CN102553600A - Method for preparing methane from synthesis gas and coproducing low-carbon mixed alcohol - Google Patents
Method for preparing methane from synthesis gas and coproducing low-carbon mixed alcohol Download PDFInfo
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- CN102553600A CN102553600A CN2010106138002A CN201010613800A CN102553600A CN 102553600 A CN102553600 A CN 102553600A CN 2010106138002 A CN2010106138002 A CN 2010106138002A CN 201010613800 A CN201010613800 A CN 201010613800A CN 102553600 A CN102553600 A CN 102553600A
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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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
Abstract
The invention discloses a catalyst for use in a reaction for preparing methane from synthesis gas and coproducing a low-carbon mixed alcohol, preparation thereof and a process for synthesizing methanol and coproducing a mixed alcohol. The catalyst consists of CuCoMAO/C or CuCoMAZnO/C, wherein M is Zn, Cr, Fe, V or Mn; A is an alkali metal or an alkaline-earth metal aid; and C is a carrier which comprises aluminium sesquioxide Al2O3, zirconium oxide ZrO, silicon dioxide SiO2 or titanium oxide TiO2. The content of copper oxide is 1-90 percent by weight of the total weight of the catalyst; the content of oxidized Co is 1-95 percent by weight of the total weight of the catalyst; the content of M oxide is 1-90 percent by weight of the total weight of the catalyst; and the content of the A oxide is 0.01-25 percent by weight of the total weight of the catalyst. A preparation process of the catalyst comprises the following steps of: soaking onto the carrier at an equal volume according to a certain sequence with a soaking method; drying at the temperature of 110 DEG C; and baking to obtain the catalyst. The synthesis gas is taken as a raw material, has a wide source, and can be obtained from coal and biomass. The catalyst has low cost and very high efficiency, and is easy to prepare; and a product can be adjusted as required, and is suitable for continuous large-scale production.
Description
Technical field
The invention belongs to the catalytic chemistry field, relate to synthesis gas and transform system methane, and the coproduction MAS, a kind of catalyst, Preparation of catalysts and application thereof that is used for low temperature synthesizing methane and coproduction MAS is provided especially.
Background technology
Enforcement along with policies such as the domestic strategy of sustainable development and reinforcement environmental protection; Domestic demand to natural gas increases substantially; Domestic gas production can not be met the need of market fully; Imbalance between supply and demand is outstanding, therefore must be by all kinds of means, multimode enlarges resource provision, satisfies the growing market demand.Be based on the rich coal energy resource structure of China's oil starvation weak breath characteristics simultaneously, development coal preparing natural gas is one of feasible mode.In the process that coal transforms, the energy efficiency of coal preparing natural gas is the highest coal utilization mode, reaches 53%, not only can significantly reduce the consumption of coal, has also reduced SO simultaneously
2, CO
2Discharging, the pollution that alleviates environment.In addition, the coal preparing natural gas can be carried through pipeline on a large scale, has increased its transportation and the security of using.
With gas reforming is that methane (synthetic natural gas) is a mature technology, and 1 ton of coal can be converted into 400m
3Synthetic natural gas, ripe at present technology has Top's rope methanation circulation technology (TREMPTM) technology, DAVY company methanation technology (CRG).Also there are ripe methanation technology in BASF AG and LURGI.Domestic comparatively familiar to methanation technology.
Whether at present, carrying out preparing methane from coal on a large scale has good economic benefit, is still waiting the actual production checking.The preparing methane from coal industry has characteristics such as investment has a big risk greatly.If can realize that coal preparing natural gas and other are raw material with coal,, can increase the ability to ward off risks of coal preparing natural gas project through the coproduction of the multiple Coal Chemical Industry product of synthesis gas system.Realize coal preparing natural gas and coal system methyl alcohol, coal system alkene, coal system oil, the coproduction of multiple coal-based product such as synthetic ammonia will realize that multiple coal-based product advantage is complementary, effectively improves the economic benefit and whole opposing risk ability of coal preparing natural gas project.In addition, China's gas very unbalanced with gas, northern area consumption in winter is big, and it is few that non-heating season is saved gas, and peaking problem is very serious.Except adopting peak regulation means such as underground natural gas storage tank, gas peak regulation generating or LNG, also can carry out peak regulation with coal preparing natural gas factory, that is to say that coal preparing natural gas factory produces natural gas winter; Other seasons can coproduction part methyl alcohol, oil, alkene; MAS, products such as synthetic ammonia.
To coal through synthesis gas system methane, and coproduction alcohol, oil, alkene, MAS, the research and development of catalyst of synthetic ammonia and technology have very big practicality and application prospect.
Summary of the invention
The object of the present invention is to provide a kind of preparing methane by synthetic gas and coproduction low carbon mixed alcohol catalyst, its technology of preparing and application.
The present invention goes back coproduction part MAS except synthesis gas changes into methane, prior art then is converted into methane to synthesis gas fully, and to be converted into target fully, this is maximum difference that copper cobalt-base catalyst provided by the invention and prior art exist.
Synthesis gas through the reactor reaction of catalyst is housed, is prepared methane and coproduction MAS; Catalyst consists of CuCoMA/C,
Wherein:
Active component Cu, in metallic element, the content in catalyst is 1.0-90.0wt%;
Active component Co, in metallic element, the content in catalyst is 1.0-90.0wt%;
Component M is an auxiliary agent, is any one or any several kinds mixing among Zn, Cr, Fe, V, the Mn, and in metallic element, its content in catalyst is 0.0-90.0wt%;
Component A is an auxiliary agent, is any one or a few mixing among Li, Na, K, Mg, Ca, Sr, the Ba, and in metallic element, its content in catalyst is 0.0-25.0wt%;
Carrier component C is Al
2O
3, ZrO, SiO
2, TiO
2In any one or a few combination, its content in catalyst is 10.0-95.0wt%.
The present invention utilizes above-mentioned catalyst to carry out the reaction of preparing methane by synthetic gas and coproduction MAS, and its reaction temperature T is 200≤T≤400 ℃, and reaction pressure P is 0.5≤P≤10.0MPa, and reaction volume air speed LHSV is 1000≤LHSV≤40000h
-1
Use hydrogen before the catalyst reaction according to the invention, or the hydrogen of inert gas dilution, or the synthesis gas reduction, react then.
The hydrogen of reaction raw materials synthesis gas according to the invention and carbon monoxide are than being H
2/ CO=2-8.
Activity of such catalysts component copper according to the invention is 20.0-50.0wt% in the content of metallic element in catalyst, and cobalt is 5.0-20.0wt% in the content of metallic element in catalyst.
The auxiliary agent M of catalyst according to the invention is that Mn and/or the content of Fe in catalyst are 1.0-15wt%.
The content of the auxiliary agent A of catalyst according to the invention in catalyst is 0.01-5.0wt%
Auxiliary agent Zn in the catalyst according to the invention is being 5.0～20.0wt% with the content of metallic element in catalyst.
The content of the carrier of catalyst according to the invention in catalyst is 60.0-75wt%.
Preparation of catalysts according to the invention adopts infusion process, and step is following:
A) by the weight ratio of each component in the said catalyst, carrier component C carried out 1～10 hour roasting purified treatment in 400～700 ℃ temperature after, cooling;
B) with the aqueous solution that contains copper, cobalt, said component A and component M metal ion step a) gained sample is carried out incipient impregnation, flooded 2～12 hours;
C) with the sample behind the step b) gained dipping through 60～90 ℃ of evaporates to dryness, 100～150 ℃ of dryings, 400-800 ℃ roasting 1～20 hour, promptly obtain said catalyst.
Metal described in the present invention is all quoted with the nitrate form, is mixed with the aqueous solution of metal ion.The step of preparing aqueous solution of metal ions and impregnated carrier all can be carried out with reference to routine techniques.
Be used for after the Preparation of Catalyst of the present invention will reducing processing by method of the present invention before the reaction.
The carbon number n of MAS according to the invention is: 1≤n≤4 comprise methyl alcohol, ethanol, propyl alcohol, butanols, isobutanol.
The present invention adopts cheap raw material, utilizes simple infusion process, has prepared the new catalyst of methanation of a kind of synthesis gas part and coproduction MAS.Because synthesis gas can obtain from coal gasification, thereby can realize the coproduction of coal preparing natural gas and other multiple Coal Chemical Industry product, it is complementary to reach multiple coal-based product advantage, effectively improves the economic benefit and whole opposing risk ability of coal preparing natural gas project.
Description of drawings
Fig. 1 is copper cobalt-base catalyst CuCoFeK/Al
2O
3Under different reaction temperatures to H
2/ CO=2: the catalytic performance of 1 synthesis gas methanation and coproduction MAS.(catalyst quality: 1g CuCoFeK/Al
2O
3Unstripped gas is formed: H
2/ CO/Ar=64/32/4; Synthesis gas flow velocity: Syngas=60ml/min; Reaction pressure: P=5.0MPa; Activation condition: 400 ℃ of following 5h)
Fig. 2 is copper cobalt-base catalyst CuCoFeK/Al
2O
3Under different reaction temperatures to H
2/ CO=3: the catalytic performance of 1 synthesis gas methanation and coproduction MAS.(catalyst quality: 1g CuCoFeK/Al
2O
3Unstripped gas is formed: H
2/ CO/Ar=72/24/4; Synthesis gas flow velocity: Syngas=60ml/min; Reaction pressure: P=4.0MPa; Activation condition: 400 ℃ of following 5h)
Fig. 3 is copper cobalt-base catalyst CuCoFeK/ZrO
2Under different reaction temperatures to H
2/ CO=2: the catalytic performance of 1 synthesis gas methanation and coproduction MAS.(catalyst quality: 1g CuCoFeK/ZrO
2Unstripped gas is formed: H
2/ CO/Ar=64/32/4; Synthesis gas flow velocity: Syngas=60ml/min; Reaction pressure: P=5.0MPa; Activation condition: 430 ℃ of following 5h)
The specific embodiment
Embodiment 1 Preparation of catalysts mode
1.1 Preparation of catalysts process
In 10 gram gama-aluminas or the Zirconia carrier, use corresponding nitrate, in certain sequence, the equal-volume step impregnation forms through 400-800 ℃ of roasting on support C.Use hydrogen during reaction, or the hydrogen of inert gas dilution, or synthesis gas (H
2Gaseous mixture with CO) reduction is reacted then.
1.2 catalyst 30%CuO-10%CoO-1%Fe
2O
3-0.5%K
2O/Al
2O
3Preparation
5.85g Al
2O
3Carrier carries out the roasting purified treatment in 550 ℃ temperature.After the cooling, carry out incipient impregnation.Cu (NO with 9.06g
3)
33H
2O, the Co (NO of 3.93g
3)
26H
2O, 0.054g KNO
3Fe (NO with 0.51g
3)
39H
2O is dissolved in the 5.0ml deionized water, adopts equi-volume impregnating to be impregnated into 5.85gAl to this mixed aqueous solution
2O
3On the carrier, at 80 ℃ of excessive solvents of water-bath evaporation.The gained sample is dry 12h in 120 ℃ of baking ovens, and dry back sample places Muffle furnace, is warmed up to 550 ℃ with the heating rate of 2 ℃/min, and roasting 5h obtains catalyst 30%CuO-10%CoO-1%Fe
2O
3-0.5%K
2O/Al
2O
3
The analytical method of embodiment 2 products
Products obtained therefrom is analyzed with Agilent 7890A.Chromatogram is furnished with dual detector FID and TCD, and a ten-way valve is arranged, can be so that product gets into packed column and capillary column simultaneously respectively.Data are with the Chemstation software processes of Agilent.
The concrete chromatographic condition of Agilent is following:
Chromatogram: Agilent 7890A
FID chromatographic column: HP-PONA 19091S-001,50mx0.2mm (internal diameter), 0.5 μ m thickness
Carrier gas: helium, 2.5ml/min
Post oven temperature, degree: 35 ℃ keep 5min
35-150℃，5℃/min
150 ℃ keep 10min
Injection port: shunting (100: 1) temperature: 170 ℃
250 ℃ of detector: FID
TCD chromatographic column: carbon molecular sieve post, TDX-01 2mx2mm (internal diameter)
Carrier gas: helium, 20ml/min
Post oven temperature, degree: 35 ℃ keep 5min
35-150℃，5℃/min
150 ℃ keep 10min
Injection port: temperature: 170 ℃
200 ℃ of detector: TCD
The catalytic perfomance of embodiment 3 preparing methane by synthetic gas and coproduction MAS
In tubular fixed-bed reactor, prepared catalyst has been carried out the catalytic perfomance test evaluation of preparing methane by synthetic gas and coproduction MAS.According to requirement of the present invention, the technique initialization of preparing methane by synthetic gas and coproduction MAS as follows:
Raw material is formed: H2/CO/Ar argon gas (Ar) is interior mark
Reaction pressure: 3.0MPa or 5.0MPa
The weight of catalyst: 1.0g
The granularity of catalyst: 40-60 order
The height of beds :～10mm
When beginning to investigate, at first with catalyst at 4500 ℃, pure hydrogen, or add carrier gas, or reduction 5 hours under the condition of synthesis gas drop to the temperature of bed the temperature of appointment then, feed synthesis gas and react.Being heated by electric furnace of reactor, the control of reaction temperature is confirmed by the thermocouple that inserts beds.Unstripped gas and product gas are formed through the Angilent7890 gas chromatographic detection, and this chromatogram has two detectors: hydrogen flame detector and thermal conductivity detector (TCD).The hydrocarbon that hydrogen flame detector detects in the product distributes, and thermal conductivity detector (TCD) detects the hydrogen in raw material and the product, carbon monoxide, carbon dioxide with, methane and interior mark argon gas.The composition of two detectors is integrated as intermediary with methane.Only if other explanation is arranged, the instance below the present invention all carries out under above-mentioned experiment condition.
Because experiment is carried out under different reaction conditions, resulting MAS selectivity is also different, and product can be regulated on demand.Here the carbon number n of gained MAS is: 1≤n≤4 comprise methyl alcohol, ethanol, propyl alcohol, butanols and isomers thereof.Its result such as Fig. 1～shown in Figure 3.
Claims (10)
1. a catalyst that is used for preparing methane by synthetic gas and coproduction MAS is characterized in that catalyst consists of CuCoMA/C,
Wherein:
Active component Cu, in metallic element, the content in catalyst is 1.0-90.0wt%;
Active component Co, in metallic element, the content in catalyst is 1.0-90.0wt%;
Component M is an auxiliary agent, is any one or a few mixing among Zn, Cr, Fe, V, the Mn, and in metallic element, its content in catalyst is 0.0-90.0wt%;
Component A is an auxiliary agent, is any one or a few mixing among Li, Na, K, Mg, Ca, Sr, the Ba, and in metallic element, its content in catalyst is 0.0-25.0wt%;
Carrier component C is Al
2O
3, ZrO, SiO
2, TiO
2In any one or a few combination, its content in catalyst is 10.0-95.0wt%.
2. according to the described catalyst of claim 1, it is characterized in that the content of said active ingredient copper in catalyst is 20.0-50.0wt%, the content of cobalt in catalyst is 5.0-20.0wt%.
3. according to the described catalyst of claim 1, it is characterized in that the auxiliary agent M of said catalyst is that Mn and/or Fe are 1.0-15wt% in the content of metallic element in catalyst.
4. according to the described catalyst of claim 1, it is characterized in that said auxiliary agent A is 0.01-5.0wt% in the content of metallic element in catalyst
5. according to the described catalyst of claim 1, it is characterized in that said Zn is 5.0～20.0wt% in the content of metallic element in catalyst.
6. according to the described catalyst of claim 1, it is characterized in that the content of said carrier in catalyst is 60.0-75wt%.
7. the said Preparation of catalysts method of claim 1 is characterized in that, said employing infusion process, and step is following:
A) by the weight ratio of each component in the said catalyst, carrier component C carried out 1～10 hour roasting purified treatment in 400～700 ℃ temperature after, cooling;
B) with the aqueous solution that contains copper, cobalt, said component A and component M metal ion step a) gained sample is carried out incipient impregnation, flooded 2～12 hours;
C) with the sample behind the step b) gained dipping through 70～90 ℃ of evaporates to dryness, 100～150 ℃ of dryings, 400-800 ℃ roasting 1～20 hour, promptly obtain said catalyst.
8. the method for preparing methane by synthetic gas and coproduction MAS is characterized in that, with synthesis gas through the reactor reaction of the said catalyst of claim 1 being housed, preparation methane and coproduction MAS; The reaction temperature T of said preparing methane by synthetic gas and coproduction MAS is 200≤T≤400 ℃, and reaction pressure P is 0.5≤P≤10.0MPa, and reaction volume air speed LHSV is 1000≤LHSV≤40000h
-1
9. according to the described method of claim 8, it is characterized in that, use hydrogen before the said catalyst reaction, or the hydrogen of inert gas dilution, or the synthesis gas reduction, reacting then, the hydrogen of said reaction raw materials synthesis gas and carbon monoxide are than being H
2/ CO=2-8.
10. according to the described method of claim 8, the carbon number n of said MAS is: 1≤n≤4 comprise methyl alcohol, ethanol, propyl alcohol, butanols, isobutanol.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103553861A (en) * | 2013-10-29 | 2014-02-05 | 西南化工研究设计院有限公司 | System and technology for synthesis of methanol and co-production of methane by using synthesis gas |
| CN103691442A (en) * | 2013-12-03 | 2014-04-02 | 辽宁石油化工大学 | Catalyst for synthesis of isobutanol from synthesis gas and preparation method of catalyst |
| CN104725187A (en) * | 2015-02-15 | 2015-06-24 | 北京宝塔三聚能源科技有限公司 | Technology for directly preparing ethyl alcohol and co-generating methane from synthesis gas |
| CN105289622A (en) * | 2015-11-11 | 2016-02-03 | 中国石油大学(华东) | Catalyst used for dehydrogenation preparation of monoolefine by saturated alkane |
| CN106582700A (en) * | 2016-11-29 | 2017-04-26 | 中国科学院山西煤炭化学研究所 | Graphene-supported catalyst for preparation of low-carbon mixed alcohol from syngas, preparation method and application |
| CN107159213A (en) * | 2017-05-12 | 2017-09-15 | 浙江工业大学 | One kind is used for high H2/ CO is than catalyst of gas synthesis methane and preparation method thereof |
| CN107335444A (en) * | 2017-06-12 | 2017-11-10 | 中国海洋石油总公司 | A kind of synthesis gas prepares low-carbon alcohols effective catalyst and preparation method thereof |
| CN107376937A (en) * | 2017-08-14 | 2017-11-24 | 河南省科学院能源研究所有限公司 | A kind of order mesoporous composite catalyst and its preparation method and application |
| CN112939734A (en) * | 2019-11-26 | 2021-06-11 | 山西华顿实业有限公司 | Technical method for preparing low-carbon mixed alcohol and natural gas by using coal through synthesis gas one-step method |
| CN113617363A (en) * | 2021-08-30 | 2021-11-09 | 武汉强丰新特科技有限公司 | Supported multi-metal oxide catalyst and preparation method and application thereof |
| CN114349602A (en) * | 2020-10-12 | 2022-04-15 | 中石化南京化工研究院有限公司 | Process for synthesizing low-carbon mixed alcohol by taking coal synthesis gas as raw material and carrying out methanation in series |
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| CN1316298A (en) * | 2000-03-02 | 2001-10-10 | 艾尼股份公司 | Load type cobalt-base catalyst |
| CN101195553A (en) * | 2006-12-07 | 2008-06-11 | 中国石油化工股份有限公司 | Hydrocarbon synthesizing method |
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2010
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Patent Citations (2)
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| CN1316298A (en) * | 2000-03-02 | 2001-10-10 | 艾尼股份公司 | Load type cobalt-base catalyst |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103553861A (en) * | 2013-10-29 | 2014-02-05 | 西南化工研究设计院有限公司 | System and technology for synthesis of methanol and co-production of methane by using synthesis gas |
| CN103691442B (en) * | 2013-12-03 | 2016-08-24 | 辽宁石油化工大学 | A kind of synthesis gas isobutanol catalyst and preparation method thereof |
| CN103691442A (en) * | 2013-12-03 | 2014-04-02 | 辽宁石油化工大学 | Catalyst for synthesis of isobutanol from synthesis gas and preparation method of catalyst |
| CN104725187A (en) * | 2015-02-15 | 2015-06-24 | 北京宝塔三聚能源科技有限公司 | Technology for directly preparing ethyl alcohol and co-generating methane from synthesis gas |
| CN105289622B (en) * | 2015-11-11 | 2019-01-08 | 中国石油大学(华东) | Saturated alkane dehydrogenation prepares the application of the catalyst of monoolefine |
| CN105289622A (en) * | 2015-11-11 | 2016-02-03 | 中国石油大学(华东) | Catalyst used for dehydrogenation preparation of monoolefine by saturated alkane |
| CN106582700A (en) * | 2016-11-29 | 2017-04-26 | 中国科学院山西煤炭化学研究所 | Graphene-supported catalyst for preparation of low-carbon mixed alcohol from syngas, preparation method and application |
| CN107159213A (en) * | 2017-05-12 | 2017-09-15 | 浙江工业大学 | One kind is used for high H2/ CO is than catalyst of gas synthesis methane and preparation method thereof |
| CN107159213B (en) * | 2017-05-12 | 2020-12-15 | 浙江工业大学 | For high H2Catalyst for synthesizing methane by using gas with/CO ratio and preparation method thereof |
| CN107335444A (en) * | 2017-06-12 | 2017-11-10 | 中国海洋石油总公司 | A kind of synthesis gas prepares low-carbon alcohols effective catalyst and preparation method thereof |
| CN107376937A (en) * | 2017-08-14 | 2017-11-24 | 河南省科学院能源研究所有限公司 | A kind of order mesoporous composite catalyst and its preparation method and application |
| CN112939734A (en) * | 2019-11-26 | 2021-06-11 | 山西华顿实业有限公司 | Technical method for preparing low-carbon mixed alcohol and natural gas by using coal through synthesis gas one-step method |
| CN114349602A (en) * | 2020-10-12 | 2022-04-15 | 中石化南京化工研究院有限公司 | Process for synthesizing low-carbon mixed alcohol by taking coal synthesis gas as raw material and carrying out methanation in series |
| CN113617363A (en) * | 2021-08-30 | 2021-11-09 | 武汉强丰新特科技有限公司 | Supported multi-metal oxide catalyst and preparation method and application thereof |
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| CN102553600B (en) | 2014-06-25 |
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