CN1352231A - Hydrogenating and pour point depressing catalyst and its preparing method - Google Patents
Hydrogenating and pour point depressing catalyst and its preparing method Download PDFInfo
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Abstract
The present invention is a kind of hydrogenating pour point depressing catalyst and its preparation. The catalyst has aluminosilicate molecular sieve as matrix, which is mixed with small amount of adhesive and formed into carrier; and VIII and VIB metal as hydrogenating component. The catalyst features its acidity of 0.05-0.15 mMol/g at 380 deg.c. During its preparation, the carrier is high temperature roasted to reduce its acidity. Wax containing diesel oil fraction and lubricant oil fraction may be catalytically dewaxed by using the catalyst at this can lower the freezing point of the oil product and improve flow property at low temperature.
Description
The present invention relates to a kind of distillate and lubricating oil distillate Hydrodewaxing catalyst and preparation method thereof.
Need carry out dewaxing treatment when producing low-coagulation diesel oil or lubricant base,, improve the low-temperature fluidity of product to reduce zero pour with waxy feeds oil.In distillate and lubricating oil dewaxing technology, the catalytic dewaxing technology is low because of its less investment, process cost, strong and operational condition relaxes, condensation point reduces advantages such as amplitude is big and receives much concern to adaptability to raw material.Its dewaxing principle is under certain operational condition, raw material is mixed with hydrogen pass through beds, in this bed, hydrocracking reaction takes place having on the catalyzer of selecting the type cracking performance in normal paraffin in the raw material and short-side chain isoparaffin, generate low molecular hydrocarbon, and other component does not change substantially, finally reaches the purpose that reduces pour point (or condensation point).
U.S. Patent No. 3,894,438,3,894,439,4,173,148,4,181,598 and 4,437,975 have described the catalytic dewaxing process of oil product.
Because catalytic dewaxing is that the wax molecule in the stock oil is cracked into small molecule hydrocarbon, separates from oil product, certainly will cause certain liquid to receive (liquid product total recovery) and diesel oil, lubricating oil distillate loss like this.The liquid receipts of WITH CATALYTIC DEWAXING TECHNIQUE process and diesel oil, lubricating oil distillate yield wax content and the operational condition, depend primarily on the essence of catalytic dewaxing catalyst in depending on raw material.
The hydrodewaxing key problem in technology is a Study of Catalyst, and adopting the mesopore aluminosilicate molecular sieves usually is matrix, adds a little binder and metal component and makes.The special pore passage structure of this molecular sieve only allows normal paraffin and a small amount of short-side chain isoparaffin to enter in its duct, and hyperbranched isoparaffin, naphthenic hydrocarbon and aromatic hydrocarbons exclusion.Used molecular sieve has ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35 and ZSM-38 etc.U.S. Pat 3,894,938; 4,176,050; 4,181,598; 4,222,855; 4,229,282 and 4,247,388 pairs of above-mentioned molecular sieves should be used as detailed descriptionthe.
Hydrodewaxing catalyst is a dual-function catalyst, metal component provides and adds the dehydrogenation activity center, ZSM-5 equimolecular sieve provides proper pore structure and acid sites, the carbonium ion reaction mechanism is followed in the cracking reaction of normal paraffin on the ZSM-5 molecular sieve, alkane molecule generates alkene in the dehydrogenation of metal active center, and this alkene obtains a H on the ZSM-5 acid site
+Generate carbonium ion, simultaneous isomerization, the carbonium ion instability of this isomery, on acid sites, be cracked into a low-molecular olefine and a low molecule carbonium ion, if the two all hydrogenation generate corresponding alkane, reaction terminating then, scission reaction that Here it is.Certainly, reaction mechanism is not simple like this, and one time the cracked product can continue reaction, and the cracked degree of depth depends on catalyst hydrogenation activity and tart coupling, the matching degree difference, and cracking severity is also different.
If the acid site of molecular sieve is a lot, acidity is very strong again, then can cause the over-drastic scission reaction, generate a large amount of gases, make purpose product one diesel oil or lubricating oil distillate yield losses, reduce the economy of raw material, must take measures the acid site and the strength of acid of catalyzer are controlled at a suitable scope.The method that reduces catalyst acidity has multiple, as the molecular sieve that adopts high silica alumina ratio or make the molecular sieve positively charged ion and alkalimetal ion exchanges, or with methods such as steam-treated.
Patent of invention CN85 100324B has reported a kind of distillate Hydrodewaxing catalyst and preparation method thereof, it is matrix that this catalyzer adopts direct method synthetic ZSM-5 molecular sieve, handle the back through modification and add that a little binder is mixedly pinched, extruded moulding, carrier is made in drying, roasting, with the soluble metal salt solution impregnation, support active metal component again, catalyzer is made in drying, roasting, handled 10 hours through high-temperature water vapor again, just can use.Wherein, double roasting all carries out under 500～550 ℃ temperature, and steam-treated then must carried out under the temperature more than 550 ℃ more than 10 hours continuously, just can make the acidity of catalyzer moderate, satisfy service requirements, and activity of such catalysts, selectivity are still waiting to improve.The steam-treated process because of consuming time long, energy consumption is big and treatment capacity is less etc., and reason often becomes the bottleneck that Hydrodewaxing catalyst is produced.Catalytic dewaxing catalyst prepared in the above-mentioned United States Patent (USP) has also adopted the steam-treated process.
United States Patent (USP) 4,790 is though 928 adopted the high-temperature roasting technology, but it is with the molecular sieve high-temperature roasting, be not the high-temperature roasting carrier, the molecular sieve after the roasting may be introduced some other acid site again in the shaping of catalyst process, influence activity of such catalysts and selectivity.This method molecular sieve is through also needing roasting once just can make carrier after the high-temperature roasting and behind the tackiness agent mixing moulding, and the operation of roasting pulverulent material is complicated, easily produces environmental issues such as dust.
The object of the present invention is to provide high strength of acid of a kind of activity, selectivity and suitable diesel oil, the lubricating oil distillate catalytic dewaxing catalyst of acid amount, another object of the present invention is to provide a kind of simple and convenient process for preparing of above-mentioned catalyzer.
Catalyzer of the present invention contains following component by weight, the shape slective cracking molecular sieve: 60～90%, and alumina adhesive: 9～39%, hydrogenation active metals component: surplus.The character of catalyzer is pore volume: 0.10-0.30cm
3/ g, specific surface area: 180-300m
2/ g, tap density: 0.70-0.95g/cm
3, 380 ℃ of acidity: 0.05～0.15mMol/g.
Described shape slective cracking molecular sieve is preferably selected ZSM series molecular sieve for use, as ZSM-5, ZSM-8, ZSM-11, ZSM-22, ZSM-23, ZSM-35 etc., also can select a mao molecular sieve, mercerising molecular sieve for use.The principal element that influences the catalytic dewaxing catalyst performance is the character of contained molecular sieve wherein.Discover that by intensive under the identical situation of character such as molecular sieve crystallinity, grain size, foreign matter content, the silica alumina ratio of molecular sieve is bigger to the acidity influence of catalyzer, silica alumina ratio is high more, and acidity is low more, therefore should adopt the high silica alumina ratio molecular sieve.But silica alumina ratio is too high, also can produce degree of crystallinity problem on the low side, and this shape selectivity to Hydrodewaxing catalyst can be very disadvantageous.Silica alumina ratio is 25～120, and particularly silica alumina ratio is 40～70 ZSM-5 molecular sieve, and carrier has good shape slective cracking performance after high-temperature roasting.The content of molecular sieve is preferably: 65～85%.
The hydrogenation active metals component is VIII family and/or group vib metal preferably, as Pt, Pd, Ni, Co, Mo, W etc., perhaps their mixture.Active metal component is preferably Ni, and NiO content (to catalyzer) is 1.0-6.0m%, can contain the WO of 0-15m% simultaneously
3
Described tackiness agent is meant what one or more and peptizing agent in the compounds such as activated alumina or its precursor, silicon oxide, magnesium oxide and water mixing and stirring formed.It accounts for the 9-39m% of catalyst weight.Described aluminum oxide is activated alumina or its precursor, is industrial aperture, mesopore or the macroporous aluminium oxide that generally adopts.Its pore volume is 0.2-1.0ml/g, and specific surface area is 100-400m
2/ g.Described peptizing agent refers to mineral acid and/or organic acid, the anionic salt of strongly-acid (as aluminum nitrate), mineral acid can be nitric acid, hydrochloric acid, sulfuric acid etc., organic acid is formic acid, acetate, oxalic acid, citric acid etc., also can be that several peptizing agents mix use, use simultaneously as nitric acid and acetate use simultaneously, acetate and citric acid.
Described extrusion aid is meant the material that helps extrusion molding, as sesbania powder, carbon black, Graphite Powder 99, citric acid etc.The consumption of extrusion aid accounts for the 1-10m% of total material butt.
Preparation of catalysts method of the present invention is: molecular sieve, tackiness agent and extrusion aid are mixed in proportion pinch even, extruded moulding, (80～120 ℃ of wet bar dryings, 4～12 hours), (700～830 ℃ of roastings, 1～6 hour) make carrier, carrier floods (1～4 hour) in the aqueous solution that contains tungsten salt and/or nickel salt, filtration, dry (40～110 ℃, 4～12 hours), roasting (480～600 ℃, 1～6 hour) makes finished catalyst.Said tungsten salt and nickel salt preferably are respectively ammonium metawolframate and nickelous nitrate.
The strength of acid of catalytic dewaxing catalyst of the present invention and acid amount are suitable, are a kind of activity, selectivity and the diesel oil that has good stability, lubricating oil distillate catalytic dewaxing catalyst.Catalyzer of the present invention is used for distillate such as diesel oil, lubricating oil catalytic dewaxing process, can above-mentioned raw materials be processed into low-coagulation diesel oil or lubricant base under than the demulcent processing condition, keeps higher liquid yield and purpose product yield simultaneously.
Catalyzer of the present invention adopts the high-temperature roasting carrier to regulate catalyst property, has advantages such as flow process is short, method is simple, cost is low, effect is obvious.The high-temperature roasting support of the catalyst on the one hand makes wherein that the surface acid property of molecular sieve component reaches service requirements, passivation simultaneously the part catalyst activity that has of tackiness agent, reduced the generation of side reaction, improved selectivity of catalyst and stability.
The acidity of catalyzer is to adopt the TPDE method to measure among the present invention, and this method is adsorbate with the pyridine, measures pyridine in the acidity of chemisorbed on catalyst amount as catalyzer on recording quartz spring weight absorption instrument.The concrete operations step is: accurately take by weighing and grind to form 20-40 purpose support samples 250-300mg, put into the sample hanging scaffold of absorption instrument, 5 * 10
-2Under the Pa vacuum tightness, 500 ℃ purify sample, are cooled to 380 ℃ then, after instrument baseline to be recorded was steady, the millivolt number (Va) when reading 380 ℃ after the sample purification cut off vacuum system, carry out pyridine adsorption, after adsorption curve reaches balance, be communicated with vacuum system and take off physical adsorption.Reach 5 * 10 in vacuum tightness
-2Pa after the desorption curve reaches balance, takes off physical adsorption and finishes, and reads the millivolt number (Vd) of this moment, calculates the acidity of carrier with following formula.
In the formula: A-acidity, mMol/g, i.e. the millimole number of unit weight catalyst surface absorption pyridine.
The millivolt number that reads 380 ℃ the time after the Va-sample purification.
Vd-380 ℃ is taken off the millivolt number that reads after the physical adsorption.
The sensitivity of S-instrument.
The gram molecular weight of M-pyridine.
Nt wt net weight mg behind the Wa-sample deduction moisture content.
Further set forth the present invention with embodiment below, but the present invention is not limited thereto.
Embodiment 1
(1) gets little porous aluminum oxide (pore volume 0.49ml/g, specific surface area 229m
2/ g) 40.5g adds 69.4g water purification and 8.1ml concentrated nitric acid, mixes, and cooks composite adhesives.
(2) get HZSM-5 (silica alumina ratio is 50) 126.3g, sesbania powder 3.0g and above-mentioned tackiness agent mix and pinch extruded moulding.
(3) wet bar is under 100 ± 10 ℃ of conditions dry 4 hours, and roasting is 4 hours under 730 ℃ of conditions, makes carrier.
(4) get the 24.9g nickelous nitrate and dissolve, be made into 200ml solution with water purification.
(5) above-mentioned carrier 100g is put into steeping fluid, flooded 2 hours, filter then, under 100 ℃ of conditions dry 4 hours, 480 ℃ of roastings 3 hours, catalyst A, its character sees Table 1.To the catalytic dewaxing of straight run content of wax diesel oil distillate, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3.
Embodiment 2
(1) gets mesoporous aluminas (pore volume 0.75ml/g, specific surface area 330m
2/ g) 81.1g adds 73.0g water purification and 10.7ml concentrated nitric acid, mixes, and cooks composite adhesives.
(2) get HZSM-5 (silica alumina ratio is 45) 140.0g, carbon black 6.0g and above-mentioned tackiness agent mix and pinch extruded moulding.
(3) wet bar is under 110 ℃ of conditions dry 4 hours, and roasting is 3 hours under 750 ℃ of conditions, makes carrier.
(4) get the 47.9g ammonium metawolframate and the 51.6g nickelous nitrate dissolves with water purification, be made into 200ml solution.
(5) above-mentioned carrier 100g is put into steeping fluid, flooded 2 hours, filter then, under 100 ℃ of conditions dry 4 hours, 540 ℃ of roastings 3 hours, catalyst B, its character sees Table 1.To straight run content of wax diesel oil distillate and lubricating oil distillate (hydrocracking tail oil) catalytic dewaxing, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3,4.
Embodiment 3
(1) gets macroporous aluminium oxide (pore volume 0.96ml/g, specific surface area 318m
2/ g) 64.3g adds 45.5g water purification and 8.0ml concentrated nitric acid and 4.0g citric acid, mixes, and cooks composite adhesives.
(2) getting HZSM-5 (silica alumina ratio is 38) 114.1g and above-mentioned tackiness agent mixes and to pinch extruded moulding.
(3) wet bar is under 110 ℃ of conditions dry 4 hours, and roasting is 3 hours under 770 ℃ of conditions, makes carrier.
(4) get the 33.0g nickelous nitrate and dissolve, be made into 200ml solution with water purification.
(5) above-mentioned carrier 100g is put into steeping fluid, flooded 2 hours, filter then, under 100 ℃ of conditions dry 4 hours, 480 ℃ of roastings 3 hours, catalyst A, its character sees Table 1.To the catalytic dewaxing of straight run content of wax diesel oil distillate, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3.
Embodiment 4
Except that the silica alumina ratio of HZSM-5 is 95, the maturing temperature of carrier is 700 ℃, all the other conditions are basic identical with embodiment 1, make catalyzer D, and its character sees Table 1.To the catalytic dewaxing of straight run content of wax diesel oil distillate, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3.
Embodiment 5
Except that the silica alumina ratio of HZSM-5 is 30, the maturing temperature of carrier is 820 ℃, all the other conditions are basic identical with embodiment 2, make catalyzer E, and its character sees Table 1.To the catalytic dewaxing of straight run content of wax diesel oil, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3.
Comparative example 1
Make the reference catalyst F that passes through steam-treated according to CN85100324B, its character sees Table 1.To straight run content of wax diesel oil distillate and hydrocracking tail oil catalytic dewaxing, stock oil character sees Table 2 with this catalyzer, and processing condition and evaluation result see Table 3,4.
Table 1 catalyzer physico-chemical property
| Catalyzer | ????A | ????B | ????C | ????D | ????E | ????F |
| Molecular sieve content (to carrier), SiO in the m% molecular sieve 2/Al 2O 3(mole) NiO (to catalyzer), m% WO 3(to catalyzer), 380 ℃ of acidity of m%, mM/g pore volume, cm 3/ g specific surface, m 2/ g mean pore size, nm tap density, g/cm 3 | ?80.0 ?50 ?1.32 ?0 ?0.078 ?0.189 ?242.8 ?2.31 ?0.76 | ??70.0 ??45 ??1.45 ??10.89 ??0.086 ??0.180 ??229.7 ??2.40 ??0.82 | ?70.0 ?38 ?1.78 ?0 ?0.092 ?0.183 ?239.2 ?2.29 ?0.79 | ??80.0 ??90 ??1.32 ??0 ??0.069 ??0.212 ??251.7 ??2.46 ??0.74 | ???70.0 ???30 ???1.78 ???11.3 ???0.057 ???0.194 ???220.6 ???2.19 ???0.83 | ??80.0 ??38 ??1.69 ??0 ??-- ??0.221 ??252.3 ??2.39 ??0.72 |
Table 2 stock oil character
| Title | Straight run content of wax diesel oil | Hydrocracking tail oil |
| Density (20 ℃), kg/m 3Boiling range, ℃ IBP/10% 30%/50% 70%/90% 95%/EBP sulphur, μ g/g nitrogen, μ g/g kinematic viscosity, mm 250 ℃ of 100 ℃ of condensation points of/s, ℃ wax content, m% | ????822.4 ????288/315 ????323/328 ????332/336 ????339/342 ????445 ????51 ????-- ????-- ????24 ????26.5 | ????831.4 ????330/370 ????392/412 ????438/478 ????496/519 ????8.0 ????1.5 ????11.88 ????3.897 ????37 ????22.8 |
Table 3 straight(-run) diesel distillate catalytic dewaxing evaluation result
| Processing condition | ??A | ???B | ???C | ??D | ??E | ??F |
| Pressure, MPa temperature, ℃ air speed, h -1(v) product distributes hydrogen-oil ratio, m% C 1-C 4??C 5-170 ℃ of total liquid of cut＞170 ℃ cut are received, m%＞170 ℃ cut condensation point, ℃ | ?4.0 ?350 ?1.0 ?420 ?7.9 ?26.5 ?65.6 ?92.1 ?-24 | ??4.0 ??350 ??1.0 ??420 ??8.3 ??27.2 ??64.5 ??91.7 ??-22 | ??4.0 ??350 ??1.0 ??420 ??8.1 ??29.1 ??62.8 ??91.9 ??-28 | ?4.0 ?350 ?1.0 ?420 ?7.5 ?27.7 ?64.8 ?92.5 ?-33 | ?4.0 ?350 ?1.0 ?420 ?5.3 ?24.5 ?70.2 ?94.7 ?-20 | ?4.0 ?350 ?1.0 ?420 ?9.5 ?33.9 ?56.6 ?90.5 ?-18 |
By table 3 as seen, under identical processing condition, A, B, C, D and E catalyzer are to the diesel oil distillate catalytic dewaxing, and it is bigger that the condensation point of diesel oil distillate reduces amplitude, product diesel oil distillate and total liquid are received higher, illustrate that catalyst activity height, the selectivity of acidity between 0.05-0.15mMol/g is good.Illustrate that catalyzer of the present invention is better than existing catalyzer, and Preparation of Catalyst flow process of the present invention is simple, the catalyzer cost is low.
Table 4 lubricating oil catalytic dewaxing evaluation result
| Processing condition | ??B | ??F |
| Pressure, Mpa temperature, ℃ air speed, h -1(v) product distributes hydrogen-oil ratio, m% C 1-C 4??C 5-170 ℃ of 170-320 ℃＞320 ℃ (lubricating oil distillate) liquid are received, m%＞320 ℃ cut oiliness pour point, ℃ kinematic viscosity (40 ℃) mm 2/s | ?8.0 ?310 ?1.0 ?800 ?14.6 ?20.5 ?1.2 ?63.7 ?85.4 ?-20 ?21.5 | ?8.0 ?310 ?1.0 ?800 ?25.3 ?15.0 ?1.0 ?58.4 ?74.7 ?-18 ?21.9 |
As seen from Table 4, catalyzer of the present invention is to hydrocracking tail oil catalytic dewaxing, C
1-C
4Gas yield is low, and liquid is received and reached more than the 85m%, and than the high approximately 10m% of reference catalyst,＞320 ℃ of lubricating oil distillate yields also improve a lot, and lubricating oil distillate basis oiliness is suitable with reference catalyst gained data.This presentation of results catalyzer of the present invention is better than existing lubricating oil catalytic dewaxing catalyzer.
Claims (15)
1, a kind of catalytic dewaxing catalyst is made of following component by weight: shape slective cracking molecular sieve 60～90%, tackiness agent 9～39%, hydrogenation active metals component surplus; The character of catalyzer is: pore volume 0.10-0.30cm
3/ g, specific surface area 180-300m
2/ g, 380 ℃ of acidity are 0.05～0.15mMol/g.
2, according to the described catalyzer of claim 1, it is characterized in that described shape slective cracking molecular sieve is ZSM molecular sieve, hair molecular sieve or mercerising molecular sieve, wherein the ZSM molecular sieve is ZSM-5, ZSM-8, ZSM-11, ZSM-22, ZSM-23 or ZSM-35 molecular sieve.
3,, it is characterized in that described ZSM molecular sieve is the ZSM-5 molecular sieve according to the described catalyzer of claim 2.
4, according to the described catalyzer of claim 2, the silica alumina ratio that it is characterized in that described ZSM molecular sieve is 25～120.
5, according to the described catalyzer of claim 4, the silica alumina ratio that it is characterized in that described ZSM molecular sieve is 40～70.
6,, it is characterized in that described hydrogenation active metals component is VIII family and/or group vib metal according to the described catalyzer of claim 1.
7,, it is characterized in that described hydrogenation active metals component is one or more among Pt, Pd, Ni, Co, Mo, the W according to claim 1 or 6 described catalyzer.
8,, it is characterized in that described hydrogenation active metals component is the NiO of 1.0-6.0m% and the WO of 0-15m% according to the described catalyzer of claim 1
3
9, the described Preparation of catalysts method of a kind of claim 1, molecular sieve and tackiness agent, extrusion aid mixed in proportion pinch, moulding, drying, roasting make carrier, then with solubility hydrogenation active metals salt solution impregnated carrier, promptly can be made into catalyzer after drying, the roasting, it is characterized in that the roasting condition of carrier is: 700 ℃～830 ℃ following roastings 1～6 hour.
10, in accordance with the method for claim 9, it is characterized in that described carrier drying condition is: 80～120 ℃, 4～12 hours.
11, in accordance with the method for claim 9, the drying conditions that it is characterized in that catalyzer is 40～110 ℃, and 4～12 hours, roasting condition was 480～600 ℃, 1～6 hour.
12, in accordance with the method for claim 9, it is characterized in that described tackiness agent is to be mixed together by one or more and peptizing agent in aluminum oxide or its precursor, silicon oxide or the magnesium oxide compound and water.
13, in accordance with the method for claim 12, it is characterized in that described aluminum oxide is activated alumina or its precursor, its pore volume is 0.2-1.0ml/g, and specific surface area is 100-400m
2/ g.
14, in accordance with the method for claim 12, it is characterized in that described peptizing agent refers to mineral acid and/or organic acid, the anionic salt of strongly-acid, mineral acid is nitric acid, hydrochloric acid or sulfuric acid, and organic acid is formic acid, acetate, oxalic acid or citric acid, or several peptizing agent mixes use.
15,, it is characterized in that in the process of catalyzer add the extrusion aid that accounts for total material butt 1-10m%, extrusion aid is sesbania powder, carbon black, Graphite Powder 99 or citric acid in moulding according to the described method of claim 9.
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| CN103316710A (en) * | 2013-07-11 | 2013-09-25 | 中科合成油内蒙古有限公司 | Hydroisomerization/cracking catalyst, and preparation method and application thereof |
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| CN104646070A (en) * | 2013-11-20 | 2015-05-27 | 中国石油化工股份有限公司 | Clean preparation method of hydrogenation catalyst carrier |
| CN104646072A (en) * | 2013-11-20 | 2015-05-27 | 中国石油化工股份有限公司 | Preparation method of hydrotreating catalyst carrier |
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| CN104923286A (en) * | 2015-05-25 | 2015-09-23 | 安徽海德石油化工有限公司 | Catalyst for producing MTBE (Methyl Tert-Butyl Ether) by virtue of C4 fractions in refinery plant |
| CN105032474A (en) * | 2015-05-25 | 2015-11-11 | 安徽海德石油化工有限公司 | Supported nanometer metal catalyst used for 1-butene and production through C4 distillate cracking |
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| CN107570206A (en) * | 2016-07-04 | 2018-01-12 | 中国石油天然气股份有限公司 | Diesel oil hydrogenation pour point depression catalyst and preparation method thereof |
| CN107570207A (en) * | 2016-07-04 | 2018-01-12 | 中国石油天然气股份有限公司 | Non-noble metal distillate oil hydroisomerization catalyst and preparation method thereof |
| CN112007692A (en) * | 2019-05-31 | 2020-12-01 | 国家能源投资集团有限责任公司 | Catalyst for dewaxing lubricant base oil produced by Fischer-Tropsch wax synthesis and preparation method and application thereof |
| CN112007692B (en) * | 2019-05-31 | 2024-03-29 | 国家能源投资集团有限责任公司 | Catalyst for dewaxing lubricating oil base oil for Fischer-Tropsch wax production and preparation method and application thereof |
| CN114441369A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | Device and method for quantitatively detecting acidity of material surface |
| CN114441368A (en) * | 2020-10-31 | 2022-05-06 | 中国石油化工股份有限公司 | Device and method for quantitatively determining surface acidity of material |
| WO2024159622A1 (en) * | 2023-02-03 | 2024-08-08 | 中国石油化工股份有限公司 | Hydrogenation method and hydrogenation system for hydrocarbon oil |
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