CN105833900A - Isomerization catalyst and preparation method thereof - Google Patents

Isomerization catalyst and preparation method thereof Download PDF

Info

Publication number
CN105833900A
CN105833900A CN201610206851.0A CN201610206851A CN105833900A CN 105833900 A CN105833900 A CN 105833900A CN 201610206851 A CN201610206851 A CN 201610206851A CN 105833900 A CN105833900 A CN 105833900A
Authority
CN
China
Prior art keywords
parts
oxide
catalyst
isomerization catalyst
molecular sieve
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201610206851.0A
Other languages
Chinese (zh)
Inventor
吴明明
宋峰
李伟
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shandong Chengtai Chemical Co Ltd
Original Assignee
Shandong Chengtai Chemical Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Shandong Chengtai Chemical Co Ltd filed Critical Shandong Chengtai Chemical Co Ltd
Priority to CN201610206851.0A priority Critical patent/CN105833900A/en
Publication of CN105833900A publication Critical patent/CN105833900A/en
Pending legal-status Critical Current

Links

Classifications

    • 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
    • B01J29/80—Mixtures of different zeolites
    • 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
    • B01J29/005—Mixtures of molecular sieves comprising at least one molecular sieve which is not an aluminosilicate zeolite, e.g. from groups B01J29/03 - B01J29/049 or B01J29/82 - B01J29/89
    • 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
    • B01J35/61—Surface area
    • B01J35/615—100-500 m2/g
    • 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
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2767—Changing the number of side-chains
    • C07C5/277—Catalytic processes
    • C07C5/2775—Catalytic processes with crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/40—Special temperature treatment, i.e. other than just for template removal
    • 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
    • B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
    • 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
    • B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
    • B01J29/7007—Zeolite Beta
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Catalysts (AREA)

Abstract

The invention discloses an isomerization catalyst and a preparation method thereof. The isomerization catalyst is prepared from, by weight, 5-10 parts of tin oxide, 3-5 parts of titanium oxide, 4-8 parts of iron oxide, 3-8 parts of manganese oxide, 10-15 parts of silica, 10-15 parts of rare earth oxide, 8-10 parts of alkali earth oxide, 3-6 parts of titanium dioxide, 4-6 parts of tungsten trioxide, 4-8 parts of vanadium pentoxide, 4-6 parts of silicon fluoride, 2-3 parts of molecular sieve, 5-12 parts of silicon tetrachloride, 8-10 parts of titanium tetrachloride and 6-8 parts of a binder. The catalyst prepared through adopting the above technical scheme has 80% or above higher stability than present catalysts, and the stability of the catalyst in reactions can last for 1000h or above.

Description

A kind of isomerization catalyst and preparation method thereof
Technical field
The present invention relates to catalyst technical field, particularly relate to a kind of isomerization catalyst and preparation method thereof.
Background technology
The chemical reaction rate (can improve and also can reduce) of reactant can be changed in chemical reaction, and the quality of itself The material the most not changed before and after chemical reaction with chemical property is catalyst.Xylol is very important basis Industrial chemicals, xylol also has purposes widely in fields such as medicine, pesticide, fuel and solvents, existing main employing Dimethylbenzene adsorbing separation and three kinds of techniques of selective disproportionation of toluene produce xylol.
In petrochemical industry produces, from the C8 aromatic hydrocarbons that various techniques obtain, except containing to, in addition to adjacent three kinds of dimethylbenzene, Possibly together with ethylbenzene.As raw material, operated by isomerization, rectification and adsorbing separation etc., para-xylene product can be obtained.By In ethylbenzene with xylene boiling point closely, using rectification separating energy consumption height, efficiency low, difficulty is big, converts frequently with ethylbenzene Method, it is to avoid the accumulation of ethylbenzene in combined unit circulation logistics.Ethylbenzene converts two kinds of methods, and one is to be converted by isomery For dimethylbenzene, another kind is to generate benzene by de-ethyl.The former is limited by thermodynamics, and conversion ratio is the most relatively low, and selectivity is the most not Height, the latter's conversion of ethylbenzene is higher, and selectivity is good.But owing to ethylbenzene generates benzene, device is realizing output goal product to diformazan In the case of benzene, C 8 aromatic hydrocarbon resource demand wants many.
Along with the demand of xylene product continues to increase, C8 aromatic hydrocarbon resource of different nature is used for producing diformazan Benzene, including the C8 aromatic hydrocarbons in a certain amount of cracking of ethylene oil, thus causes producing second in the C8 aroamtic hydrocarbon raw material of dimethylbenzene Benzene content improves, and combined unit logistics circulating load improves, and the operating severity of adsorbing separation increases, and the output capacity of device is subject to Impact.Ethylbenzene high efficiency can be converted by the isomerization catalyst converting the ethylbenzene into benzene, solves the problems referred to above largely, And ethylbenzene converts the benzene fraction boiling point obtained with dimethylbenzene difference relatively greatly, rectification separates and easily realizes.It addition, join at xylol C 8 arene isomerization catalyst using ethylbenzene removing type in locking device can also make unit scale relatively save, device In actual motion, energy consumption is relatively low.
The carrier of the isomerization catalyst converting the ethylbenzene into benzene at present many by aluminium oxide or silicon oxide and one or more Zeolite collectively forms, and is loaded with one or more metal constituent elements.But, it is anti-that high isomerization all deposited by existing isomerization catalyst Answering yield low, catalyst activity is low or the problem of poor stability.
Summary of the invention
The technical problem to be solved in the present invention is to provide a kind of catalyst activity high or stable for the deficiencies in the prior art Property good, there is higher specific surface area, service life is long, isomerization catalyst that isomerization reaction yield is high and preparation side thereof Method.
For solving the above-mentioned technical problem present invention by the following technical solutions: a kind of isomerization catalyst, by following weight The raw material of part is made, stannum oxide 5-10 part, titanium oxide 3-5 part, ferrum oxide 4-8 part, manganese oxide 3-8 part, silica 1 0-15 Part, rare earth oxide 10-15 part, alkaline-earth oxide 8-10 part, titanium dioxide 3-6 part, Tungstic anhydride. 4-6 part, vanadic anhydride 4-8 part, silicon fluoride 4-6 part, molecular sieve 2-3 part, 5 12 parts of Silicon chloride., titanium tetrachloride 8-10 part, binding agent 6-8 part.
The following is further improvement of the present invention:
Molecular sieve is ZSM-5, beta-zeolite molecular sieve and the mixture of MFI molecular sieve, and mass ratio is 1-2:3-6:2-5.
Improve further:
One or more in lanthanum, cerium, praseodymium oxide of described alkaline-earth oxide element.
Improve further:
Described rare earth oxide is one or more in calcium oxide, magnesium oxide, Barium monoxide.
Improve further:
Described binding agent is aluminium oxide.
A kind of preparation method of isomerization catalyst, it is characterised in that: in turn include the following steps:
A, the stannum oxide by above-mentioned weight portion, titanium oxide, ferrum oxide, manganese oxide, silicon dioxide, rare earth oxide, alkaline earth oxidation Thing, titanium dioxide, Tungstic anhydride., vanadic anhydride, silicon fluoride, molecular sieve, Silicon chloride., titanium tetrachloride, binding agent are put into and are stirred Mix mix homogeneously in machine, add aqueous solution of nitric acid, extruded moulding after being rolled into micelle shape wet cake, be dried, roasting, prepare catalyst Semi-finished product；
B, by above-mentioned catalyst semi-finished product load activation device in, under the atmosphere of water flowing steam, be warming up to 600 DEG C-700 DEG C, And thermostatted water processes 10-15 hour prepared finished catalyst at such a temperature.
Improve further:
In step a, the concentration of aqueous solution of nitric acid is the aqueous solution of nitric acid of 0.25g/ml-0.5g/ml.
Improve further
In step a, sintering temperature is 300～1200 DEG C, and roasting time is 4～6 hours.
Improve further
In step a, baking temperature is 100 DEG C, and drying time is 4 hours.
The present invention uses technique scheme to have following technical effect that than the raising of its stability of existing catalyst More than 80%, the stability in catalyst reaction can reach more than 1000 hours；There is higher specific surface area, typically exist 150-300m2/ g range, aperture generates macroporous structure after about 1.5nm, high-temperature activation, aperture at about 20-40nm, Improve the isomerization performance of catalyst；The catalyst of the present invention has higher isomerization activity, after running 10 days continuously Its isomerization efficiency is up to 97%, and catalyst remains to keep higher active catalyst after long period of operation, and service life is 2 More than Nian.
Detailed description of the invention
Embodiment 1, a kind of isomerization catalyst, in parts by weight, including following component, stannum oxide 5 parts, titanium oxide 3 parts, oxidation Ferrum 4 parts, manganese oxide 3 parts, silica 10 part, rare earth oxide 10 parts, alkaline-earth oxide 8 parts, titanium dioxide 3 parts, three oxidations 4 parts of tungsten, vanadic anhydride 4 parts, silicon fluoride 4 parts, 2 parts of molecular sieve, 5 parts of Silicon chloride., titanium tetrachloride 8 parts, binding agent 6 parts.
Molecular sieve is ZSM-5, beta-zeolite molecular sieve and the mixture of MFI molecular sieve, and mass ratio is 1:3:2.
Described alkaline-earth oxide element is selected from lanthanum-oxides.
Described rare earth oxide is calcium oxide.
Described binding agent is aluminium oxide.
The preparation method of a kind of isomerization catalyst, in turn includes the following steps:
1) by stannum oxide 5 parts, titanium oxide 3 parts, ferrum oxide 4 parts, manganese oxide 3 parts, silica 10 part, rare earth oxide 10 parts, Alkaline-earth oxide 8 parts, titanium dioxide 3 parts, Tungstic anhydride. 4 parts, vanadic anhydride 4 parts, silicon fluoride 4 parts, 2 parts of molecular sieve, tetrachloro SiClx 5 parts, it is uniform that stirrer for mixing put into by titanium tetrachloride 8 parts, binding agent 6 parts, adds aqueous solution of nitric acid, is rolled into micelle Extruded moulding after shape wet cake, it is dried, roasting, prepares catalyst semi-finished product.
2) above-mentioned catalyst semi-finished product are loaded in activation device, under the atmosphere of water flowing steam, be warming up to 600 DEG C-700 DEG C, and thermostatted water processes 10-15 hour prepared finished catalyst at such a temperature.
In step 1, the concentration of aqueous solution of nitric acid is the aqueous solution of nitric acid of 0.25g/ml-0.5g/ml.
In step 1, sintering temperature is 300～1200 DEG C, and roasting time is 4～6 hours.
In step 1, baking temperature is 100 DEG C, and drying time is 4 hours.
Embodiment 2, a kind of isomerization catalyst, in parts by weight, including following component, stannum oxide 10 parts, titanium oxide 5 Part, ferrum oxide 8 parts, manganese oxide 8 parts, silica 15 parts, rare earth oxide 15 parts, alkaline-earth oxide 10 parts, titanium dioxide 6 Part, Tungstic anhydride. 6 parts, vanadic anhydride 8 parts, silicon fluoride 6 parts, 3 parts of molecular sieve, 12 parts of Silicon chloride., titanium tetrachloride 10 parts, Binding agent 8 parts.
Molecular sieve is ZSM-5, beta-zeolite molecular sieve and the mixture of MFI molecular sieve, and mass ratio is 2:6:5.
Described alkaline-earth oxide element selected from cerium oxide.
Described rare earth oxide is magnesium oxide.
Described binding agent is aluminium oxide.
1) by stannum oxide 10 parts, titanium oxide 5 parts, ferrum oxide 8 parts, manganese oxide 8 parts, silica 15 parts, rare earth oxide 15 parts, alkaline-earth oxide 10 parts, titanium dioxide 6 parts, Tungstic anhydride. 6 parts, vanadic anhydride 8 parts, silicon fluoride 6 parts, molecular sieve 3 Part, 12 parts of Silicon chloride., titanium tetrachloride 10 parts, binding agent 8 parts, put into stirrer for mixing uniform, add aqueous solution of nitric acid, It is rolled into extruded moulding after micelle shape wet cake, is dried, roasting, prepares catalyst semi-finished product.
2) above-mentioned catalyst semi-finished product are loaded in activation device, under the atmosphere of water flowing steam, be warming up to 600 DEG C-700 DEG C, and thermostatted water processes 10-15 hour prepared finished catalyst at such a temperature.
In step 1, the concentration of aqueous solution of nitric acid is the aqueous solution of nitric acid of 0.25g/ml-0.5g/ml.
In step 1, sintering temperature is 300～1200 DEG C, and roasting time is 4～6 hours.
In step 1, baking temperature is 100 DEG C, and drying time is 4 hours.
Embodiment 3, a kind of isomerization catalyst, in parts by weight, including following component, stannum oxide 8 parts, titanium oxide 4 parts, Ferrum oxide 6 parts, manganese oxide 6 parts, silica 13 parts, rare earth oxide 13 parts, alkaline-earth oxide 9 parts, titanium dioxide 5 parts, three Tungsten oxide 5 parts, vanadic anhydride 6 parts, silicon fluoride 5 parts, 2.5 parts of molecular sieve, 8 parts of Silicon chloride., titanium tetrachloride 9 parts, binding agent 7 parts.
Molecular sieve is ZSM-5, beta-zeolite molecular sieve and the mixture of MFI molecular sieve, and mass ratio is 1.5:5:4.
Described alkaline-earth oxide element is selected from praseodymium oxide.
Described rare earth oxide is Barium monoxide.
Described binding agent is aluminium oxide.
1) by stannum oxide 8 parts, titanium oxide 4 parts, ferrum oxide 6 parts, manganese oxide 6 parts, silica 13 parts, rare earth oxide 13 parts, alkaline-earth oxide 9 parts, titanium dioxide 5 parts, Tungstic anhydride. 5 parts, vanadic anhydride 6 parts, silicon fluoride 5 parts, molecular sieve 2.5 Part, 8 parts of Silicon chloride., titanium tetrachloride 9 parts, binding agent 7 parts, put into stirrer for mixing uniform, add aqueous solution of nitric acid, grind It is pressed into extruded moulding after micelle shape wet cake, is dried, roasting, prepares catalyst semi-finished product.
2) above-mentioned catalyst semi-finished product are loaded in activation device, under the atmosphere of water flowing steam, be warming up to 600 DEG C-700 DEG C, and thermostatted water processes 10-15 hour prepared finished catalyst at such a temperature.
In step 1, the concentration of aqueous solution of nitric acid is the aqueous solution of nitric acid of 0.25g/ml-0.5g/ml.
In step 1, sintering temperature is 300～1200 DEG C, and roasting time is 4～6 hours.
In step 1, baking temperature is 100 DEG C, and drying time is 4 hours.

Claims (9)

1. an isomerization catalyst, it is characterised in that: it is made up of the raw material of following weight portion, stannum oxide 5-10 part, titanium oxide 3-5 part, ferrum oxide 4-8 part, manganese oxide 3-8 part, silica 1 0-15 part, rare earth oxide 10-15 part, alkaline-earth oxide 8- 10 parts, titanium dioxide 3-6 part, Tungstic anhydride. 4-6 part, vanadic anhydride 4-8 part, silicon fluoride 4-6 part, molecular sieve 2-3 part, tetrachloro SiClx 5 12 parts, titanium tetrachloride 8-10 part, binding agent 6-8 part.
Isomerization catalyst the most according to claim 1, it is characterised in that: molecular sieve is ZSM-5, beta-zeolite molecular sieve With the mixture of MFI molecular sieve, mass ratio is 1-2:3-6:2-5.
Isomerization catalyst the most according to claim 1, it is characterised in that: described alkaline-earth oxide element selected from lanthanum, cerium, One or more in praseodymium oxide.
Isomerization catalyst the most according to claim 1, it is characterised in that: described rare earth oxide is calcium oxide, oxidation One or more in magnesium, Barium monoxide.
Isomerization catalyst the most according to claim 1, it is characterised in that: described binding agent is aluminium oxide.
6. the preparation method of an isomerization catalyst, it is characterised in that: in turn include the following steps:
A, the stannum oxide by above-mentioned weight portion, titanium oxide, ferrum oxide, manganese oxide, silicon dioxide, rare earth oxide, alkaline earth oxidation Thing, titanium dioxide, Tungstic anhydride., vanadic anhydride, silicon fluoride, molecular sieve, Silicon chloride., titanium tetrachloride, binding agent are put into and are stirred Mix mix homogeneously in machine, add aqueous solution of nitric acid, extruded moulding after being rolled into micelle shape wet cake, be dried, roasting, prepare catalyst Semi-finished product；
B, by above-mentioned catalyst semi-finished product load activation device in, under the atmosphere of water flowing steam, be warming up to 600 DEG C-700 DEG C, And thermostatted water processes 10-15 hour prepared finished catalyst at such a temperature.
The preparation method of isomerization catalyst the most according to claim 6, it is characterised in that: aqueous solution of nitric acid in step a The aqueous solution of nitric acid that concentration is 0.25g/ml-0.5g/ml.
The preparation method of isomerization catalyst the most according to claim 6, it is characterised in that: in step a, sintering temperature is 300～1200 DEG C, roasting time is 4～6 hours.
The preparation method of isomerization catalyst the most according to claim 6, it is characterised in that: in step a, baking temperature is 100 DEG C, drying time is 4 hours.
CN201610206851.0A 2016-04-06 2016-04-06 Isomerization catalyst and preparation method thereof Pending CN105833900A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201610206851.0A CN105833900A (en) 2016-04-06 2016-04-06 Isomerization catalyst and preparation method thereof

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201610206851.0A CN105833900A (en) 2016-04-06 2016-04-06 Isomerization catalyst and preparation method thereof

Publications (1)

Publication Number Publication Date
CN105833900A true CN105833900A (en) 2016-08-10

Family

ID=56596647

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201610206851.0A Pending CN105833900A (en) 2016-04-06 2016-04-06 Isomerization catalyst and preparation method thereof

Country Status (1)

Country Link
CN (1) CN105833900A (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108404931A (en) * 2018-05-16 2018-08-17 江苏浩日朗环保科技有限公司 Compound SCR denitration catalyst and preparation method thereof
CN110314684A (en) * 2018-03-30 2019-10-11 中国石油化工股份有限公司 A kind of n-heptane isomerization catalyst and preparation method thereof

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4467129A (en) * 1982-11-24 1984-08-21 Toray Industries, Inc. Conversion of xylenes containing ethylbenzene
CN1340601A (en) * 2000-08-30 2002-03-20 中国石油化工股份有限公司 Aromatizing catalyst for light hydrocarbon and its preparing process
US7425660B2 (en) * 2005-09-14 2008-09-16 Uop Llc Ethylbenzene conversion and xylene isomerization processes and catalysts therefor
CN102309978A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Ethyl benzene dealkylation catalyst and preparation method and application thereof
CN102309979A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Catalyst for isomerizing ethyl benzene into dimethyl benzene and preparation method and application thereof
CN102441420A (en) * 2010-10-12 2012-05-09 中国石油化工股份有限公司 C8 aromatic hydrocarbon isomerization catalyst, preparation method and application thereof
CN102500409A (en) * 2011-09-28 2012-06-20 大连理工大学 Gasoline aromatization and isomerization reforming catalyst and preparation method and applications thereof
CN103100413A (en) * 2011-10-17 2013-05-15 中国石油化工股份有限公司 Isomerization catalyst and its application

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4467129A (en) * 1982-11-24 1984-08-21 Toray Industries, Inc. Conversion of xylenes containing ethylbenzene
CN1340601A (en) * 2000-08-30 2002-03-20 中国石油化工股份有限公司 Aromatizing catalyst for light hydrocarbon and its preparing process
US7425660B2 (en) * 2005-09-14 2008-09-16 Uop Llc Ethylbenzene conversion and xylene isomerization processes and catalysts therefor
CN102309978A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Ethyl benzene dealkylation catalyst and preparation method and application thereof
CN102309979A (en) * 2010-07-07 2012-01-11 中国石油化工股份有限公司 Catalyst for isomerizing ethyl benzene into dimethyl benzene and preparation method and application thereof
CN102441420A (en) * 2010-10-12 2012-05-09 中国石油化工股份有限公司 C8 aromatic hydrocarbon isomerization catalyst, preparation method and application thereof
CN102500409A (en) * 2011-09-28 2012-06-20 大连理工大学 Gasoline aromatization and isomerization reforming catalyst and preparation method and applications thereof
CN103100413A (en) * 2011-10-17 2013-05-15 中国石油化工股份有限公司 Isomerization catalyst and its application

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
朱洪法等编著: "《炼油及石油化工"三剂"手册》", 31 January 2015 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110314684A (en) * 2018-03-30 2019-10-11 中国石油化工股份有限公司 A kind of n-heptane isomerization catalyst and preparation method thereof
CN110314684B (en) * 2018-03-30 2021-11-16 中国石油化工股份有限公司 N-heptane isomerization catalyst and preparation method thereof
CN108404931A (en) * 2018-05-16 2018-08-17 江苏浩日朗环保科技有限公司 Compound SCR denitration catalyst and preparation method thereof

Similar Documents

Publication Publication Date Title
CN101462050B (en) Mesoporous composite oxides and catalyst as well as preparation method and aromatization method thereof
WO2016192041A1 (en) Process for converting naphtha
CN102211972B (en) Application of hydrotalcite-based supported catalyst to preparation of isobutene from isobutane by dehydrogenating
JP2011148720A (en) Method for producing butadiene
CN105833900A (en) Isomerization catalyst and preparation method thereof
CN105126897B (en) A kind of molecular sieve carried copper-based catalysts of SBA 15 and preparation method and application
JP2017535423A (en) METATHESIS CATALYST ON MIXED METAL OXIDE-ZEOLITE SUPPORT AND PROCESS FOR USING THE SAME
WO2021055184A1 (en) Chromium-based catalysts and processes for converting alkanes into higher and lower aliphatic hydrocarbons
CN101786943A (en) Catalytic synthesis method for preparing cresol by toluene one-step hydroxylation reaction
CN101209423B (en) Preparation method of molecular sieve catalyst with superpower acidity
CN109414685A (en) The preparation of catalyst based on ZSM-5 and the purposes in ethylbenzene dealkylation method
CN112588314B (en) Catalyst for producing propane by converting light hydrocarbon and preparation method and application thereof
CN107866254A (en) Catalyst for the equal acid anhydride of durol gaseous oxidation system
CN107952472A (en) A kind of alkyl aromatic hydrocarbon isomerization catalyst and preparation and application
CN107952471A (en) Alkyl aromatic hydrocarbon isomerization catalyst and preparation and application
CN115475659B (en) Metal organic framework material/molecular sieve series catalyst and preparation method and application thereof
CN105289704A (en) Preparation method of C8 aromatic isomerization catalyst
CN108285151A (en) A kind of Ce same order elements LTL molecular sieves and preparation method thereof
CN106311321B (en) A kind of catalyst and preparation method and application of the zeolite of eutectic containing EU-1/ZSM-5
WO2007105875A1 (en) Preparing method of light olefin trimers and production of heavy alkylates by using thereof
CN108043435B (en) Catalyst for preparing pyromellitic dianhydride by gas-phase oxidation of durene and preparation and application thereof
CN104353443A (en) Method for preparing styrene catalyst by ethylbenzene dehydrogenation
CN103418379A (en) Catalyst for removing alkadiene in C4 and preparation method thereof
CN106140235A (en) A kind of support type catalyst for preparing cis-anhydride by n-butane oxidation and preparation method thereof
CN105498824A (en) Hydrocarbon reforming catalyst containing mesoporous molecular sieve, and preparation method thereof

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
WD01 Invention patent application deemed withdrawn after publication
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20160810