CN103316710B - Hydroisomerization/cracking catalyst, and preparation method and application thereof - Google Patents
Hydroisomerization/cracking catalyst, and preparation method and application thereof Download PDFInfo
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Abstract
The invention discloses a hydroisomerization/cracking catalyst and a preparation method thereof. The catalyst is composed of an acidic isocraking carrier and a metal active component loaded on the acidic isocraking carrier; the acidic isocraking carrier is composed of a ZSM-22 molecular sieve and an amorphous oxide; and the mass ratio of the acidic isocraking carrier to the metal active component (by metal oxide and/or metal element) is 70-99.9:0.1-30. The preparation method of the catalyst comprises the following steps: 1, mixing the amorphous oxide with the ZSM-22 molecular sieve, carrying out adjusting and kneading molding by using an acid solution, and drying and roasting to obtain the acidic isocraking carrier; and 2, dipping the acidic isocraking carrier in an aqueous solution of a soluble salt of the active metal component, and drying and roasting to obtain the catalyst. The catalyst can crack high-melting-point long-chain normal paraffins into lightweight diesel oil during hydroisomerization, generates a small amount of gases and naphtha, and effectively reduces the condensation points of products.
Description
Technical field
The present invention relates to a kind of hysomer/Cracking catalyst and preparation method thereof and application.
Background technology
F-T synthetic heavy diesel oil forms primarily of straight-chain hydrocarbons, condensation point generally at 16 ~ 25 ° of C, its low-temperature characteristics and greasy property poor, be not suitable for using at cold district.The difference of diesel oil distillate owing to wherein forming of identical boiling range, condensation point difference is very large, such as boiling range is 325 ° of C ~ 350 ° C, when isomers mass content is 18%, condensation point is 13 ° of C, and condensation point is-36 ° of C when isomers mass content is 80%, so straight-chain hydrocarbons hysomer is the highly effective means reducing its condensation point in diesel oil distillate.
Heavy diesel hysomer adopts the bifunctional catalyst with special pore structure to make high-melting-point long-chain normal paraffin in heavy diesel be converted into the lower one-sided chain isomerism alkane of fusing point.There is provided isomerized acidic site by acid carrier, metal position provides hydrogenation/dehydrogenation function.But the alkane fusing point that isomerisation degree is high is higher on the contrary, so just must control the isomerisation degree of long-chain normal paraffin molecule, this just proposes strict requirement to the Acidity of acidic components and pore structure and hydrogenation component.Acidic components will have the acid centre of moderate strength and have the pore structure of space constraint in general, and hydrogenation component has hydrogenation dehydrogenation activity fast, prevents further isomery and even the cracking of tertiary carbonium ion.
ZSM-22 molecular sieve is the new-type high silicon aluminium zeolite molecular sieve of Prof. Du Yucang.ZSM-22 molecular sieve belongs to TON topological structure, has the one-dimensional channels of ten-ring, port size
.Have benefited from having pore passage structure the most suitable and stronger surface acid characteristic, strong acidproof and carbon accumulation resisting ability, ZSM-22 molecular sieve shows very high catalytic activity and selective in alkene and isomerization of paraffins reaction, there is the unrivaled superiority of other molecular sieve, have good application prospect.US4556477, US4902406, US5707600, US5783168 disclose the preparation method of ZSM-22 molecular sieve and the application in normal alkane isomerization reaction thereof.
For the n-alkane in the heavy bavin cut of F-T synthesis, because its condensation point is higher, cause low temperature flow poor, if by means of only isomerization reaction, its condensation point often can not be made to drop to desirable effect, and viscosity index (VI) may be caused to reduce, and therefore there is the isomerized high-melting-point normal paraffin component to some isomerization reaction not easily occurring simultaneously, to carry out suitable cracking be light diesel, so also can reach the object reducing oil product condensation point.So just wish that a catalyst has shape slective cracking and isomerized multi-functional simultaneously, if adopt single molecular sieve, does not reach good effect.
Summary of the invention
The object of this invention is to provide a kind of hysomer/Cracking catalyst and preparation method thereof and application, catalyst provided by the invention is specially adapted to the hydro-isomerization/cracking pour point depression of F-T synthesis heavy diesel.
A kind of hysomer/Cracking catalyst provided by the present invention, is made up of heterogeneous acidic cracking carrier and the metal active constituent be carried on described heterogeneous acidic cracking carrier;
Described heterogeneous acidic cracking carrier is made up of ZSM-22 molecular sieve and amorphous oxide;
The mass ratio of described heterogeneous acidic cracking carrier and described metal active constituent is 70 ~ 99.9:0.1 ~ 30, and wherein, the quality of described metal active constituent is in the quality of its oxide and/or element.
In above-mentioned hysomer/Cracking catalyst, the mass ratio of described heterogeneous acidic cracking carrier and described metal active constituent specifically can be 72:28,74:26,76:24,92:8 or 96:4.
In above-mentioned hysomer/Cracking catalyst, in described heterogeneous acidic cracking carrier, the mass ratio of described ZSM-22 molecular sieve and described amorphous oxide can be 4 ~ 35:60 ~ 96, specifically can be 4 ~ 35:40 ~ 88,4.6:87.4,10.8:61.2,18.5:55.5,33.6:62.4 or 34.2:41.8;
Described amorphous oxide can be amorphous aluminum silicide or amorphous silicon magnesium.
In above-mentioned hysomer/Cracking catalyst, described amorphous oxide can be the amorphous aluminum silicide with following physicochemical property: SiO
2mass content be 20% ~ 75%, specifically can be 25%, 35%, 50%, 65% or 72%, pore volume is 0.3 ~ 1.8ml/g, specifically can be 0.58ml/g, 0.76ml/g, 0.98ml/g, 1.2ml/g or 1.38ml/g, and specific area is 200 ~ 600m
2/ g, specifically can be 330 ~ 550m
2/ g, 335.9m
2/ g, 384.5m
2/ g, 490.3m
2/ g, 510.3m
2/ g or 535.6m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 60 ~ 85% of total pore volume, specifically can be 64%, 66%, 69%, 75% or 82%, infrared acidity can be 0.05 ~ 0.8mmol/g, specifically can be 0.4mmol/g, 0.46mmol/g, 0.5mmol/g, 0.57mmol/g or 0.68mmol/g.
In above-mentioned hysomer/Cracking catalyst, described ZSM-22 molecular sieve has following physicochemical property: SiO
2/ Al
2o
3mol ratio can be 20 ~ 200, specifically can be 80 ~ 160,80,92,111,120 or 160, specific area can be 220 ~ 550m
2/ g, specifically can be 350 ~ 550m
2/ g, 368.5m
2/ g, 396.8m
2/ g, 403.6m
2/ g, 486.9m
2/ g or 535.6m
2/ g; Infrared acidity can be 0.05 ~ 0.7mmol/g, specifically can be 0.098mmol/g, 0.11mmol/g, 0.13mmol/g, 0.18/mmol/g or 0.26mmol/g, Na
2o content≤0.1%, specifically can be 0.01%, 0.02% or 0.03%, pore volume can be 0.15 ~ 0.40mL/g, specifically can be 0.19mL/g, 0.22mL/g, 0.26mL/g, 0.29mL/g or 0.35mL/g.
In above-mentioned hysomer/Cracking catalyst, described metal active constituent to be selected from the periodic table of elements at least one in VIII race and/or VI B metal;
Described metal active constituent is selected from least one in molybdenum, tungsten, cobalt, nickel, palladium and platinum.
The present invention still further provides the preparation method of above-mentioned catalyst, comprises the steps:
(1) described amorphous oxide and described ZSM-22 molecular sieve are mixed, then with acid solution carry out modulating, kneading and compacting, more namely drying and roasting obtain described heterogeneous acidic cracking carrier;
(2) by described heterogeneous acidic cracking carrier impregnation in the aqueous solution of the soluble-salt of described active metal component, then namely drying and roasting obtain described catalyst.
In above-mentioned preparation method, described acid solution can be aqueous solution of nitric acid and/or acetic acid aqueous solution;
The mass percentage concentration of described acid solution can be 3% ~ 8%, specifically can be 3%, 5%, 7% or 8%;
Described amorphous oxide crosses 200 mesh sieves.
In above-mentioned preparation method, described metal active constituent is nickel, and the soluble-salt of described metal active constituent is at least one in nickelous carbonate, nickel nitrate or nickel acetate;
Described metal active constituent is molybdenum, and the soluble-salt of described metal active constituent is at least one in ammonium molybdate, molybdic acid and molybdenum oxide;
Described metal active constituent is tungsten, and the soluble-salt of described metal active constituent is at least one in ammonium metatungstate, ethyl ammonium metatungstate and wolframic acid;
Described metal active constituent is cobalt, and the soluble-salt of described metal active constituent is at least one in basic cobaltous carbonate, cobalt nitrate and cobalt oxide;
Described metal active constituent is palladium, and the soluble-salt of described metal active constituent is at least one in palladium nitrate and ammonium nitrate palladium;
Described metal active constituent is platinum, and the soluble-salt of described metal active constituent is at least one in tetramino dinitro platinum and chloroplatinic acid.
In above-mentioned preparation method, in step (1) and step (2), the temperature of described drying all can be 100 ~ 150 ° of C, and specifically can be 100 ° of C, 110 ° of C, 120 ° of C, 130 ° of C or 150 ° C, the time all can be 4 ~ 6h, specifically can be 4h, 5h or 6h; The temperature of described roasting all can be 500 ~ 650 ° of C, and specifically can be 500 ° of C, 550 ° of C, 600 ° of C or 650 ° C, the time all can be 4 ~ 6h, specifically can be 4h, 5h or 6h.
Catalyst provided by the invention can be used for catalysis F-T synthesis heavy diesel hydro-isomerization/cracking pour point depression reaction, and its reaction condition can be: reaction pressure is 3.0 ~ 15.0Mpa, and hydrogen to oil volume ratio is 400 ~ 1500, and volume space velocity is 0.5 ~ 10.0h
-1, reaction temperature is 320 ~ 400 ° of C.
Described F-T synthesis heavy diesel refers to cut heavier in the diesel product obtained in F-T building-up process, is generally C
16 +hydrocarbon molecules, this heavy diesel has without sulphur, feature without nitrogen, low aromatic hydrocarbons, and its organic hydrocarbon is based on straight-chain hydrocarbons.
The present invention compared with prior art, has the following advantages:
(1) catalyst provided by the invention has good isomerization performance, significantly can reduce the condensation point of raw material.
(2) catalyst provided by the invention is while hydroisomerization, can be light diesel by the cracking of high-melting-point long-chain normal paraffin, and produce a small amount of gas and naphtha, effectively reduces product condensation point.
(3) catalyst provided by the invention is the isomerization-visbreaking catalyst that a kind of diesel yield height depression effeCt is good.
Detailed description of the invention
The experimental technique used in following embodiment if no special instructions, is conventional method.
Material used in following embodiment, reagent etc., if no special instructions, all can obtain from commercial channels.
The preparation of embodiment 1, hysomer/Cracking catalyst Cat-1
(1) the ZSM-22 molecular sieve (SiO of porphyrize is taken
2/ Al
2o
3mol ratio is 80, and specific area is 535.6m
2/ g, infrared acidity is 0.26mmol/g, Na
2o content is 0.02%, and pore volume is 0.35mL/g) 4.6g(butt) and amorphous aluminum silicide (SiO
2mass content be 25%, pore volume is 1.38ml/g, and specific area is 535.6m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 75% of total pore volume, and infrared acidity is 0.68mmol/g) 87.4g(butt) mixing, be placed in kneading machine mixing 30min, dilute nitric acid solution modulation with 3%, kneading are to paste, and extrusion becomes column type, catalyst diameter 1.4mm.By dry 4h under it in an oven 120 ° of C, after 600 ° of C roasting 4h, be cooled to room temperature, just available heterogeneous acidic cracking carrier.
(2) 17.55g cobalt nitrate and 5.26g ammonium nitrate palladium maceration extract are sprayed on the carrier of above-mentioned preparation, drier 6h under 100 ° of C in an oven, be cooled to room temperature after 500 ° of C roasting 6h, just can obtain catalyst Cat-1.
Wherein the mass percent of each component consists of: ZSM-22 type molecular sieve: amorphous aluminum silicide: cobalt oxide: Pd=4.6:87.4:5.0:3.0.
The catalyst Cat-1 for preparing of the present embodiment is for the hydro-isomerization/cracking pour point depression of catalysis F-T synthetic heavy diesel oil, and reaction condition is: reaction pressure is 4.0Mpa, and hydrogen to oil volume ratio is 500, and air speed is 2.0h
-1, reaction temperature is 320 ° of C.
F-T synthetic heavy bavin oil properties is as shown in table 1, and catalytic result is as shown in table 2.
The preparation of embodiment 2, hydroisomerization/Cracking catalyst Cat-2
(1) the ZSM-22 molecular sieve (SiO of porphyrize is taken
2/ Al
2o
3mol ratio is 92, and specific area is 486.9m
2/ g, infrared acidity is 0.18mmol/g, Na
2o content is 0.01%, and pore volume is 0.29mL/g) 10.8g(butt) and amorphous aluminum silicide (SiO
2mass content be 35%, pore volume is 0.98ml/g, and specific area is 490.3m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 69% of total pore volume, and infrared acidity is 0.57mmol/g) 61.2g(butt) mixing, be placed in kneading machine mixing 15min.With the acetic acid solution of 3wt% modulate, kneading to paste, extrusion becomes trifolium-shaped, catalyst diameter 1.5mm.By dry 4h under it in an oven 130 ° of C, be cooled to room temperature after 550 ° of C roasting 4h, just can obtain heterogeneous acidic cracking carrier.
(2) aqueous solution of 80.43g nickel nitrate and 8.85g ammonium metatungstate is sprayed on the carrier of above-mentioned preparation, by dry 5h under it in an oven 120 ° of C, is cooled to room temperature after 550 ° of C roasting 4h, just can obtains catalyst Cat-2.
Wherein the mass percent of each component consists of: ZSM-22 type molecular sieve: amorphous aluminum silicide: nickel oxide: tungsten oxide=10.8:61.2:20.0:8.0.
The catalyst Cat-2 for preparing of the present embodiment is for the hydro-isomerization/cracking pour point depression of catalysis F-T synthetic heavy diesel oil, and reaction condition is: reaction pressure is 6.0Mpa, and hydrogen to oil volume ratio is 1000, and air speed is 4.0h
-1, reaction temperature is 336 ° of C.
F-T synthetic heavy bavin oil properties is as shown in table 1, and catalytic result is as shown in table 2.
The preparation of embodiment 3, hydroisomerization/Cracking catalyst Cat-3
(1) the ZSM-22 molecular sieve (SiO of porphyrize is taken
2/ Al
2o
3mol ratio is 111, and specific area is 396.8m
2/ g, infrared acidity is 0.13mmol/g, Na
2o content is 0.03%, and pore volume is 0.26mL/g) 18.5g(butt) and amorphous aluminum silicide (SiO
2mass content be 50%, pore volume is 0.58ml/g, and specific area is 384.5m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 64% of total pore volume, and infrared acidity is 0.50mmol/g) 55.5g(butt) mixing, be placed in kneading machine mixing 40min, the diluted nitric acid aqueous solution modulation kneading of 5wt% is to paste, and extrusion becomes bunge bedstraw herb type, catalyst diameter 1.7mm.By dry 5h under it in an oven 120 ° of C, be cooled to room temperature after 550 ° of C roasting 6h, just can obtain heterogeneous acidic cracking carrier.
(2) 16.09g nickel nitrate, 19.91g ammonium metatungstate and 4.91g ammonium molybdate are dissolved in the water, are sprayed on the carrier of above-mentioned preparation.By dry 4h under it in an oven 150 ° of C, be cooled to room temperature after 650 ° of C roasting 3h, just can obtain catalyst Cat-3.
Wherein the mass percent of each component consists of: ZSM-22 type molecular sieve: amorphous aluminum silicide: nickel oxide: tungsten oxide: molybdenum oxide=18.5:55.5:4.0:18.0:4.0.
The catalyst Cat-3 for preparing of the present embodiment is for the hydro-isomerization/cracking pour point depression of catalysis F-T synthetic heavy diesel oil, and reaction condition is: reaction pressure is 8.0Mpa, and hydrogen to oil volume ratio is 1200, and air speed is 10.0h
-1, reaction temperature is 390 ° of C.
F-T synthetic heavy bavin oil properties is as shown in table 1, and catalytic result is as shown in table 2.
The preparation of embodiment 4, hydroisomerization/Cracking catalyst Cat-4
(1) the ZSM-22 molecular sieve (SiO of porphyrize is taken
2/ Al
2o
3mol ratio is 120, and specific area is 403.6m
2/ g, infrared acidity is 0.11mmol/g, Na
2o content is 0.02%, and pore volume is 0.22mL/g) 33.6g(butt) and amorphous aluminum silicide (SiO
2mass content be 65%, pore volume is 1.2ml/g, and specific area is 510.3m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 82% of total pore volume, and infrared acidity is 0.46mmol/g) 62.4g(butt) mixing, be placed in kneading machine mixing 40min, the acetic acid aqueous solution modulation kneading of 7wt% is to paste, and extrusion becomes butterfly-type, catalyst diameter 2.0mm.By dry 6h under it in an oven 120 ° of C, be cooled to room temperature after 500 ° of C roasting 6h, just can obtain heterogeneous acidic cracking carrier.
(2) 2.65g chloroplatinic acid and 5.26g ammonium nitrate palladium are dissolved in the water obtain maceration extract and be sprayed on the carrier of above-mentioned preparation, by dry 4h under it in an oven 130 ° of C, be cooled to room temperature after 600 ° of C roasting 5h, just can obtain catalyst Cat-4.
Wherein the mass percent of each component consists of: ZSM-22 type molecular sieve: amorphous aluminum silicide: platinum: palladium=33.6:62.4:1.0:3.0.
The catalyst Cat-4 for preparing of the present embodiment is for the hydro-isomerization/cracking pour point depression of catalysis F-T synthetic heavy diesel oil, and reaction condition is: reaction pressure is 15.0Mpa, and hydrogen to oil volume ratio is 1500, and air speed is 7.0h
-1, reaction temperature is 360 ° of C.
F-T synthetic heavy bavin oil properties is as shown in table 1, and catalytic result is as shown in table 2.
The preparation of embodiment 5, hydroisomerization/Cracking catalyst Cat-5
(1) the ZSM-22 molecular sieve (SiO of porphyrize is taken
2/ Al
2o
3mol ratio is 160, and specific area is 368.5m
2/ g, infrared acidity is 0.098mmol/g, Na
2o content is 0.02%, and pore volume is 0.19mL/g) 41.8g(butt) and amorphous aluminum silicide (SiO
2mass content be 72%, pore volume is 0.76ml/g, and specific area is 335.9m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 66% of total pore volume, and infrared acidity is 0.40mmol/g) 34.2g(butt) mixing, be placed in kneading machine mixing 40min, the diluted nitric acid aqueous solution modulation kneading of 8wt% is to paste, and extrusion becomes clover, catalyst diameter 2.0mm.By dry 6h under it in an oven 100 ° of C, be cooled to room temperature after 650 ° of C roasting 3h, just can obtain heterogeneous acidic cracking carrier.
(2) 96.52g nickel nitrate aqueous solution is sprayed on the carrier of above-mentioned preparation, by dry 5h under it in an oven 110 ° of C, is cooled to room temperature after 650 ° of C roasting 4h, just can obtains catalyst Cat-5.
Wherein the mass percent of each component consists of: ZSM-22 type molecular sieve: amorphous aluminum silicide: nickel oxide=34.2:41.8:24.0.
The catalyst Cat-4 for preparing of the present embodiment is for the hydro-isomerization/cracking pour point depression of catalysis F-T synthetic heavy diesel oil, and reaction condition is: reaction pressure is 12.0Mpa, and hydrogen to oil volume ratio is 800, and air speed is 6.0h
-1, reaction temperature is 350 ° of C.
F-T synthetic heavy bavin oil properties is as shown in table 1, and catalytic result is as shown in table 2.
As can be seen from the data in table 2, when adopting catalyst of the present invention to be used for F-T diesel oil hydrogenation pour point depression production low-coagulation diesel oil, the selective height of straight chain alkane isomerization, heavy bavin can cracking be to a certain degree light bavin, has very high diesel oil distillate yield and good depression effeCt.In addition, catalyst activity and selectivity after running 3168h does not find to reduce, and illustrates that catalyst of the present invention has good stability.
Table 1 feedstock oil character
Table 2 experimental result
Claims (8)
1. hysomer/Cracking catalyst, is characterized in that:
Described catalyst is made up of heterogeneous acidic cracking carrier and the metal active constituent be carried on described heterogeneous acidic cracking carrier;
Described heterogeneous acidic cracking carrier is made up of ZSM-22 molecular sieve and amorphous oxide;
Described amorphous oxide is the amorphous aluminum silicide with following physicochemical property: SiO
2mass content be 20% ~ 75%, pore volume is 0.3 ~ 1.8ml/g, and specific area is 200 ~ 600m
2/ g, the pore volume in the hole between 3 ~ 15nm accounts for 60 ~ 85% of total pore volume, and infrared acidity is 0.05 ~ 0.8mmol/g;
The mass ratio of described heterogeneous acidic cracking carrier and described metal active constituent is 70 ~ 99.9:0.1 ~ 30, and wherein, the quality of described metal active constituent is in the quality of its oxide and/or element;
Described catalyst application is in the hysomer/cracking reaction of F-T synthesis heavy diesel.
2. hysomer/Cracking catalyst according to claim 1, is characterized in that: in described heterogeneous acidic cracking carrier, and the mass ratio of described ZSM-22 molecular sieve and described amorphous oxide is 4 ~ 35:60 ~ 96.
3. hysomer/Cracking catalyst according to claim 1, is characterized in that: described ZSM-22 molecular sieve has following physicochemical property: SiO
2/ Al
2o
3mol ratio be 20 ~ 200, specific area is 420 ~ 750m
2/ g, infrared acidity is 0.05 ~ 0.7mmol/g, Na
2o content≤0.1%, pore volume is 0.25 ~ 0.40mL/g.
4. hysomer/Cracking catalyst according to claim 1, is characterized in that: described metal active constituent to be selected from the periodic table of elements at least one in VIII race and/or VI B metal.
5. the preparation method of catalyst described in claim 1, comprises the steps:
(1) described amorphous oxide and described ZSM-22 molecular sieve are mixed, then with acid solution carry out modulating, kneading and compacting, more namely drying and roasting obtain described heterogeneous acidic cracking carrier;
(2) by described heterogeneous acidic cracking carrier impregnation in the aqueous solution of the soluble-salt of described active metal component, then namely drying and roasting obtain described catalyst.
6. preparation method according to claim 5, is characterized in that: described acid solution is aqueous solution of nitric acid and/or acetic acid aqueous solution;
The mass percentage concentration of described acid solution is 3% ~ 8%;
Described amorphous oxide crosses 200 mesh sieves.
7. the preparation method according to claim 5 or 6, is characterized in that: described metal active constituent is nickel, and the soluble-salt of described metal active constituent is at least one in nickelous carbonate, nickel nitrate or nickel acetate;
Described metal active constituent is molybdenum, and the soluble-salt of described metal active constituent is at least one in ammonium molybdate, molybdic acid and molybdenum oxide;
Described metal active constituent is tungsten, and the soluble-salt of described metal active constituent is at least one in ammonium metatungstate, ethyl ammonium metatungstate and wolframic acid;
Described metal active constituent is cobalt, and the soluble-salt of described metal active constituent is at least one in basic cobaltous carbonate, cobalt nitrate and cobalt oxide;
Described metal active constituent is palladium, and the soluble-salt of described metal active constituent is at least one in palladium nitrate and ammonium nitrate palladium;
Described metal active constituent is platinum, and the soluble-salt of described metal active constituent is at least one in tetramino dinitro platinum and chloroplatinic acid.
8. preparation method according to claim 5, is characterized in that:
In step (1) and step (2), the temperature of described drying is 100 ~ 150 DEG C, and the time is 4 ~ 6h; The temperature of described roasting is 500 ~ 650 DEG C, and the time is 4 ~ 6h.
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| CN101143333A (en) * | 2006-09-15 | 2008-03-19 | 中国石油化工股份有限公司 | Hydrogenating and pour point depressing catalyst and its preparing method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1352231A (en) * | 2000-11-08 | 2002-06-05 | 中国石油化工股份有限公司 | Hydrogenating and pour point depressing catalyst and its preparing method |
| CN1952074A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Hydrodewaxing catalyst for diesel oil distillate and its preparing method |
| CN101143333A (en) * | 2006-09-15 | 2008-03-19 | 中国石油化工股份有限公司 | Hydrogenating and pour point depressing catalyst and its preparing method |
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