CN105214717A - 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, the method is included in sieve synthesis procedure the molecular sieve with TON and MTT topological structure adding alkaline-earth metal and prepare the modification of the alkaline-earth metal isomorphous; Again by roasting after molecular sieve and activated alumina extruded moulding, carrier after roasting is carried out ammonia and exchange modification, then put into alcohol-amine aqueous solution and soak 5min ~ 1 hour in room temperature ~ 70 DEG C, modified support is obtained subsequently in oven dry, finally modified carrier is adopted infusion process or ion-exchange supported active metals, obtain catalyst through super-dry, roasting.The catalyst that the inventive method prepares, for the isomerization dewaxing of lube cut, produces low pour point, base oil of high viscosity index lubricant, has catalyst strong acid and weak acid ratio is low, isomerization dewaxing reactivity and selective height; The feature that lube base oil pour point is low, yield is high.
Description
Technical field
The present invention relates to preparation method of a kind of isomerization dewaxing catalyst, the particularly isomerization dewaxing catalyst producing lube base oil and preparation method thereof.
Background technology
Lubricating oil, is one of large product of petroleum industry four, plays a part very important in the development of modern industry.The main at present production technology of high-end OIL IN LUBRICATING OIL PRODUCTION has the process such as catalytic dewaxing and isomerization dewaxing.Wherein Isodewaxing Technology is the lubricating oil processing technology of emerging advanced person in the world, it can process the higher raw material of the content of wax, by the wax component isomery with very high viscosity index (HVI) and higher condensation point is turned to the lubricating oil component with the low condensation point of viscosity higher exponential sum, instead of be low boiling component by its cracking, therefore improve the yield of base oil, remain viscosity index (VI).Isodewaxing Technology not only has very high product yield, and can obtain the lube base oil of high-quality, has very high industrial value.
Isomerization dewaxing utilizes type of the selecting effect with the molecular sieve in special duct, make long-chain normal paraffin generation isomerization reaction, thus reduce lube base oil pour point, have the advantages that base oil yield is high, receive great concern in recent years, pertinent literature report is more.
The core of isomerization dewaxing technique is catalyst, and the key of isomerization dewaxing catalyst is the matching problem of acid site and metal center, and the molecular sieve in catalyst mainly provides acid site, and noble metal active component provides hydrogenation/dehydrogenation center.Higher acid amount, suitable acid strength, higher metal dispersity are desirable isomerization dewaxing catalysts.
US Patent No. 4710485,5135638,5282598,5376260, disclose the noble metal isomerization dewaxing catalyst utilizing and have TON, MTT and AEL supporting Pt and/or Pd, the preparation method of catalyst adopts infusion process or ion-exchange.US Patent No. 7141529B2,5246566 discloses and utilizes alkali metal or alkaline-earth metal to molecular sieve modified, and the method for Molecular regulator sieve acid amount improves the selective of catalyst.Chinese patent CN1448480A discloses a kind of with the method for making of the SAPO-11 molecular sieve isomerization dewaxing catalyst that is main carriers, improves the activity of catalyst by utilizing organic amine to the acidity that catalyst carrier pretreatment retains molecular sieve.Chinese patent CN1488733A discloses a kind of preparation method of isomerization dewaxing catalyst, adopts the Novel phosphoric acid aluminum molecular screen with AEL structure, has surface acidity strong, the feature that middle pore size distribution is many.
How to improve the focus that lube base oil yield is research always, base oil yield and acidic zeolite matter closely bound up, it is with weak acid acid molar ratio example excessive mostly to there is strong acid acid amount in catalyst prepared by conventional method, cause overreaction in course of reaction and then cracking reaction occurs, affecting base oil yield.Processing method common at present modifies means mainly through molecular sieve surface, in order to poison or the nonselective acid centre of outer surface of catalyst deactivation, as technology such as phosphorus deposition, Carbon deposition, modified metal oxide and silanization treatment.Above technology can only improve base oil yield to a certain extent.
Summary of the invention
Object of the present invention by with alkali earth metal same order elements is carried out to Al element in molecular sieve and by large molecule organic amine to the method for catalyst external surface strong acidic site passivation, control the ratio of catalyst strong acid and weak acid, improve catalyst choice.
In catalyst preparation process, we find that the acidity that carrier is excessively strong and too much acid amount can increase the isomerization degree of depth thus cause base oil yield low, are reduced by the ratio adding molecular sieve strong acid that alkaline-earth metal same order elements Al obtains and weak acid when Zeolite synthesis.Meanwhile, shaping carrier can be reduced catalyst external surface strong acid acid amount through the process of excessive molecule organic amine, reduce the ratio of carrier strong acid and weak acid further.Thus the selective of catalyst is significantly improved.
The invention provides a kind of preparation method of lube base oil isomerization dewaxing catalyst, wherein said catalytic component and the mass percentage of component are: wherein molecular sieve content is 20 ~ 80%, activated alumina content is 19-79.9%, group VIII metal content 0.1 ~ 1.0%; Comprise following preparation process:
1) molecular sieve with TON and MTT topological structure of alkaline-earth metal isomorphous modification is prepared; Wherein molecular sieve mole consists of: (0.5 ~ 2.0) MO:(0.05 ~ 0.2) M1
2o:Al
2o
3: (30 ~ 100) SiO
2, the wherein M one that to be K or Na, M1 be in Mg, Ca, Ba; Molecular sieve total acid content 1.0 ~ 1.5mmol/g, strong acid and weak acid ratio are 0.3 ~ 0.5:1;
2) by roasting after molecular sieve and activated alumina mixed-forming;
3) one in the carrier ammonium nitrate after roasting, ammonium chloride, ammonium sulfate is carried out ammonia and exchange modification;
4) carrier modified for ammonia is soaked 5min ~ 1 hour in alcohol-amine aqueous solution in room temperature ~ 70 DEG C, dry 6 ~ 12 hours afterwards in 90 ~ 120 DEG C, the ratio that carrier strong acid and weak acid acid are measured is reduced to 0.2 ~ 0.4:1 further;
Wherein, the amine of described alcohol-amine aqueous solution is selected from the large molecule organic amine of molecular weight > 150;
5) by step 4) modified carrier adopts infusion process or ion-exchange supported active metals, then obtains catalyst through super-dry, roasting.
According to preparation method of the present invention, wherein said molecular sieve is the one in ZSM-22 and ZSM-23.
According to preparation method of the present invention, wherein group VIII metal is selected from the one in Pt, Pd.
According to preparation method of the present invention, the alcohol wherein in alcohol-amine aqueous solution is ethanol.
According to preparation method of the present invention, the amine in wherein said alcohol-amine aqueous solution is the one in decyl amine, lauryl amine and cetylamine.
According to preparation method of the present invention, in wherein said alcohol-amine aqueous solution, the concentration of amine is 0.1 ~ 1.0wt%.
Catalyst of the present invention is used for the isomerization dewaxing of lube cut, produces low pour point, base oil of high viscosity index lubricant, has following characteristics:
1, catalyst strong acid and weak acid ratio < 0.4:1;
2, the selective height of isomerization dewaxing;
3, lube base oil pour point is low, yield is high.
Detailed description of the invention
Below in conjunction with specific embodiment, technical solution of the present invention is further described.
Embodiment 1
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al
2o
3), 8.65g magnesium sulfate (content of MgO 16.2wt%) is dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 10.8gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) 115g ethylenediamine is added reactor to stir, then temperature is risen to 160 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains MgO/Na by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the Mg-ZSM-22 molecular screen primary powder of 0.82:0.42:1:55.9.
(2) carrier is shaping
1) by 41.2gMg-ZSM-22,80gSB powder (butt 75wt%, Al
2o
3content > 99%), 1.2g methylcellulose mixes; 2) 71g5wt% dilute nitric acid solution is configured; 3) by 2) and 1) kneading 40min in kneading machine, then extruded moulding, extrude the bunge bedstraw herb that diameter is 2.0 × 1.8mm; 4) bunge bedstraw herb type carrier will be obtained after 120 DEG C of dry 6h at N
2under atmosphere, 400 DEG C of roasting 6h, then change blowing air, are warming up to 550 DEG C of roasting 4h, and then breaking into length is that 3-8mm is for subsequent use.
(3) carrier ammonia exchanges
Aqueous ammonium nitrate solution 50g shaping carrier being put into 500mL0.5moL/L stirs and is heated to 90 DEG C and exchanges 2h, and then washing and filtering is to filtrate in neutral, and then 110 DEG C of dry 2h, then in 450 DEG C of roasting 4h.Repeat aforesaid operations, exchange 2 times altogether.
(4) alcohol-amine aqueous solution process
Be dissolved in by 0.2g decyl amine in 100g ethanol, the carrier after then being exchanged by 50g ammonium is immersed, and is heated to 70 DEG C, takes out in 120 DEG C of dry 10h after soaking 1h.
(5) noble-metal-supported
Get the carrier of 50g after alcohol-amine aqueous solution process, then 30gPt content 0.67wt% chloroplatinic acid aqueous solution is added drop-wise on carrier, in 110 DEG C of dry 6h after room temperature volumetric dipping 8h, then in 350 DEG C of roasting 4h.
Embodiment 2
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al
2o
3), 12.98g magnesium sulfate (content of MgO 16.2wt%) is dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 10.8gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) 115g ethylenediamine is added reactor to stir, then temperature is risen to 160 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains MgO/Na by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the Mg-ZSM-22 molecular screen primary powder of 1.15:0.39:1:61.
(2) carrier is shaping
With embodiment 1 step (2).
(3) carrier ammonia exchanges
With embodiment 1 step (3)
(4) alcohol-amine aqueous solution process
Be dissolved in by 0.3g lauryl amine in 100g ethanol, the carrier after then being exchanged by 50g ammonium is immersed, and is heated to 50 DEG C, takes out in 120 DEG C of dry 10h after soaking 0.5h.
(5) noble-metal-supported
Get the carrier of 50g after alcohol-amine aqueous solution process, then 30gPt content 0.67wt% chloroplatinic acid aqueous solution is dropped on carrier, in 110 DEG C of dry 6h after room temperature volumetric dipping 8h, then in 350 DEG C of roasting 4h.
Embodiment 3
(1) Mg-ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al
2o
3), 16.23g magnesium sulfate (content of MgO 16.2wt%) is dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 10.8gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) 115g ethylenediamine is added reactor to stir, then temperature is risen to 160 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains MgO/Na by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the Mg-ZSM-22 molecular screen primary powder of 1.52:0.43:1:58.6.
(2) carrier is shaping
With embodiment 1 step (2).
(3) carrier ammonia exchanges
With embodiment 1 step (3)
(4) alcohol-amine aqueous solution process
Be dissolved in by 0.4g cetylamine in 100g ethanol, the carrier after then being exchanged by 50g ammonium is immersed, and is heated to 50 DEG C, takes out in 120 DEG C of dry 10h after soaking 20min.
(5) noble-metal-supported
Get the carrier of 50g after alcohol-amine aqueous solution process and put into beaker, then 500mL water is added, stir, be warming up to 80 DEG C, then add ammoniacal liquor, regulate solution ph 8 ~ 9, then add the dichloro four ammino platinum solution that 10mLPt content is 0.02g/mL, keep solution ph 8 ~ 9 by ammoniacal liquor, exchange 24h, then after washing, filtration, 2h, 450 DEG C of roasting 4h are dried in 110 DEG C.
Embodiment 4
(1) Ca-ZSM-23 Zeolite synthesis
1) by 34g aluminum sulfate (17.2wt%Al
2o
3), 11.41g anhydrous nitric acid calcium (analyzing pure) is dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 55.0gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) by 120gN, dinethylformamide adds reactor and stirs, and then temperature is risen to 170 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains CaO/K by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the Ca-ZSM-23 molecular screen primary powder of 1.16:0.45:1:51.
(2) carrier is shaping
With embodiment 1 step (2).
(3) carrier ammonia exchanges
With embodiment 1 step (3).
(4) alcohol-amine aqueous solution process
Be dissolved in by 0.2g lauryl amine in 100g ethanol, the carrier after then being exchanged by 50g ammonium is immersed, and is heated to 70 DEG C, takes out in 120 DEG C of dry 10h after soaking 1h.
(5) noble-metal-supported
Get the carrier of 50g after alcohol-amine aqueous solution process, then 30gPd content 0.67wt% chlorine palladium aqueous acid is dropped on carrier, in 110 DEG C of dry 6h after room temperature volumetric dipping 8h, then in 350 DEG C of roasting 4h.
Embodiment 5
(1) Ba-ZSM-23 Zeolite synthesis
1) by 34g aluminum sulfate (17.2wt%Al
2o
3), 18.16g barium nitrate (analyzing pure) is dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 55.0gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) by 120gN, dinethylformamide adds reactor and stirs, and then temperature is risen to 170 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains CaO/K by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the Ba-ZSM-23 molecular screen primary powder of 1.17:0.4:1:49.
(2) carrier is shaping
With embodiment 1 step (2).
(3) carrier ammonia exchanges
With embodiment 1 step (3).
(4) alcohol-amine aqueous solution process
Be dissolved in by 0.2g lauryl amine in 100g ethanol, the carrier after then being exchanged by 50g ammonium is immersed, and is heated to 70 DEG C, takes out in 120 DEG C of dry 10h after soaking 1h.
(5) noble-metal-supported
Get the carrier of 50g after alcohol-amine aqueous solution process, then 30gPt content 0.67wt% chlorine palladium aqueous acid is dropped on carrier, in 110 DEG C of dry 6h after room temperature volumetric dipping 8h, then in 350 DEG C of roasting 4h.
Comparative example
(1) ZSM-22 Zeolite synthesis
1) by 25.8g aluminum sulfate (17.2wt%Al
2o
3) be dissolved in 200g water; 2) 1400mL deionized water is added 5L autoclave, add 10.8gNaOH and stir; 3) by 518g alkaline silica sol (30wt%SiO
2) add reactor, continue to stir; 4) by 1) solution add reactor continue stir; 5) 115g ethylenediamine is added reactor to stir, then temperature is risen to 160 DEG C of crystallization 96h; 6) then through washing, filter, dry 10h obtains Na by filter cake and at 110 DEG C
2o/Al
2o
3/ SiO
2mol ratio is the ZSM-22 molecular screen primary powder of 0.39:1:56.
(2) carrier is shaping
1) by 41.2gZSM-22,80gSB powder (butt 75wt%, Al
2o
3content > 99%), 1.2g methylcellulose mixes; 2) 71g5wt% dilute nitric acid solution is configured; 3) by 2) and 1) kneading 40min in kneading machine, then extruded moulding, extrude the bunge bedstraw herb that diameter is 2.0 × 1.8mm; 4) bunge bedstraw herb type carrier will be obtained after 120 DEG C of dry 6h at N
2under atmosphere, 400 DEG C of roasting 6h, then change blowing air, are warming up to 550 DEG C of roasting 4h, and then breaking into length is that 3-8mm is for subsequent use.
(3) carrier ammonia exchanges
Aqueous ammonium nitrate solution 50g shaping carrier being put into 500mL0.5moL/L stirs and is heated to 90 DEG C and exchanges 2h, and then washing and filtering is to filtrate in neutral, and then 110 DEG C of dry 2h, then in 450 DEG C of roasting 4h.Repeat aforesaid operations, exchange 2 times altogether.
(4) noble-metal-supported
Get the carrier after the exchange of 50g ammonia, then 30gPt content 0.67wt% chloroplatinic acid aqueous solution is dropped on carrier, in 110 DEG C of dry 6h after room temperature volumetric dipping 8h, then in 350 DEG C of roasting 4h.
Composition and performance evaluation
Molecular sieve and shaping carrier adopt NH
3-TPD carries out Acidity sign, and molecular sieve composition and catalyst metal content adopt XRF to characterize, and the results are shown in Table 1 and 2.
Table 1 molecular sieve composition and Acidity
Table 2 catalyst metal content and Acidity
The performance evaluation of catalyst of the present invention is carried out on 20mL high-pressure hydrogenation fixed bed evaluating apparatus, and the procatalyst of reaction is through reduction, and reducing condition is hydrogen dividing potential drop 6MPa, temperature 300 DEG C, time 2 h.Reaction condition is hydrogen dividing potential drop 6MPa, temperature 320 DEG C, volume space velocity 1.2h
-1, light oil volume ratio 500.
The present invention is raw materials used is Huizhou hydrocracking tail oil, and main character is as following table 3:
Table 3 hydrocracking tail oil main character
Catalyst isomerization dewaxing Evaluation results is in table 4.
The Evaluation results of table 4 catalyst
| 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. the preparation method of a lube base oil isomerization dewaxing catalyst, it is characterized in that, described catalytic component and the mass percentage of component are: wherein molecular sieve content is 20 ~ 80%, activated alumina content is 19-79.9%, group VIII metal content 0.1 ~ 1.0%; Comprise following preparation process:
1) molecular sieve with TON and MTT topological structure of alkaline-earth metal isomorphous modification is prepared; Wherein molecular sieve mole consists of: (0.5 ~ 2.0) MO:(0.05 ~ 0.2) M1
2o:Al
2o
3: (30 ~ 100) SiO
2, the wherein M one that to be K or Na, M1 be in Mg, Ca, Ba; Molecular sieve total acid content 1.0 ~ 1.5mmol/g, strong acid and weak acid ratio are 0.3 ~ 0.5:1;
2) by roasting after molecular sieve and activated alumina mixed-forming;
3) one in the carrier ammonium nitrate after roasting, ammonium chloride, ammonium sulfate is carried out ammonia and exchange modification;
4) carrier modified for ammonia is soaked 5min ~ 1 hour in alcohol-amine aqueous solution in room temperature ~ 70 DEG C, dry 6 ~ 12 hours afterwards in 90 ~ 120 DEG C, the ratio that carrier strong acid and weak acid acid are measured is reduced to 0.2 ~ 0.4:1 further; Wherein, the amine of described alcohol-amine aqueous solution is selected from the large molecule organic amine of molecular weight > 150;
5) by step 4) modified carrier adopts infusion process or ion-exchange supported active metals, then obtains catalyst through super-dry, roasting.
2. preparation method according to claim 1, is characterized in that, described molecular sieve is the one in ZSM-22 and ZSM-23.
3. preparation method according to claim 1, is characterized in that, group VIII metal is selected from the one in Pt, Pd.
4. preparation method according to claim 1, is characterized in that, the alcohol in alcohol-amine aqueous solution is ethanol.
5. preparation method according to claim 1, is characterized in that, the amine in said alcohol-amine aqueous solution is the one in decyl amine, lauryl amine and cetylamine.
6. preparation method according to claim 1, in alcohol-amine aqueous solution, amine concentration is 0.1 ~ 1.0wt%.
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| CN106732752A (en) * | 2016-12-16 | 2017-05-31 | 中国海洋石油总公司 | A kind of preparation method of C5, C6 alkane isomerization catalyst |
| CN108144644A (en) * | 2016-12-04 | 2018-06-12 | 中国科学院大连化学物理研究所 | A kind of hydroisomerisation catalysts and its preparation and application |
| 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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| CN105214717B (en) | 2017-07-28 |
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