CN103316707A - Catalyst and method for catalytic cracking of petroleum hydrocarbons - Google Patents

Catalyst and method for catalytic cracking of petroleum hydrocarbons Download PDF

Info

Publication number
CN103316707A
CN103316707A CN2012100746728A CN201210074672A CN103316707A CN 103316707 A CN103316707 A CN 103316707A CN 2012100746728 A CN2012100746728 A CN 2012100746728A CN 201210074672 A CN201210074672 A CN 201210074672A CN 103316707 A CN103316707 A CN 103316707A
Authority
CN
China
Prior art keywords
catalyst
petroleum hydrocarbon
molecular sieve
accounts
weight
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
CN2012100746728A
Other languages
Chinese (zh)
Inventor
吉媛媛
司宇辰
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.)
Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
Original Assignee
Sinopec Beijing Research Institute of Chemical Industry
China Petroleum and Chemical Corp
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 Sinopec Beijing Research Institute of Chemical Industry, China Petroleum and Chemical Corp filed Critical Sinopec Beijing Research Institute of Chemical Industry
Priority to CN2012100746728A priority Critical patent/CN103316707A/en
Publication of CN103316707A publication Critical patent/CN103316707A/en
Pending legal-status Critical Current

Links

Classifications

    • 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

  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Catalysts (AREA)

Abstract

The invention relates to a catalyst and a method for catalytic cracking of petroleum hydrocarbons. The catalyst comprises molecular sieves, filling materials, and modification components. The catalyst and the method provided by the invention can improve the yield of low-carbon olefin and the utilization rate of petroleum hydrocarbons. Besides, products with high added value can be obtained by means of the catalyst and the method.

Description

The method of petroleum hydrocarbon catalytic pyrolysis catalyst and catalytic pyrolysis petroleum hydrocarbon
Technical field
The present invention relates to the method for a kind of petroleum hydrocarbon catalytic pyrolysis catalyst and catalytic pyrolysis petroleum hydrocarbon, particularly use the method for acquisition low-carbon alkene and the high added value product of this catalyst oil pyrolysis hydrocarbon.
Background technology
Produce technology take ethene and propylene as the purpose product by cracking petroleum hydrocarbon, adopt tube furnace steam heat cracking technology more than 98%.The yield of ethene and propylene summation depends on reaction condition to a great extent, such as cracking temperature, the time of staying and water-oil factor, also depends on the composition of cracking stock such as naphtha simultaneously.The ethene that is obtained by this technique and the yield of propylene summation generally are no more than 45wt%, and the ratio of the amount of propylene and ethene is less than 1, and the yield of the low value-added product such as methane is higher.This technique is produced ethene being higher than under 840 ℃ the temperature usually, thus energy consumption large, cracking reacting furnace material is had relatively high expectations.In addition, the product that obtains distributes non-adjustable and the petroleum hydrocarbon effective rate of utilization is lower.
Produce technology take ethene and propylene as the purpose product by petroleum hydrocarbon catalytic pyrolysis, reaction temperature low (less than 750 ℃) on the one hand, energy consumption is little; On the other hand, because the effect of catalyst, product distributes and can regulate, and propylene and ethylene ratio are apparently higher than thermal cracking.But when reaction temperature was higher than 600 ℃, because molecular sieve catalyst, carbon deposit was serious in the course of reaction, and condensed-nuclei aromatics product one-tenth amount is larger, thereby has reduced the effective rate of utilization of petroleum hydrocarbon.
In addition, carrying out the technology that the carbochain cleavage reaction is produced oil product take petroleum hydrocarbon as raw material, comprise catalytic cracking and hydrocracking, this technology is mainly produced high-octane rating (about motor method 80) gasoline and diesel oil by mink cell focus and the residual oil of processing and is rich on a small quantity the cracked gas of propylene and butylene.Although catalytic cracking technology also can obtain the low-carbon alkene of certain yield, primary product is oil product, and coke content is also very high.
Produced by petroleum hydrocarbon catalytic pyrolysis take ethene and propylene in the technology of purpose product, the performance of catalyst directly affects final product.Catalytic cracking catalyst is often take molecular sieve as main active component.
Patent US20100105974 discloses the catalyst that the molecular sieve by two kinds of different pore sizes and performance forms, with the yield that improves low-carbon alkene and the circulation cracking that reduces light component alkane.Patent CN200810043110.0 discloses the method for preparing a kind of coexisting molecular sieve, and it solves single, the acid weak and active not high problem of aperture of porous material in the catalyst.
Because the performance of molecular sieve can not be applicable to the cracking reaction requirement fully, therefore need to carry out modification to molecular sieve.Patent CN200980104219.3 discloses the catalyst that uses manganese and simultaneously modification of phosphorus to be comprised of zeolite, clay and inorganic composite.
The petroleum hydrocarbon catalytic pyrolysis catalyst of prior art for pursuing high one way ethene and propene yield, has improved the cracking degree of one way petroleum hydrocarbon, but can not take into account the effective rate of utilization of petroleum hydrocarbon, and product structure is single or product quality is lower.
Summary of the invention
For existing above-mentioned technical problem in the prior art, the present invention proposes a kind of petroleum hydrocarbon catalytic pyrolysis catalyst.Compare with the catalyst of prior art, its particle diameter is less and use different modified components so that not only the yield of low-carbon alkene is higher and utilization rate petroleum hydrocarbon is also higher.Simultaneously, can also obtain other high added value product.The invention still further relates to the method for using this petroleum hydrocarbon catalytic pyrolysis catalyst catalytic pyrolysis petroleum hydrocarbon.
According to a first aspect of the invention, provide a kind of petroleum hydrocarbon catalytic pyrolysis catalyst, it is made of molecular sieve, filler and modified component.
In one embodiment, molecular sieve is the ZSM type, its SiO 2With Al 2O 3Mol ratio be 20: 1-800: 1, particle diameter is 50-900nm; Filler is Al 2O 3And SiO 2In one or both; Modified component is lanthanide series, alkali metal and phosphorus.In a preferred embodiment, molecular sieve is the ZSM-5 type, its SiO 2With Al 2O 3Mol ratio be 25: 1-500: 1, particle diameter is 100-800nm.
Nano level molecular sieve is so that the catalytic capability of catalyst is stronger.This is owing to the small particle diameter molecular sieve so that the diffusion distance shortens, thereby so that ethene and propylene that reaction generates easily diffuse out the productive rate that has improved low-carbon alkene from the duct of molecular sieve.Simultaneously, the aromatisation trend of product reduces.
In one embodiment, molecular sieve accounts for the 20-80wt% of total catalyst weight, and described filler accounts for the 15-75wt% of total catalyst weight, and described modified component accounts for the 0.12-20wt% of total catalyst weight.
In a specific embodiment, modified component comprises a kind of, phosphorus and the lanthanum in sodium and the potassium.Wherein, the phosphorus in the modified component accounts for the 0.1-10wt% of total catalyst weight, and lanthanum accounts for the 0.01-5wt% of total catalyst weight, and alkali metal accounts for the 0.01-5wt% of total catalyst weight.
In modified component, lanthanide series metal and phosphorus make the stable effect of framework of molecular sieve aluminium except having, and also have the effect that catalyzer coke content is reduced.The synergy of each component in the catalyst, the ability of particularly nano level molecular sieve and lanthanide series metal, phosphorus and alkali metal are obviously lower alkene aromatisation and further coking, the such content of aromatic hydrocarbons in the product, and petrol content increases, thereby make the content of the content of the n-alkane in the gasoline fraction and alkene very low, improved the octane number of gasoline fraction.
According to the present invention, petroleum hydrocarbon catalytic pyrolysis catalyst is made by following steps:
At first, with molecular sieve and filler take mass ratio as 4: 1-1: 4 mix and moulding, for example are shaped to material strip by the extrusion method through mixture.
Then, material strip is carried out drying.
Then, carry out loaded modified to material strip.
At last, again the material strip after the loaded modified component is carried out drying, roasting, obtain required catalyst.
Modified component can be introduced modified component in the catalyst by existing methods such as ion-exchange, infusion process or mixing methods.
The solution that contains modified component is the aqueous solution of lanthanide metal compound, alkali metal compound and phosphorus element-containing compound.Preferably, lanthanide metal compound is lanthanum nitrate, and alkali metal compound is preferably sodium nitrate or potassium nitrate, and the phosphorus element-containing compound is ammonium dihydrogen phosphate (ADP).
According to a second aspect of the invention, a kind of method of catalytic pyrolysis petroleum hydrocarbon is provided, comprise: petroleum hydrocarbon and fixed bed petroleum hydrocarbon catalytic pyrolysis catalyst haptoreaction are generated low-carbon alkene and gasoline, and wherein reaction condition is: temperature 450-750 ℃, pressure 0-0.09MPa, water-oil factor 0-3, petroleum hydrocarbon weight space velocity 0.1-20h -1Employed petroleum hydrocarbon catalytic pyrolysis catalyst is petroleum hydrocarbon catalytic pyrolysis catalyst mentioned above.
In a preferred embodiment, reaction condition is: temperature 550-620 ℃, pressure 0.01-0.05MPa, water-oil factor 0-1.5, petroleum hydrocarbon weight space velocity 0.5-8h -1
According to the present invention, the pressure of catalytic cracking reaction is lower, and this requires greatly to reduce to reaction unit, can greatly reduce the investment to reaction unit, reduces cost.And because system pressure and reaction temperature are lower, the degree of safety of whole system is also higher.In addition, lower reaction temperature is also so that the amount of low value-added product such as methane is also very low.
In one embodiment, petroleum hydrocarbon is naphtha and/or C 4-C 18Alkane.In another embodiment, the low-carbon alkene that obtains is ethene and propylene, and gasoline is C 5-C 10Alkane.
Compared with prior art, method by petroleum hydrocarbon catalytic pyrolysis catalyst of the present invention and catalytic pyrolysis petroleum hydrocarbon, particularly use lanthanide series, phosphorus and alkali metal as the altered contents of petroleum hydrocarbon catalytic pyrolysis catalyst and use simultaneously nano level molecular sieve, when obtaining high yield low-carbon alkene, the yield of the high-knock rating gasoline that added value is higher is also higher.In addition, the catalysis of the application of the invention is split and method, is guaranteeing that the fixed-bed catalytic cleavage reaction pressure is lower, and reaction unit is required under the low advantage, has improved the standby olefins yield of traditional fixed-bed catalytic cracking.And because system pressure and reaction temperature are lower, the degree of safety of whole system is also higher.Lower reaction temperature is also so that the amount of low value-added product such as methane is also very low.
The specific embodiment
The below will be described further the method for petroleum hydrocarbon catalytic pyrolysis catalyst of the present invention and catalytic pyrolysis petroleum hydrocarbon.
Embodiment 1:
SiO 2With Al 2O 3Mol ratio be that 440: 1, particle diameter are that ZSM-5 molecular sieve and the aluminium oxide of 500-900nm mixed and be shaped to material strip take mass ratio as 3: 1.Then, material strip at first at 100 ℃ of lower dry 10h, is processed at 560 ℃ of lower roasting 4h again.Then this material strip is placed the solution that contains diammonium hydrogen phosphate, lanthanum nitrate and sodium nitrate to soak 2 hours, filter, drying is 10 hours under 100 ℃, again 560 ℃ of lower roastings 4 hours, obtains catalyst.By analysis, phosphorus, lanthanum and sodium account for respectively 2.30wt%, 0.09wt% and the 0.06wt% of total catalyst weight in this catalyst.
The catalyst that obtains is estimated in the Miniature tube type fixed bed reactors.Experiment condition is: industrial common naphtha (composition sees Table 1, and wherein the aromatic hydrocarbons weight content is 8.76wt%), the boiling range scope is 49-188 ℃.Reaction condition sees Table 2, and reaction result sees Table 3.
Embodiment 2:
The difference of the preparation method of catalyst and embodiment 1 only is the SiO of ZSM-5 molecular sieve 2With Al 2O 3Mol ratio be that 180: 1, particle diameter are 500-900nm, other processes are identical with embodiment 1 with experimental technique.By analysis, phosphorus, lanthanum and sodium account for respectively 1.10wt%, 0.15wt% and the 0.12wt% of total catalyst weight in this catalyst.
The catalyst that obtains is estimated in the Miniature tube type fixed bed reactors.Reaction condition sees Table 2, and reaction result sees Table 3.
Embodiment 3:
The preparation method of catalyst and prepared catalyst are all with identical with embodiment 1.
The catalyst that obtains is estimated in the Miniature tube type fixed bed reactors.Reaction condition sees Table 2, and reaction result sees Table 3.
Embodiment 4:
The difference of the preparation method of catalyst and embodiment 1 only is that alkali metal compound is potassium nitrate, and other processes are identical with embodiment 1 with experimental technique.By analysis, phosphorus, lanthanum and potassium account for respectively 2.18wt%, 0.08wt% and the 0.07wt% of total catalyst weight in this catalyst.
The catalyst that obtains is tested in the Miniature tube type fixed bed reactors.Reaction condition sees Table 2, and reaction result sees Table 3.
Table 1
Figure BDA0000145130590000051
Table 2
Embodiment 1 Embodiment 2 Embodiment 3 Embodiment 4
Reaction temperature (℃) 600 600 580 600
Weight space velocity (h -1) 1 1 5 1
Water-oil factor (w/w) 0.5 0.5 0 0.5
Pressure (MPa) 0.02 0.01 0.02 0.01
Table 3
Yield (wt%) Embodiment 1 Embodiment 2 Embodiment 3 Embodiment 4
Methane 2.83 3.24 4.68 2.56
Ethane+propane 9.07 9.49 8.30 8.76
Ethene+propylene 36.24 37.03 28.41 37.02
Propylene/ethylene 1.56 1.82 1.84 1.56
Butane 2.31 2.58 1.96 2.02
Butylene 7.81 8.19 6.61 7.46
C 6-C 10Aromatic hydrocarbons 20.80 19.32 28.60 22.07
C 5-C 10Alkane 17.70 17.08 17.43 17.18
C 5-C 10N-alkane 2.47 2.30 3.32 2.10
C 5-C 10Alkene 0.98 0.93 1.34 0.73
C 10+ ＜0.5 ＜0.5 ＜0.5 ＜0.5
C in table 3 nThe carbon number of expression hydrocarbon, C 10+The expression carbon number is at the hydrocarbon more than 10.
Can find out by above-described embodiment, the method for the petroleum hydrocarbon catalytic pyrolysis catalyst of the application of the invention and catalytic pyrolysis petroleum hydrocarbon, the total recovery of ethene and propylene is higher, simultaneously gasoline fraction (that is, C 5-C 10Alkane) yield is also higher, is 37.02% such as the total recovery of ethene and propylene among the embodiment 4, and the gasoline fraction yield is 18.96wt%, and the content of the alkene in the gasoline fraction and n-alkane is also very low, and namely the quality of gasoline is higher.In addition, obtaining has a certain amount of aromatic hydrocarbons, and product category is abundanter.
Compare with thermal cracking processes with fluid catalystic cracking (FCC) process, the method of the application of the invention and catalyst, the total recovery of ethene and propylene is higher, reach 37.03wt% such as embodiment 2, near the total recovery 40-45wt% of ethene and the propylene of thermal cracking processes, be higher than the total recovery 12-25wt% of fluid catalystic cracking ethene and propylene.
In the method for the invention, reaction pressure is lower, all is lower than 0.1MPa, and this requirement to reaction unit reduces greatly.And because system pressure and reaction temperature are lower, the degree of safety of whole system is also higher.In addition, lower reaction temperature is also so that the amount of low value-added product such as methane is also very low.
Therefore, by method of the present invention and catalyst, not only can obtain ethene and the propylene of high yield, and the yield of the high-knock rating gasoline of high added value is also higher, the utilization rate of petroleum hydrocarbon is also higher.In addition, method of the present invention is also lower to the requirement of reaction unit, and the degree of safety of whole system is also higher.
Although invention has been described with reference to preferred embodiment, without departing from the scope of the invention, can carry out various improvement to it.The present invention is not limited to disclosed embodiment in the literary composition, but comprises all technical schemes in the scope that falls into claim.

Claims (10)

1. a petroleum hydrocarbon catalytic pyrolysis catalyst is characterized in that, described catalyst is made of molecular sieve, filler and modified component.
2. catalyst according to claim 1 is characterized in that, described molecular sieve is the ZSM type, its SiO 2With Al 2O 3Mol ratio be 20: 1-800: 1, particle diameter is 50-900nm; Filler is Al 2O 3And SiO 2In one or both; Modified component is lanthanide series, alkali metal and phosphorus.
3. catalyst according to claim 2 is characterized in that, described molecular sieve is the ZSM-5 type, its SiO 2With Al 2O 3Mol ratio be 25: 1-500: 1, particle diameter is 100-800nm.
4. each described catalyst in 3 according to claim 1, it is characterized in that, described molecular sieve accounts for the 20-80wt% of total catalyst weight, and described filler accounts for the 15-75wt% of total catalyst weight, and described modified component accounts for the 0.12-20wt% of total catalyst weight.
5. catalyst according to claim 4 is characterized in that, described modified component comprises a kind of, phosphorus and the lanthanum in sodium and the potassium.
6. catalyst according to claim 5 is characterized in that, the phosphorus in the described modified component accounts for the 0.1-10wt% of total catalyst weight, and lanthanum accounts for the 0.01-5wt% of total catalyst weight, and alkali metal accounts for the 0.01-5wt% of total catalyst weight.
7. the method for a catalytic pyrolysis petroleum hydrocarbon, it is characterized in that, petroleum hydrocarbon and fixed bed petroleum hydrocarbon catalytic pyrolysis catalyst haptoreaction are generated low-carbon alkene and gasoline, and wherein reaction condition is: temperature 450-750 ℃, pressure 0-0.09MPa, water-oil factor 0-3, petroleum hydrocarbon weight space velocity 0.1-20h -1, described petroleum hydrocarbon catalytic pyrolysis catalyst is each described catalyst in the claims.
8. method according to claim 7 is characterized in that, described reaction condition is: temperature 550-620 ℃, pressure 0.01-0.05MPa, water-oil factor 0-1.5, petroleum hydrocarbon weight space velocity 0.5-8h -1
9. method according to claim 8 is characterized in that, described petroleum hydrocarbon is naphtha and/or C 4-C 18Alkane.
10. method according to claim 8 is characterized in that, described low-carbon alkene is ethene and propylene, and described gasoline is C 5-C 10Alkane.
CN2012100746728A 2012-03-20 2012-03-20 Catalyst and method for catalytic cracking of petroleum hydrocarbons Pending CN103316707A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN2012100746728A CN103316707A (en) 2012-03-20 2012-03-20 Catalyst and method for catalytic cracking of petroleum hydrocarbons

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN2012100746728A CN103316707A (en) 2012-03-20 2012-03-20 Catalyst and method for catalytic cracking of petroleum hydrocarbons

Publications (1)

Publication Number Publication Date
CN103316707A true CN103316707A (en) 2013-09-25

Family

ID=49185921

Family Applications (1)

Application Number Title Priority Date Filing Date
CN2012100746728A Pending CN103316707A (en) 2012-03-20 2012-03-20 Catalyst and method for catalytic cracking of petroleum hydrocarbons

Country Status (1)

Country Link
CN (1) CN103316707A (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104557400A (en) * 2013-10-29 2015-04-29 中国石油化工股份有限公司 Method for producing propylene by naphtha catalytic cracking
CN106629768A (en) * 2015-11-02 2017-05-10 中国石油化工股份有限公司 Synthetic method for uniform nanosized ZSM-5 molecular sieve

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3900526A (en) * 1972-05-02 1975-08-19 Phillips Petroleum Co Selective removal of 1,2 polyenes and acetylenic compounds from conjugated-diene feed using a nickel, iron or cobalt arsenide catalyst
CN101664692A (en) * 2008-09-05 2010-03-10 中国石油化工股份有限公司 Catalyst for preparation of propylene and ethylene from mixed C4 alkenes and application thereof
CN102040227A (en) * 2009-10-20 2011-05-04 中国石油化工股份有限公司 Ultrafine grain molecular sieve for preparation of low-carbon alkene by petroleum hydrocarbon cracking as well as catalyst and application thereof

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3900526A (en) * 1972-05-02 1975-08-19 Phillips Petroleum Co Selective removal of 1,2 polyenes and acetylenic compounds from conjugated-diene feed using a nickel, iron or cobalt arsenide catalyst
CN101664692A (en) * 2008-09-05 2010-03-10 中国石油化工股份有限公司 Catalyst for preparation of propylene and ethylene from mixed C4 alkenes and application thereof
CN102040227A (en) * 2009-10-20 2011-05-04 中国石油化工股份有限公司 Ultrafine grain molecular sieve for preparation of low-carbon alkene by petroleum hydrocarbon cracking as well as catalyst and application thereof

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104557400A (en) * 2013-10-29 2015-04-29 中国石油化工股份有限公司 Method for producing propylene by naphtha catalytic cracking
CN104557400B (en) * 2013-10-29 2017-01-04 中国石油化工股份有限公司 A kind of naphtha catalytic cracking produces the method for propylene
CN106629768A (en) * 2015-11-02 2017-05-10 中国石油化工股份有限公司 Synthetic method for uniform nanosized ZSM-5 molecular sieve

Similar Documents

Publication Publication Date Title
CN103361114A (en) Process for producing high-octane gasoline from carbon-rich four-carbon five-carbon hexaalkane raw material
CN103319293B (en) Method for preparing light olefins and gasoline by catalytically cracking petroleum hydrocarbons and employed catalyst
CN103157502A (en) Catalyst of preparing ethylene and propylene by carbinol and / or dimethyl ether, preparing method and application thereof
CN103361113B (en) Process for producing high-octane gasoline by using raw material rich in carbon, four carbon, five carbon and six alkane
CN103509601B (en) Technological process for co-production of propane by aromatization of carbon tetrad-hydrocarbon
CN101875851B (en) Non-hydrogenation upgrading method for liquefied gas fractions
CN102794195B (en) Catalyst suitable for enhancing gasoline octane number of fuel and lowering olefin content and application thereof
CN103509600B (en) Method for producing high-octane gasoline blending component by mixed carbon four-hydrocarbon aromatization
CN101724432B (en) Method for producing high-octane gasoline by light hydrocarbon non-hydrogenation modification
CN109675616B (en) Catalytic conversion catalyst for producing more butene, preparation method of catalytic conversion catalyst and catalytic conversion method for producing more butene
CN101722025B (en) Catalyst for mixing C4 olefins to prepare propylene and ethylene, and using method thereof
CN103316707A (en) Catalyst and method for catalytic cracking of petroleum hydrocarbons
CN101020844B (en) Catalyst for reducing olefin content in mixed material of liquified gas and gasoline
CN100406416C (en) Method of preparing ethylene and propylene and catalyst used in said method
CN110947417B (en) Catalyst for producing propane and gasoline from alkane, preparation method and application
CN102286297B (en) Method for increase production of propylene and ethylene
CN1212376C (en) Light hydrocarbon non-hydrogenation modified catalyst, preparing process and application thereof
CN104557377B (en) The method of oxygenatedchemicals and naphtha coupled reaction production ethylene and propylene
CN102807465A (en) Method for producing propane and gasoline by using butane
CN103623862B (en) A kind of Catalysts and its preparation method being produced gasoline component by oil refinery dry gas
CN102286292B (en) Method for increase production of propylene and ethylene by pyrolyzing C4 raffinate
CN106221786A (en) A kind of method for transformation of Petroleum
CN101580737A (en) Preparation method of molecular sieve catalyst for milling aromatization reaction of distilled gasoline and liquefied gas
CN102899084B (en) Method for co-production of ethylene cracking raw material by aromatization of carbon tetrad
CN102285854B (en) Method for increasing yields of propylene, ethylene and butadiene

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C12 Rejection of a patent application after its publication
RJ01 Rejection of invention patent application after publication

Application publication date: 20130925