CN100593528C - Method for producing ethene and propene by catalytic oxidation cracking naphtha - Google Patents

Method for producing ethene and propene by catalytic oxidation cracking naphtha Download PDF

Info

Publication number
CN100593528C
CN100593528C CN200610118534A CN200610118534A CN100593528C CN 100593528 C CN100593528 C CN 100593528C CN 200610118534 A CN200610118534 A CN 200610118534A CN 200610118534 A CN200610118534 A CN 200610118534A CN 100593528 C CN100593528 C CN 100593528C
Authority
CN
China
Prior art keywords
zsm
naphtha
zeolite
propene
petroleum naphtha
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.)
Active
Application number
CN200610118534A
Other languages
Chinese (zh)
Other versions
CN101190865A (en
Inventor
姚晖
谢在库
马广伟
杨为民
陈亮
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.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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 China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN200610118534A priority Critical patent/CN100593528C/en
Publication of CN101190865A publication Critical patent/CN101190865A/en
Application granted granted Critical
Publication of CN100593528C publication Critical patent/CN100593528C/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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

Abstract

The invention relates to a method of producing ethylene and propylene by naphtha catalytic cracking, and mainly solves the problem that in naphtha catalytic cracking reaction, the catalyst has short service life due to coking, thereby requiring a large amount of vapor or inert gases for diluting. The invention adopts naphtha of C4-C10 hydrocarbon as raw material; the raw material hydrocarbon, after being vaporized, is mixed with the inert gases, then the mixture contacts with catalyst to produce the ethylene and the propylene in reaction conditions of temperature of 580 - 750 DEG C, gauge reaction pressure of 0.05 to 0.5MPa, weight space velocity, weight ration of water to naphtha of 0 to 5:1 and mole ratio of naphtha/O2 in mixture of the raw material and the inert gases. The catalyst technical proposal is that at least one of ZSM-5/mordenite accrete molecular sieves, ZSM-5/beta zeolite accrete molecular sieves or ZSM-5/Y-zeolite accrete molecular sieves is adopted as catalyst, therebyproperly solving the problem. The invention is used for industrial production of the ethylene and the propylene by the naphtha catalytic cracking.

Description

The method of producing ethene and propene by catalytic oxidation cracking naphtha
Technical field
The present invention relates to a kind of method of producing ethene and propene by catalytic oxidation cracking naphtha.
Background technology
Ethylene, propylene is the basic material of petrochemical complex, and producing the most frequently used method of ethylene, propylene at present is steam heat hydrocarbon cracking raw material (based on petroleum naphtha).The steam heat cracking naphtha exists that facility investment is big, temperature of reaction is high, processing condition are harsh, to reaction boiler tube material requirements height, shortcoming such as loss is big, production capacity is low.
It is one of hot subject of being concerned about of people that the catalytic pyrolysis hydro carbons is produced ethylene, propylene.Calendar year 2001, the Japan scholar was a raw material with light naphthar, and adopting the 10%La/ZSM-5 zeolite molecular sieve is catalyzer, and 650 ℃ of temperature, the steam feed ratio is 0.64, under the condition of material concentration 9.6 volume % (nitrogen dilution), has obtained 61% ethylene, propylene yield.Catalytic pyrolysis reduces greatly than water vapour thermo-cracking temperature, but also exists the easy coking of catalyzer, life-span weak point, must feed shortcomings such as a large amount of water vapour or inert gas dilution.
The patent CN104442 of the Dalian Chemistry and Physics Institute has described hydro carbons gas phase oxidative cracking petroleum naphtha coproduction carbon monoxide technology.Under 600～950 ℃ of temperature of normal pressure, the empty reactor of silica tube (i.d.6 millimeter * 300 millimeter), C/O mol ratio 1.5～6.0 in the unstripped gas, aerating oxygen (using nitrogen dilution) or air, cracking normal hexane have obtained 34.43% ethene and 14.62% propene yield.This patent relates to is oxidation thermal cracking reaction process without catalyzer, compares the steam heat cracking and has reduced temperature of reaction, has reduced coking.
The document that relates to catalytic oxidative cracking has only the chapter 6 of the Ph D dissertation of the Dalian Chemistry and Physics Institute " research of high-carbon hydrocarbon oxicracking producing light olefins ".Choose H type, 10%La modification and alkalescence (0.25%Li/MgO) ZSM-5 catalyzer in the literary composition and investigated the catalytic oxidative cracking reactivity worth of normal hexane and hexanaphthene.In the empty reactor of above-mentioned silica tube (i.d.6 millimeter * 300 millimeter), nitrogen dilution is than 90%, under 830 ℃ of the temperature, uses HZSM-5 catalytic oxidative cracking normal hexane, obtained about 36% yield of ethene and about 22.5% propene yield.Last author reaches a conclusion: the ZSM-5 catalyzer of rare earth La modification has good catalytic performance, and basic catalyst does not have catalytic activity.H type ZSM-5 catalyzer is not suitable as the catalyzer of oxicracking process because the active centre is capped easily in reaction process.
Summary of the invention
Technical problem to be solved by this invention is a prior art in short problem of naphtha catalytic pyrolysis preparing ethylene propylene reacting middle catalyst life-span, and a kind of method of new producing ethene and propene by catalytic oxidation cracking naphtha is provided.When this method had high ethylene, propylene yield, catalyzer had the advantage than the long life.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of method of producing ethene and propene by catalytic oxidation cracking naphtha, and with C 4～C 10The petroleum naphtha of hydrocarbon is a raw material, and the back and oxygenous gas of raw material hydrocarbon vaporization mixes, and is 580～750 ℃ in temperature of reaction, is 0.05～0.5MPa in the gauge pressure reaction pressure, and weight space velocity is 0.5～3 hour -1, water/petroleum naphtha weight ratio is 0～5: 1, petroleum naphtha/O in the material mixed gas 2Mol ratio is under 0.3～5.0: 1 condition, and material mixed gas and catalyzer contact reacts generate ethylene, propylene, and wherein catalyst system therefor is selected from least a in ZSM-5/ mercerization zeolite symbiosis molecular screen or the ZSM-5/ beta zeolite coexisting molecular sieve.
In the technique scheme, the SiO of coexisting molecular sieve 2/ Al 2O 3Mol ratio is 10～300, and more preferably scope is 20～100; Oxygenous gas preferred version is the mixed gas of pure oxygen, air or pure oxygen and nitrogen; The temperature of reaction preferable range is 600～650 ℃; In gauge pressure reaction pressure preferable range is 0.05～0.15MPa; The weight space velocity preferable range is 0.5～1.5 hour -1Water/petroleum naphtha weight ratio preferable range is＞0～3: 1; Petroleum naphtha/O in the material mixed gas 2The mol ratio preferable range is 0.5～3.0: 1; Contain inert nitrogen gas in the material mixed gas, its amount accounts for 10～80% of volume of gas.
The present invention has fed oxygenous gas owing to adopted coexisting molecular sieve as naphtha cracking petroleum naphtha catalyzer in the reaction, be 580～750 ℃ in temperature of reaction, is 0.05～0.5MPa in the gauge pressure reaction pressure, and weight space velocity is 0.5～3 hour -1, water petroleum naphtha weight ratio is 0～5: 1, petroleum naphtha/O in the material mixed gas 2Mol ratio is that petroleum naphtha is through catalytic pyrolysis under 0.3～5.0: 1 the condition, and its ethylene, propylene total recovery has reached 48.64%; Catalyst life has reached 28 hours simultaneously, compares with under the obstructed oxygen-containing gas situation of simple ZSM-5 catalyzer, and its life-span has improved 600%, has obtained better technical effect.
In order to check and rate activity of such catalysts, with the fixed-bed micro-reactor of 12 mm dias, catalyzer loading amount 12 grams use the petroleum naphtha of Shanghai Gaoqiao petrochemical industry to be raw material.Used raw material petroleum naphtha index is listed in table 1.
Table 1 feed naphtha index
Project Data
Density (20 ℃) kilogram/rice 3 704.6
Boiling range is boiling range ℃ just 40
Whole boiling range ℃ 160
Saturated vapor pressure (20 ℃) kPa 50.2
Alkane % (weight %) 65.18
Normal paraffin % (weight %) in the alkane ＞32.5
Naphthenic hydrocarbon % (weight %) 28.44
Alkene % (weight %) 0.17
Aromatic hydrocarbons % (weight %) 6.21
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
Get 284 gram Starsos, become solution A with 300 gram dissolved in distilled water, get 33.3 gram Tai-Ace S 150, make solution B with 100 gram distilled water, B solution is slowly poured in the A solution, the powerful stirring, add 24.4 gram quadrols then, after stirring 20 fens clock times, regulate pH value 11.5 with dilute sulphuric acid, the mole proportioning of controlling colloidal sol is: Si: Al: quadrol: H 2O=1: 0.1: 0.4: 40, add the crystal seed that contains ZSM-5 and mordenite presoma, stir and after 30 minutes mixing solutions is put into autoclave, 180 ℃ of insulations 40 hours, take out washing, 150 ℃ of oven dry, 550 ℃ of roastings then, make the coexisting molecular sieve of ZSM-5 and mordenite, with the XRD diffraction quantitatively as can be known in the coexisting molecular sieve ZSM-5 and mordenite weight content be respectively 95% and 5%.With concentration is 5% ammonium nitrate solution, 70 ℃ of exchanges twice, 550 ℃ of roastings then, repeat twice after, make Hydrogen ZSM-5 and mercerization zeolite symbiosis molecular screen.
[embodiment 2]
Get 284 gram Starsos, become solution A with 300 gram dissolved in distilled water, get 16.7 gram Tai-Ace S 150, make solution B with 100 gram distilled water, B solution is slowly poured in the A solution, the powerful stirring, add 12.2 gram quadrols and 29.4 gram tetraethyl ammonium hydroxides (mixed templates is designated as M) then, after stirring 20 fens clock times, regulate pH value 11 with dilute sulphuric acid, the mole proportioning of controlling colloidal sol is: Si: Al: M: H 2O=1: 0.05: 0.4: 40, add 2.8 gram β zeolite seed crystals, mixing solutions is put into autoclave, 160 ℃ of insulations 40 hours, take out washing, 150 ℃ of oven dry, 550 ℃ of roastings then, make ZSM-5/ beta zeolite coexisting molecular sieve, the XRD diffracting spectrum is shown in curve among Fig. 11, with the XRD diffraction quantitatively as can be known in the coexisting molecular sieve ZSM-5 weight percentage be 94.6%, the β zeolite is 5.4%.With concentration is 5% ammonium nitrate solution, 70 ℃ of exchanges twice, 550 ℃ of roastings then, repeat twice after, make Hydrogen ZSM-5/ beta zeolite coexisting molecular sieve.
[embodiment 3]
Get 284 gram Starsos, become solution A with 300 gram dissolved in distilled water, get 33.3 gram Tai-Ace S 150, make solution B with 100 gram distilled water, B solution is slowly poured in the A solution, the powerful stirring, add 24.4 gram quadrols then, after stirring 20 fens clock times, regulate pH value 11.5 with dilute sulphuric acid, the mole proportioning of controlling colloidal sol is: Si: Al: quadrol: H 2O=1: 0.1: 0.4: 40, add 2.8 gram Y zeolite crystal seeds, mixing solutions is put into autoclave, 130 ℃ of insulations 40 hours, take out washing, 150 ℃ of oven dry, 550 ℃ of roastings then, make ZSM-5/Y zeolite coexisting molecular sieve.Quantitatively contain 94.5% ZSM-5 and 5.5% Y zeolite as can be known in the coexisting molecular sieve by weight percentage with the XRD diffraction.With concentration is 5% ammonium nitrate solution, 70 ℃ of exchanges twice, 550 ℃ of roastings then, repeat twice after, make Hydrogen ZSM-5/Y zeolite coexisting molecular sieve.
[embodiment 4～6]
The Hydrogen ZSM-5/Y zeolite coexisting molecular sieve that the Hydrogen ZSM-5/ mercerization zeolite symbiosis molecular screen that embodiment 1 is made, the Hydrogen ZSM-5/ beta zeolite coexisting molecular sieve that embodiment 2 makes and embodiment 3 make makes mechanical mixture by the mixed of equivalent weight.
Coexisting molecular sieve kind and the SiO of embodiment 1～6 2/ Al 2O 3Mol ratio is summarized in table 2.
Table 2
Embodiment The coexisting molecular sieve kind SiO 2/Al 2O 3Mol ratio
1 ZSM-5 and mercerization zeolite symbiosis molecular screen 20
2 ZSM-5/ beta zeolite coexisting molecular sieve 40
3 ZSM-5/Y zeolite coexisting molecular sieve 20
4 ZSM-5/ mordenite+ZSM-5/ β zeolite 25
5 ZSM-5/ mordenite+ZSM-5/Y zeolite 20
6 ZSM-5/ mordenite+ZSM-5/ β zeolite+ZSM-5/Y zeolite 22
Under 650 ℃ temperature of reaction, use the coexisting molecular sieve catalyzer of embodiment 1～6, water/petroleum naphtha weight ratio is 1: 1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is under 0.93: 1 the condition, to check and rate above-mentioned catalyzer, and it is listed to obtain data such as table 3.
Table 3
Embodiment Weight space velocity (hour -1) Reaction pressure (MPa) Yield of ethene (weight %) Propene yield (weight %) Total recovery (weight %)
1 0.5 0.10 28.82 16.69 45.51
2 0.5 0.11 26.33 18.57 44.90
3 0.5 0.15 25.18 17.91 43.09
4 0.5 0.25 22.37 15.33 37.70
5 0.5 0.14 28.38 16.55 44.93
6 1.0 0.18 23.39 17.13 40.52
[embodiment 7～18]
With embodiment 1～6, adjust the material of preparation colloidal sol, obtain different sorts and SiO 2/ Al 2O 3The coexisting molecular sieve of mol ratio is summarized in table 4.
Table 4
Embodiment The coexisting molecular sieve kind SiO 2/Al 2O 3Mol ratio
7 ZSM-5 and mercerization zeolite symbiosis molecular screen 40
8 ZSM-5 and mercerization zeolite symbiosis molecular screen 100
9 ZSM-5/ beta zeolite coexisting molecular sieve 60
10 ZSM-5/ beta zeolite coexisting molecular sieve 100
11 ZSM-5/Y zeolite coexisting molecular sieve 50
12 ZSM-5/Y zeolite coexisting molecular sieve 100
13 ZSM-5/ mordenite+ZSM-5/ β zeolite 60
14 ZSM-5/ mordenite+ZSM-5/ β zeolite 100
15 ZSM-5/ mordenite+ZSM-5/Y zeolite 50
16 ZSM-5/ mordenite+ZSM-5/Y zeolite 100
17 ZSM-5/ mordenite+ZSM-5/ β zeolite+ZSM-5/Y zeolite 50
18 ZSM-5/ mordenite+ZSM-5/ β zeolite+ZSM-5/Y zeolite 100
Under 650 ℃ temperature of reaction, use the coexisting molecular sieve catalyzer of embodiment 7～18, water/petroleum naphtha weight ratio is 1: 1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is under 0.93: 1 the condition, to check and rate above-mentioned catalyzer, and it is listed to obtain data such as table 5.
Table 5
Embodiment Weight space velocity (hour -1) Reaction pressure (MPa) Yield of ethene (weight %) Propene yield (weight %) Total recovery (weight %)
7 0.5 0.35 19.98 23.93 43.91
8 1.0 0.18 16.74 22.41 39.15
9 0.5 0.10 16.43 27.87 44.51
10 1.0 0.12 16.48 27.90 44.38
11 0.5 0.24 15.84 26.38 42.22
12 1.0 0.10 14.64 29.09 43.73
13 0.5 0.49 20.27 25.14 45.41
14 1.0 0.10 21.92 22.36 44.28
15 1.0 0.05 23.22 21.81 45.03
16 1.5 0.08 24.91 19.24 44.15
17 1.0 0.06 26.16 20.20 46.36
18 1.5 0.05 24.41 18.60 43.01
[embodiment 19～30]
With embodiment 1～6, further adjust the material of preparation colloidal sol, obtain different sorts and SiO 2/ Al 2O 3The coexisting molecular sieve of mol ratio is summarized in table 6.
Table 6
Embodiment The coexisting molecular sieve kind SiO 2/Al 2O 3Mol ratio
19 ZSM-5 and mercerization zeolite symbiosis molecular screen 12
20 ZSM-5 and mercerization zeolite symbiosis molecular screen 300
21 ZSM-5/ beta zeolite coexisting molecular sieve 16
22 ZSM-5/ beta zeolite coexisting molecular sieve 300
23 ZSM-5/Y zeolite coexisting molecular sieve 12
24 ZSM-5/Y zeolite coexisting molecular sieve 300
25 ZSM-5/ mordenite+ZSM-5/ β zeolite 12
26 ZSM-5/ mordenite+ZSM-5/ β zeolite 300
27 ZSM-5/ mordenite+ZSM-5/Y zeolite 12
28 ZSM-5/ mordenite+ZSM-5/Y zeolite 300
29 ZSM-5/ mordenite+ZSM-5/ β zeolite+ZSM-5/Y zeolite 16
30 ZSM-5/ mordenite+ZSM-5/ β zeolite+ZSM-5/Y zeolite 300
Under 650 ℃ temperature of reaction, use the coexisting molecular sieve catalyzer of embodiment 19～30, water/petroleum naphtha weight ratio is 1: 1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is under 0.93: 1 the condition, to check and rate above-mentioned catalyzer, and it is listed to obtain data such as table 7.
Table 7
Embodiment Weight space velocity (hour -1) Reaction pressure (MPa) Yield of ethene (weight %) Propene yield (weight %) Total recovery (weight %)
19 0.5 0.32 20.08 20.48 40.56
20 1.0 0.10 16.69 25.38 42.07
21 0.5 0.45 21.75 19.11 40.86
22 1.0 0.12 17.71 24.23 42.94
23 1.0 0.13 17.78 23.20 40.99
24 1.0 0.09 16.55 24.41 40.96
25 1.0 0.24 16.87 22.82 39.65
26 1.0 0.15 20.31 18.78 39.09
27 1.0 0.13 20.05 19.84 39.89
28 1.0 0.10 21.36 18.86 40.23
29 1.5 0.05 22.82 17.64 40.46
30 1.5 0.05 19.81 19.88 39.69
[embodiment 31～40]
Under 650 ℃ temperature of reaction, use ZSM-5 and the mercerization zeolite symbiosis molecular screen catalyzer of embodiment 1, weight space velocity is 1 hour -1, water/petroleum naphtha weight ratio is 2: 1, is 0.14MPa in the gauge pressure reaction pressure, under the condition of bubbling air, changes petroleum naphtha/O in the unstripped gas by changing air flow quantity 2Mol ratio is checked and rated above-mentioned catalyzer, and it is listed to obtain data such as table 8.
Table 8 is at different petroleum naphtha/O 2Each component yield under the mol ratio condition
Figure C20061011853400091
[embodiment 41～47]
Under 650 ℃ temperature of reaction, use ZSM-5 and the mercerization zeolite symbiosis molecular screen catalyzer of embodiment 1, weight space velocity is 1 hour -1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is 0.93: 1, is under the condition of 0.15MPa in the gauge pressure reaction pressure, changes water/petroleum naphtha weight ratio, checks and rates above-mentioned catalyzer, and it is listed to obtain data such as table 9.
Each component yield that table 9 obtains under different water-oil ratio conditions
Figure C20061011853400092
[embodiment 48～52]
Use ZSM-5 and the mercerization zeolite symbiosis molecular screen catalyzer of embodiment 1, weight space velocity is 1 hour -1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is 0.93: 1, is 0.10MPa in the gauge pressure reaction pressure, and water/petroleum naphtha weight ratio is under 2: 1 the condition, changes temperature of reaction, checks and rates above-mentioned catalyzer, and it is listed to obtain data such as table 10.
Each component yield that table 10 obtains under condition of different temperatures
Figure C20061011853400101
[embodiment 53～59]
Under 650 ℃ temperature of reaction, use ZSM-5 and the mercerization zeolite symbiosis molecular screen catalyzer of embodiment 1, weight space velocity is 1 hour -1, feed pure oxygen, petroleum naphtha/O in the unstripped gas 2Mol ratio is 0.93: 1, is 0.12MPa in the gauge pressure reaction pressure, and water/petroleum naphtha weight ratio is under 2: 1 the condition, changes the amount of the nitrogen that feeds, and checks and rates above-mentioned catalyzer, and it is listed to obtain data such as table 11.
Table 11 is in different N 2Each the component yield that obtains under the amount condition
[embodiment 60]
Under 650 ℃ temperature of reaction, use ZSM-5 and the mercerization zeolite symbiosis molecular screen catalyzer of embodiment 1, weight space velocity is 1 hour -1, bubbling air, petroleum naphtha/O in the unstripped gas 2Mol ratio is 0.93: 1, is 0.15MPa in the gauge pressure reaction pressure, and water/petroleum naphtha weight ratio is under 2: 1 the condition, to check and rate above-mentioned catalyzer, obtains data such as table 12 is listed under the different reaction times.
Each component yield that table 12 obtains under different time
Figure C20061011853400111
[comparative example 1]
Under 650 ℃ temperature of reaction, use pure ZSM-5 molecular sieve catalyst, weight space velocity is 1 hour -1, do not feed oxygen-containing gas, be 0.18MPa in the gauge pressure reaction pressure, water/petroleum naphtha weight ratio is under 3: 1 the condition, to check and rate above-mentioned catalyzer, it is listed to obtain data such as table 10.
Table 11 does not feed each component yield that oxygen-containing gas obtains with ZSM-5 under different time

Claims (6)

1, a kind of method of producing ethene and propene by catalytic oxidation cracking naphtha is with C 4～C 10The petroleum naphtha of hydrocarbon is a raw material, and the back and oxygenous gas of raw material hydrocarbon vaporization mixes, and is 580～750 ℃ in temperature of reaction, is 0.05～0.5MPa in the gauge pressure reaction pressure, and weight space velocity is 0.5～3 hour -1, water/petroleum naphtha weight ratio is 0～5: 1, petroleum naphtha/O in the material mixed gas 2Mol ratio is under 0.3～5.0: 1 the condition, and material mixed gas and catalyzer contact reacts generate ethylene, propylene, and wherein catalyst system therefor is selected from least a in ZSM-5/ mercerization zeolite symbiosis molecular screen or the ZSM-5/ beta zeolite coexisting molecular sieve.
2,, it is characterized in that the SiO of coexisting molecular sieve according to the method for the described producing ethene and propene by catalytic oxidation cracking naphtha of claim 1 2/ Al 2O 3Mol ratio is 10～300; Oxygenous gas is the mixed gas of pure oxygen, air or pure oxygen and nitrogen; Temperature of reaction is 600～650 ℃; In the gauge pressure reaction pressure is 0.05～0.15MPa; Weight space velocity is 0.5～1.5 hour-1.
3,, it is characterized in that the SiO of coexisting molecular sieve according to the method for the described producing ethene and propene by catalytic oxidation cracking naphtha of claim 2 2/ Al 2O 3Mol ratio is 20～100.
4, according to the method for the described catalytic oxidative cracking petroleum naphtha of claim 1 production second propylene, it is characterized in that water/petroleum naphtha weight ratio is＞0～3: 1.
5,, it is characterized in that petroleum naphtha/O in the material mixed gas according to the method for the described producing ethene and propene by catalytic oxidation cracking naphtha of claim 1 2Mol ratio is 0.5～3.0: 1.
6, according to the method for the described producing ethene and propene by catalytic oxidation cracking naphtha of claim 1, it is characterized in that containing in the material mixed gas inert nitrogen gas, its amount accounts for 10～80% of volume of gas.
CN200610118534A 2006-11-21 2006-11-21 Method for producing ethene and propene by catalytic oxidation cracking naphtha Active CN100593528C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN200610118534A CN100593528C (en) 2006-11-21 2006-11-21 Method for producing ethene and propene by catalytic oxidation cracking naphtha

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN200610118534A CN100593528C (en) 2006-11-21 2006-11-21 Method for producing ethene and propene by catalytic oxidation cracking naphtha

Publications (2)

Publication Number Publication Date
CN101190865A CN101190865A (en) 2008-06-04
CN100593528C true CN100593528C (en) 2010-03-10

Family

ID=39486085

Family Applications (1)

Application Number Title Priority Date Filing Date
CN200610118534A Active CN100593528C (en) 2006-11-21 2006-11-21 Method for producing ethene and propene by catalytic oxidation cracking naphtha

Country Status (1)

Country Link
CN (1) CN100593528C (en)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102285853A (en) * 2010-06-18 2011-12-21 中国石油化工股份有限公司 Method for increasing yield of propylene and ethylene by using cracked C4 as raw material
CN103087765B (en) * 2011-10-28 2015-09-16 中国石油化工股份有限公司 A kind of production method of low-carbon alkene

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
.石油化工，第35卷第9期. 2006
以乙二胺为模版剂合成Y/ZSM-5复合分子筛. 贾卫等
以乙二胺为模版剂合成Y/ZSM-5复合分子筛. 贾卫等.石油化工，第35卷第9期. 2006 *

Also Published As

Publication number Publication date
CN101190865A (en) 2008-06-04

Similar Documents

Publication Publication Date Title
CN101191069B (en) Method for preparing ethene and propene by naphtha catalysis cracking
EP2364342B1 (en) Catalytic cracking process of a stream of hydrocarbons for maximization of light olefins
CN107418619A (en) A kind of preparation method of aromatic naphtha
CN101279881B (en) Method for preparing ethylene and propylene by benzin naphtha catalytic pyrolysis
CN100554229C (en) The method of naphtha catalytic pyrolysis preparing ethylene propylene
CN103058814B (en) Method for producing aromatic hydrocarbon and olefin from liquefied gas
CN100451089C (en) Method of preparing ethylene, propylene and aromatic hydrocarbons by catalytic cracking gasoline
CN101347746B (en) Catalyst for producing olefin hydrocarbon by catalytic pyrolysis of naphtha
CN101190864B (en) Catalyst for preparing ethene and propene by catalysis cracking
CN101747129A (en) Method for producing light olefins through catalytic conversion
CN100395314C (en) Aromatization catalyst, preparation method, and application
CN100593528C (en) Method for producing ethene and propene by catalytic oxidation cracking naphtha
CN101899324B (en) Catalytic conversion method for producing light diesel oil with high hexadecane value and low olefin gasoline
CN101428233B (en) Catalyst for catalytic pyrolysis
CN107540502A (en) The method that oxygen-containing compound material is catalytically conveted to ethene, propylene and aromatic hydrocarbons
CN109569703B (en) Catalyst for producing gasoline component from naphtha and methanol, preparation method and application
CN1978411B (en) Combined technological low-molecular olefins
CN101279880B (en) Method for preparing ethylene propylene by catalytic pyrolysis of light oil
CN101190417B (en) Catalyst for preparing ethylene and propylene by catalytic cracking method
CN101348408B (en) Method for preparing ethylene and propylene by catalytic pyrolysis of benzin naphtha
KR102321624B1 (en) Catalyst for residue fluid catalytic cracking system having high yielding diesel and preparing method thereof
CN101870632A (en) Method for producing low-carbon olefin
CN101555187B (en) Method for preparing ethylene propylene through white oil catalytic cracking
CN102079992B (en) Catalytic conversion method for producing high-cetane number light diesel oil and low-olefin gasoline
CN103360196B (en) A kind of method by methyl alcohol highly selective preparing propone

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
C14 Grant of patent or utility model
GR01 Patent grant