CN108246352A - A kind of C5, C6 linear chain olefin skeleton isomerism catalyst and its preparation method and application - Google Patents
A kind of C5, C6 linear chain olefin skeleton isomerism catalyst and its preparation method and application Download PDFInfo
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- CN108246352A CN108246352A CN201611236399.9A CN201611236399A CN108246352A CN 108246352 A CN108246352 A CN 108246352A CN 201611236399 A CN201611236399 A CN 201611236399A CN 108246352 A CN108246352 A CN 108246352A
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- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/65—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38, as exemplified by patent documents US4046859, US4016245 and US4046859, respectively
- B01J29/66—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the ferrierite type, e.g. types ZSM-21, ZSM-35 or ZSM-38, as exemplified by patent documents US4046859, US4016245 and US4046859, respectively containing iron group metals, noble metals or copper
- B01J29/67—Noble metals
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- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- 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
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
-
- 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
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
Abstract
A kind of C5、C6The preparation method of linear chain olefin skeleton isomerism catalyst, includes the following steps：Step 1, by 35 molecular sieves of H ZSM and activated alumina according to 320:100~700:100 quality compares kneading；The mixture of organic acid soln and Pd solution is added to kneading in the mixture of 35 molecular sieves of H ZSM and activated alumina by step 2 by several times, and the mixture and the quality of 35 molecular sieves of H ZSM and the mixture of activated alumina of organic acid soln and Pd solution are 60:100~170:100；And step 3, above-mentioned kneading material extrusion is shaped, 100~130 DEG C of dry 1~3h, 500~550 DEG C of 3 4h of roasting.The present invention is by under hydro condition, by the linear alkene component (C in catalytic gasoline5 =、C6 =) same carbon number band branched-chain alkene component is partially converted into, improve the octane number of gasoline.Before and after conversion, the hydro carbons race composition of gasoline is constant, and research octane number (RON) can improve 0.5 1.0 units.
Description
Technical field
The present invention relates to the methods more particularly to one kind that a kind of full fraction catalytic gasoline or catalysis heavy petrol octane number improve
The preparation process of the olefin skeletal isomerization catalyst i.e. start-up method and process conditions of the olefin skeletal isomerization catalyst.
Background technology
The environmental problem of getting worse brought to alleviate motor vehicle exhaust emission, emission performance requirement of the China to motor petrol
(S contents olefin(e) centent) is increasingly harsher.The gasoline pool composition in China, catalytically cracked gasoline account for more than 70%, catalytic cracking vapour
Oily desulfurization, Olefin decrease become the major measure of production cleaning motor petrol.Catalytic gasoline is during desulfurization, Olefin decrease, octane
Value can also lose.How under the premise of the sulfur content of catalytic gasoline, olefin(e) centent reach requirement, make catalytic gasoline octane number few
Loss not even loss becomes one of hot subject of current oil refining technical field.
At present, in view of the above-mentioned problems, industrial production is there are mainly two types of process program, as shown in Figure 1 and Figure 2.Wherein, it is catalyzed
Octane number is promoted, and is mainly realized by the way that hydrocarbon isomerization, aromatisation occur on solid acid catalyst.
Single branched chain isomer occurs by linear paraffin on highly acid H-ZSM-5 or H- beta-zeolite catalyst for CN1488722A
To improve the octane number of catalytic gasoline.Since acidic zeolite used is stronger, in initial reaction stage, occur a large amount of hydrocarbon-based polymeric,
Cracking side-reaction causes isomery hydrocarbon-selective poor, and the easy coking deactivation of catalyst.
CN 10508908A propose a kind of hydrofinishing catalytic gasoline octane value recovering technology.A kind of catalysis is invented
Gasoline hydrogenation modifying catalyst, composition include：3-8%MoO3, 1-3%CoO, 3-5%NiO, 50-70%SAPO-11 and Al-
Ti composite oxides.The catalyst is in 1-3MPa, 300-360 DEG C, 1-4h-1, under conditions of hydrogen-oil ratio 200-600, pass through alkane
Highly branched chain hydroisomerizing realizes the promotion of treated gasoline octane number.
The catalyst supplements desulfurization-octane value recovering bifunctional catalyst for hydrofined gasoline, at present in grand celebration stone
Change, Fushun petrochemical industry Deng Jijia refineries carry out commercial Application.On the easy neutralizing molecule sieve of alkaline metal oxide on the catalyst
Acid centre, and then influence catalyst alkane highly-branched chain isomerousization performance.At present, the catalyst is in the industry of Fushun petrochemical industry
Using there is the problem of hydro-upgrading product gasoline octane number does not rise anti-drop.
Fushun petrochemical industry research institute develops a kind of gasoline hydrogenation modifying catalyst F0-35M (M agent).M agent passes through alkene
Aromatisation makes up catalytic gasoline loss of octane number caused by some olefin saturation in unifining process, and further drop
Low content of olefin in gasoline.M- agent is urged at present in many enterprises such as Urumchi petrochemical industry, Yumen refinery and GHC-11 hydrodesulfurizations
Agent is used in combination.380-400 DEG C of the use condition of M agent, 1.8-2.2MPa, hydrogen-oil ratio 300-400, volume space velocity 3-5h-1, with
Modification feed gasoline is compared, and upgraded products gasoline Research octane number can at most improve 1 unit.
Using M agent, need first to be passivated it and presulfurization, as the gasoline upgrading agent with CN10508908A inventions,
Its start-up process is complicated, cumbersome.
The C of domestic catalytic gasoline5 =、C6 =Shared mass fraction is substantially in 10%-20%, all kinds of light dydrocarbons, C 6 olefin octane
Value is as follows：
Normal olefine in catalytic gasoline is converted into isomeric olefine can be new as improve catalytic gasoline octane number one
Thinking.
Invention content
The purpose of the present invention is to provide a kind of C5、C6Linear chain olefin skeleton isomerism catalyst and its preparation method and application.
To achieve the above object, the present invention provides a kind of C5、C6The preparation method of linear chain olefin skeleton isomerism catalyst, packet
Include following steps：
Step 1, by H-ZSM-35 molecular sieves and activated alumina according to 320:100~700:100 quality compares kneading；
The mixture of organic acid soln and Pd solution is added to H-ZSM-35 molecular sieves and active oxidation by step 2 by several times
Kneading in the mixture of aluminium, the mixing of organic acid soln and the mixture and H-ZSM-35 molecular sieves and activated alumina of Pd solution
The quality of object is 60:100~170:100；And
Step 3 shapes above-mentioned kneading material extrusion, 100~130 DEG C of dry 1~3h, 500~550 DEG C of roasting 3-4h.
Further, SiO in the H-ZSM-35 molecular sieves2With Al2O3Mass ratio for 20~90, crystallite dimension 1.0
~3.0 μm.
Further, the activated alumina is γ-Al2O3, BET specific surface area is 230~290m2/ g, hole appearance 0.3~
1.0ml/g。
Further, the organic acid soln is the citric acid solution of 0.1~1.0mol/L and the vinegar of 0.1~1.0mol/L
One or both of acid solution.
Further, the Pd solution is the [Pd (NH of 5~20wt%3)4](NO3)2Aqueous solution.
Further, the mass ratio of organic acid soln and organic acid soln in the mixture of Pd solution and Pd solution is 220:
1~270:1.
Further, in the mixture and H-ZSM-35 molecular sieves of organic acid soln and Pd solution and mixing for activated alumina
It closes and extrusion lubricant is added in the kneading process of object, the extrusion lubricant is one kind or two in sesbania powder and methylcellulose
Kind.
To achieve the above object, the present invention also provides catalyst prepared by a kind of above-mentioned preparation method, the catalyst
Use condition is 1.5~2.5MPa of pressure, 300~400 DEG C of temperature, 3.0~5.0h of volume space velocity-1, hydrogen to oil volume ratio 150~
250。
To achieve the above object, the answering in catalytic gasoline octane number is promoted the present invention also provides a kind of catalyst
With.
Further, the catalytic gasoline is catalytic gasoline of whole fraction, C6~C13Hydro carbons mass fraction>99% urges
Change heavy petrol.
The beneficial effects of the invention are as follows：The catalyst prepared with the method for the invention will be catalyzed vapour under hydro condition
Linear alkene component (C in oil5 =、C6 =) same carbon number band branched-chain alkene component is partially converted into, improve the octane number of gasoline.Turn
Before and after change, the hydro carbons race composition of gasoline is constant, and research octane number (RON) can improve 0.5-1.0 unit.
Description of the drawings
Fig. 1 is the process flow chart that catalytic gasoline reduces loss of octane number during desulfurization, Olefin decrease in the prior art.
Fig. 2 is another technique stream that catalytic gasoline reduces loss of octane number during desulfurization, Olefin decrease in the prior art
Cheng Tu.
Specific embodiment
It elaborates below to the embodiment of the present invention：The present embodiment is carried out lower based on the technical solution of the present invention
Implement, give detailed embodiment and process, but protection scope of the present invention is not limited to following embodiments.
A kind of C5、C6The preparation method of linear chain olefin skeleton isomerism catalyst, includes the following steps：
Step 1, by H-ZSM-35 molecular sieves and activated alumina according to 320:100~700:100 quality compares kneading；
The mixture of organic acid soln and Pd solution is added to H-ZSM-35 molecular sieves and active oxidation by step 2 by several times
Kneading in the mixture of aluminium, the mixing of organic acid soln and the mixture and H-ZSM-35 molecular sieves and activated alumina of Pd solution
The quality of object is 60:100~170:100；And
Step 3 shapes above-mentioned kneading material extrusion, 100~130 DEG C of dry 1~3h, 500~550 DEG C of roasting 3-4h.
Further, SiO in the H-ZSM-35 molecular sieves2With Al2O3Mass ratio for 20~90, crystallite dimension 1.0
~3.0 μm.
Further, the activated alumina is γ-Al2O3, BET specific surface area is 220~290m2/ g, hole appearance 0.3~
1.0ml/g。
Further, the organic acid soln is the citric acid solution of 0.1~1.0mol/L and the vinegar of 0.1~1.0mol/L
One or both of acid solution.
Further, the Pd solution is the [Pd (NH of 5~20wt%3)4](NO3)2Aqueous solution.
Further, the mass ratio of organic acid soln and organic acid soln in the mixture of Pd solution and Pd solution is 220:
1~270:1.
Further, in the mixture and H-ZSM-35 molecular sieves of organic acid soln and Pd solution and mixing for activated alumina
It closes and extrusion lubricant is added in the kneading process of object, the extrusion lubricant is one kind or two in sesbania powder and methylcellulose
Kind.
Catalyst prepared by a kind of above-mentioned preparation method, the use condition of the catalyst is 1.5~2.5MPa of pressure, temperature
Spend 300~400 DEG C, 3.0~5.0h of volume space velocity-1, hydrogen to oil volume ratio 150~250.
A kind of application of catalyst in catalytic gasoline octane number is promoted.
Further, the catalytic gasoline is catalytic gasoline of whole fraction, C6~C13Hydro carbons mass fraction>99% urges
Change heavy petrol.
It is prepared by olefin skeletal heterogeneous catalyst:
Embodiment 1：
1) 650g H-ZSM-35 powder, 100g γ-Al2O3Powder, the mixing of 10g methylcellulose powders, are sent into NH-06 and mix
It pinches and abundant kneading is carried out in machine.Wherein ZSM-35 molecular sieve is derived from Chinese medicines group (SiO2With Al2O3Mass ratio:32)；γ-Al2O3
For Ju Hua Chinalcos product, BET specific surface area：276m2/ g, pore volume 0.96cc/g.
2) 8g acetic acid (AR), 8g citric acids (AR) are dissolved in 200g deionized waters, fully dissolved.
3) by 1.8g 10m% [Pd (NH3)4](NO3)2Aqueous solution is instilled in 300g deionized waters, is sufficiently mixed.
4) match solution by step 2) and 3) to mix, 4 penetrating kneading machines of mixed solution point, with consolidating in step 1)
The abundant kneading of body mixture.
5) the kneading material in step 4) is extruded into 3.2 clover bar shapeds of Φ, 120 DEG C of dry 3h, 500 DEG C of roastings of Muffle furnace
4h。
Embodiment 2：
1) 327gH-ZSM-35 powder, 100g γ-Al2O3Powder, the mixing of 5g methylcellulose powders, are sent into NH-06 kneadings
Abundant kneading is carried out in machine.Wherein ZSM-35 molecular sieve is derived from Chinese medicines group (SiO2With Al2O3Mass ratio:21)；γ-Al2O3For
Ju Hua Chinalcos product, BET specific surface area：276m2/ g, pore volume 0.96cc/g.
2) 10g citric acids are dissolved in 253g deionized waters, then 0.9g20m% [Pd (NH is added dropwise3)4](NO3)2It is water-soluble
Liquid.
3) step 2) is matched into solution and disposably adds in kneading machine, with the abundant kneading of solid mixture in step 1).
4) the kneading material in step 3) is extruded into 3.2 clover bar shapeds of Φ, 120 DEG C of dry 3h, 500 DEG C of roastings of Muffle furnace
4h。
Embodiment 3：
1) by 120g H-ZSM-35 powder, 37g γ-Al2O3Powder, 1.5g sesbania powders, the mixing of 1.5g methylcellulose,
Middle ZSM-35 molecular sieve is derived from Petroleum Univ. new function material laboratory (SiO2With Al2O3Mass ratio：89), γ-Al2O3
For China Aluminum Co., Ltd's product, BET specific surface area：234m2/ g, pore volume 0.40cc/g.
2) 6.2g acetic acid (AR) is dissolved in 110g water, then 0.9g 15m% [Pd (NH is added dropwise3)4](NO3)2Aqueous solution.
3) solid mixture obtained by step 1) is matched solution with step 2) to mix, abundant kneading.
4) the kneading material in step 3) is extruded into 3.2 clover bar shapeds of Φ, 120 DEG C of dry 3h, 500 DEG C of roastings of Muffle furnace
4h。
According to the catalyst sample that embodiment 1-3 methods are prepared, Main Analysis data are shown in Table 1.
1 olefin skeletal heterogeneous catalyst of table analyzes data
The scheme that goes into operation and process conditions：
Embodiment 4：
Catalyst prepared by embodiment 1 is ground, broken catalyst is sieved with 20 mesh and 30 the polished standard screens
Point, the catalyst 11.5g of 20-30 mesh is taken, is packed into 20ml fixed bed reactors.
In atmosphere of hydrogen (2.0MPa), reaction bed temperature rises to 320 DEG C with 40 DEG C/h from room temperature, 320 DEG C of constant temperature
4h, then catalyst test apparatus start oil inlet, reaction temperature is carried with 30 DEG C/h to 380 DEG C again.
Catalytic gasoline used in the present embodiment is the full fraction catalytic gasoline from Yumen oil plant, and process conditions are：Temperature
380-400 DEG C of degree, pressure 2.0MPa, hydrogen-oil ratio (v/v) 200, volume space velocity 4.0h-1。
Embodiment 5：
Feedstock oil after evaluating apparatus oil inlet 312h, is switched to catalysis weight by the evaluating catalyst scheme as described in embodiment 4
Gasoline (comes from Yumen oil plant), remaining process conditions is constant.
Embodiment 6：
Catalyst prepared by embodiment 2 and embodiment 3 is ground respectively, broken catalyst 20 mesh and 30 purposes
Standard screen is sieved, and the catalyst of 20-30 mesh respectively takes 6g, is packed into 20ml fixed bed reactors together.
In atmosphere of hydrogen (2.0MPa), reaction bed temperature rises to 320 DEG C with 40 DEG C/h from room temperature, 320 DEG C of constant temperature
4h, then catalyst test apparatus start oil inlet.
Catalytic gasoline used in the present embodiment is to be catalyzed heavy petrol from Yumen oil plant, and process conditions are：Temperature 320-
400 DEG C, pressure 2.0MPa, hydrogen-oil ratio (v/v) 200, volume space velocity 4.0h-1。
Experimental raw oil, the sampling of experimental products oil involved by embodiment 4-6, carry out chromatography and octane number test,
Analysis result is shown in Table 2-table 7.Wherein, chromatography used is the 7890A gas-chromatographies of agilent company production, and octane number is entrusted
Support Research Institute of Petro-Chemical Engineering is tested.
2 embodiment 4-5 C of table5、C6Olefin skeletal isomerization situation
Remarks：1. during entire evaluation experimental, experimental provision liquid yield>99%；
2. the listed reaction time calculates since experimental provision is into full fraction catalytic gasoline in table 2.
3 embodiment 4-5 experiments of table are formed with petrol hydrocarbon types
4 embodiment 4-5 experimental raws of table-product gasoline research octane number (RON)
Remarks：1. catalytic gasoline product is the accumulated product sample of 300-312 hours experimental provision oil inlet time；
2. it is catalyzed the accumulated product sample that heavy petrol product is 348-360 hours experimental provision oil inlet time.
5 embodiment of table, 6 C6Olefin skeletal isomerization situation
Remarks：1. during entire evaluation experimental, experimental provision liquid yield>99%；
2. the listed reaction time calculates since experimental provision is into full fraction catalytic gasoline in table 2.
6 embodiment of table, 6 experiment is formed with petrol hydrocarbon types
76 experimental raws of embodiment of table-product gasoline research octane number (RON)
Remarks：It is catalyzed the accumulated product sample that heavy petrol product is 250-262 hours experimental provision oil inlet time.
According to table 2-7 institutes column data, it was therefore concluded that：According to the method that embodiment 1-6 is provided, part straight chain C5 =、C6 =Hair
Raw skeletal isomerization has certain effect to the octane number improvement of catalytic gasoline, and the hydro carbons of catalytic gasoline composition does not change substantially.
Certainly, the present invention can also have other various embodiments, without deviating from the spirit and substance of the present invention, ripe
Various corresponding changes and deformation, but these corresponding changes and deformation can be made according to the present invention by knowing those skilled in the art
The protection domain of the claims in the present invention should all be belonged to.
Claims (10)
1. a kind of C5、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that include the following steps：
Step 1, by H-ZSM-35 molecular sieves and activated alumina according to 320:100~700:100 quality compares kneading；
The mixture of organic acid soln and Pd solution is added to H-ZSM-35 molecular sieves and activated alumina by step 2 by several times
Kneading in mixture, organic acid soln and the mixture of Pd solution and the mixture of H-ZSM-35 molecular sieves and activated alumina
Quality is 60:100~170:100；And
Step 3 shapes above-mentioned kneading material extrusion, 100~130 DEG C of dry 1~3h, 500~550 DEG C of roasting 3-4h.
2. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that described
SiO in H-ZSM-35 molecular sieves2With Al2O3Mass ratio for 20~50, crystallite dimension is 1.0~3.0 μm.
3. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that described
Activated alumina is γ-Al2O3, BET specific surface area is 230~290m2/ g, hole hold 0.3~1.0ml/g.
4. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that described
Organic acid soln is one or both of the citric acid solution of 0.1~1.0mol/L and the acetum of 0.1~1.0mol/L.
5. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that described
Pd solution is the [Pd (NH of 5~20wt%3)4](NO3)2Aqueous solution.
6. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that organic
The mass ratio of acid solution and organic acid soln in the mixture of Pd solution and Pd solution is 220:1~270:1.
7. C according to claim 15、C6The preparation method of linear chain olefin skeleton isomerism catalyst, which is characterized in that having
Machine acid solution in the mixture of Pd solution and the kneading process of H-ZSM-35 molecular sieves and the mixture of activated alumina with adding in
Extrusion lubricant, the extrusion lubricant are one or both of sesbania powder and methylcellulose.
8. catalyst prepared by preparation method according to any one of claims 1 to 7, which is characterized in that the catalyst
Use condition is 1.5~2.5MPa of pressure, 300~400 DEG C of temperature, 3.0~5.0h of volume space velocity-1, hydrogen to oil volume ratio 150~
250。
9. application of the catalyst according to any one of claims 8 in catalytic gasoline octane number is promoted.
10. application of the catalyst according to claim 9 in catalytic gasoline octane number is promoted, which is characterized in that described
Catalytic gasoline is catalytic gasoline of whole fraction, C6~C13Hydro carbons mass fraction>99% catalysis heavy petrol.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5510560A (en) * | 1993-08-30 | 1996-04-23 | Texaco Inc. | Skeletal isomerization of n-olefins to iso-olefins on binded ferrierite zeolites |
| CN1142787A (en) * | 1993-12-29 | 1997-02-12 | 壳牌石油公司 | Process for preparing a zeolite catalyst for the isomerizing of linear olefins to issolefins |
| CN1143356A (en) * | 1993-12-29 | 1997-02-19 | 壳牌石油公司 | Process for isomerizing linear olefins to isoolefins |
| CN102600886A (en) * | 2012-02-07 | 2012-07-25 | 王伟跃 | Catalyst for preparing iso-olefins by isomerizing straight-chain olefins and preparation method of catalyst |
-
2016
- 2016-12-28 CN CN201611236399.9A patent/CN108246352A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5510560A (en) * | 1993-08-30 | 1996-04-23 | Texaco Inc. | Skeletal isomerization of n-olefins to iso-olefins on binded ferrierite zeolites |
| CN1142787A (en) * | 1993-12-29 | 1997-02-12 | 壳牌石油公司 | Process for preparing a zeolite catalyst for the isomerizing of linear olefins to issolefins |
| CN1143356A (en) * | 1993-12-29 | 1997-02-19 | 壳牌石油公司 | Process for isomerizing linear olefins to isoolefins |
| CN102600886A (en) * | 2012-02-07 | 2012-07-25 | 王伟跃 | Catalyst for preparing iso-olefins by isomerizing straight-chain olefins and preparation method of catalyst |
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