CN114618500A - Method for preparing catalyst for synthesizing methanol from carbon dioxide and hydrogen - Google Patents
Method for preparing catalyst for synthesizing methanol from carbon dioxide and hydrogen Download PDFInfo
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- CN114618500A CN114618500A CN202210430413.8A CN202210430413A CN114618500A CN 114618500 A CN114618500 A CN 114618500A CN 202210430413 A CN202210430413 A CN 202210430413A CN 114618500 A CN114618500 A CN 114618500A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 333
- 239000003054 catalyst Substances 0.000 title claims abstract description 133
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 120
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 65
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 58
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 56
- 239000001257 hydrogen Substances 0.000 title claims abstract description 56
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 56
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 54
- 238000004519 manufacturing process Methods 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 9
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 8
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 229910002482 Cu–Ni Inorganic materials 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 229910045601 alloy Inorganic materials 0.000 claims description 6
- 239000000956 alloy Substances 0.000 claims description 6
- 238000012216 screening Methods 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 claims description 6
- 238000002360 preparation method Methods 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- 229910002651 NO3 Inorganic materials 0.000 claims description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 3
- 229910005790 SnSiO Inorganic materials 0.000 claims description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 claims description 3
- 239000008367 deionised water Substances 0.000 claims description 3
- 229910021641 deionized water Inorganic materials 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000000643 oven drying Methods 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 235000012239 silicon dioxide Nutrition 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 229910052725 zinc Inorganic materials 0.000 claims description 3
- 239000011701 zinc Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 30
- 229910001868 water Inorganic materials 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000036632 reaction speed Effects 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 241000282414 Homo sapiens Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
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- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/80—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with zinc, cadmium or mercury
-
- 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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/835—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with germanium, tin or lead
-
- B01J35/19—
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
- C07C29/154—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing copper, silver, gold, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
- C07C29/156—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/04—Methanol
-
- 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 method for preparing a catalyst for synthesizing methanol from carbon dioxide and hydrogen, wherein the catalyst for synthesizing methanol from carbon dioxide and hydrogen is formed by mixing a shift catalyst and a methanol synthesis catalyst, wherein the shift catalyst is suitable for being used at 1-2Mpa and 180-plus-350 ℃, the methanol synthesis catalyst is suitable for being used at 1-2Mpa and 190-plus-310 ℃, and the shift catalyst and the methanol synthesis catalyst are mixed according to the mixing proportion as follows: the ratio of the shift catalyst to the methanol synthesis catalyst is 1-5; the ratio of the shift catalyst to the methanol synthesis catalyst is between 5 and 1. The invention mixes the conversion reaction and the methanol synthesis reaction kinetics according to the actual operation pressure and temperature process parameters of the carbon dioxide and hydrogen methanol synthesis plant, and the ratio of the conversion catalyst to the methanol synthesis catalyst is 0.2-5, so as to better complete the production process of synthesizing methanol from carbon dioxide and hydrogen.
Description
Technical Field
The invention relates to the technical field of methanol synthesis, in particular to a method for preparing a catalyst for synthesizing methanol from carbon dioxide and hydrogen.
Background
Since the industrial revolution, the content of carbon dioxide in the atmosphere rises from 276ppm to 415ppm at present, and the rising trend is accelerated, so that the greenhouse effect of the earth is increasingly intensified and the life of the earth is threatened. The carbon neutralization concept has become a common consensus, and the carbon resource utilization pattern must be changed at present in human beings. The reduction of carbon emission in production and the reduction of carbon dioxide present in the atmosphere is a good direction for the synthesis of methanol from carbon dioxide and hydrogen.
With the gradual rise of energy occupation ratios of clean energy sources such as solar energy, wind energy, hydraulic energy, geothermal energy, tidal energy and the like, the hydrogen production amount by water electrolysis rises, and the prospect of synthesizing methanol from carbon dioxide and hydrogen for carbon emission reduction is promising.
The current methanol synthesis catalyst is accepted by industrial application in the aspects of reaction speed and single-pass conversion rate for the process of synthesizing methanol from carbon monoxide, carbon dioxide and hydrogen, and the conditions of low reaction speed and low single-pass conversion rate exist in the process of synthesizing methanol from carbon dioxide and hydrogen; the catalyst specially and newly introduced for synthesizing methanol from carbon dioxide and hydrogen is not only low in reaction speed and low in single-pass conversion rate, but also complex in manufacturing process and high in cost.
The catalyst with changed carbon monoxide and the catalyst for synthesizing the methanol are widely applied to the field of chemical industry, the application temperature and the pressure parameter of the two catalysts have a common intersection, the application temperature range of the catalyst is changed to 180-430 ℃, and the application temperature range of the catalyst for synthesizing the methanol is 190-310 ℃.
Disclosure of Invention
The present invention is directed to a method for preparing a catalyst for synthesizing methanol from carbon dioxide and hydrogen, so as to solve the above problems in the prior art.
In order to achieve the purpose, the invention provides the following technical scheme: a catalyst for synthesizing methanol from carbon dioxide and hydrogen is prepared from the shift catalyst (1-2 MPa, 180-350 deg.C) and the methanol synthesizing catalyst (1-2 MPa, 190-310 deg.C).
Preferably, the shift catalyst production method is as follows:
s1: co-precipitating a nitrate solution of copper and zinc with a sodium carbonate solution, the copper nitrate solution: zinc nitrate solution: sodium carbonate solution 1:1: 2;
s2: washing with deionized water, filtering, and oven drying at 110 deg.C;
s3: then roasting at 350 ℃ in air for 150 ℃ for half an hour, raising the temperature by 50 ℃ within the interval, and roasting for 3 hours at 350 ℃;
s4: and finally, heating to 500 ℃, roasting for 2h, cooling, forming, crushing and screening to obtain the CuO-ZnO catalyst, namely a shift catalyst, wherein a 20-40-mesh screen is adopted for screening.
Preferably, the method for producing the synthetic methanol catalyst comprises the following steps:
s1, reducing CuO and NiO by using silicon dioxide as a carrier;
s2: obtaining Cu-Ni alloy loaded on the surface of the SnSiO carrier;
s3: the Cu-Ni alloy is crushed to be used as a methanol synthesis catalyst.
Preferably, the method for producing a methanol catalyst by synthesizing carbon dioxide and hydrogen is not limited to the method described in claims 2 to 3.
Preferably, the shift catalyst used to manufacture the catalyst for synthesizing methanol from carbon dioxide and hydrogen may be a commercially available catalyst.
Preferably, the synthetic methanol catalyst used to manufacture the carbon dioxide and hydrogen synthetic methanol catalyst may be a commercially available catalyst.
Preferably, the method for preparing the methanol catalyst by synthesizing carbon dioxide and hydrogen comprises the following steps:
mixing a shift catalyst and a methanol synthesis catalyst according to the following mixing ratio: the ratio of the shift catalyst to the methanol synthesis catalyst is 1-5; the ratio of the shift catalyst to the methanol synthesis catalyst is between 5 and 1.
Preferably, in the manufacturing process of the methanol synthesis catalyst by carbon dioxide and hydrogen:
a. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed and loaded;
b. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed and loaded;
c. the shift catalyst and the synthetic methanol catalyst in the synthetic tower for producing methanol are mixed and loaded layer by layer and evenly.
Compared with the prior art, the invention has the beneficial effects that: the invention discloses a catalyst for synthesizing methanol from carbon dioxide and hydrogen, which is suitable for synthesizing methanol from carbon dioxide and hydrogen, and the specific scheme is to prepare a shift catalyst suitable for synthesizing methanol from carbon dioxide and hydrogen at 1-12 Mpa and 180-350 ℃, prepare a catalyst suitable for synthesizing methanol from carbon dioxide to 12Mpa and 190-310 ℃, mix and load the shift reaction and the methanol synthesis reaction kinetics according to the pressure and temperature technological parameters of the actual operation of a plant for synthesizing methanol from carbon dioxide and hydrogen, wherein the ratio of the shift catalyst to the methanol synthesis catalyst is 0.2-5, so that the production process for synthesizing methanol from carbon dioxide and hydrogen can be well completed.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "both ends", "one end", "the other end", and the like indicate orientations or positional relationships only for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "disposed," "connected," and the like are to be construed broadly, such as "connected," which may be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in a specific case to those of ordinary skill in the art.
The embodiment provided by the invention comprises the following steps:
the first embodiment is as follows:
a catalyst for synthesizing methanol from carbon dioxide and hydrogen is prepared from the shift catalyst (1-2 MPa, 180-350 deg.C) and the methanol synthesizing catalyst (1-2 MPa, 190-310 deg.C).
The shift catalyst manufacturing method is as follows:
s1: co-precipitating a nitrate solution of copper and zinc with a sodium carbonate solution, the copper nitrate solution: zinc nitrate solution: sodium carbonate solution 1:1: 2;
s2: washing with deionized water, filtering, and oven drying at 110 deg.C;
s3: then roasting at 350 ℃ in air for 150 ℃ for half an hour, raising the temperature by 50 ℃ within the interval, and roasting for 3 hours at 350 ℃;
s4: and finally, heating to 500 ℃, roasting for 2h, cooling, forming, crushing and screening to obtain the CuO-ZnO catalyst, namely a shift catalyst, wherein a 20-40-mesh screen is adopted for screening.
The preparation method of the methanol synthesis catalyst comprises the following steps:
s1, reducing CuO and NiO by using silicon dioxide as a carrier;
s2: obtaining Cu-Ni alloy loaded on the surface of the SnSiO carrier;
s3: the Cu-Ni alloy is crushed to be used as a methanol synthesis catalyst.
The method for manufacturing the carbon dioxide and hydrogen synthetic methanol catalyst is not limited to the above-described method, and the shift catalyst for manufacturing the carbon dioxide and hydrogen synthetic methanol catalyst may be a commercially available catalyst, and the synthetic methanol catalyst for manufacturing the carbon dioxide and hydrogen synthetic methanol catalyst may be a commercially available catalyst.
The second embodiment:
the preparation method of the catalyst for synthesizing methanol by carbon dioxide and hydrogen comprises the following steps:
mixing a shift catalyst and a methanol synthesis catalyst according to the following mixing ratio: the ratio of the conversion catalyst to the methanol synthesis catalyst is between 1 and 5; the ratio of the shift catalyst to the methanol synthesis catalyst is between 5 and 1.
In the manufacturing process of the catalyst for synthesizing methanol from carbon dioxide and hydrogen:
a. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed;
b. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed and loaded;
c. the shift catalyst and the synthetic methanol catalyst in the synthetic tower for producing methanol are mixed and loaded layer by layer and evenly.
Example three:
the gas pressure at the inlet of the synthesis tower is 8.0Mpa, 200 ℃, 2272.22kmol/H CO2 and 2272.22kmol/H H2Namely 100 tons of carbon dioxide and hydrogen with equal molar mass enter a methanol synthesis tower for reaction. The outlet temperature of the synthesis tower is 254.45 ℃, 1937.58kmol/h of CO2, 112.626kmol/h of CO and 222.015kmol/h of CH3OH, 334.641kmol/H of H2O, 1493.55kmol/H of H2。
7.114 tons of methanol are produced, the per-pass conversion rate of carbon dioxide is 14.73 percent, the per-pass conversion rate of hydrogen is 34.27 percent, and the reaction temperature is within the bearing range of the catalyst.
Example four:
CO at 8.0Mpa at 200 deg.C and 2272.22kmol/h at inlet of synthesizing tower23408.33kmol/H of H2Namely, 100 tons of carbon dioxide and 1.5 times of molar mass of hydrogen enter a methanol synthesis tower for reaction.
The outlet temperature of the synthesis tower is 264.06 ℃, 1822.87kmol/h of CO2146.32kmol/h CO, 303.025kmol/h CH3OH, 449.35kmol/H of H2O, 2352.93kmol/H of H2。
9.709 tons of methanol are produced, the conversion per pass of carbon dioxide is 19.77 percent, the conversion per pass of hydrogen is 30.96 percent, and the reaction temperature is within the bearing range of the catalyst.
Example five:
CO at 8.0Mpa at 200 deg.C and 2272.22kmol/h at inlet of synthesizing tower24544.44kmol/H of H2Namely, 100 tons of carbon dioxide and 2 times of molar mass of hydrogen enter a methanol synthesis tower for reaction.
The outlet temperature of the synthesis tower is 269.48 ℃, 1726.53kmol/h of CO2172.066kmol/h CO, 373.62kmol/h CH3OH, 545.69kmol/H of H2O, 3251.51kmol/H of H2。
11.971 tons of methanol are produced, the conversion per pass of carbon dioxide is 24.02 percent, the conversion per pass of hydrogen is 28.45 percent, and the reaction temperature is within the bearing range of the catalyst.
Example six:
CO at 8.0Mpa at 200 deg.C and 2272.22kmol/h at inlet of synthesizing tower26816.663kmol/H of H2Namely, 100 tons of carbon dioxide and 3 times of molar mass of hydrogen enter a methanol synthesis tower for reaction.
The outlet temperature of the synthesis tower is 274.72 ℃, 1569.46kmol/h of CO2207.22kmol/h CO, 495.54kmol/h CH3OH, 702.765kmol/H of H2O, 5122.82kmol/H of H2。
15.878 tons of methanol are produced, the per-pass conversion rate of carbon dioxide is 30.92 percent, the per-pass conversion rate of hydrogen is 24.85 percent, and the reaction temperature is within the bearing range of the catalyst.
Example seven:
CO at 8.0Mpa at 200 deg.C and 2272.22kmol/h at inlet of synthesizing tower29088.88kmol/H of H2Namely, 100 tons of carbon dioxide and 4 times of molar mass of hydrogen enter a methanol synthesis tower for reaction.
The outlet temperature of the synthesis tower is 276.63 ℃, 1443.02kmol/h of CO2228.35kmol/h CO, 600.84kmol/h CH3OH, 829.2kmol/H of H2O, 7058kmol/H H2。
19.252 tons of methanol are produced, the conversion per pass of carbon dioxide is 36.49%, the conversion per pass of hydrogen is 22.34%, and the reaction temperature is within the bearing range of the catalyst.
Example eight:
CO at 8.0Mpa at 200 deg.C and 2272.22kmol/h at inlet of synthesizing tower211361.11kmol/H of H2Namely, 100 tons of carbon dioxide and 5 times of molar mass of hydrogen enter a methanol synthesis tower for reaction.
The outlet temperature of the synthesis tower is 277.07 ℃, 1336.53kmol/h of CO2240.772kmol/h CO, 694.91kmol/h CH3OH, 935.69kmol/H of H2O, 9035.59kmol/H of H2。
22.266 tons of methanol are produced, the conversion per pass of carbon dioxide is 41.18 percent, the conversion per pass of hydrogen is 20.47 percent, and the reaction temperature is within the bearing range of the catalyst.
It will be evident to those skilled in the art that the invention is not limited to the details of the foregoing illustrative embodiments, and that the present invention may be embodied in other specific forms without departing from the spirit or essential attributes thereof. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.
Claims (8)
1. A manufacturing method of a catalyst for synthesizing methanol by carbon dioxide and hydrogen is characterized in that: the catalyst for synthesizing methanol from carbon dioxide and hydrogen is formed by mixing a shift catalyst and a methanol synthesis catalyst, wherein the shift catalyst is suitable for being used at the temperature of 1-2Mpa and 350 ℃ in 180 ℃ and the methanol synthesis catalyst is suitable for being used at the temperature of 1-2Mpa and 310 ℃ in 190 ℃.
2. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: the method for producing the shift catalyst comprises the following steps:
s1: co-precipitating a nitrate solution of copper and zinc with a sodium carbonate solution, the copper nitrate solution: zinc nitrate solution: sodium carbonate solution 1:1: 2;
s2: washing with deionized water, filtering, and oven drying at 110 deg.C;
s3: then roasting at 350 ℃ in air for 150 ℃ for half an hour, raising the temperature by 50 ℃ within the interval, and roasting for 3 hours at 350 ℃;
s4: and finally, heating to 500 ℃, roasting for 2h, cooling, forming, crushing and screening to obtain the CuO-ZnO catalyst, namely a shift catalyst, wherein a 20-40-mesh screen is adopted for screening.
3. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: the preparation method of the methanol synthesis catalyst comprises the following steps:
s1, reducing CuO and NiO by using silicon dioxide as a carrier;
s2: obtaining Cu-Ni alloy loaded on the surface of the SnSiO carrier;
s3: the Cu-Ni alloy is crushed to be used as a methanol synthesis catalyst.
4. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: the method for producing a methanol catalyst by synthesizing carbon dioxide and hydrogen is not limited to the method described in claims 2 to 3.
5. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: the shift catalyst used to make the carbon dioxide and hydrogen methanol synthesis catalyst may be a commercially available catalyst.
6. The method of claim 1, wherein the catalyst comprises at least one of the following components: the synthetic methanol catalyst used to manufacture the carbon dioxide and hydrogen synthetic methanol catalyst may be a commercially available catalyst.
7. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: the preparation method of the catalyst for synthesizing methanol from carbon dioxide and hydrogen comprises the following steps:
mixing a shift catalyst and a methanol synthesis catalyst according to the mixing proportion: the ratio of the shift catalyst to the methanol synthesis catalyst is 1-5; the ratio of the shift catalyst to the methanol synthesis catalyst is between 5 and 1.
8. The method for manufacturing a catalyst for synthesizing methanol from carbon dioxide and hydrogen according to claim 1, wherein: in the manufacturing process of the catalyst for synthesizing methanol from carbon dioxide and hydrogen:
a. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed and loaded;
b. the shift catalyst and the methanol synthesis catalyst in the synthesis tower for producing methanol are uniformly mixed;
the shift catalyst and the synthetic methanol catalyst in the synthetic tower for producing methanol are mixed and loaded layer by layer and evenly.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116060084A (en) * | 2022-11-01 | 2023-05-05 | 扬州晨化新材料股份有限公司 | Alumina-supported copper-rare earth metal oxide catalyst and preparation method thereof |
Citations (4)
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| CN116060084A (en) * | 2022-11-01 | 2023-05-05 | 扬州晨化新材料股份有限公司 | Alumina-supported copper-rare earth metal oxide catalyst and preparation method thereof |
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