CN1465436A - Catalyst for normal paraffin isomerization and use thereof - Google Patents
Catalyst for normal paraffin isomerization and use thereof Download PDFInfo
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- CN1465436A CN1465436A CNA02132476XA CN02132476A CN1465436A CN 1465436 A CN1465436 A CN 1465436A CN A02132476X A CNA02132476X A CN A02132476XA CN 02132476 A CN02132476 A CN 02132476A CN 1465436 A CN1465436 A CN 1465436A
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Abstract
The present invention discloses a normal paraffin isomerization catalyst and its appliation. Said catalyst contains heteropolyacid or heteropolyacid salt whose weight ratio is 0.5-90%, and the described heteropolyacid or heteropolyacid salt is the heteropolyacid or heteropolyacid salt or its its mixture whose centre atom is P or Si and coordination atom is at least one element of W, Mo and V. Said catalyst can be used for isomerization of C4-C12 normal paraffins, specially for isomerization of n-butane. Said catalyst has good reaction property, stability, activity and selectivity.
Description
Technical field
The present invention relates to a kind of heteropoly acid catalyst that is used for normal alkane isomerization, and in the presence of this catalyst, the reaction process of normal alkane isomerization.
Background technology
In the isomerization of paraffins reaction, need have the acid catalyst of strong acid center.Up to now, adopt sulfuric acid, hydrofluoric acid, aluminium chloride and trichloride antimony etc. as catalyst usually; Because they can cause metal erosion and contaminated environment, thereby process units need adopt expensive resistant material, and strict day by day along with environmental requirement, and the disposal cost of dead catalyst becomes more and more higher.In addition, it also is comparatively difficult isolating these catalyst from product.The another kind of catalyst that is adopted in alkane isomerization is the solid acid catalyst of noble metal such as supporting Pt and halogens, but this class catalyst is very responsive to water, and reaction raw materials needs strict dehydration.
In recent years, with SO
4 2-/ ZrO
2For the solid super acid catalyst of representing has caused great concern, this class catalyst at room temperature gets final product the isomerization of catalysis normal butane, but its stable extreme difference, inactivation is exceedingly fast, and reason mainly is a carbon distribution, does not also have prospects for commercial application at present.
Heteropoly acid and heteropolyacid salt be as the novel catalysis material of a class, with acidity, " accurate liquid phase " behavior of its uniqueness, and has highly acid and strong oxidizing property, advantages such as corrosion and pollution problem not simultaneously, is subjected to paying attention to widely in the catalyticing research field.
USP 5,750, and 457 disclose a kind of Cs that supports precious metals pd
2.5H
0.5PW
12O
40Catalyst is used for the normal butane isomerization reaction under hydro condition, can obtain the better result of n-butane conversion 33.6%, iso-butane selectivity 95.5%.
But, adopt carried heteropoly acid type catalyst to be used for particularly normal butane isomerization of low-carbon alkanes, do not appear in the newspapers as yet.
A shortcoming when heteropoly acid or heteropolyacid salt are used as solid acid catalyst is that its acidity particularly its acid strength is unstable under common reaction condition.In the highly acid reaction system of needs, can make catalysqt deactivation because of its acid strength reduces gradually; In the more weak reaction system of the acid strength of needs, stronger acid site can cause disadvantageous side reactions such as polymerization, coking again.
Summary of the invention
The object of the present invention is to provide a kind of heteropoly acid catalyst that is used for normal alkane isomerization.
Another object of the present invention is to provide a kind of use above-mentioned heteropoly acid catalyst, and keep the normal alkane isomerization reaction process of its higher level of reactivity energy.
Realize above-mentioned purpose, heteropoly acid catalyst of the present invention contains heteropoly acid or the heteropolyacid salt of weight ratio 0.5-90%, and preferred range is 3-50%.
The heteropoly acid of indication of the present invention or heteropolyacid salt are that central atom is a kind of element among P, the Si, heteropoly acid or the heteropolyacid salt that coordination atom is at least a element among W, Mo, the V.Wherein more easily preparation, stability better, price also lower be phosphotungstic acid, silico-tungstic acid or its salt of Keggin structure.These heteropoly acids or heteropolyacid salt can use as the active component of aforementioned heteropoly acid catalyst separately, also more than one heteropoly acid or heteropolyacid salt can be mixed use.
Can be with heteropoly acid or heteropolyacid salt and some inorganic matter, as one or more the mixture mixed-forming in silica, aluminium oxide, titanium dioxide, carborundum, active carbon, alumina silicate, magnesium silicate etc. and the carbide resin, be beneficial to catalyst and keep certain shape and intensity.
Advantageously make so-called carried heteropoly acid type catalyst.For example, can adopt infusion process, with the solution impregnation of heteropoly acid or heteropolyacid salt to carrier with certain pore structure, as silica, active carbon, aluminium oxide, titanium dioxide, carborundum, alumina silicate, carbide resin etc., afterwards can drying, roasting etc. handles the back as catalyst, also can directly be used as catalyst.
Carried heteropoly acid type catalyst can improve the intensity and the specific area of catalyst, reduces the consumption of heteropoly acid or heteropolyacid salt, reduces the catalyst cost, and the catalytic performance of catalyst is also had bigger change.The difference of the reaction system of using according to catalyst can adopt the load capacity of different carriers and heteropoly acid or heteropolyacid salt.
Characteristics of heteropoly acid catalyst are that its acid strength and its water content have direct relation.Foregoing heteropoly acid catalyst, in use, when particularly handling without high-temperature roasting, its acid strength gradually changes often.A kind ofly may be, with the prolongation in reaction time, the contained moisture content of heteropoly acid or heteropolyacid salt loses gradually in the catalyst, and acid strength improved before this thereupon, reduces gradually again afterwards, and this is very disadvantageous to catalytic reaction.
The normal alkane isomerization technology of the employing heteropoly acid catalyst that the present invention proposes, can be according to the needs of different carbon number normal alkane isomerization reactions, make the acidity of heteropoly acid catalyst keep needed intensity effectively, thereby obtain more stable catalytic performance.The method that is adopted is to add a certain amount of water and/or hydrogen in reaction atmosphere.
The existence of the water of certain dividing potential drop under the uniform temperature can slow down the dewatering speed of heteropoly acid or heteropolyacid salt greatly, its water content is remained on the proper level, thereby keep certain acid strength.The dividing potential drop scope of suitable water is the 2-200 millimetres of mercury.Under different temperatures, it is different keeping the required water partial pressure of same acid strength; Generally speaking, temperature is high more, and required water partial pressure is also high more.
In reaction system, add an amount of hydrogen, also can improve the stability of heteropoly acid or heteropolyacid salt catalyst acid strength greatly.Its mechanism of action then mechanism of action with water is different.Suitable hydrogen partial pressure is 0.01-5MPa.
Also water and hydrogen can be joined in the reaction system simultaneously, so that the acid strength of heteropoly acid catalyst keeps stable.
The normal alkane isomerization heteropoly acid catalyst that the present invention proposes can be used for the isomerization of C4～C12 n-alkane.Dewater and/or hydrogen outside, the remainder in the reaction feed can be pure n-alkane; Also can be the mixture of different carbon number n-alkanes and other hydro carbons, wherein the weight percentage of n-alkane be 30～100%; Also can contain the catalyst reaction performance and not have ever-present impurity in the dysgenic raw material of industry.
In general, the carbon number of n-alkane is low more, and it is strong more that the required acidity of isomerization reaction takes place, and adopt different catalyst compositions and water partial pressure and/or hydrogen partial pressure, so that catalyst keeps required acid strength, adopt reaction conditions such as corresponding temperature, air speed simultaneously.
When the material that adopts normal butane or contain normal butane was reaction raw materials, reaction temperature was 200-400 ℃, and reaction pressure is 0.05-10MPa, and the weight space velocity of normal butane is 0.05-10 hour
-1Reaction temperature is high more, and n-butane conversion is high more, but because the isomerization reaction of normal butane is exothermic reaction, and temperature is too high, will be subjected to the restriction of thermodynamical equilibrium, conversion ratio can reduce on the contrary.The normal butane air speed reduces, and its conversion ratio improves, but also is subjected to the restriction of thermodynamical equilibrium.
Advantage of the present invention and effect:
1. adopt carried heteropoly acid type catalyst to be used for the particularly isomerization reaction of normal butane of n-alkane, can under higher alkane air speed, obtain higher activity and selectivity, in reaction atmosphere, keep certain water partial pressure and/or hydrogen partial pressure, can improve the normal alkane isomerization performance of carried heteropoly acid type catalyst and improve its stability greatly.
2. adopt heteropoly acid catalyst catalyst and applied isomerization reaction technology, have characteristics such as free from environmental pollution, that etching apparatus, activity and selectivity are not higher, reactivity worth is stable.
The specific embodiment
Be embodiments of the invention below, but the present invention is not limited to following examples.
Embodiment 1, preparation catalyst
With the spherical silica gel (SiO about a certain amount of diameter 2mm
2) with watery hydrochloric acid washing, immersion 2 hours, being washed till neutrality with deionized water, roasting is 4 hours in 350 ℃ of muffle furnaces.Take by weighing the SiO of 10 grams through above-mentioned processing
2, application of vacuum at room temperature 2 hours; Get 2.5 gram phosphotungstic acids and be dissolved in 10 ml deionized water, splash in the carrier under the vacuum condition, the sample behind the dipping continues to handle 1 hour under vacuum condition, and is dry in 120 ℃ of baking ovens then, makes catalyst A (20wt%H
3PW
12O
40/ SiO
2).
Embodiment 2, preparation catalyst
Press the method for embodiment 1, just change phosphotungstic acid into silico-tungstic acid, make catalyst B (20wt%H
4SiW
12O
40/ SiO
2).
Embodiment 3, preparation catalyst
A certain amount of 20-40 purpose active carbon was soaked 4 hours with watery hydrochloric acid, be washed till neutrality with deionized water then, drying is 16 hours in 120 ℃ of baking ovens.Take by weighing the active carbon of 10 grams, application of vacuum at room temperature 2 hours through above-mentioned processing; Get 2.5 gram phosphotungstic acids and be dissolved in 7 ml deionized water, splash in the carrier under the vacuum condition, the sample behind the dipping continues to handle 1 hour under vacuum condition, and is dry in 120 ℃ of baking ovens then, makes catalyst C (20wt%H
3PW
12O
40/ C).
Embodiment 4, preparation catalyst
Press the method for embodiment 1, just the addition of phosphotungstic acid changes 0.53 gram, 6.7 grams respectively into, makes catalyst D (5wt%H
3PW
12O
40/ SiO
2) and catalyst E (40wt%H
3PW
12O
40/ SiO
2).
Embodiment 5, preparation catalyst
Press the method for embodiment 1, just in phosphotungstic acid aqueous solution, add 3.1 gram Nickelous nitrate hexahydrates again, make catalyst F (5%Ni-20wt%H
3PW
12O
40/ SiO
2).
Embodiment 6, preparation catalyst
Connect the method for embodiment 1, just phosphotungstic acid changes into and respectively adds phosphotungstic acid 5 grams, silico-tungstic acid 5 grams, makes catalyst G (10%H
4SiW
12O
40-10wt%H
3PW
12O
40/ SiO
2).
Embodiment 7, preparation catalyst
Press the method for embodiment 1, just the addition of phosphotungstic acid changes 0.05 gram, 23 grams, 90 grams respectively into, makes catalyst.
Embodiment 8, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, and activation is 2 hours under 300 ℃, hydrogen atmosphere, switches then to contain normal butane and react 300 ℃ of reaction temperatures, reaction pressure 0.6MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, react sample analysis after 1 hour, n-butane conversion 28.8%, iso-butane selectivity 81.9%.
Embodiment 9, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 0.6MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H
2Be 1 with the mol ratio of normal butane, hydrogen partial pressure is 0.3MPa, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 36.4 92.0
4 35.7 91.6
6 36.6 90.6
8 37.4 86.6
Embodiment 10, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H2 and normal butane mol ratio be 3, hydrogen partial pressure is 2.8MPa, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 24.9 90.8
4 21.4 91.3
6 22.1 94.0
8 20.6 92.6
Embodiment 11, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 275 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H2 and normal butane mol ratio be 1, hydrogen partial pressure is 1.8MPa, reacts sample analysis after 1 hour, n-butane conversion 22.3%, iso-butane selectivity 95.5%.
Embodiment 12, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 240 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H2 and normal butane mol ratio be 1, hydrogen partial pressure is 1.8MPa, reacts sample analysis after 1 hour, n-butane conversion 15.1%, iso-butane selectivity 96.1%.
Embodiment 13, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switching the normal butane that contains 10% iso-butane then reacts, the mol ratio of 300 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), H2 and normal butane is 1, hydrogen partial pressure is 1.8MPa, and the normal butane weight space velocity is respectively 0.1h
-1, 0.5h
-1, 1.0h
-1, 1.5h
-1, 5h
-1, 10h
-1, n-butane conversion is respectively 42.1%, 35.3%, 26.7%, 20.0%, 12.2%, 10.1%, and the iso-butane selectivity is respectively 84.6%, 89.6%, 88.9%, 92.9%, 95.4%, 96.2%.
Embodiment 14, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, N2 and normal butane mol ratio be 1, hydrogen partial pressure is 1.8MPa, and brings the steam that dividing potential drop is 13 millimetress of mercury into nitrogen, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 39.6 82.1
4 34.3 83.1
6 33.8 78.3
8 28.8 77.5 embodiment 15, catalyst A are used for normal butane isomerization reaction with pack into the stainless steel fixed bed reactors of internal diameter 9mm of 5 gram catalyst A, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 3.8MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H
2Be 1 with the mol ratio of normal butane, hydrogen partial pressure is 1.8MPa, and brings the steam that dividing potential drop is 13 millimetress of mercury into hydrogen, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 39.4 86.1
4 37.6 87.4
6 36.7 87.5
8 36.9 84.8
Embodiment 16, catalyst A are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 0.1MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H
2Be 0.5 with the mol ratio of normal butane, hydrogen partial pressure is 0.03MPa, and brings the steam that dividing potential drop is 48 millimetress of mercury into hydrogen, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 28.4 88.9
4 27.9 90.2
6 29.6 89.7
8 28.7 90.0
Embodiment 17, catalyst B normal butane isomerization reaction evaluating
5 gram catalyst B are packed in the stainless steel fixed bed reactors of internal diameter 9mm, and activation is 2 hours under 300 ℃, hydrogen atmosphere, switches the normal butane that contains 10% iso-butane then and reacts 300 ℃ of reaction temperatures, reaction pressure 5MPa, normal butane weight space velocity 0.3h
-1, react sample analysis after 1 hour, n-butane conversion 16.3%, iso-butane selectivity 87.4%.
Embodiment 18, catalyst B are used for the normal butane isomerization reaction
5 gram catalyst A are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 7.1MPa (absolute pressure), normal butane weight space velocity 0.3h
-1, H
2Be 2 with the mol ratio of normal butane, hydrogen partial pressure is 4.6MPa, and brings the steam that dividing potential drop is 4.8 millimetress of mercury into hydrogen, sample analysis the results are shown in following table behind the reaction different time.
Reaction time/h n-butane conversion/% iso-butane selectivity/%
2 43.2 85.1
4 41.5 87.8
6 40.9 86.2
8 41.2 85.8
Embodiment 19, catalyst C normal butane isomerization reaction evaluating pack 5 gram catalyst C in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 5MPa, normal butane weight space velocity 0.3h
-1, hydrogen partial pressure is 5MPa, and brings the steam that dividing potential drop is 2 millimetress of mercury into hydrogen, reacts sample analysis after 3 hours, n-butane conversion 17.8%, iso-butane selectivity 85.8%.
Embodiment 20, catalyst D normal butane isomerization reaction evaluating
5 gram catalyst D are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 0.5MPa, normal butane weight space velocity 0.3h
-1, react sample analysis after 1 hour, n-butane conversion 12.5%, iso-butane selectivity 86.2%.
Embodiment 21, catalyst E normal butane isomerization reaction evaluating
5 gram catalyst E are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 0.5MPa, normal butane weight space velocity 0.3h
-1, hydrogen partial pressure is 3MPa, and brings the steam that dividing potential drop is 20 millimetress of mercury into hydrogen, reacts sample analysis after 1 hour, n-butane conversion 42.5%, iso-butane selectivity 77.2%.
Embodiment 22, catalyst F normal butane isomerization reaction evaluating
5 gram catalyst F are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 300 ℃ of reaction temperatures, reaction pressure 3.7MPa, normal butane weight space velocity 0.3h
-1, hydrogen partial pressure is 1.8MPa, and brings the steam that dividing potential drop is 70 millimetress of mercury into hydrogen, reacts sample analysis after 1 hour, n-butane conversion 11.9%, iso-butane selectivity 80.3%.
Embodiment 23, catalyst G normal butane isomerization reaction evaluating
5 gram catalyst G are packed in the stainless steel fixed bed reactors of internal diameter 9mm, activation is 2 hours under 300 ℃, hydrogen atmosphere, switch the normal butane that contains 10% iso-butane then and react 350 ℃ of reaction temperatures, reaction pressure 2.1MPa (absolute pressure), normal butane weight space velocity 0.5h
-1, hydrogen partial pressure is 2MPa, and brings the steam that dividing potential drop is 100 millimetress of mercury into hydrogen, reacts sample analysis after 1 hour, n-butane conversion 25.9%, iso-butane selectivity 90.3%.
Comparative example:
Adopt the Pd-Cs2.5H0.5PW12O40 catalyst to be used for normal butane isomerization, 300 ℃ of reaction temperatures, reaction pressure are normal pressure, normal butane weight space velocity 0.078h-1, H2: He: N2: normal butane (mol ratio)=1: 9: 9: 1, n-butane conversion 12.9%, iso-butane selectivity 78.3%.
Above-mentioned embodiment of the present invention all can only be thought can not limit the present invention to explanation of the present invention, claims have been pointed out scope of the present invention, therefore, in implication suitable and any change in the scope, all should think to be included in the scope of claims with claims of the present invention.
Claims (10)
1. catalyst that is used for normal alkane isomerization, it is characterized in that: contain the heteropoly acid of weight ratio 0.5-90% or the inorganic matter of heteropolyacid salt and weight ratio 10-99.5% in the catalyst, described heteropoly acid or heteropolyacid salt are that central atom is that P or Si, coordination atom are heteropoly acid or heteropolyacid salt or its mixture of at least a element among W, Mo, the V.
2. according to the described catalyst of claim 1, it is characterized in that: described heteropoly acid or heteropolyacid salt are phosphotungstic acid, silico-tungstic acid or its salt or their mixture.
3. according to claim 1 or 2 described catalyst, it is characterized in that: described heteropolyacid salt is normal salt or acid salt, except that hydrogen ion, cation wherein is one or more the mixture in ammonium ion, alkali metal ion, alkaline-earth metal ions and Cr, Mn, Fe, Co, Ni, Pt, Pd, the Cu transition metal ions.
4. according to claim 1 or 2 described catalyst, it is characterized in that: contain the heteropoly acid of weight ratio 3-50% or the inorganic matter of heteropolyacid salt and weight ratio 70-97% in the described heteropoly acid catalyst.
5, according to the described catalyst of claim 1, it is characterized in that: inorganic matter is one or more the mixture that contains in silica, aluminium oxide, titanium oxide, carborundum, alumina silicate, magnesium silicate, active carbon, the carbide resin in the described heteropoly acid catalyst.
6, a kind of normal alkane isomerization reaction method, that is be used for the isomerization reaction of C4～C12 n-alkane, it is characterized in that using the described catalyst of claim 1.
7. according to the described reaction method of claim 6, it is characterized in that: have water and/or hydrogen to exist in the reaction atmosphere, wherein the dividing potential drop of water is the 2-200 millimetres of mercury, and the dividing potential drop of hydrogen is
8, according to the described reaction method of claim 6, it is characterized in that: the weight percentage of n-alkane is 30～100% in the reaction raw materials.
9, in accordance with the method for claim 6, it is characterized in that: described n-alkane is a normal butane.
10, in accordance with the method for claim 9, it is characterized in that: reaction temperature is 200～400 ℃, and reaction pressure is 0.05-10MPa, and the weight space velocity of normal butane is 0.05-10 hour
-1
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| CN100528349C (en) * | 2005-12-21 | 2009-08-19 | 中国科学院山西煤炭化学研究所 | Catalyst for oxo-synthesis of dimethyl ether to produce methylal, preparation method and application thereof |
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| CN106334570A (en) * | 2015-07-09 | 2017-01-18 | 中国石油化工股份有限公司 | N-alkane isomerization catalyst and preparation method thereof |
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| CN106635162A (en) * | 2015-10-28 | 2017-05-10 | 中国石油化工股份有限公司 | Low-carbon alkane isomerization method |
| CN107029797A (en) * | 2017-04-06 | 2017-08-11 | 福州大学 | A kind of preparation and application of low-carbon normal hydrocarbon class isomerization catalyst |
| CN110878001A (en) * | 2019-11-29 | 2020-03-13 | 温州大学 | Process for the isomerization of (Z) -olefins to (E) -olefins |
| CN111957352A (en) * | 2020-08-27 | 2020-11-20 | 长春工业大学 | Palladium or platinum and heteropoly acid co-loaded zirconium-based microporous coordination polymer composite material and preparation method thereof |
| CN115746923A (en) * | 2022-10-21 | 2023-03-07 | 中国科学院广州能源研究所 | Method for preparing aviation fuel from lignin derivatives |
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