industrial value.
Isomerization dewaxing is that the type of selecting for utilizing the molecular sieve with special duct is acted on, and long-chain normal paraffin is occurred isomerization
Reaction, so as to reduce lube base oil pour point, with base oil yield it is high the characteristics of, greatly paid close attention in recent years, phase
Close document report more.
The core of isomerization dewaxing technique is catalyst, and the key of isomerization dewaxing catalyst is acid site and metal center
Molecular sieve in matching problem, catalyst mainly provides acid site, and noble metal active component provides hydrogenation/dehydrogenation center.It is higher
Sour amount, suitable acid strength, higher metal dispersity be preferable isomerization dewaxing catalyst.
United States Patent (USP) US4710485,5135638,5282598,5376260, are disclosed using with TON, MTT and AEL
The noble metal isomerization dewaxing catalyst of supporting Pt and/or Pd, the preparation method of catalyst uses infusion process or ion-exchange.
United States Patent (USP) US7141529B2,5246566 are disclosed using alkali metal or alkaline-earth metal to molecular sieve modified, adjust molecular sieve
The method of acid amount improves the selectivity of catalyst.Chinese patent CN1448480A disclose it is a kind of using SAPO-11 molecular sieves as
The preparation method of the isomerization dewaxing catalyst of main carriers, retains molecular sieve by using organic amine to catalyst carrier pretreatment
Acidity improves the activity of catalyst.Chinese patent CN1488733A discloses a kind of preparation method of isomerization dewaxing catalyst,
It is strong with surface acidity using the novel phosphoric acid aluminum molecular screen with AEL structure, the characteristics of middle pore size distribution is more.
How focus that lube base oil yield be always research is improved, and base oil yield ceases with acidic zeolite matter
Correlation, there is strong acid acid amount in catalyst prepared by conventional method and weak acid acid molar ratio example is excessive mostly, cause in course of reaction
Degree reacts and then occurs cracking reaction, influences base oil yield.Processing method common at present is mainly repaiied by molecular sieve surface
Decorations means, to poison or catalyst deactivation outer surface non-selective acid centre, such as phosphorus deposition, Carbon deposition, metal
The technology such as modified oxide and silanization treatment.Above technology can only improve base oil yield to a certain extent.
The content of the invention
The purpose of the present invention carries out same order elements to Al elements in molecular sieve and by big by using alkali earth metal
The ratio of the method that molecule organic amine is passivated to catalyst external surface strong acidic site, control catalyst strong acid and weak acid, improves catalysis
Agent selectivity.
In catalyst preparation process, it has been found that the too strong acidity of carrier and excessive acid amount can increase isomerization depth
So as to cause base oil yield low, by adding the molecular sieve strong acid that alkaline-earth metal same order elements Al is obtained in Zeolite synthesis
Reduced with the ratio of weak acid.Meanwhile, shaping carrier can be reduced into catalyst external surface strong acid by the processing of macromolecular organic amine
Acid amount, further reduces the ratio of carrier strong acid and weak acid.So that the selectivity of catalyst is greatly improved.
The invention provides a kind of preparation method of lube base oil isomerization dewaxing catalyst, wherein described catalyst
The weight/mass percentage composition of component and component is：Wherein molecular sieve content is that 20~80%, active oxidation aluminium content is 19-
79.9%, group VIII metal content 0.1~1.0%；Including following preparation process：
1) molecular sieve with TON or MTT topological structures of alkaline-earth metal isomorphous modification is prepared；Wherein molecular sieve mole group
Turn into：(0.5~2.0) MO：(0.05~0.2) M12O:Al2O3:(30~100) SiO2, wherein M be K or Na, M1 be Mg, Ca,
One kind in Ba；Molecular sieve 1.0~1.5mmol/g of total acid content, strong acid and weak acid ratio are 0.3~0.5:1；
2) it will be calcined after molecular sieve and activated alumina mixed-forming；
3) carrier after roasting is subjected to ammonia with one kind in ammonium nitrate, ammonium chloride, ammonium sulfate and exchanges modification；
4) the modified carrier of ammonia is soaked into 5min~1 hour in alcohol-amine aqueous solution in room temperature~70 DEG C, after 90~
120 DEG C dry 6~12 hours, carrier strong acid and the ratio of weak acid acid amount is further decreased to 0.2~0.4:1；Wherein, it is described
The amine of alcohol-amine aqueous solution is selected from molecular weight ＞ 150 macromolecular organic amine；
5) by step 4) modified carrier uses infusion process or ion-exchange supported active metals, then through overdrying
Dry, roasting obtains catalyst.
According to preparation method of the present invention, wherein described molecular sieve is one kind in ZSM-22 and ZSM-23.
According to preparation method of the present invention, the wherein one kind of group VIII metal in Pt, Pd.
According to preparation method of the present invention, the wherein alcohol in alcohol-amine aqueous solution is ethanol.
According to preparation method of the present invention, wherein the amine in described alcohol-amine aqueous solution is decyl amine, lauryl amine and 16
One kind in amine.
According to preparation method of the present invention, wherein the concentration of amine is 0.1~1.0wt% in described alcohol-amine aqueous solution.
Catalyst of the present invention is used for the isomerization dewaxing of lube cut, production low pour point, high-viscosity index lubricating oil basis
Oil, has the characteristics that：
1st, catalyst strong acid and weak acid ratio ＜ 0.4:1；
2nd, isomerization dewaxing selectivity is high；
3rd, lube base oil pour point is low, high income.
Embodiment
Technical solution of the present invention is further described with reference to specific embodiment.
Embodiment 1
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al2O3), 8.65g magnesium sulfate (content of MgO 16.2wt%) be dissolved in 200g water
In；2) 1400mL deionized waters are added into 5L autoclaves, adds 10.8gNaOH stirrings；3) by 518g alkaline silica sols
(30wt%SiO2) reactor is added, continue to stir；4) 1) solution is added into reactor to continue to stir；5) 115g ethylenediamines are added
Enter reactor stirring, temperature is then risen into 160 DEG C of crystallization 96h；6) and then by washing, filtering, by filter cake and at 110 DEG C
Dry 10h and obtain MgO/Na2O/Al2O3/SiO2Mol ratio is 0.82:0.42:1:55.9 Mg-ZSM-22 molecular screen primaries
Powder.
(2) carrier is molded
1) by 41.2g Mg-ZSM-22,80g SB powder (butt 75wt%, Al2O3Content ＞ 99%), 1.2g Methyl celluloses
Element mixing；2) 71g 5wt% dilute nitric acid solutions are configured；3) by 2) with 1) the kneading 40min in kneading machine, then extruded moulding,
Extrude a diameter of 2.0 × 1.8mm bunge bedstraw herb；4) bunge bedstraw herb type carrier will be obtained after 120 DEG C of dry 6h in N2Under atmosphere,
400 DEG C of roasting 6h, then change blowing air, are warming up to 550 DEG C of roasting 4h, then break into length standby for 3-8mm.
(3) carrier ammonia is exchanged
50g shaping carriers are put into 500mL 0.5moL/L aqueous ammonium nitrate solution and are stirred and heated to 90 DEG C of exchanges
2h, is washed out filtering to filtrate in neutrality, then 110 DEG C of dry 2h, are then calcined 4h in 450 DEG C.Aforesaid operations are repeated, altogether
Exchange 2 times.
(4) alcohol-amine aqueous solution processing
0.2g decyl amine is dissolved in 100g ethanol, the carrier after then 50g ammoniums are exchanged is immersed, and is heated to 70 DEG C,
Taken out after immersion 1h in 120 DEG C of dry 10h.
(5) noble-metal-supported
Carriers of the 50g after alcohol-amine aqueous solution processing is taken, then 30g Pt content 0.67wt% chloroplatinic acid aqueous solutions are dripped
It is added on carrier, then incipient impregnation 8h is calcined 4h after 110 DEG C of dry 6h in 350 DEG C at room temperature.
Embodiment 2
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al2O3), 12.98g magnesium sulfate (content of MgO 16.2wt%) be dissolved in 200g water
In；2) 1400mL deionized waters are added into 5L autoclaves, adds 10.8gNaOH stirrings；3) by 518g alkaline silica sols
(30wt%SiO2) reactor is added, continue to stir；4) 1) solution is added into reactor to continue to stir；5) 115g ethylenediamines are added
Enter reactor stirring, temperature is then risen into 160 DEG C of crystallization 96h；6) and then by washing, filtering, by filter cake and at 110 DEG C
Dry 10h and obtain MgO/Na2O/Al2O3/SiO2Mol ratio is 1.15:0.39:1:61 Mg-ZSM-22 molecular screen primary powders.
(2) carrier is molded
The step of be the same as Example 1 (2).
(3) carrier ammonia is exchanged
The step of be the same as Example 1 (3)
(4) alcohol-amine aqueous solution processing
0.3g lauryl amines are dissolved in 100g ethanol, the carrier after then 50g ammoniums are exchanged is immersed, and is heated to 50
DEG C, taken out after immersion 0.5h in 120 DEG C of dry 10h.
(5) noble-metal-supported
Carriers of the 50g after alcohol-amine aqueous solution processing is taken, then 30g Pt content 0.67wt% chloroplatinic acid aqueous solutions are dripped
Add on carrier, then incipient impregnation 8h is calcined 4h after 110 DEG C of dry 6h in 350 DEG C at room temperature.
Embodiment 3
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al2O3), 16.23g magnesium sulfate (content of MgO 16.2wt%) be dissolved in 200g water
In；2) 1400mL deionized waters are added into 5L autoclaves, adds 10.8gNaOH stirrings；3) by 518g alkaline silica sols
(30wt%SiO2) reactor is added, continue to stir；4) 1) solution is added into reactor to continue to stir；5) 115g ethylenediamines are added
Enter reactor stirring, temperature is then risen into 160 DEG C of crystallization 96h；6) and then by washing, filtering, by filter cake and at 110 DEG C
Dry 10h and obtain MgO/Na2O/Al2O3/SiO2Mol ratio is 1.52:0.43:1:58.6 Mg-ZSM-22 molecular screen primaries
Powder.
(2) carrier is molded
The step of be the same as Example 1 (2).
(3) carrier ammonia is exchanged
The step of be the same as Example 1 (3)
(4) alcohol-amine aqueous solution processing
0.4g cetylamines are dissolved in 100g ethanol, the carrier after then 50g ammoniums are exchanged is immersed, and is heated to 50
DEG C, taken out after immersion 20min in 120 DEG C of dry 10h.
(5) noble-metal-supported
Take carriers of the 50g after alcohol-amine aqueous solution processing to be put into beaker, then add 500mL water, stirring is warming up to
80 DEG C, ammoniacal liquor is then added, solution ph 8~9 is adjusted, the ammino of dichloro four that 10mL Pt contents are 0.02g/mL is then added
Platinum solution, solution ph 8~9 is kept by ammoniacal liquor, exchanges 24h, and then scrubbed, filtering dries 2h, 450 DEG C after 110 DEG C
It is calcined 4h.
Embodiment 4
(1) Ca-ZSM-23 Zeolite synthesis
1) by 34g aluminum sulfate (17.2wt%Al2O3), 11.41g anhydrous nitric acids calcium (analysis pure) is dissolved in 200g water；2) will
1400mL deionized waters add 5L autoclaves, add 55.0gNaOH stirrings；3) by 518g alkaline silica sols (30wt%
SiO2) reactor is added, continue to stir；4) 1) solution is added into reactor to continue to stir；5) by 120g N, N- dimethyl formyls
Amine adds reactor stirring, and temperature then is risen into 170 DEG C of crystallization 96h；6) and then by washing, filtering, by filter cake and in 110
10h is dried at DEG C and obtains CaO/K2O/Al2O3/SiO2Mol ratio is 1.16:0.45:1:51 Ca-ZSM-23 molecular screen primaries
Powder.
(2) carrier is molded
The step of be the same as Example 1 (2).
(3) carrier ammonia is exchanged
The step of be the same as Example 1 (3).
(4) alcohol-amine aqueous solution processing
0.2g lauryl amines are dissolved in 100g ethanol, the carrier after then 50g ammoniums are exchanged is immersed, and is heated to 70
DEG C, taken out after immersion 1h in 120 DEG C of dry 10h.
(5) noble-metal-supported
Carriers of the 50g after alcohol-amine aqueous solution processing is taken, then 30g Pd content 0.67wt% chlorine palladiums aqueous acid is dripped
Add on carrier, then incipient impregnation 8h is calcined 4h after 110 DEG C of dry 6h in 350 DEG C at room temperature.
Embodiment 5
(1) Ba-ZSM-23 Zeolite synthesis
1) by 34g aluminum sulfate (17.2wt%Al2O3), 18.16g barium nitrates (analysis pure) are dissolved in 200g water；2) will
1400mL deionized waters add 5L autoclaves, add 55.0gNaOH stirrings；3) by 518g alkaline silica sols (30wt%
SiO2) reactor is added, continue to stir；4) 1) solution is added into reactor to continue to stir；5) by 120g N, N- dimethyl formyls
Amine adds reactor stirring, and temperature then is risen into 170 DEG C of crystallization 96h；6) and then by washing, filtering, by filter cake and in 110
10h is dried at DEG C and obtains CaO/K2O/Al2O3/SiO2Mol ratio is 1.17:0.4:1:49 Ba-ZSM-23 molecular screen primaries
Powder.
(2) carrier is molded
The step of be the same as Example 1 (2).
(3) carrier ammonia is exchanged
The step of be the same as Example 1 (3).
(4) alcohol-amine aqueous solution processing
0.2g lauryl amines are dissolved in 100g ethanol, the carrier after then 50g ammoniums are exchanged is immersed, and is heated to 70
DEG C, taken out after immersion 1h in 120 DEG C of dry 10h.
(5) noble-metal-supported
Carriers of the 50g after alcohol-amine aqueous solution processing is taken, then 30g Pt content 0.67wt% chlorine palladiums aqueous acid is dripped
Add on carrier, then incipient impregnation 8h is calcined 4h after 110 DEG C of dry 6h in 350 DEG C at room temperature.
Comparative example
(1) ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al2O3) be dissolved in 200g water；2) it is 1400mL deionized waters addition 5L is high
Reactor is pressed, 10.8gNaOH stirrings are added；3) by 518g alkaline silica sols (30wt%SiO2) reactor is added, continue to stir；
4) 1) solution is added into reactor to continue to stir；5) 115g ethylenediamines are added into reactor stirring, temperature is then risen to 160 DEG C
Crystallization 96h；6) and then by washing, filtering, Na is obtained by filter cake and in drying 10h at 110 DEG C2O/Al2O3/SiO2Rub
You are than being 0.39:1:56 ZSM-22 molecular screen primary powders.
(2) carrier is molded
1) by 41.2g ZSM-22,80g SB powder (butt 75wt%, Al2O3Content ＞ 99%), 1.2g methylcellulose is mixed
Close；2) 71g 5wt% dilute nitric acid solutions are configured；3) by 2) with 1) the kneading 40min in kneading machine, then extruded moulding, extrusion
A diameter of 2.0 × 1.8mm bunge bedstraw herb；4) bunge bedstraw herb type carrier will be obtained after 120 DEG C of dry 6h in N2Under atmosphere, 400 DEG C
6h is calcined, then changes blowing air, 550 DEG C of roasting 4h is warming up to, then breaks into length standby for 3-8mm.
(3) carrier ammonia is exchanged
50g shaping carriers are put into 500mL 0.5moL/L aqueous ammonium nitrate solution and are stirred and heated to 90 DEG C of exchanges
2h, is washed out filtering to filtrate in neutrality, then 110 DEG C of dry 2h, are then calcined 4h in 450 DEG C.Aforesaid operations are repeated, altogether
Exchange 2 times.
(4) noble-metal-supported
The carrier after the exchange of 50g ammonia is taken, then 30g Pt content 0.67wt% chloroplatinic acid aqueous solutions are added dropwise on carrier,
Then incipient impregnation 8h is calcined 4h after 110 DEG C of dry 6h in 350 DEG C at room temperature.
Composition and performance evaluation
Molecular sieve and shaping carrier use NH3- TPD carries out Acidity sign, molecular sieve composition and catalyst metal content
Characterized using XRF, the results are shown in Table 1 and 2.
The molecular sieve of table 1 is constituted and Acidity
The catalyst metal content of table 2 and Acidity
The performance evaluation of catalyst of the present invention is carried out on 20mL high-pressure hydrogenation fixed bed evaluating apparatus, is urged before reaction
Agent is by reduction, and reducing condition is hydrogen dividing potential drop 6MPa, 300 DEG C of temperature, time 2 h.Reaction condition is hydrogen dividing potential drop 6MPa, temperature
320 DEG C of degree, volume space velocity 1.2h-1, light oil volume ratio 500.
The raw materials used present invention is Huizhou hydrocracking tail oil, main character such as table 3 below：
The hydrocracking tail oil main character of table 3
Catalyst isomerization dewaxing Evaluation results are shown in Table 4.
The Evaluation results of the catalyst of table 4
| Project | Hydrogenation products pour point, DEG C | Liquid is received, % | Base oil yield, % |
| Embodiment 1 | -38 | 97 | 76 |
| Embodiment 2 | -42 | 97 | 78 |
| Embodiment 3 | -35 | 96 | 77 |
| Embodiment 4 | -37 | 96 | 77 |
| Embodiment 5 | -36 | 97 | 76 |
| Comparative example 1 | -38 | 94 | 73 |
Claims (6)
1. a kind of preparation method of lube base oil isomerization dewaxing catalyst, it is characterised in that described catalytic component and
The weight/mass percentage composition of component is：Wherein molecular sieve content is that 20~80%, active oxidation aluminium content is 19-79.9%, VIII
Race's tenor 0.1~1.0%；Including following preparation process：
1) molecular sieve with TON or MTT topological structures of alkaline-earth metal isomorphous modification is prepared；Wherein molecular sieve mole is constituted
For：(0.5~2.0) MO：(0.05~0.2) M12O:Al2O3:(30~100) SiO2, wherein M is K or Na, M1 are Mg, Ca, Ba
In one kind；Molecular sieve 1.0~1.5mmol/g of total acid content, strong acid and weak acid ratio are 0.3~0.5:1；
2) it will be calcined after molecular sieve and activated alumina mixed-forming；
3) carrier after roasting is subjected to ammonia with one kind in ammonium nitrate, ammonium chloride, ammonium sulfate and exchanges modification；
4) by the modified carrier of ammonia in alcohol-amine aqueous solution room temperature~70 DEG C soak 5min~1 hour, after 90~120 DEG C
Drying 6~12 hours, makes carrier strong acid and the ratio of weak acid acid amount be further decreased to 0.2~0.4:1；Wherein, described alcohol-amine
The amine of solution is selected from molecular weight ＞ 150 macromolecular organic amine；
5) by step 4) modified carrier uses infusion process or ion-exchange supported active metals, then by drying, roasting
Burning obtains catalyst.
2. preparation method according to claim 1, it is characterised in that described molecular sieve is in ZSM-22 and ZSM-23
It is a kind of.
3. preparation method according to claim 1, it is characterised in that the one kind of group VIII metal in Pt, Pd.
4. preparation method according to claim 1, it is characterised in that the alcohol in alcohol-amine aqueous solution is ethanol.
5. preparation method according to claim 1, it is characterised in that the amine in described alcohol-amine aqueous solution is decyl amine, 12
One kind in amine and cetylamine.
6. amine concentration is 0.1~1.0wt% in preparation method according to claim 1, alcohol-amine aqueous solution.
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| CN108144644B (en) * | 2016-12-04 | 2019-12-06 | 中国科学院大连化学物理研究所 | hydroisomerization catalyst, preparation and application thereof |
| CN106732752B (en) * | 2016-12-16 | 2019-07-19 | 中国海洋石油集团有限公司 | A kind of preparation method of C5, C6 alkane isomerization catalyst |
| CN116116456A (en) * | 2023-03-07 | 2023-05-16 | 国家能源集团宁夏煤业有限责任公司 | Modified Pt/ZSM-23 catalyst, preparation method and application thereof |
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| US5246566A (en) * | 1989-02-17 | 1993-09-21 | Chevron Research And Technology Company | Wax isomerization using catalyst of specific pore geometry |
| CN1169917C (en) * | 2002-04-04 | 2004-10-06 | 中国石油化工股份有限公司 | Isomerization dewaxing catalyst and its prepn. |
| US7141529B2 (en) * | 2003-03-21 | 2006-11-28 | Chevron U.S.A. Inc. | Metal loaded microporous material for hydrocarbon isomerization processes |
| CN1277613C (en) * | 2003-10-24 | 2006-10-04 | 中国石油化工股份有限公司 | Hydroprocessing catalyst and its prepn process |
| CN100457869C (en) * | 2005-10-19 | 2009-02-04 | 中国石油化工股份有限公司 | Dewaxing catalyst for lubricant oil distillate and its uses |
| CN1990104A (en) * | 2005-12-30 | 2007-07-04 | 中国科学院大连化学物理研究所 | Molecular sieve catalyst, preparing method and use thereof |
| JP5468957B2 (en) * | 2010-03-29 | 2014-04-09 | Ｊｘ日鉱日石エネルギー株式会社 | Hydroisomerization catalyst, method for producing the same, method for dewaxing hydrocarbon oil, method for producing hydrocarbon, and method for producing lubricating base oil |
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Address after: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Applicant after: China National Offshore Oil Corporation Applicant after: CNOOC TIANJIN CHEMICAL RESEARCH & DESIGN INSTITUTE CO., LTD. Applicant after: CNOOC Energy Development Co., Ltd. Address before: 100010 Beijing, Chaoyangmen, North Street, No. 25, No. Applicant before: China National Offshore Oil Corporation Applicant before: CNOOC Tianjin Chemical Research & Design Institute Applicant before: CNOOC Energy Development Co., Ltd. |
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