CN1915509A - Catalyst of fluid bed for preparing ethane and propylene through catalytic cracking - Google Patents

Catalyst of fluid bed for preparing ethane and propylene through catalytic cracking Download PDF

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Publication number
CN1915509A
CN1915509A CNA2005100287958A CN200510028795A CN1915509A CN 1915509 A CN1915509 A CN 1915509A CN A2005100287958 A CNA2005100287958 A CN A2005100287958A CN 200510028795 A CN200510028795 A CN 200510028795A CN 1915509 A CN1915509 A CN 1915509A
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China
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catalyst
span
propylene
grams
catalytic pyrolysis
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CNA2005100287958A
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CN100430134C (en
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姚晖
谢在库
马广伟
肖景娴
陈亮
杨为民
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
China Petrochemical Corp
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Priority to CNB2005100287958A priority Critical patent/CN100430134C/en
Priority to KR1020060076882A priority patent/KR101270191B1/en
Priority to JP2006221462A priority patent/JP5465822B2/en
Priority to US11/503,925 priority patent/US20070042904A1/en
Publication of CN1915509A publication Critical patent/CN1915509A/en
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Publication of CN100430134C publication Critical patent/CN100430134C/en
Priority to US12/365,146 priority patent/US7686942B2/en
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    • 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

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Abstract

A catalyst for preparing ethene and propene by catalytic cracking of petroleum naphtha on fluidized bed is composed of the carrier chosen from SiO2, Al2O3 and their mixture and the active component Mo1.0VaPbAcBdOx. It has high low-temp activity, selectivity and low reaction temp.

Description

The fluid catalyst of preparing ethylene propylene from catalytic pyrolysis
Technical field
The present invention relates to a kind of fluid catalyst of preparing ethylene propylene from catalytic pyrolysis.
Background technology
The main method of preparing ethylene and propylene is the steam heat cracking at present.Maximum raw material that adopts is a naphtha.But the steam heat cracking naphtha exists the reaction temperature height, and the process conditions harshness requires height, the shortcoming that loss is big to equipment especially furnace tube material.Seek a kind of suitable catalyst for cracking, overcome above-mentioned shortcoming, more and more become the problem that people are concerned about.
It is active component that the patent US4620051 of U.S. Phillips company and US4705769 have adopted with manganese oxide or iron oxide, has added rare-earth elements La, and the oxide catalyst of alkaline-earth metal Mg, cracking C 3, C 4Raw material.Mn, Mg/Al 2O 3Catalyst is in breadboard fixed bed reactors, and 700 ℃, the mol ratio of water and butane is 1: 1, and the conversion ratio of butane can reach 80%, ethene, and the selectivity of propylene is 34% and 20%.These two patents are claimed also can use naphtha and fluidized-bed reactor.
It is 12CaO7Al that the patent CN1317546A of Italy En Niqiemu company relates to chemical formula 2O 3The steam cracking reaction catalyst.Raw material can be used naphtha, 720～800 ℃ of operating temperatures, and under 1.1～1.8 atmospheric pressure, 0.07～0.2 second time of contact, the productive rate of ethene and propylene can reach 43%.
The patent USSR Pat1298240.1987 of the former Soviet Union Zr that is carried on float stone or the pottery 2O 3, air speed is 2-5 hour on 660～780 ℃ of middle-scale devices of temperature -1, water/naphtha weight ratio 1: 1.With n-alkane C 7～17, cyclohexane, direct steaming gasoline are raw material, ethylene yield can reach 46%, propylene 8.8%.
Chinese patent CN1480255A introduces a kind of oxide catalyst, is raw material with naphtha, and at 780 ℃ of following preparing ethylene propylene from catalytic pyrolysis, the diene yield can reach 47%.
In sum, existing preparing ethylene propylene from catalytic pyrolysis technology, reaction temperature is higher, but that the ethylene, propylene yield increases is not obvious.
Summary of the invention
Technical problem to be solved by this invention is to overcome existing catalytic pyrolysis technology to have the reaction temperature height, and active down not high, the problem that selectivity is bad of catalyst system therefor low temperature provides a kind of fluid catalyst of new preparing ethylene propylene from catalytic pyrolysis.It is low to use this catalyst to have reaction temperature, and the catalyst activity is good, the advantage that the ethylene, propylene selectivity is good.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of fluid catalyst of preparing ethylene propylene from catalytic pyrolysis, contain and be selected from SiO 2, Al 2O 3Or the carrier of its mixture and with the following composition of atomic ratio measuring chemical formula:
Mo 1.0V aP bA cB dO x
A is selected from least a in the rare earth element in the formula;
B is selected from least a element among VIII, IB, IIB, VIIB, VIB, IA or the IIA;
The span of a is 0.01～0.5;
The span of b is 0.01～0.5;
The span of c is 0.01～0.5;
The span of d is 0.01～0.5;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein the catalyst carrier consumption is 20～80% of catalyst weight by weight percentage.
In the technique scheme, the value preferable range of a is 0.01～0.3; The value preferable range of b is 0.01～0.3; The value preferable range of c is 0.01～0.3; The value preferable range of d is 0.01～0.3.VIII family element preferred version is to be selected from least a among Fe, Co or the Ni; IB family element preferred version is to be selected from least a among Cu or the Ag; IIB family element preferred version is for being selected from Zn; IA family element preferred version is to be selected from least a among Li, Na or the K; IIA element preferred version is to be selected from least a among Ca, Mg, Sr or the Ba.The rare earth element preferred version is to be selected from least a among La or the Ce; Catalyst carrier consumption preferable range by weight percentage is 30～50% of a catalyst weight.
Preparation of catalysts method of the present invention is as follows: the raw material that used Mo element adopts is ammonium molybdate or phosphomolybdic acid; What V element was used is ammonium metavanadate or vanadic anhydride; What component A used is corresponding nitrate, oxalates or oxide; What B component was used is corresponding nitrate, oxalates, acetate or soluble halide; Used P elements derives from phosphoric acid, triammonium phosphate, diammonium hydrogen phosphate, ammonium dihydrogen phosphate (ADP).To be the slurries that will add each component element and carrier carry out spray-drying adding hot reflux in 70～80 ℃ the water-bath to the forming mode of preparation catalyst after 5 hours.The powder that obtains roasting in muffle furnace, temperature are 600～750 ℃, and roasting time is 3～10 hours.
The present invention is owing to adopted a series of transition metal and rare earth metals that cryogenic absorption, oxidation-reduction quality and difunctional soda acid position cooperate that have, and it has stronger low temperature active, raw material is played the effect of oxidation catalysis.Under 600～650 ℃ of relatively low temperature conditions, catalyst is used for the naphtha catalytic cracking reaction, makes the diene yield can reach 44.76%, obtains better technical effect.
Catalyst involved in the present invention has adopted above-mentioned preparation method.In order to check and rate activity of such catalysts, be raw material with naphtha (specific targets see Table 1), range of reaction temperature is 580～650 ℃.Catalyst loading is 0.5～2 gram naphtha/gram catalyst hour, and water/naphtha weight ratio is 0.5～3: 1.The internal diameter of fluidized-bed reactor is 39 millimeters, reaction pressure 0.15MPa.The product of obtaining (ethylene, propylene) yield height, selectivity is good.
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) 65.2
N-alkane % 32.5
Cycloalkane % 28.4
Alkene % (weight) 0.17
Aromatic hydrocarbons % (weight) 6.2
The invention will be further elaborated below by embodiment.
The specific embodiment
[embodiment 1]
Get 3 gram ammonium metavanadates, add 100 ml waters, splash into 2 milliliter 80% phosphoric acid, add oxalic acid 3 grams, be heated to the ammonium metavanadate dissolving, obtain solution (I).
Get ammonium molybdate 30 grams again, ferric nitrate 7.61 grams, chromic nitrate 10.88 grams, lanthanum nitrate 4.08 grams are dissolved in them in 250 ml waters together, obtain solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
(I) pours (II) into solution, places in 70～80 ℃ of water-baths to heat, and adds silica 30 grams that weigh up, aluminium oxide 3 grams.Refluxed 5 hours, and used the spray dryer dry forming again.
Behind the powder sieving with gained, place muffle furnace to be warming up to 740 ℃, calcination 5 hours.After the cooling, in mortar,, cross 100 mesh sieves with the catalyst pulverize.
The catalyst chemical formula that obtains is: Mo 1.0V 0.15P 0.10Fe 0.11Cr 0.16La 0.06O x+ 34.1% carrier
Carry out the catalyst activity evaluation under the following conditions:
The fluidized-bed reactor of 39 millimeters internal diameters, 650 ℃ of reaction temperatures, pressure 0.15MPa.Water/naphtha weight ratio 3: 1, catalyst loading amount are 20 grams, and load is 1 gram naphtha/gram catalyst hour.Collect gaseous product, carry out gas chromatographic analysis, product distributes and sees Table 2.
The main gas-phase product of table 2 distributes and the diene productive rate
Product Content (H 2Volume %, all the other weight %)
Hydrogen (volume %) 16.5
Methane 14.5
Ethane 2.20
Ethene 32.19
Propane 0.486
Propylene 15.59
C 4 3.33
Other 15.20
Conversion ratio 85.53
Yield of ethene 30.09
Propene yield 14.58
The diene yield 44.67
[embodiment 2]
Make solution (I) with embodiment 1.
Other gets 30 gram ammonium molybdates, ferric nitrate 7.61 grams, and zinc nitrate 5.88 grams, cerous nitrate 5.60 grams are dissolved in 250 ml waters, get solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
The catalyst chemical formula that obtains is: Mo 1.0V 0.15P 0.10Fe 0.11Zn 0.12Ce 0.08O x+ 37.8% carrier
Catalyst is investigated condition with embodiment 1, and the product that obtains distributes and the diene yield sees Table 3.
The gas-phase product of table 3 embodiment 2 distributes and the diene productive rate
Product Content (H 2Volume %, all the other weight %)
Hydrogen (volume %) 16.08
Methane 14.56
Ethane 2.11
Ethene 32.34
Propane 0.43
Propylene 15.08
C 4 6.41
Other 12.99
Conversion ratio 83.63
Yield of ethene 30.53
Propene yield 14.23
The diene yield 44.76
[embodiment 3]
Make solution (I) with embodiment 1.
Other gets 30 and restrains ammonium molybdates, ferric nitrate 7.61 grams, and nickel nitrate 7.29 grams, lanthanum nitrate 5.60 grams, calcium nitrate 5.18 grams are dissolved in 250 ml waters, get solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
Obtaining the catalyst chemical formula is: Mo 1.0V 0.15P 0.10Fe 0.11Ni 0.15Ca 0.13La 0.08O x+ 35.1% carrier
Catalyst is investigated condition with embodiment 1, the product yield that obtains, and ethene: 25.77%, propylene: 15.29%, diene: 41.06%.
[embodiment 4]
Make solution (I) with embodiment 1.
Other gets 30 and restrains ammonium molybdates, ferric nitrate 7.61 grams, and nickel nitrate 7.29 grams, cerous nitrate 5.44 grams, copper nitrate 6.30 grams are dissolved in 250 ml waters, get solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
Obtaining the catalyst chemical formula is: Mo 1.0V 0.15P 0.10Fe 0.11Ni 0.15Cu 0.15Ce 0.07O x+ 35.3% carrier
Catalyst is investigated condition with embodiment 1, the product yield that obtains, and ethene: 29.02%, propylene: 12.40%, diene: 41.43%.
[embodiment 5]
Make solution (I) with embodiment 1.
Other gets 30 and restrains ammonium molybdates, cobalt nitrate 5.49 grams, and zinc nitrate 5.60 grams, cerous nitrate 5.44 grams, potassium nitrate 1.10 grams are dissolved in 250 ml waters, get solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
The catalyst chemical formula that obtains is: Mo 1.0V 0.15P 0.10Co 0.11Zn 0.11K 0.06Ce 0.07O x+ 37.3% carrier
Catalyst is investigated condition with embodiment 1, the product yield that obtains, and ethene: 36.74%, propylene: 7.17%, diene: 43.91%.
[embodiment 6]
Make solution (I) with embodiment 1.
Other gets 30 and restrains phosphomolybdic acids, cobalt nitrate 5.49 grams, and nickel nitrate 5.32 grams, cerous nitrate 5.44 grams, 50% manganese nitrate solution 10.81 grams are dissolved in 250 ml waters, get solution (II).Dissolving 2.24 gram diammonium hydrogen phosphates are poured into solution (II) in 100 ml waters, have precipitation and generate.
Obtaining the catalyst chemical formula is: Mo 1.0V 0.13P 0.17Co 0.1Ni 0.1Mn 0.16Ce 0.07O x+ 35.6% carrier
Catalyst is investigated condition with embodiment 1, the product yield that obtains, and ethene: 36.00%, propylene: 5.47%, diene: 41.47%.

Claims (5)

1, a kind of fluid catalyst of preparing ethylene propylene from catalytic pyrolysis contains and is selected from SiO 2, Al 2O 3Or the carrier of its mixture and with the following composition of atomic ratio measuring chemical formula:
Mo 1.0V aP bA cB dO x
A is selected from least a in the rare earth element in the formula;
B is selected from least a element among VIII, IB, IIB, VIIB, VIB, IA or the IIA;
The span of a is 0.01～0.5;
The span of b is 0.01～0.5;
The span of c is 0.01～0.5;
The span of d is 0.01～0.5;
X satisfies the required oxygen atom sum of each element valence in the catalyst;
Wherein the catalyst carrier consumption is 20～80% of catalyst weight by weight percentage.
2, according to the fluid catalyst of the described preparing ethylene propylene from catalytic pyrolysis of claim 1, the span that it is characterized in that a is 0.01～0.3, and the span of b is 0.01～0.3, and the span of c is 0.01～0.3, and the span of d is 0.01～0.3.
3,, it is characterized in that VIII family element is selected from least a among Fe, Co or the Ni according to the fluid catalyst of the described preparing ethylene propylene from catalytic pyrolysis of claim 1; IB family element is selected from least a among Cu or the Ag; IIB family element is selected from Zn; IA family element is selected from least a among Li, Na or the K; The IIA element is selected from least a among Ca, Mg, Sr or the Ba.
4,, it is characterized in that rare earth element is selected from least a among La or the Ce according to the fluid catalyst of the described preparing ethylene propylene from catalytic pyrolysis of claim 1.
5,, it is characterized in that the catalyst carrier consumption is 30～50% of catalyst weight by weight percentage according to the fluid catalyst of the described preparing ethylene propylene from catalytic pyrolysis of claim 1.
CNB2005100287958A 2005-08-15 2005-08-15 Catalyst of fluid bed for preparing ethane and propylene through catalytic cracking Active CN100430134C (en)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CNB2005100287958A CN100430134C (en) 2005-08-15 2005-08-15 Catalyst of fluid bed for preparing ethane and propylene through catalytic cracking
KR1020060076882A KR101270191B1 (en) 2005-08-15 2006-08-14 Method for preparation of ethylene and propylene by catalytic cracking using a fluid-bed catalyst
JP2006221462A JP5465822B2 (en) 2005-08-15 2006-08-15 Fluidized bed catalysts for the production of ethylene and propylene by catalytic cracking.
US11/503,925 US20070042904A1 (en) 2005-08-15 2006-08-15 Fluid-bed catalyst for the preparation of ethylene and propylene by catalytic cracking
US12/365,146 US7686942B2 (en) 2005-08-15 2009-02-03 Method for preparation of ethylene and propylene by catalytic cracking using a fluid-bed catalyst

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CN100430134C CN100430134C (en) 2008-11-05

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112322333A (en) * 2020-10-21 2021-02-05 中国石油大学(北京) Alkane-alkene co-cracking catalyst and alkane-alkene mixed catalytic cracking method

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4621162A (en) * 1985-07-25 1986-11-04 Phillips Petroleum Company Method for conversion of C3 and C4 hydrocarbons to olefinic products
CN1055285C (en) * 1997-12-11 2000-08-09 中国石油化工总公司 Catalyst for propylene and isobutylene ammoxidation fluidized bed

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112322333A (en) * 2020-10-21 2021-02-05 中国石油大学(北京) Alkane-alkene co-cracking catalyst and alkane-alkene mixed catalytic cracking method

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