CN1978409A - Method for preparing propyladehyde raw material by methane oxidation coupling and gas-phase oxidation coupling - Google Patents
Method for preparing propyladehyde raw material by methane oxidation coupling and gas-phase oxidation coupling Download PDFInfo
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- CN1978409A CN1978409A CN 200510022186 CN200510022186A CN1978409A CN 1978409 A CN1978409 A CN 1978409A CN 200510022186 CN200510022186 CN 200510022186 CN 200510022186 A CN200510022186 A CN 200510022186A CN 1978409 A CN1978409 A CN 1978409A
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Abstract
A preparation method of propionaldehyde raw material by oxidative coupling and gaseous oxidative catenation makes two different modes of reaction in one reaction tube to get a mixture of two reaction products, meanwhile, the molar concentration ratio of CO, H2 and C2H4 is near 1:1:1, which can be directly used in the synthesis of propionaldehyde through ethylene hydroformylation.
Description
Technical field:
The present invention relates to the technology that a kind of methane oxidation coupling and gaseous oxidation coupling prepares ethene and synthetic gas simultaneously.
Background technology:
Along with the consumption of oil and the increase year by year of Sweet natural gas proven reserve, significant change has taken place in the world energy sources consumption structure since the eighties in 20th century, and people more and more pay attention to the chemical utilization of Sweet natural gas.Up to the present, methane conversion mainly contains two kinds of approach.A kind of is direct method, and namely for methane obtains required purpose product by single step reaction, as methyl alcohol, formaldehyde and ethene etc.Because the problem of economic benefit, direct method still is in the laboratory study stage at present.
Another kind is the indirect method of present industrial employing, and namely for methane is converted into synthetic gas earlier, uses synthesis gas preparation methyl alcohol then, as: CO+H
2→ CH
3OH, the H of reaction needed
2/ CO ratio is generally 2.Industrial methane preparing synthetic gas is by methane-steam reforming realization, promptly
The shortcoming of this method is H
2/ CO is than the value that is higher than the synthesizing methanol needs, and facility investment is big, the energy consumption height.
Other routes of studying comprise methane carbon dioxide reformation and the methane portion oxidation that uses solid catalyst, and their common problem is that the carbon distribution on the catalyzer is more serious.
Methane oxidation coupling is considered to most promising methane chemical utilization approach.In in the past 20 years, Chinese scholars has been developed the methane oxidation coupling system of being applicable to higher hydrocarbon catalyst for reaction, mainly comprise alkali, alkaline earth, rare earth and variable valence metal oxide, muriate etc., oxysalt and mixture class catalyzer also are the methane oxidative coupling catalysts of excellent property in addition.Chinese patent 91104243.1 has provided the methane oxidative coupling catalyst of a class excellent property, the consisting of of such catalyzer: with SiO
2Or Al
2O
3Be carrier, the compound of the basic metal of at least a tungstenic or phosphorus, alkaline-earth metal or ammonium, at least a can be the metal oxide of higher hydrocarbon with methane conversion.On such catalyzer, obtained C up to 25%
2The hydrocarbon yield.But the problem that exists in the methane oxidation coupling is, ethylene selectivity is low, and its yield is far from reaching industrialization demands.
Publication number at us is in the patent of CN1559674A, proposed a kind of under the oxygen existence condition methane and carbonic acid gas co-activating produce the method for ethene and synthetic gas simultaneously, purpose is to obtain containing CO/H
2/ C
2H
4The product mixed air of mol ratio=1: 1: 1, this mixed air can be used for the raw material of the synthetic propionic aldehyde of ethene carbonylation.The problem that exists is CO
2Transformation efficiency is low, and the ethene volumetric molar concentration is lower than CO and H in the product
2Concentration.
Propionic aldehyde is a kind of important Organic Chemicals, is widely used in fields such as rubber, plastics, coating, medicine, agricultural chemicals and foodstuff additive, is mainly used in to produce propionic acid and propyl alcohol, and market is widely used.The present domestic propionic aldehyde that has only minimum scale or other product by-products, required main dependence on import.The synthetic propionic aldehyde technology of the independently developed second hydroformylation of China has reached the level of external same device.Reaction has catalytic activity preferably to rhodium phosphine complex catalyzer described in Chinese patent CN1168129A and CN1125712 to ethene hydroformylation; and publication number has used a kind of water miscible using rhodium complex catalysts for the CN1434015A patent; make ethene hydroformylation be reflected in the two-phase system and carry out, solved separating and problem such as poisoning of catalyst inactivation of product and catalyzer.Technology that we can say the synthetic propionic aldehyde of ethene hydroformylation is comparatively ripe.
Goal of the invention:
Coupling process by methane oxidation coupling and gaseous oxidation prepares ethene and synthetic gas simultaneously, is the ethene hydroformylation system propionic aldehyde gas of directly supplying raw materials; Overcome the deficiencies in the prior art, improve the selectivity of methane conversion and target product.
Technical scheme:
With pack into the middle part of crystal reaction tube of 0.05～1g methane oxidative coupling catalyst, the quartz sand that is used for regulating the gas phase dead volume is equipped with at the catalytic bed two ends, and its volume is 1～5mL, with electric tube furnace (4 in the respective figure) system is heated; (750～850 ℃) changed logical unstripped gas when system was warming up to temperature of reaction in argon gas stream, and kept homo(io)thermism, unstripped gas consist of CH
4/ O
2=2～5 (volume ratios), overall flow rate are 60～180mL/min; Behind the stable reaction 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Methane conversion is 5%～25%, target product CO and C
2H
4Overall selectivity reach 50%～80%.
Methane oxidative coupling catalyst used in the present invention can be that the patent No. is any catalyzer described in 91104243.1, and such catalyzer is with SiO
2Or Al
2O
3Be carrier, the compound of the basic metal of at least a tungstenic or phosphorus, alkaline-earth metal or ammonium, at least a can be the metal oxide of higher hydrocarbon with methane conversion, as: Mn2Wt%-Na
2WO
44Wt%/SiO
2, Mn2Wt%-Na
2WO
44Wt%/TiO
2Or Zn2Wt%-Na
2WO
44Wt%SiO
2Or other disclosed OCM (methane oxidation coupling) catalyzer with better catalyst performance.
The employed atmosphere of reaction system temperature-rise period can be rare gas element, air or oxygen.
Methane gas is pure methane gas or methane-rich gas (Sweet natural gas, oil field gas and refinery gas etc.) among the present invention.
The relative proportion that changes among the present invention between methane gas phase free-radical oxidn and the oxidative coupling is to realize by the size that changes catalyst consumption and gas phase dead volume.
The adjusting that product is formed among the present invention also can recently realize by changing temperature of reaction, the overall flow rate of unstripped gas and the alcoxyl of unstripped gas.
Description of drawings:
Crystal reaction tube used in the present invention as shown in drawings, below in conjunction with accompanying drawing invention is further described: electric tube furnace (4 in the accompanying drawing) constant temperature head of district 12cm, use temperature scope≤1000 ℃, programmed temperature control instrument carries out temperature control by thermopair to it, can realize temperature programming.Quartz reaction bore 1.2cm, long 70cm.The quartz inner pipe diameter is 0.8cm, wherein is inserted with the temperature that a thermopair is used for measuring catalytic bed.Unstripped gas (CH
4And O
2Gas mixture) 1 position feeds from accompanying drawing, the methane gas phase oxidation takes place in 2 position in the accompanying drawings, then passes through methane oxidative coupling catalyst bed (in the accompanying drawing 3), and oxidative coupling of methane takes place, reacted gas mixture is derived through side pipe.
The invention effect:
Compared with the prior art, the present invention has following characteristics and advantage:
1. the reaction of two kinds of different modes is coupled, and occurs in same reaction tube, can obtain the product mixtures of two kinds of reactions, and regulates the composition that two kinds of relative scales between the reaction are regulated product. That is: the oxidative coupling reaction of methane then through the methane oxidative coupling catalyst bed, occurs at the methane gas phase free-radical oxidation of the upstream of catalyst generation by dynamics Controlling in the reaction gas that contains methane, oxygen.
2. the coupling of two kinds of differential responses modes makes ethene in the gained product, the molar concentration approximately equal of carbon monoxide and hydrogen, the gained gaseous mixture can be directly used in the process by ethene hydroformylation propionic aldehyde processed described in the patent that publication number is CN1434015A without separation, has removed process and the expense of product separation from.
C
2H
4+CO+H
2→CH
3CH
2CHO
3. compare with simple oxidative coupling of methane, this enabling objective product increases, and has improved total target selection. The overall selectivity of target product is 50%～80% among the present invention, selective far above target product ethene in the methane oxidation coupling process.
4. the reaction of two kinds of different modes is carried out in same reaction tube, and reaction unit is oversimplified.
Below by embodiment in detail the present invention is described in detail.
Embodiment 1
With 0.2g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.2: 1: 1.1 a product gas mixture, and methane conversion is 21.4%, target product CO+C
2H
4Overall selectivity be 62.1%.
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 3mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 4.5, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 0.9: 1: 1.1 a product gas mixture, and methane conversion is 10.6%, target product CO+C
2H
4Overall selectivity be 56.2%.
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 150mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.0: 1: 0.9 a product gas mixture, and methane conversion is 19.9%, target product CO+C
2H
4Overall selectivity be 68.3%.
Embodiment 4
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 180mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.1: 1: 0.8 a product gas mixture, and methane conversion is 19.1%, target product CO+C
2H
4Overall selectivity be 72.3%.
With 0.15g methane oxidative coupling catalyst (Zn2Wt%-Na
2WO
44Wt%/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 2.1: 1: 1.2 a product gas mixture, and methane conversion is 13.5%, target product CO+C
2H
4Overall selectivity be 69.8%.
Embodiment 6
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%/TiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.4: 1: 1.1 a product gas mixture, and methane conversion is 16.6%, target product CO+C
2H
4Overall selectivity be 62.9%.
Embodiment 7
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 750 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 4.5, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.3: 1: 0.4 a product gas mixture, and methane conversion is 5.02%, target product CO+C
2H
4Overall selectivity be 64.4%.
Embodiment 8
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 850 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 4.5, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.5: 1: 1.5 a product gas mixture, and methane conversion is 22.8%, target product CO+C
2H
4Overall selectivity be 68.3%.
Embodiment 9
With 0.15g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 60mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 2.2: 1: 0.7 a product gas mixture, and methane conversion is 19.6%, target product CO+C
2H
4Overall selectivity be 70.6%.
Embodiment 10
With 0.05g methane oxidative coupling catalyst (Mn2Wt%-Na
2WO
44Wt%/SiO
2) being contained in the mid-way of reaction tubes, the quartz sand of 1mL is equipped with at the two ends of catalytic bed, rises to 800 ℃ in argon gas, changes into to contain CH
4/ O
2Than the unstripped gas that is 3, the overall flow rate of unstripped gas is 120mL/min.After stablizing 30min, with the composition of gas mixture after the Agilent GC1790 detection reaction.Obtained containing CO/H
2/ C
2H
4Mol ratio is 1.3: 1: 0.4 a product gas mixture, and methane conversion is 17.9%, target product CO+C
2H
4Overall selectivity be 79.0%.
Reaction result is compared in tabulation below:
| Embodiment number | Methane conversion | CO+C 2H 4Selectivity | CO+C 2H 4Yield | CO/H 2/C 2H 4Mol ratio | C 2H 4/C 2H 6Mol ratio |
| 1 | 21.4 | 62.1 | 13.3 | 1.2∶1∶1.1 | 3.1 |
| 2 | 10.6 | 56.2 | 6.0 | 0.9∶1∶1.1 | 1.6 |
| 3 | 19.9 | 68.3 | 13.6 | 1.0∶1∶0.9 | 3.4 |
| 4 | 19.1 | 72.3 | 13.8 | 1.1∶1∶0.8 | 4.9 |
| 5 | 13.5 | 69.8 | 9.4 | 2.1∶1∶1.2 | 2.0 |
| 6 | 16.6 | 62.9 | 10.4 | 1.4∶1∶1.1 | 2.2 |
| 7 | 5.0 | 64.4 | 3.2 | 1.3∶1∶0.4 | ∞ |
| 8 | 22.8 | 68.3 | 15.6 | 1.5∶1∶1.5 | 4.0 |
| 9 | 19.6 | 70.6 | 13.8 | 2.2∶1∶0.7 | 3.0 |
| 10 | 17.9 | 79.0 | 14.1 | 1.3∶1∶0.4 | 6.1 |
Claims (4)
1. method of producing the propionic aldehyde raw material by methane oxidation coupling and gaseous oxidation coupling, be to use methane oxidative coupling catalyst, its characteristics are pack into the middle part of crystal reaction tube with methane oxidative coupling catalyst 0.05～1g, adorn the quartz sand of 1～5mL at the catalytic bed two ends, feed argon gas, be warming up to 750～850 ℃, convert reactor feed gas to, feed gas volume is than being CH
4/ O
2=2～5, flow velocity is 60～180mL/min, and temperature of reaction is 750～850 ℃, and reaction product is formed the detection by Agilent GC1790, and methane conversion is 5%～25%, target product CO and C
2H
4Overall selectivity reach 50～80%.
2. by the described method of claim 1, it is characterized in that used methane oxidative coupling catalyst is: Mn2Wt%-Na
2WO
44Wt%/SiO
2, Mn2Wt%-Na
2WO
44Wt%/TiO
2Or Zn2Wt%-Na
2WO
44Wt%/SiO
2
3. by the described method of claim 1, it is characterized in that the volume ratio CH of unstripped gas
4/ O
2=3～4.5.
4. by the described method of claim 1, it is characterized in that temperature of reaction is at 800～850 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100221861A CN100551884C (en) | 2005-12-02 | 2005-12-02 | A kind of method of producing the propionic aldehyde raw material by methane oxidation coupling and gaseous oxidation coupling |
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|---|---|---|---|
| CNB2005100221861A CN100551884C (en) | 2005-12-02 | 2005-12-02 | A kind of method of producing the propionic aldehyde raw material by methane oxidation coupling and gaseous oxidation coupling |
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| Publication Number | Publication Date |
|---|---|
| CN1978409A true CN1978409A (en) | 2007-06-13 |
| CN100551884C CN100551884C (en) | 2009-10-21 |
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|---|---|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010133461A1 (en) * | 2009-05-20 | 2010-11-25 | Basf Se | System and method for producing superior hydrocarbons from methane |
| CN102093157A (en) * | 2009-12-09 | 2011-06-15 | 中国科学院兰州化学物理研究所 | Joint process for preparing ethylene and synthesis gas by direct conversion of methane |
| CN106278786A (en) * | 2015-05-21 | 2017-01-04 | 中国科学院大连化学物理研究所 | A kind of alkane and CO2the method producing hydroformylation raw material |
| CN109311666A (en) * | 2016-06-30 | 2019-02-05 | 陶氏环球技术有限责任公司 | The technique for converting propionic aldehyde for methane |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20170060067A (en) * | 2014-12-09 | 2017-05-31 | 사빅 글로벌 테크놀러지스 비.브이. | Methods of producing ethylene and synthesis gas by combining the oxidative coupling of methane and dry reforming of methane reactions |
| CN106986736B (en) * | 2016-01-21 | 2019-06-25 | 中国石化工程建设有限公司 | A kind of hydrocarbon production technique and hydrocarbon production device |
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2005
- 2005-12-02 CN CNB2005100221861A patent/CN100551884C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2010133461A1 (en) * | 2009-05-20 | 2010-11-25 | Basf Se | System and method for producing superior hydrocarbons from methane |
| CN102093157A (en) * | 2009-12-09 | 2011-06-15 | 中国科学院兰州化学物理研究所 | Joint process for preparing ethylene and synthesis gas by direct conversion of methane |
| CN106278786A (en) * | 2015-05-21 | 2017-01-04 | 中国科学院大连化学物理研究所 | A kind of alkane and CO2the method producing hydroformylation raw material |
| CN106278786B (en) * | 2015-05-21 | 2019-08-06 | 中国科学院大连化学物理研究所 | A kind of alkane and CO2The method for producing hydroformylation raw material |
| CN109311666A (en) * | 2016-06-30 | 2019-02-05 | 陶氏环球技术有限责任公司 | The technique for converting propionic aldehyde for methane |
| CN109311666B (en) * | 2016-06-30 | 2022-07-19 | 陶氏环球技术有限责任公司 | Process for converting methane to propanal |
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|---|---|
| CN100551884C (en) | 2009-10-21 |
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Assignee: Sichuan Shenlian Biotech Co.,Ltd. Assignor: Sichuan University Contract fulfillment period: 2009.10.30 to 2014.10.30 contract change Contract record no.: 2009510000156 Denomination of invention: Method for preparing propyladehyde raw material by methane oxidation coupling and gas-phase oxidation coupling Granted publication date: 20091021 License type: Exclusive license Record date: 20091116 |
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