CN103464210A - Light-hydrocarbon isomerization catalyst and method for preparing same - Google Patents
Light-hydrocarbon isomerization catalyst and method for preparing same Download PDFInfo
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- 239000003054 catalyst Substances 0.000 title claims abstract description 86
- 238000006317 isomerization reaction Methods 0.000 title claims abstract description 24
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title abstract description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000011347 resin Substances 0.000 claims abstract description 13
- 229920005989 resin Polymers 0.000 claims abstract description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 12
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims abstract description 10
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims abstract description 10
- 229910052763 palladium Inorganic materials 0.000 claims abstract description 7
- 238000002360 preparation method Methods 0.000 claims description 18
- 229930195733 hydrocarbon Natural products 0.000 claims description 16
- 150000002430 hydrocarbons Chemical class 0.000 claims description 15
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 239000002904 solvent Substances 0.000 claims description 8
- GPNDARIEYHPYAY-UHFFFAOYSA-N palladium(ii) nitrate Chemical compound [Pd+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O GPNDARIEYHPYAY-UHFFFAOYSA-N 0.000 claims description 7
- 238000001994 activation Methods 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 150000002940 palladium Chemical class 0.000 claims description 4
- 238000000197 pyrolysis Methods 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims description 2
- 238000002791 soaking Methods 0.000 claims 1
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052731 fluorine Inorganic materials 0.000 abstract description 7
- 239000011737 fluorine Substances 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 4
- 239000007791 liquid phase Substances 0.000 abstract description 2
- 150000001805 chlorine compounds Chemical class 0.000 abstract 2
- 238000000151 deposition Methods 0.000 abstract 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 6
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- 239000002131 composite material Substances 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 230000004048 modification Effects 0.000 description 6
- 238000012986 modification Methods 0.000 description 6
- 239000010457 zeolite Substances 0.000 description 6
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000004913 activation Effects 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- -1 Hydrogen hydrocarbon Chemical class 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical group C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007123 defense Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005216 hydrothermal crystallization Methods 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229910052680 mordenite Inorganic materials 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses light-hydrocarbon isomerization catalyst and a method for preparing the light-hydrocarbon isomerization catalyst. Resin ribbon ball-shaped active carbon having high specific surface area and a micro-hole structure serves as the carrier, is roasted under high temperature and is activated through hydrogen fluoride to obtain a carrier with high specific surface area and a mesoporous structure, palladium loading is then carried out according to a liquid phase deposition method, and modifying is carried out through fluorine-containing chlorides at the same time to obtain the light-hydrocarbon isomerization catalyst. The light-hydrocarbon isomerization catalyst has extremely large specific surface area and a proper hole structure, and has good isomerization performance after modifying is carried out through the fluorine-containing chlorides. High activity of the light-hydrocarbon isomerization catalyst can still be kept after long-period operation and the light-hydrocarbon isomerization catalyst is long in service life.
Description
Technical field
The present invention relates to a kind of method for preparing catalyst, particularly a kind of catalyst for isomerizing light hydrocarbon and preparation method thereof.
Technical background
C5, C6 alkane isomerization technique are that the n-alkane in raw material is converted into to corresponding isohydrocarbon, and increasing the gasoline lightweight is partly the octane number of " front end ", make the boiling range of gasoline and octane number have one reasonably to distribute.Due to isomerized oil be a kind of low-sulfur, without the environmental friendly product of aromatic hydrocarbons and alkene, can meet new environmental protection requirement, so C5, C6 alkane isomerization technique occupy an important position in Clean Fuel Production.
CN1270990A provides a kind of catalyst for isomerizing light hydrocarbon, VIII family metal and composite zeolite carrier by 0.01～2.0 heavy % form, described composite zeolite carrier is comprised of the aluminium oxide of 10～90 heavy % and the composite zeolite of 10～90 heavy %, the modenite of the Beta zeolite that wherein composite zeolite is 1～99 heavy % and 1～99 heavy %.Described catalyst is, after h-mordenite, Hydrogen Beta zeolite and aluminium oxide are mixed, make complex carrier through roasting, then load VIII family metal-made to obtain.This catalyst is applicable to C
5/ C
6isomerization of paraffins, can effectively improve their octane number.But this catalyst exists, and technological process is long, service life shorter problem.
Preparation method and the application of a CN102941115A positive structure hydrocarbons hydrogenation isomerization catalyst.This preparation method comprises the following steps: after deionized water and phosphorus source are mixed, add respectively ,Gui source, aluminium source and micropore template, stir, then add mesoporous template, stir and obtain colloidal sol and carry out ageing, add matrix, carry out the Dynamic Hydrothermal crystallization; To product washed, separated, dry, roasting, obtain step hole SAPO-11/ γ-Al
2o
3composite; Adopt equi-volume impregnating, the metal active constituent step impregnation is arrived to described step hole SAPO-11/ γ-Al
2o
3on composite, then through room temperature dry, dry, roasting, obtain positive structure hydrocarbons hydrogenation isomerization catalyst.This catalyst when keeping higher positive structure hydrocarbons hydrogenation isomerisation conversion, have good two side chains and highly-branched chain isomerous body selectively, but this catalyst still exists that technological process is grown, service life shorter problem.
The stability of catalyst ubiquity carrier to load metal of the prior art is low, and catalyst is short service life, and the shortcomings such as low conversion rate need to be done the more deep Improvement that carries out.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of catalyst for isomerizing light hydrocarbon and preparation method thereof.
It is support material that the resin based sphere active carbon with high-specific surface area and microcellular structure is take in the present invention, high-temperature roasting is also used hydrogen fluoride to be activated, obtain the carrier that high-specific surface area and central hole structure increase, then by liquid phase sedimentation supported palladium, use containing fluorochloride and carry out modification simultaneously, thereby obtain catalyst for isomerizing light hydrocarbon.
The invention provides a kind of catalyst for isomerizing light hydrocarbon and preparation method thereof, realize by following steps:
1). the preparation of carrier:
Resin based sphere active carbon is moved into to pyrolysis in the electric tube furnace that passes to nitrogen stream, slowly heat up and rise to 600～1200 ℃ from room temperature, (preferably 800 ℃), after intensification finishes, nitrogen is switched to the hydrogen fluoride that flow is 3L-8L/ hour (preferably 5L/ hour) activation process 2～10 hours, (preferably 5 hours), product is chilled to room temperature.Obtain catalyst carrier;
2). load operation:
The preferred 4h of 2～5h(will be soaked) in the catalyst carrier alcohol solvent, the mass ratio of catalyst carrier and alcohol solvent is the preferred 1:3 of 1:1-1:5(), then add and account for the palladium salt that the catalyst carrier mass percent is 1～5% and carry out load, palladium salt can be palladium bichloride, palladium nitrate, palladium etc., preferably palladium nitrate, load time is 10-40 hour, (preferably 30 hours); Add afterwards the fluorochloride that contains that the catalyst carrier mass percent is 5～10%, 0～30 ℃ (preferably 15 ℃), react the preferred 15h of 10～20h(), product, through separating, cleaning with ethanol, is dried, and obtains catalyst for isomerizing light hydrocarbon.
Resin based sphere active carbon is commercially available prod, by macropore phenylethylene resin series polymer, through roasting, is made, and has higher specific area, and as the resin based sphere active carbon that Shanxi enterprise of Cui Hong Science and Technology Ltd. produces, specific area is greater than 800m
2/ g.
Containing the preferred CCl of fluorochloride
3f, CHCl
2f, more preferably CCl
3f.
The specific area of the catalyst carrier obtained is 200-800m
2/ g, have the mesopore of 70%-90% and the micropore of 10%-30% in catalyst carrier.
Adopt preparation method of the present invention, there is following beneficial effect:
1: the carrier of the catalyst obtained has high specific area and suitable pore structure, can greatly improve the stability of carrier to load metal, and then improves the isomerization performance of catalyst.
2: fluorine-containing muriatic modification makes catalyst have higher isomerization performance.
3: there is higher isomerization activity, move continuously 10 days after its optimal conversion up to 89%, the product octane number is up to 80%-85%, catalyst still can keep higher active catalyst after long period of operation, be more than 2 years service life.
The specific embodiment
Following instance is only to further illustrate the present invention, is not the restriction the scope of protection of the invention.
Embodiment 1:
Resin based sphere active carbon, Shanxi Cui Hong Science and Technology Ltd. produces
Sphere diameter is at 0.3-1.2mm, specific area (BET) 950-1200 (m
2/ g), pore volume 0.6-0.75ml/g.
1). the preparation of carrier:
Resin based sphere active carbon is moved into to pyrolysis in the electric tube furnace pass to nitrogen stream, slowly heat up and rise to 800 ℃ from room temperature, to the rear 5L/ hour flow of temperature, nitrogen is switched to hydrogen fluoride activation process 5h, product is chilled to room temperature.Obtain catalyst carrier.In catalyst carrier, mesopore accounts for 82%, and micropore accounts for 18%.
2). load operation
Catalyst carrier is soaked in alcohol solvent to 4h, the mass ratio of catalyst carrier and alcohol solvent is 1:3, adds and accounts for the palladium nitrate that the catalyst carrier mass percent is 3%, and load time is 30 hours.Then add the CCl that the catalyst carrier mass percent is 7%
3f, 15 ℃ of reaction 15h, product, through separating, cleans with ethanol, dries, and obtains carrying the resin carbon catalyst prod of palladium, is numbered KRB-1.In catalyst, mesopore accounts for 83%, and micropore accounts for 17%.
Embodiment 2
Add in step 2 and account for the palladium nitrate that the catalyst carrier mass percent is 1%, the other the same as in Example 1.Products obtained therefrom is numbered KRB-2.In catalyst carrier, mesopore accounts for 85%, and micropore accounts for 15%.
Embodiment 3
Add in step 2 and account for the palladium nitrate that the catalyst carrier mass percent is 5%, the other the same as in Example 1.Products obtained therefrom is numbered KRB-3.In catalyst carrier, mesopore accounts for 81%, and micropore accounts for 19%.
Embodiment 4
Add in step 2 and account for the CCl that the catalyst carrier mass percentage concentration is 5%
3f, the other the same as in Example 1.Products obtained therefrom is numbered KRB-4.In catalyst carrier, mesopore accounts for 86%, and micropore accounts for 14%.
Embodiment 5
Add in step 2 and account for the CCl that the catalyst carrier mass percentage concentration is 5%
3f, the other the same as in Example 2.Products obtained therefrom is numbered KRB-5.In catalyst carrier, mesopore accounts for 82%, and micropore accounts for 18%.
Embodiment 6
Add in step 2 and account for the CCl that the catalyst carrier mass percentage concentration is 5%
3f, the other the same as in Example 3.Products obtained therefrom is numbered KRB-6.In catalyst carrier, mesopore accounts for 84%, and micropore accounts for 16%.
Embodiment 7
Add in step 2 and account for the CCl that the catalyst carrier mass percent is 10%
3f, the other the same as in Example 1.Products obtained therefrom is numbered KRB-7.In catalyst carrier, mesopore accounts for 87%, and micropore accounts for 13%.
Embodiment 8
Add in step 2 and account for the CCl that the catalyst carrier mass percent is 10%
3f, the other the same as in Example 2.Products obtained therefrom is numbered KRB-8.In catalyst carrier, mesopore accounts for 81%, and micropore accounts for 19%.
Embodiment 9
Add in step 2 and account for the CCl that the catalyst carrier mass percent is 10%
3f, the other the same as in Example 3.Products obtained therefrom is numbered KRB-9.In catalyst carrier, mesopore accounts for 84%, and micropore accounts for 16%.
Comparative example 1:
Catalyst carrier adopts modenite to activate without hydrogen fluoride, and without fluorine-containing muriatic modification, the other the same as in Example 1.In catalyst carrier, mesopore accounts for 19%, and micropore accounts for 81%.Products obtained therefrom is numbered KRB-10.
Comparative example 2:
Catalyst carrier adopts resin based sphere active carbon, but without the hydrogen fluoride activation, and without fluorine-containing muriatic modification, the other the same as in Example 1.In catalyst carrier, mesopore accounts for 66%, and micropore accounts for 34%.Products obtained therefrom is numbered KRB-11.
Comparative example 3:
In step 1, resin based sphere active carbon activates without hydrogen fluoride, the other the same as in Example 1.In catalyst carrier, mesopore accounts for 67%, and micropore accounts for 33%.Products obtained therefrom is numbered KRB-12.
Comparative example 4:
In step 2, resin based sphere active carbon is without fluorine-containing muriatic modification, the other the same as in Example 1.In catalyst carrier, mesopore accounts for 77%, and micropore accounts for 23%.Products obtained therefrom is numbered KRB-13.
Embodiment 10. catalyst are for the evaluation of light hydrocarbon isomerization reaction
Experiment adopts CDS2804 type micro-trans-chromatogram arrangement continuously.From the gas cylinder decompression, by mass flowmenter, detected; Pentane is carried by the high pressure micro pump, and enters reactor after H2 mixing preheating.Hydrogen hydrocarbon mol ratio=2.5, reactor is φ 10mm * 2mm stainless steel tube, catalyst hydrogenation gas reduction 4h, the constant temperature zone in the reactor middle part, 250 ℃ of reaction temperatures, pressure 1MPa, top and the bottom filling quartz sand.Tail gas by the needle-valve adjust flux after the air defense, catalyst activity means with the n-pentane isomerization conversion ratio.
Table 1: the comparison of the test specimen n-pentane isomerization conversion ratio that different process is made
As shown in Table 1: product isomerisation conversion of the present invention is higher, and can use for a long time, this is because its shape selective had and restriction aperture are very effective to suppressing side reaction, this is because hydrogen fluoride activation rear catalyst micropore volume reduces, mesopore rolls up, and fluorine-containing muriatic modification simultaneously makes catalyst have good isomerization performance.Catalyst of the present invention has the product octane number of higher isomerization activity and Geng Gao, has market prospects preferably.
Claims (9)
1. the preparation method of a catalyst for isomerizing light hydrocarbon comprises the following steps realization:
1). the preparation of carrier:
Resin based sphere active carbon is moved into to pyrolysis in the electric tube furnace that passes to nitrogen stream, slowly heat up and rise to 600～1200 ℃ from room temperature, after heat up finishing, nitrogen is switched to hydrogen fluoride that flow is 3L-8L/ hour activation process 2～10 hours, product is chilled to room temperature, obtains catalyst carrier;
2). load operation:
To in the catalyst carrier alcohol solvent, soak 2～5h, the mass ratio of catalyst carrier and alcohol solvent is 1:1-1:5, then add to account for the palladium salt that the catalyst carrier mass percent is 1～5% and carry out load, and, load time is 10-40h; Add afterwards the fluorochloride that contains that the catalyst carrier mass percent is 5～10%, 0～30 ℃ of reaction 10～20h, product, through separating, cleaning with ethanol, is dried, and obtains catalyst for isomerizing light hydrocarbon.
2. preparation method according to claim 1, is characterized in that: in step 1), slowly heat up and rise to 800 ℃ from room temperature, hydrogen fluoride activation process 5 hours.
3. preparation method according to claim 1, is characterized in that: step 2) in, will in the catalyst carrier alcohol solvent, soaking 4h, the mass ratio of catalyst carrier and alcohol solvent is 1:3, load time is 30h.
4. preparation method according to claim 1, is characterized in that: step 2) in, add the fluorochloride that contains that the catalyst carrier mass percent is 5～10%, 15 ℃ of reaction 15h.
5. preparation method according to claim 1, it is characterized in that: palladium salt is palladium bichloride, palladium nitrate, palladium or palladium nitrate.
6. preparation method according to claim 1, is characterized in that: containing fluorochloride, be CCl
3f or CHCl
2f.
7. preparation method according to claim 1, it is characterized in that: the specific area of the catalyst carrier that step 1) obtains is 200-800m
2/ g, have the mesopore of 70%-90% and the micropore of 10%-30% in catalyst carrier.
8. the catalyst for isomerizing light hydrocarbon that the arbitrary preparation method of claim 1-7 obtains.
9. the application of the described catalyst of claim 8 in light hydrocarbon isomerization.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310449902.9A CN103464210B (en) | 2013-09-27 | 2013-09-27 | Light-hydrocarbon isomerization catalyst and method for preparing same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310449902.9A CN103464210B (en) | 2013-09-27 | 2013-09-27 | Light-hydrocarbon isomerization catalyst and method for preparing same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103464210A true CN103464210A (en) | 2013-12-25 |
| CN103464210B CN103464210B (en) | 2015-07-22 |
Family
ID=49789381
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310449902.9A Expired - Fee Related CN103464210B (en) | 2013-09-27 | 2013-09-27 | Light-hydrocarbon isomerization catalyst and method for preparing same |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105562107A (en) * | 2015-12-21 | 2016-05-11 | 王金明 | N-pentane isomerization catalyst |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0552069B1 (en) * | 1992-01-15 | 1996-04-24 | Institut Francais Du Petrole | Lowering of the benzene content in gasolines by isomerisation |
| US6080904A (en) * | 1993-07-22 | 2000-06-27 | Mobil Oil Corporation | Isomerization process |
| CN1328114A (en) * | 2000-06-13 | 2001-12-26 | 大庆石油学院 | Catalyst for isomerizing light hydrocarbon and its preparing process |
-
2013
- 2013-09-27 CN CN201310449902.9A patent/CN103464210B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0552069B1 (en) * | 1992-01-15 | 1996-04-24 | Institut Francais Du Petrole | Lowering of the benzene content in gasolines by isomerisation |
| US6080904A (en) * | 1993-07-22 | 2000-06-27 | Mobil Oil Corporation | Isomerization process |
| CN1328114A (en) * | 2000-06-13 | 2001-12-26 | 大庆石油学院 | Catalyst for isomerizing light hydrocarbon and its preparing process |
Non-Patent Citations (1)
| Title |
|---|
| LUO LIWEN ET AL.: "Study of Modification and Performance of HZSM-5 Catalyst for Isomerization of Light Paraffin", 《PETROLEUM SCIENCE》, vol. 2, no. 2, 31 December 2005 (2005-12-31), pages 112 - 115 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105562107A (en) * | 2015-12-21 | 2016-05-11 | 王金明 | N-pentane isomerization catalyst |
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Address after: 062451 Cangzhou City, Hebei Province Hejian City Gu Xian Xiang Xi Liu Zhuang Applicant after: Kai Rui environmental protection Science and Technology Co., Ltd. Address before: 062451, Hebei City, Cangzhou Province Hejian City West Zhuang Industrial Zone Applicant before: Kairui Chemical Co., Ltd. |
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