CN108085058B - A kind of method of hydrocarbon ils deeply de-aromatizing - Google Patents
A kind of method of hydrocarbon ils deeply de-aromatizing Download PDFInfo
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- CN108085058B CN108085058B CN201611031935.1A CN201611031935A CN108085058B CN 108085058 B CN108085058 B CN 108085058B CN 201611031935 A CN201611031935 A CN 201611031935A CN 108085058 B CN108085058 B CN 108085058B
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 10
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 10
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 10
- 239000003054 catalyst Substances 0.000 claims abstract description 31
- 239000000047 product Substances 0.000 claims abstract description 27
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000001257 hydrogen Substances 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 10
- 229910052593 corundum Inorganic materials 0.000 claims abstract description 9
- 229910001845 yogo sapphire Inorganic materials 0.000 claims abstract description 9
- 230000003197 catalytic effect Effects 0.000 claims abstract description 5
- 239000012263 liquid product Substances 0.000 claims abstract description 5
- 230000006835 compression Effects 0.000 claims abstract description 3
- 238000007906 compression Methods 0.000 claims abstract description 3
- 238000002156 mixing Methods 0.000 claims abstract description 3
- 239000002283 diesel fuel Substances 0.000 claims description 10
- 239000003350 kerosene Substances 0.000 claims description 9
- 239000011148 porous material Substances 0.000 claims description 6
- 229910052763 palladium Inorganic materials 0.000 claims description 5
- 239000002904 solvent Substances 0.000 claims description 5
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- 230000002378 acidificating effect Effects 0.000 claims description 2
- 239000012071 phase Substances 0.000 claims 2
- 239000007791 liquid phase Substances 0.000 claims 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 abstract description 23
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052717 sulfur Inorganic materials 0.000 abstract description 9
- 239000011593 sulfur Substances 0.000 abstract description 9
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 5
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 4
- 231100000572 poisoning Toxicity 0.000 abstract description 3
- 230000000607 poisoning effect Effects 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 22
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- 150000004767 nitrides Chemical class 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 229910000510 noble metal Inorganic materials 0.000 description 3
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- SMZOGRDCAXLAAR-UHFFFAOYSA-N aluminium isopropoxide Chemical compound [Al+3].CC(C)[O-].CC(C)[O-].CC(C)[O-] SMZOGRDCAXLAAR-UHFFFAOYSA-N 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- -1 aluminium oxide-titanium oxide compound Chemical class 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 210000000988 bone and bone Anatomy 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 229960000935 dehydrated alcohol Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000001027 hydrothermal synthesis Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 150000002940 palladium Chemical class 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/44—Palladium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of methods of hydrocarbon ils deeply de-aromatizing.Key step are as follows: under relatively mild operating condition (middle pressure 3-7MPa, 180-270 DEG C of temperature), enter hydrogenator after feedstock oil and hydrogen mixing, it is contacted with catalytic hydro-dearomatization catalyst, product after reaction is isolated to gas-phase product and liquid product, gas-phase product is recycled after compression, liquid product is then isolated to the product of low aromatic hydrocarbons, and the catalytic hydro-dearomatization catalyst is the PtPd/Al of high dispersive2O3Catalyst.This method reaction condition is mild, and reaction pressure is mesolow, and reaction temperature is low, and air speed is high, and target product arene content is low, PtPd/Al2O3Catalyst shows very high hydrogenation activity and sulfur resistive, nitrogen poisoning performance.
Description
Technical field
The present invention relates to a kind of hydrofinishing process of hydrocarbon ils, relate more specifically to one kind with order mesoporous Al2O3PtPd
Catalyst is used for the method compared with deeply de-aromatizing under temperate condition.
Background technique
Aromatic compound imperfect combustion generates the master that a large amount of fine particulates (PM2.5) are atmosphere pollution in fuel oil
Cause.With the enhancing of people's environmental consciousness, in order to improve air quality, the aromatic hydrocarbons that countries in the world all strictly limit in fuel oil contains
Amount.Regulation Determination of Benzene In Gasoline is not higher than 35vol% lower than 1vol%, arene content in the state's V standard that will implement；In diesel oil
Arene content is not higher than 15vol%；The aromatic hydrocarbons of high-content causes the decline of aviation kerosine smoke point, thermostability poor；It is molten in order to improve
Aromatic hydrocarbons, it is specified that very low concentration must be down to by service performance and the safety and sanitation of agent oil.Therefore, Exploitation Depth Porous deproteinized bone
Technology is for the energy and the great important meaning of environmental protection.
US5609752 disclose it is a kind of improve distillate Cetane number method, this method can be used for processing catalytic diesel oil,
Straight-run diesel oil, gas oil (doing to 390 DEG C or so) or its miscella.Used catalyst activity component is platinum family and Mo, W
At least one of, carrier is the beta-molecular sieve of hydro-thermal process, using aluminium oxide as binder.However, the catalyst sulfur resistive, nitrogen are malicious
Change ability is poor, it is desirable that the sulfur content of feedstock oil is lower than 1ppm lower than 20ppm, nitrogen content.And catalyst have to pass through reduction,
Vulcanize two procedures, operation is relative complex, can not achieve the purpose of deeply de-aromatizing.
CN105080598A discloses a kind of aluminium oxide-titanium oxide compound, the palladium system of beta-molecular sieve composite carrier load urges
Agent is used for aromatic hydrogenation treatment process.By the content of modulation different carriers, it is strong to obtain suitable specific surface area, Kong Rong and acid
Then palladium is immersed on complex carrier by the carrier of degree, reduction obtains the palladium series catalyst of composite carrier load.Study table
It is bright, the aromatic hydrogenation saturated activity and sulfur resistive ability of catalyst can be significantly improved using acid carrier.The catalyst carrier
Containing acid stronger molecular sieve, the reaction of catalytic cracking is caused to increase, the yield of target oil product reduces.
US6210563 discloses a kind of method of hydrotreating for improving diesel cetane-number.This method is used to handle boiling range
175-400 DEG C light cycle oil, heavy-cycle oil, solvent naphtha etc..It requires the sulfur content of charging not higher than 600ppm, nitrogen content
Higher than 50ppm.This method uses novel noble metal/Large pore molecular sieve catalyst, which may be implemented the selection of aromatic hydrocarbons
Property ring-opening reaction, can be improved the Cetane number of diesel product.But the catalyst will also result in a degree of catalysis and split
Solution, reduces the yield of target oil product, also, can not achieve the target of deeply de-aromatizing.
United States Patent (USP) US5258346 discloses a kind of aromatic hydrocarbon hydrogenation catalyst of reduction-state Ni as active component, can be with
Hydrogenation aromatics-removing for the especially heavier hydrocarbon-fraction of various oil products.The patent thinks that the pore size distribution for improving catalyst is to improve to urge
The key of agent sulfur poisoning resistance.But it can be seen that the sulfur resistive ability of the catalyst is still limited, from embodiment
Seeking the sulfur content in raw material is only 4ppm, and therefore, it is difficult to industrially carry out practical application.
Summary of the invention
The present invention is intended to provide a kind of Subnano-class PtPd noble metal catalyst with ordered mesoporous aluminium oxide load is used for
Compared with the method that aromatic hydrocarbons in hydrocarbon ils is removed in depth under temperate condition.
The technical solution adopted by the present invention are as follows:
A) enter hydrogenator after feedstock oil and hydrogen mixing, contacted with catalytic hydro-dearomatization catalyst；
B the product after) reacting is isolated to gas-phase product and liquid product, and gas-phase product is recycled after compression,
Liquid product is then isolated to the product of low aromatic hydrocarbons.
The step A) described in feedstock oil be various hydrocarbon ils, selected from various diesel oil distillates, kerosene distillate, gasoline fraction,
One of solvent naphtha or two kinds or more.Sulfur content in feedstock oil should not exceed 500ppm, optimal situation be 150ppm with
Under；Nitrogen content in raw material is not more than 200ppm, and optimal situation is in 50ppm or less.
The step A) described in catalyst be sub-nanometer scale PtPd/Al2O3Catalyst；PtPd is in catalyst
Mass percent is 0.5-2.5%, preferably 1-1.5%；The mass ratio of PtPd is 1:10-10:1, preferably 1:4；Described
Al2O3For ordered mesopore structure, wherein mesoporous pore size is uniform, pore size 4-8nm, vertical length direction ([001] face) hole shape
Shape is hexagon, and Lewis acidic site is 800-1200 μm of ol/g.Specific surface area is 260m2/ g, Kong Rongwei 0.86cm3/g。
Process conditions are as follows: hydrogen partial pressure 3-7MPa, preferably 5MPa；180-270 DEG C of reaction temperature, preferably 220 DEG C；Volume
Air speed 1.0-12h-1, preferably 5h-1；Hydrogen to oil volume ratio 100-800Nm3/m3, preferably 500Nm3/m3。
Method provided by the invention can handle including diesel oil distillate, kerosene distillate, gasoline the adaptable of feedstock oil
Various hydrocarbon ils including fraction, solvent naphtha.The high income of arene engaging scraping rate and target product, arene content can be down in product
Mass percent 0.1% hereinafter, target product yield mass percent 99% or more.The noble metal catalyst aromatic hydrocarbons of use adds
Hydrogen activity is high, and resisting sulfide, nitride poisoning performance are strong, and stability is good, and reaction condition is mild, and air speed is high.
Specific embodiment
In order to further illustrate the present invention, following embodiment is enumerated, but it is not intended to limit each accessory claim and is defined
Invention scope.
Catalyst preparation step employed in embodiment is as follows:
A. it weighs 2.0g P123 to be dissolved in 40ml dehydrated alcohol, the concentrated nitric acid that 3ml mass concentration is 65% is added dropwise, acutely
It is added with stirring 4.08g aluminium isopropoxide, being vigorously stirred is completely dissolved aluminium isopropoxide.
B. PtPd/Al is pressed2O3In the 1wt% mass percent of PtPd, PtPd mass ratio be that 1:4 prepares chloroplatinic acid, chlorine
Change palladium solution 1ml, be added dropwise in above-mentioned solution dropwise, continues to stir 5h.
C. mixed solution in b is placed in 60 DEG C of environment, evaporates dry alcohol solvent, continue aging 48h.
D. by solid obtained in above-mentioned steps, 400 DEG C is risen to from room temperature with the heating rate of 1 DEG C/min, roasts 4h.
E. by solid obtained in above-mentioned steps, with the heating rate of 5 DEG C/min and 60ml/g hydrogen flowing quantity, at 250 DEG C
It is restored, by obtained solid powder tabletting, sieving, taking partial size is 20-40 mesh solid particle, obtains as-reduced metal catalysis
Agent 1wt%PtPd/Al2O3。
Embodiment 1
The present embodiment is using diesel oil distillate as feedstock oil, arene content 36.5%, sulfide content 500ppm, nitride
Content is 70ppm.The feedstock oil is mixed with hydrogen, the volume ratio of hydrogen and feedstock oil is 500Nm3/m3, reaction pressure is
5MPa, reaction temperature are 220 DEG C, air speed 5h-1.After hydrotreating, arene content is down in obtained diesel product
1.4%, diesel yield 99%.
Comparative example 1
Using diesel oil distillate feedstock oil in the same manner as in Example 1 and process conditions, only catalyst uses PtPd/Y points instead
Son sieve, the mass ratio that the mass percent of PtPd is 1%, PtPd is 1:4.Arene content is in obtained diesel product
24.2%, diesel yield 98%.
Embodiment 2
It is 26.4% in addition to feedstock oil is changed to arene content, sulfide content 150ppm, amount of nitrides is 10ppm's
Diesel oil；Air speed is changed to 7h-1.According to same operating method in embodiment 1, arene content is in obtained diesel product
0.8%, diesel yield 99%.
Comparative example 2
Using diesel oil distillate feedstock oil in the same manner as in Example 2 and process conditions, only catalyst uses PtPd/Y points instead
Son sieve, the mass ratio that the mass percent of PtPd is 1%, PtPd is 1:4.Arene content is 15% in obtained diesel product,
Diesel yield is 97.8%.
Embodiment 3
It is 24% in addition to feedstock oil is changed to arene content, sulfide content 50ppm, amount of nitrides is the coal of 5ppm
Oil.According to same operating method in embodiment 1, less than 0.2%, kerosene yield is arene content in obtained kerosene products
99%.
Comparative example 3
Using kerosene distillate feedstock oil in the same manner as in Example 3 and process conditions, only catalyst uses PtPd/Y points instead
Son sieve, the mass ratio that the mass percent of PtPd is 1%, PtPd is 1:4.Arene content is 12% in obtained kerosene products,
Kerosene yield is 98%.
Claims (8)
1. a kind of method of hydrocarbon ils deeply de-aromatizing, key step are as follows:
A) enter hydrogenator after feedstock oil and hydrogen mixing, contacted with catalytic hydro-dearomatization catalyst；
B the product after) reacting is isolated to gas-phase product and liquid product, and gas-phase product is recycled after compression, liquid phase
Product is then isolated to product of the aromatics quality content less than 2%；
The step A) in the catalyst that uses for the PtPd/Al of sub-nanometer scale2O3Catalyst；
Step A) described in sub-nanometer scale PtPd/Al2O3The mass percent of PtPd is 0.5-2.5% in catalyst；Described
Al2O3For ordered mesopore structure, wherein mesoporous pore size is uniform, pore size 4-8nm, and vertical length direction is [001] face shape
Shape is hexagon, and Lewis acidic site is 800-1200 μm of ol/g.
2. according to method of claim 1, it is characterised in that: step A) described in feedstock oil be various hydrocarbon ils.
3. according to method for claim 2, it is characterised in that: the various hydrocarbon ils are selected from various diesel oil distillates, kerosene distillate, vapour
One of oil distillate, solvent naphtha or two kinds or more.
4. according to method of claim 1, it is characterised in that: the mass ratio of the Pt and Pd is 1:10-10:1.
5. according to method of claim 1, it is characterised in that: step A) described in sub-nanometer scale PtPd/Al2O3In catalyst
The mass percent of PtPd is 1-1.5%.
6. according to method for claim 4, it is characterised in that: the mass ratio of the Pt and Pd is 1:4.
7. according to method of claim 1, it is characterised in that: reactor uses fixed bed reactors, process conditions are as follows: hydrogen partial pressure
3-7MPa, reaction temperature 180-270oC, volume space velocity 1.0-12h-1, hydrogen to oil volume ratio 100-800Nm3/m3。
8. according to the method for claim 1, it is characterised in that: the Al2O3Specific surface area be 260m2/ g, Kong Rongwei
0.86cm3/g。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611031935.1A CN108085058B (en) | 2016-11-22 | 2016-11-22 | A kind of method of hydrocarbon ils deeply de-aromatizing |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611031935.1A CN108085058B (en) | 2016-11-22 | 2016-11-22 | A kind of method of hydrocarbon ils deeply de-aromatizing |
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| Publication Number | Publication Date |
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| CN108085058A CN108085058A (en) | 2018-05-29 |
| CN108085058B true CN108085058B (en) | 2019-07-12 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102205241A (en) * | 2010-03-31 | 2011-10-05 | 中国石油化工股份有限公司 | Aromatic hydrogenated saturated catalyst and application thereof |
| CN102424411A (en) * | 2011-09-15 | 2012-04-25 | 暨南大学 | Preparation method for ordered mesoporous gamma-Al2O3 |
| CN103539173A (en) * | 2013-10-06 | 2014-01-29 | 太原理工大学 | Highly thermostable and ordered mesoporous alumina material and preparation method thereof |
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| JP2005518326A (en) * | 2002-02-15 | 2005-06-23 | ロディア・シミ | Mesoporous compounds containing mineral phases of alumina and particles of cerium, titanium or zirconium oxide and optionally solid solution elements in these particles, their preparation and their use |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102205241A (en) * | 2010-03-31 | 2011-10-05 | 中国石油化工股份有限公司 | Aromatic hydrogenated saturated catalyst and application thereof |
| CN102424411A (en) * | 2011-09-15 | 2012-04-25 | 暨南大学 | Preparation method for ordered mesoporous gamma-Al2O3 |
| CN103539173A (en) * | 2013-10-06 | 2014-01-29 | 太原理工大学 | Highly thermostable and ordered mesoporous alumina material and preparation method thereof |
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