CN105664999A - Preparation method of nickel-based catalyst and application of nickel-based catalyst to methanation of synthesized gas - Google Patents
Preparation method of nickel-based catalyst and application of nickel-based catalyst to methanation of synthesized gas Download PDFInfo
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- 239000003054 catalyst Substances 0.000 title claims abstract description 110
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 28
- 238000002360 preparation method Methods 0.000 title claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 68
- 239000007787 solid Substances 0.000 claims abstract description 25
- 239000000843 powder Substances 0.000 claims abstract description 15
- 238000006722 reduction reaction Methods 0.000 claims abstract description 10
- 238000007873 sieving Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 8
- 230000015572 biosynthetic process Effects 0.000 claims description 44
- 238000003786 synthesis reaction Methods 0.000 claims description 44
- 238000000034 method Methods 0.000 claims description 27
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 21
- 238000003756 stirring Methods 0.000 claims description 19
- 238000007789 sealing Methods 0.000 claims description 14
- 125000001967 indiganyl group Chemical group [H][In]([H])[*] 0.000 claims description 7
- 238000001994 activation Methods 0.000 claims description 4
- 239000002808 molecular sieve Substances 0.000 claims description 4
- SPIFDSWFDKNERT-UHFFFAOYSA-N nickel;hydrate Chemical compound O.[Ni] SPIFDSWFDKNERT-UHFFFAOYSA-N 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- MQRWBMAEBQOWAF-UHFFFAOYSA-N acetic acid;nickel Chemical compound [Ni].CC(O)=O.CC(O)=O MQRWBMAEBQOWAF-UHFFFAOYSA-N 0.000 claims description 3
- 229940078494 nickel acetate Drugs 0.000 claims description 3
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 claims description 3
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 claims description 3
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 20
- 238000010438 heat treatment Methods 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000001035 drying Methods 0.000 abstract 2
- 238000007598 dipping method Methods 0.000 abstract 1
- 230000000630 rising effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 41
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 27
- 230000008569 process Effects 0.000 description 16
- 239000003245 coal Substances 0.000 description 9
- 230000008859 change Effects 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 7
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 5
- 239000008367 deionised water Substances 0.000 description 5
- 229910021641 deionized water Inorganic materials 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000001802 infusion Methods 0.000 description 2
- 239000013335 mesoporous material Substances 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000012018 catalyst precursor Substances 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/041—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41
- B01J29/042—Mesoporous materials having base exchange properties, e.g. Si/Al-MCM-41 containing iron group metals, noble metals or copper
- B01J29/044—Iron group metals or copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/03—Catalysts comprising molecular sieves not having base-exchange properties
- B01J29/0308—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41
- B01J29/0316—Mesoporous materials not having base exchange properties, e.g. Si-MCM-41 containing iron group metals, noble metals or copper
- B01J29/0333—Iron group metals or copper
-
- B01J35/647—
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
Abstract
The invention discloses a preparation method of a nickel-based catalyst and application of the nickel-based catalyst to methanation of synthesized gas. The preparation method includes: using a common excessive dipping method, drying with a drying oven, sieving, performing microwave heating treatment on the solid powder obtained after the sieving, and cooling to obtain the catalyst. The application of the prepared catalyst to the methanation reaction of the synthesized gas is characterized in that after the reduction reaction of the catalyst in H2 atmosphere, the heated synthesized gas containing CO is allowed to contact with the nickel-based catalyst, the catalyst is activated by gradual temperature rising, and the temperature is lowered to certain temperature for stable reaction. The catalyst is high in catalyzing activity during the methanation reaction of the synthesized gas, good in product selectivity, high in strength and long in service life. The preparation method of the catalyst is simple and easy to operate, clean and environmental friendly, wide in practicality and high in economic benefit.
Description
Technical field
The present invention relates to coal preparing natural gas field, particularly to the preparation method of a kind of nickel-base catalyst and the application in synthesis gas methanation.
Background technology
It is known that, energy reserves amount is obtained with regard to the whole world, the reserves of oil and natural gas are only with 40-60, the reserves of coal can utilize more than 150 years, and biomass energy is the reproducible energy, therefore, obtain synthesis gas by coal or gasification of biomass, become the effective way making up source of the gas deficiency then through methanation for synthetic natural gas. Coal preparing natural gas is with coal for raw material, via the synthesis gas produced after coal gasification, processes then through methanation, produces calorific value and meets the substitute natural gas of regulation. The technological process of coal preparing natural gas mainly includes coal gasification, Partial Transformation, purified synthesis gas and four parts of synthesis gas methanation.
Coal preparing natural gas technology path it is crucial that synthesis gas methanation technology, the core of synthesis gas methanation technology is then the catalyst of methanation. For the methanation reaction of synthesis gas, the component with higher catalytic activity has Ru, Ni, Fe, Co etc. Although Ru catalyst based catalysis activity is the highest, but expensive, limit its large-scale commercial Application; The selectivity of Co catalyst based CO methanation reaction is poor; Fe is catalyst based cheap, and activity is higher, but easily because carbon distribution problem causes catalysqt deactivation; Ni is catalyst based, and due to catalysis activity height, selectivity is good, moderate, thus obtains extensive concern, thus Ni is catalyst based at present is the Main System studying CO methanation catalyst both at home and abroad. Patent DE2952683 discloses one using Co and the Ni species methanation catalyst as active component, this catalyst is that mixed oxide or the silicon dioxide of aluminium oxide or aluminium oxide and silicon dioxide are used as carrier material, catalytic performance is improved by the salt containing magnesium being added the mode of synthetic mixture, and catalyst for carrying out at the temperature lower than 500 DEG C, the temperature range of catalyst is narrow; Patent CN101391218 adopt infusion process first prepare catalyst carrier, the then nitrate solution of impregnated activated component and auxiliary agent again, prepare catalyst through super-dry, roasting.Owing to methanation reaction speed is exceedingly fast, active constituent nickel should be distributed is advisable on the surface of the catalyst, and infusion process be able to make Ni be distributed in carrier surface with thin-shell type, thus catalyst light-off temperature is low, and under low temperature, catalysis activity is good; But the method gained catalyst carrier absorption Ni ability is relatively low, the CO being not suitable for high concentration converts.
Synthesis gas methanation be concentration in synthesis gas is about 20% CO and a small amount of CO2With H2Carrying out methanation reaction, reaction is a strong exothermal reaction, and adiabatic temperature rise is big, methanation reaction during high temperature is affected by chemical equilibrium, can not carrying out completely, therefore in existing synthesis gas methanation process, the mode being generally adopted at least two reactors in series carries out. In order to improve utilization rate of equipment and installations and production efficiency, first reactor must operate at high temperature under high pressure, catalyst have to have good low temperature active and high-temperature stability (250-600 DEG C), second reactor need to carry out under medium and low temperature (250-450 DEG C), makes unconverted synthesis gas in first reactor reach to convert completely. At present, High Temperature High Pressure methanation catalyst technology is mainly provided by offshore company, such as the rope company of Top of the Dai Wei company of Britain and Denmark. Ni of the prior art is catalyst based in methanation, Nickel tetracarbonyl. is easily generated during low temperature, cause that active component Ni runs off, and catalytic methanation process is strong exothermal reaction, heat is as removed not in time, and high temperature can cause sintering of catalyst, causes that active component Ni granule becomes big, side reaction simultaneously increases, and causes the catalysqt deactivations such as carbon distribution.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art, the preparation method that the invention provides a kind of high-performance nickel-base catalyst, catalyst prepared by the method can be applicable to micro channel reactor system, can all keep significantly high activity under low temperature and higher temperature conditions.
Another object of the present invention is to provide the application in synthesis gas methanation of the above-mentioned nickel-base catalyst.
For realizing the first goal of the invention, the preparation method that the present invention provides a kind of nickel-base catalyst, comprise the steps:
(1) nickel source being made nickel solution, then sieved by carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor, and in mass parts, described nickel source is 2.2-6.6 part, and described molecular sieve MCM-41 is 2-6 part;
(2) by mixed liquor at 60-100 DEG C of lower sealing, opening sealing after stirring 8-14 hour, at 60-100 DEG C, heated and stirred is to being evaporated into solid;
(3) within 8-14 hour, grind into pressed powder by dry under 60-160 DEG C of condition for solid, sieve, after the pressed powder microwave treatment after sieving, cooling, obtain nickel-base catalyst.
Further, described nickel source is six water nickel nitrates, Nickel dichloride., nickel acetate or nickel sulfate.
Further, sieve described in as crossing 80-100 mesh sieve.
Further, described microwave power is 500W-1000W; Described microwave treatment time is 3-15min.
Further, a kind of nickel-base catalyst, it is prepared from according to above-mentioned method.
For realizing the second goal of the invention, for the invention provides the application in synthesis gas methanation of a kind of nickel-base catalyst:
The air speed of described synthesis gas methanation reaction is 1000-100000h-1, reaction pressure is 0.1-10MPa, and reaction temperature is 350-700 DEG C; H in described synthesis gas2It is 2.5-3.5:1 with the volume ratio of CO.
Further, the activation process of described reacting middle catalyst is: take catalyst at H2In atmosphere, at 450-550 DEG C of temperature, reduction reaction 1-6h;Being contacted with nickel-base catalyst by synthesis gas containing CO, with 200-250 DEG C for origin temp, every 50-60 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 2-4 hour, until being raised to 600-700 DEG C;
Compared with prior art, the beneficial effects of the present invention is:
1. the present invention is by improving methanation catalyst carrier, the 11203 of routine are substituted with ordered mesoporous material MCM-41, Ni base MCM-41 catalyst is prepared by the introducing of ordered mesoporous material MCM-41 carrier, and then improve specific surface area and high temperature resistant property, the problem solving methanation catalyst low temperature and thermostability now of catalyst. Owing to orderly Mesoporous silica MCM 41 has high specific surface area, relatively large aperture and regular regulatable duct (2-50nm) structure, and under high temperature, still can keep its pore passage structure, therefore can reach to improve catalyst activity and high temperature resistant property.
2. the present invention is directed to the engineering design of the Ni base MCM-41 molecular sieve catalyst of synthesis gas methanation flow process, develop low temperature, highly active Ni base MCM-41 molecular sieve catalyst, catalyst cheaper starting materials, wide material sources. Method for preparing catalyst is simple, and relatively common roasting is wanted quickly, to use microwave treatment presoma, and high efficiency of energy utilizes, environmental protection.
3. the catalyst in the present invention has significantly high conversion ratio when low-temp reaction, as conversion ratio can be made at 250 DEG C to reach more than 95%. The catalyst of the present invention can also run under high air speed, pressure and reaction temperature, and CO conversion ratio is high and does not have the generation of carbon distribution. The catalyst of the present invention is not having any additive to deposit in case, at reaction pressure 0.1-10MPa, air speed 1000-100000h-1, running more than when reaction temperature 450 DEG C 100 hours, CO conversion ratio is higher than 95%, methane selectively more than 85%, and does not have the generation of carbon distribution.
Accompanying drawing explanation
The catalyst activity figure that Fig. 1 provides for the embodiment of the present invention 1;
The catalyst activity figure that Fig. 2 provides for comparative example 1 of the present invention;
The catalyst that Fig. 3 provides for the embodiment of the present invention 1 is through the methanation catalyst performance trend figure of more than 100h;
Images of transmissive electron microscope before the reaction that Fig. 4 provides for the embodiment of the present invention 1;
Images of transmissive electron microscope before the reaction that Fig. 5 provides for comparative example 1 of the present invention.
Detailed description of the invention
Below in conjunction with embodiment, the present invention is described in further detail.
Embodiment 1:
A kind of preparation method of nickel-base catalyst:
(1) being put in the beaker equipped with 60g deionized water by 4.4g six water nickel nitrate, stir and make nickel solution, then sieved by 4g carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor;
(2) by mixed liquor at 80 DEG C of lower sealings, opening sealing after stirring 11 hours, at 80 DEG C, heated and stirred is to being evaporated into solid;
(3) solid is put in 110 DEG C of baking ovens, take out solid after dry 12 hours, dry solid is ground into pressed powder, cross 100 mesh sieves, by the pressed powder after sieving after power is process 15min in 800W microwave device, cooling, obtain nickel-base catalyst.
The application in synthesis gas methanation of a kind of nickel-base catalyst:
Take 2.1g nickel-base catalyst at H2In atmosphere, in methanation reaction container, at 500 DEG C of temperature, reduction reaction 2h, the synthesis gas containing CO is heated to 250 DEG C before contact nickel-base catalyst, the synthesis gas containing CO after heating is contacted with nickel-base catalyst, with 250 DEG C for origin temp, every 50 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 3 hours, until being raised to 650 DEG C, now complete the activation process of catalyst;Reduce the temperature to 350 DEG C of stably reaction more than 1000 hours, the processes now stably generated in a large number for methane; The air speed of synthesis gas methanation reaction is 30000h-1, reaction pressure is 1.5MPa, H in synthesis gas2It is 3:1 with the volume ratio of CO.
Activity rating adopts the fixed bed reactors of Φ 10mm, and as shown in Fig. 1, Fig. 3 and Fig. 4, the catalyst of the present invention is all significantly high at high temperature or cryogenic conditions activity, and when temperature is raised to 650 DEG C, the highest CO conversion ratio is 95%, CH4Selectivity is 90%, and catalytic reaction runs more than 1000 hours when temperature 350 DEG C, and CO conversion ratio is substantially free of change and higher than 95%, and methane selectively is substantially free of change and maintains more than 85%.
Embodiment 2:
A kind of preparation method of nickel-base catalyst:
(1) being put in the beaker equipped with 80g deionized water by 2.2g Nickel dichloride., stir and make nickel solution, then sieved by 6g carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor;
(2) by mixed liquor at 100 DEG C of lower sealings, opening sealing after stirring 14 hours, at 100 DEG C, heated and stirred is to being evaporated into solid;
(3) solid is put in 150 DEG C of baking ovens, take out solid after dry 10 hours, dry solid is ground into pressed powder, cross 80 mesh sieves, by the pressed powder after sieving after power is process 10min in 1000W microwave device, cooling, obtain nickel-base catalyst.
A kind of nickel-base catalyst application process in synthesis gas methanation:
Take 5g catalyst at H2In atmosphere, in methanation reaction container, at 450 DEG C of temperature, reduction reaction 6h, the synthesis gas containing CO is heated to 200 DEG C before contact nickel-base catalyst, the synthesis gas containing CO after heating is contacted with nickel-base catalyst, with 200 DEG C for origin temp, every 60 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 2 hours, until being raised to 700 DEG C, now complete the activation process of catalyst; Reduce the temperature to 600 DEG C of reactions more than 500 hours, the process now stably generated in a large number for methane; The air speed of synthesis gas methanation reaction is 1000h-1, reaction pressure is 0.1MPa, H in synthesis gas2It is 4.5:1 with the volume ratio of CO;
Activity rating adopts the fixed bed reactors of Φ 10mm, and this catalyst can have the CO conversion ratio of 95%, 90%CH low temperature 200 DEG C4Selectivity, when temperature is raised to 700 DEG C, the highest CO conversion ratio is 99%, CH4Selectivity is 90%. When reaction run more than when temperature 600 DEG C 500 little time, CO conversion ratio is substantially free of change and higher than 97%, and methane selectively is substantially free of change and maintains more than 90%.
Embodiment 3:
A kind of preparation method of nickel-base catalyst:
(1) being put in 60g deionized water by 6.6g nickel acetate, stir and make nickel solution, then sieved by 2g carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor;
(2) by mixed liquor at 60 DEG C of lower sealings, opening sealing after stirring 13 hours, at 60 DEG C, heated and stirred is to being evaporated into solid;
(3) solid is put in 60 DEG C of baking ovens, take out solid after dry 14 hours, dry solid is ground into pressed powder, cross 90 mesh sieves, by the pressed powder after sieving after power is process 3min in 500W microwave device, cooling, obtain nickel-base catalyst.
The application in synthesis gas methanation of a kind of nickel-base catalyst:
Take 3.8g catalyst at H2In atmosphere, in methanation reaction container, at 550 DEG C of temperature, reduction reaction 1h, the synthesis gas containing CO is heated to 220 DEG C before contact nickel-base catalyst, the synthesis gas containing CO after heating is contacted with nickel-base catalyst, with 220 DEG C for origin temp, every 55 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 4 hours, until being raised to 600 DEG C, then dropping to 350 DEG C and reacting 1000 hours;The air speed of reduction reaction is 50000h-1, reaction pressure is 5MPa, H in synthesis gas2It is 2.8:1 with the volume ratio of CO.
Activity rating adopts the fixed bed reactors of Φ 10mm, and the catalyst of the present invention is all significantly high at high temperature or cryogenic conditions activity, and when temperature is raised to 600 DEG C, the highest CO conversion ratio is 94%, CH4Selectivity is 88%, and catalytic reaction runs more than 1000 hours when temperature 350 DEG C, and CO conversion ratio is substantially free of change and higher than 92%, and methane selectively is substantially free of change and maintains more than 81%.
Embodiment 4:
A kind of preparation method of nickel-base catalyst:
(1) being put in the beaker equipped with 120g deionized water by 5.0g nickel sulfate, stir and make nickel solution, then sieved by 5g carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor;
(2) by mixed liquor at 90 DEG C of lower sealings, opening sealing after stirring 13 hours, at 100 DEG C, heated and stirred is to being evaporated into solid;
(3) solid is put in 160 DEG C of baking ovens, take out solid after dry 8 hours, dry solid is ground into pressed powder, cross 100 mesh sieves, by the pressed powder after sieving after power is process 12min in 1000W microwave device, cooling, obtain nickel-base catalyst.
A kind of nickel-base catalyst application process in synthesis gas methanation:
Take 4g catalyst at H2In atmosphere, in methanation reaction container, at 500 DEG C of temperature, reduction reaction 4h, the synthesis gas containing CO is heated to 200 DEG C before contact nickel-base catalyst, the synthesis gas containing CO after heating is contacted with nickel-base catalyst, with 200 DEG C for origin temp, every 60 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 4 hours, until being raised to 700 DEG C, then drop to 630 DEG C of reactions more than 500 hours; The air speed of reduction reaction is 100000h-1, reaction pressure is 10MPa, H in synthesis gas2It is 4.5:1 with the volume ratio of CO;
Activity rating adopts the fixed bed reactors of Φ 10mm, and this catalyst can have the CO conversion ratio of 93%, 91%CH low temperature 200 DEG C4Selectivity, when temperature is raised to 700 DEG C, the highest CO conversion ratio is 99%, CH4Selectivity is 90%. When reaction run more than when temperature 630 DEG C 500 little time, CO conversion ratio is substantially free of change and higher than 95%, and methane selectively is substantially free of change and maintains more than 91%.
Comparative example 1:
The preparation method of comparative catalyst:
(1) being put in 60g deionized water by 4.4g six water nickel nitrate, stir and make nickel solution, then sieved by 4g carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor;
(2) by mixed liquor at 80 DEG C of lower sealings, opening sealing after stirring 11 hours, at 80 DEG C, heated and stirred is to being evaporated into solid;
(3) solid is put in 110 DEG C of baking ovens, solid is taken out after dry 12 hours, dry solid is ground into pressed powder, cross 100 mesh sieves, the pressed powder after sieving is put in crucible, places in Muffle furnace, temperature is per minute incremental with 10 DEG C, it is raised to 650 DEG C, and keeps 4 hours, after cooling, obtain comparative catalyst.
Comparative catalyst's application process in synthesis gas methanation:
Take 2.1g comparative catalyst at H2In atmosphere, in methanation reaction container, at 500 DEG C of temperature, reduction reaction 2h, the synthesis gas containing CO is heated to 250 DEG C before contact nickel-base catalyst, the synthesis gas containing CO after heating is contacted with nickel-base catalyst, with 250 DEG C for origin temp, every 50 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 3 hours, until being raised to 650 DEG C, then dropping to 350 DEG C and reacting more than 200 hours.
Activity rating adopts the fixed bed reactors of Φ 10mm, as shown in Figure 2 and Figure 5, catalyst prepared by the method is under high temperature or cryogenic conditions, activity is all low than the catalyst using the method for the embodiment of the present invention 1 to prepare, catalyst prepared by the method is when temperature is raised to 650 DEG C, the highest CO conversion ratio is 90%, CH4Selectivity is 85%. When temperature is too high, namely react and run more than 100 hours when 350 DEG C of temperature, catalyst activity reduces substantially, CO conversion ratio significantly drops to 76% from up to 94%, the catalyst activity of reaction and CO conversion ratio As time goes on continuous decrease, until reaction terminates reaction in 200 hours.
The present invention is with MCM-41 for carrier, nickel-base catalyst is prepared by microwave treatment catalyst precursor, this catalyst preparation process is simple, energetically develop the methanation catalyst activity in low-temp reaction temperature, the catalyst of the present invention also has resistant to elevated temperatures characteristic simultaneously, range of reaction temperature is wide, provides possibility for later industrial reaction is energy-conservation.
Above example is only the exemplary embodiment of the present invention, is not used in the restriction present invention, and protection scope of the present invention is defined by the claims. The present invention in the essence of the present invention and protection domain, can be made various amendment or equivalent replacement by those skilled in the art, and this amendment or equivalent replacement also should be regarded as being within the scope of the present invention.
Claims (7)
1. the preparation method of nickel-base catalyst, it is characterised in that comprise the steps:
(1) nickel source being made nickel solution, then sieved by carrier molecule in MCM-41 addition nickel solution, stir to obtain mixed liquor, and in mass parts, described nickel source is 2.2-6.6 part, and described molecular sieve MCM-41 is 2-6 part;
(2) by mixed liquor at 60-100 DEG C of lower sealing, opening sealing after stirring 8-14 hour, at 60-100 DEG C, heated and stirred is to being evaporated into solid;
(3) within 8-14 hour, grind into pressed powder by dry under 60-160 DEG C of condition for solid, sieve, after the pressed powder microwave treatment after sieving, cooling, obtain nickel-base catalyst.
2. method according to claim 1, it is characterised in that described nickel source is six water nickel nitrates, Nickel dichloride., nickel acetate or nickel sulfate.
3. method according to claim 1, it is characterised in that described in sieve into cross 80-100 mesh sieve.
4. method according to claim 1, it is characterised in that described microwave power is 500W-1000W; Described microwave treatment time is 3-15min.
5. a nickel-base catalyst, it is characterised in that the method described in any one of claim 1-4 is prepared from.
6. the nickel-base catalyst application in synthesis gas methanation, it is characterised in that the air speed of described synthesis gas methanation reaction is 1000-100000h-1, reaction pressure is 0.1-10MPa, and reaction temperature is 350-700 DEG C; H in described synthesis gas2It is 2.5-3.5:1 with the volume ratio of CO.
7. application according to claim 6, it is characterised in that the activation process of described reacting middle catalyst is: take catalyst at H2In atmosphere, at 450-550 DEG C of temperature, reduction reaction 1-6h; Being contacted with nickel-base catalyst by synthesis gas containing CO, with 200-250 DEG C for origin temp, every 50-60 DEG C is a gradient, and each gradient rises a gradient after keeping reaction 2-4 hour, until being raised to 600-700 DEG C.
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| CN111036286A (en) * | 2019-12-24 | 2020-04-21 | 昆明理工大学 | Preparation method and application of MCM-41 molecular sieve supported nickel-based catalyst |
| CN112517015A (en) * | 2020-11-13 | 2021-03-19 | 华东理工大学 | Activation method of nickel-based methanation catalyst |
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