CN111992213A - Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol - Google Patents
Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol Download PDFInfo
- Publication number
- CN111992213A CN111992213A CN202010961675.8A CN202010961675A CN111992213A CN 111992213 A CN111992213 A CN 111992213A CN 202010961675 A CN202010961675 A CN 202010961675A CN 111992213 A CN111992213 A CN 111992213A
- Authority
- CN
- China
- Prior art keywords
- core
- catalyst
- sio
- shell
- guaiacol
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 83
- LHGVFZTZFXWLCP-UHFFFAOYSA-N guaiacol Chemical compound COC1=CC=CC=C1O LHGVFZTZFXWLCP-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 239000011258 core-shell material Substances 0.000 title claims abstract description 44
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 229960001867 guaiacol Drugs 0.000 title claims abstract description 33
- 238000002360 preparation method Methods 0.000 title claims abstract description 16
- 238000009903 catalytic hydrogenation reaction Methods 0.000 title description 2
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 33
- 229910052681 coesite Inorganic materials 0.000 claims abstract description 32
- 229910052906 cristobalite Inorganic materials 0.000 claims abstract description 32
- 229910052682 stishovite Inorganic materials 0.000 claims abstract description 32
- 229910052905 tridymite Inorganic materials 0.000 claims abstract description 32
- 239000002105 nanoparticle Substances 0.000 claims abstract description 20
- 229910017052 cobalt Inorganic materials 0.000 claims abstract description 9
- 239000010941 cobalt Substances 0.000 claims abstract description 9
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 5
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 4
- 229910052684 Cerium Inorganic materials 0.000 claims abstract description 3
- 239000001257 hydrogen Substances 0.000 claims description 24
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 22
- 229910052739 hydrogen Inorganic materials 0.000 claims description 22
- 239000008367 deionised water Substances 0.000 claims description 21
- 229910021641 deionized water Inorganic materials 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 239000000047 product Substances 0.000 claims description 20
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims description 19
- 239000000243 solution Substances 0.000 claims description 18
- 239000002994 raw material Substances 0.000 claims description 16
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 230000035484 reaction time Effects 0.000 claims description 14
- 238000003756 stirring Methods 0.000 claims description 14
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 12
- 239000002243 precursor Substances 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 12
- LZZYPRNAOMGNLH-UHFFFAOYSA-M Cetrimonium bromide Chemical compound [Br-].CCCCCCCCCCCCCCCC[N+](C)(C)C LZZYPRNAOMGNLH-UHFFFAOYSA-M 0.000 claims description 11
- 239000002244 precipitate Substances 0.000 claims description 11
- 238000001704 evaporation Methods 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 9
- 239000000725 suspension Substances 0.000 claims description 9
- 238000010907 mechanical stirring Methods 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 8
- 229910003243 Na2SiO3·9H2O Inorganic materials 0.000 claims description 6
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 229910052751 metal Inorganic materials 0.000 claims description 5
- 239000002184 metal Substances 0.000 claims description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 229910052710 silicon Inorganic materials 0.000 claims description 4
- 239000010703 silicon Substances 0.000 claims description 4
- NWZSZGALRFJKBT-KNIFDHDWSA-N (2s)-2,6-diaminohexanoic acid;(2s)-2-hydroxybutanedioic acid Chemical compound OC(=O)[C@@H](O)CC(O)=O.NCCCC[C@H](N)C(O)=O NWZSZGALRFJKBT-KNIFDHDWSA-N 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine monohydrate Substances O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000001291 vacuum drying Methods 0.000 claims description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 claims description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 2
- 229910002651 NO3 Inorganic materials 0.000 claims description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 2
- -1 hydrogen Chemical class 0.000 claims description 2
- 229910016287 MxOy Inorganic materials 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 3
- 239000002904 solvent Substances 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 238000001308 synthesis method Methods 0.000 abstract description 2
- 229910052911 sodium silicate Inorganic materials 0.000 description 4
- 229910003082 TiO2-SiO2 Inorganic materials 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 3
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- 238000003917 TEM image Methods 0.000 description 2
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910052593 corundum Inorganic materials 0.000 description 2
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 2
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 2
- 238000009776 industrial production Methods 0.000 description 2
- 229920005610 lignin Polymers 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910001845 yogo sapphire Inorganic materials 0.000 description 2
- 239000002841 Lewis acid Substances 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 229910020489 SiO3 Inorganic materials 0.000 description 1
- 239000001361 adipic acid Substances 0.000 description 1
- 235000011037 adipic acid Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 150000007517 lewis acids Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- AISMNBXOJRHCIA-UHFFFAOYSA-N trimethylazanium;bromide Chemical compound Br.CN(C)C AISMNBXOJRHCIA-UHFFFAOYSA-N 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Images
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
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/002—Mixed oxides other than spinels, e.g. perovskite
-
- 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
- B01J23/74—Iron group metals
- B01J23/75—Cobalt
-
- 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
- B01J23/83—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 rare earths or actinides
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
- B01J35/396—Distribution of the active metal ingredient
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
-
- 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
- C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
- C07C29/19—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds in six-membered aromatic rings
- C07C29/20—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds in six-membered aromatic rings in a non-condensed rings substituted with hydroxy groups
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
Abstract
The invention belongs to the field of preparation of catalysts, and particularly relates to a preparation method of a core-shell type catalyst for preparing cyclohexanol by catalyzing hydrogenation and deoxidation of guaiacol. Firstly, preparing cobalt nano-particles by using a solvent reduction method, and then preparing the cobalt nano-particles by using a post-synthesis method to obtain the cobalt nano-particles taking Co as a core and M as a corexOy‑SiO2Co @ M as shellxOy‑SiO2A core-shell catalyst, wherein M ═ Ce, Ti, and Al. The catalyst has the advantages of simple preparation process, low cost, low energy consumption and low reaction pressure and temperature. In addition, the productThe obtained core-shell catalyst shows good reaction activity in the guaiacol hydrodeoxygenation reaction, has good stability, can be roasted and recycled after reaction, and has good economic benefit.
Description
Technical Field
The invention belongs to the technical field of catalyst preparation, and particularly relates to a preparation method of a core-shell type catalyst for preparing cyclohexanol by catalyzing hydrogenation and deoxidation of guaiacol.
Background
Cyclohexanol is an important chemical raw material and is widely applied to a plurality of industrial production fields. Can be used for producing adipic acid, hexamethylene diamine, caprolactam and the like, can also be used as a raw material for fuel production, and cyclohexane prepared by hydrogenation and dehydration is one of main components of gasoline. Furthermore, cyclohexanol is also used in solvents, paints, pharmaceuticals, plasticizers, and the like. Currently, the industrial production of cyclohexanol is mainly realized by oxidation of cyclohexane and hydrogenation of phenol, which is not in accordance with the strategy of sustainable development and increases the consumption of fossil energy.
Guaiacol has a high proportion in phenolic compounds obtained by pyrolysis of lignin, and lignin has a wide reserve in nature. The method for preparing cyclohexanol by using guaiacol hydrodeoxygenation has low production cost and saves energy. Recently, the transition metal catalyst shows better reaction activity in the guaiacol hydrodeoxygenation reaction, has unique advantages compared with catalysts such as noble metals, sulfides and the like, and is low in cost, green and clean.
In the patent CN107649169A, a catalyst prepared by loading any two or three active components of Ni, Co, Cu, Mg, Al and Fe on a molecular sieve is used for catalyzing guaiacol hydrodeoxygenation to prepare cyclohexanol, the reaction is carried out under the conditions of high pressure (3-6 MPa) and long reaction time (6-10 h), and the conversion rate of guaiacol and cyclohexanol selectivity are low.
Disclosure of Invention
The invention aims to improve the catalytic activity of a Co-based catalyst, improve the yield of cyclohexanol and reduce the reaction energy consumption, and a core-shell type catalyst with high catalytic activity for catalyzing hydrogenation and deoxidation of guaiacol to prepare cyclohexanol is prepared, and in order to realize the aim, the technical scheme of the invention is as follows:
a preparation method of a core-shell type catalyst for catalyzing hydrogenation deoxidation of guaiacol to prepare cyclohexanol comprises the following steps:
(1) preparing two parts of hexadecyl trimethyl ammonium bromide (CTAB) aqueous solution with equal volume, wherein one part contains hydrazine hydrate, and the other part contains a cobalt source precursor and a sodium hydroxide solution which are measured;
wherein the concentration of Cetyl Trimethyl Ammonium Bromide (CTAB) in the solution is 0.1 mol/L; the precursor of the cobalt source is Co (NO)3)2·6H2O, the concentration of the sodium hydroxide solution is 1 mol/L;
(2) mixing the prepared two parts of Cetyl Trimethyl Ammonium Bromide (CTAB) aqueous solutions, and mechanically stirring for 1-2 hours at 80 ℃;
(3) and (3) taking out the product obtained in the step (2), alternately washing the product for 2-3 times by using ethanol and deionized water, and carrying out vacuum drying at 50 ℃ overnight to obtain the Co nanoparticles.
(4) Dispersing the Co nano particles obtained in the step (3) in a mixed solution of deionized water and ethanol;
(5) preparing a metal carrier precursor and a silicon source precursor into a mixed solution, adding the mixed solution and an alkali solution into the suspension obtained in the step (4) in a parallel flow manner under mechanical stirring at the temperature of 60-80 ℃, and stirring for 0.5 h;
wherein, the metal carrier precursor is nitrate, acetate or chloride of M, wherein, M is Ce, Ti and Al; the precursor of the silicon source is Na2SiO3·9H2O; the alkali solution is (NH)4)2CO3Solution, Na2CO3One of the solutions;
(6) taking out the obtained precipitate, filtering, washing to neutrality, placing the precipitate in n-butyl alcohol, stirring and evaporating at 50 ℃, placing the precipitate in an oven at 100 ℃ for 12 hours, and reducing the catalyst in hydrogen flow at 400-450 ℃ for 3-4 hours before use to obtain the core-shell type catalyst Co @ MxOy-SiO2；
The mass fraction of Co in the obtained core-shell type catalyst is 10 percent, and M isxOy:SiO2The mass ratio of (A) to (B) is 1:2 to 3.
The invention also provides an application of the core-shell catalyst, which comprises the following specific steps:
adding 0.2-0.4 g of catalyst into a fixed bed tubular reactor, introducing a guaiacol raw material and hydrogen, reacting at 160-220 ℃, under the reaction pressure of 2MPa for 2-4 h, and collecting generated cyclohexanol, wherein the catalyst is the core-shell catalyst.
Wherein hydrogen gasVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1。
The preparation method of the core-shell catalyst has the beneficial effects that:
the invention firstly utilizes a solvent reduction method to prepare cobalt nanoparticles, and then utilizes a post-synthesis method to prepare cobalt nanoparticles with Co as a core and M as a corexOy-SiO2Co @ M as shellxOy-SiO2A core-shell catalyst. The purpose of introducing silica into the shell is to increase the specific surface area of the support, and more lewis acid sites can be obtained by calcination. The purpose of introducing the M oxide is to ensure that the catalyst can form more oxygen vacancies after roasting reduction, which is beneficial to the breaking of C-O bonds and improves the yield of cyclohexanol.
The catalyst has low cost and simple preparation method, and the prepared core-shell catalyst has good stability, can still keep good catalytic activity after a long-time reaction, and obtains cyclohexanol with higher yield in the hydrogenation and deoxidation reaction of guaiacol.
Drawings
Figure 1 is a graph of the conversion of guaiacol over time for two different catalysts.
FIG. 2 shows the catalyst Co @ CeO2-SiO2Transmission electron micrograph (D).
FIG. 3 shows catalyst Co @ TiO2-SiO2Transmission electron micrograph (D).
Detailed Description
The present invention is further described below with reference to examples, but is not limited thereto.
Example 1
A preparation method of a core-shell type catalyst comprises the following steps:
(1) two portions of 20mL, 0.1mol/L are prepared respectivelyCetyl trimethylammonium bromide (CTAB). Wherein one part contains 6g hydrazine hydrate and one part contains 0.54g Co (NO)3)2·6H2O and 1.8mL of 1mol/L NaOH;
(2) mixing the prepared two CTAB solutions, and sealing for 2h at 80 ℃;
(3) taking out the product obtained in the step (2), alternately washing the product with ethanol and deionized water for 2-3 times, and carrying out vacuum drying at 50 ℃ overnight to obtain 0.11g of Co nanoparticles;
(4) preparing Co nanoparticles for many times, and dispersing 0.31g of Co nanoparticles in a mixed solution of 80mL of deionized water and 20mL of ethanol;
(5) 1.724g Ce (CH)3COO)3、8.83g Na2SiO3·9H2O was dissolved in 50mL of deionized water to obtain 6.5g (NH)4)2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 60 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol at 50 ℃, stirring, evaporating to dryness, placing in an oven at 100 ℃ for 12h, and reducing the catalyst in hydrogen flow at 400 ℃ for 3h before use to obtain Co @ CeO2-SiO2The core-shell catalyst has an active component Co mass fraction of 10 percent and mCeO2:mSiO2＝1:2。
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ CeO was added2-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 100%, and the yield of the cyclohexanol is 94.5%. After 480h, the guaiacol conversion was 97.2%.
Example 2
(1) - (3) same as in example 1;
(4) preparing Co nano particles for multiple times, taking 0.187g of Co, and the rest is the same as example 1 (4);
(5) 1.32g of TiCl4、5.30g Na2SiO3·9H2Dissolving O in 50mL deionized water, and taking 5g of Na2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 80 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol at 50 ℃, stirring, evaporating to dryness, placing in an oven at 100 ℃ for 12h, reducing the catalyst in hydrogen flow at 400 ℃ for 3h before use to obtain Co @ TiO2-SiO2The core-shell catalyst has an active component Co mass fraction of 10 percent and mTiO2:mSiO2＝1:2。
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ TiO was added2-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 99.4%, and the yield of the cyclohexanol is 92.3%. After 480h, the guaiacol conversion was 95.8%.
Example 3
(1) - (3) same as in example 1;
(4) co nanoparticles were prepared several times, taking 0.125g Co, the rest being the same as example (1);
(5) 2.72g of Al (NO)3)3·9H2O、3.5g Na2SiO3·9H2Dissolving O in 50mL deionized water, and taking 5g of Na2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 60 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol at 50 ℃, stirring, evaporating to dryness, placing in an oven at 100 ℃ for 12h, and reducing the catalyst in hydrogen flow at 400 ℃ for 3h before use to obtain Co @ Al2O3-SiO2Core-shell catalysts, active groupsThe mass fraction of Co is 10 percent, and the mass fraction of mAl2O3: mSiO2 is 1: 2.
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ Al was added2O3-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 95.6%, and the yield of the cyclohexanol is 87.8%. After 480h, the guaiacol conversion was 91.5%.
Example 4
(1) - (3) same as in example 1;
(4) preparing Co nano particles for many times, taking 0.32g of Co nano particles, and the rest is the same as the example (1);
(5) 1.33g of Ce (CH)3COO)3、10.22g Na2SiO3·9H2O was dissolved in 50mL of deionized water, and 8g of Na was taken2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 60 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol at 50 ℃, stirring, evaporating to dryness, placing in an oven at 100 ℃ for 12h, and reducing the catalyst in hydrogen flow at 400 ℃ for 3h before use to obtain Co @ CeO2-SiO2The core-shell catalyst has an active component Co mass fraction of 10 percent and mAl2O3:mSiO2＝1:3。
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ CeO was added2-SiO2(1:3) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 99.1%, and the yield of the cyclohexanol is 92.9%.
Example 5
(1) - (3) same as in example 1;
(4) preparing Co nano particles for many times, taking 0.25g of Co nano particles, and the rest is the same as the example (1);
(5) 1.32g of TiCl4、7.95g Na2SiO3·9H2O was dissolved in 50mL of deionized water, and 6g of Na was taken2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 80 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol at 50 ℃, stirring, evaporating to dryness, placing in an oven at 100 ℃ for 12h, reducing the catalyst in hydrogen flow at 400 ℃ for 3h before use to obtain Co @ TiO2-SiO2The core-shell catalyst has an active component Co mass fraction of 10 percent and mTiO2:mSiO2＝1:3。
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ TiO was added2-SiO2(1:3) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 98.5%, and the yield of the cyclohexanol is 91.8%.
Example 6
(1) - (3) same as in example 1;
(4) co nanoparticles were prepared several times, and 0.164g of Co nanoparticles was collected, and the remainder was the same as in example (1)
(5) 2.72g of Al (NO)3)3·9H2O、5.25g Na2SiO3·9H2Dissolving O in 50mL deionized water, and taking 5g of Na2CO3Dissolving in 50mL of deionized water, adding the two into the suspension in the step (4) in a parallel flow manner under the condition of mechanical stirring at 60 ℃, and keeping for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol, stirring at 50 deg.C, evaporating to dryness, placing in oven at 100 deg.C for 12 hr, and using catalystReducing the mixture for 3 hours at 400 ℃ in hydrogen flow to obtain Co @ Al2O3-SiO2The core-shell catalyst has an active component Co mass fraction of 10 percent and mAl2O3:mSiO2＝1:3。
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ Al was added2O3-SiO2(1:3) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 94.7%, and the yield of the cyclohexanol is 86.7%.
Example 7
(1) - (6) same as in example 1.
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ CeO was added2-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 4h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 100%, and the yield of the cyclohexanol is 95.7%.
Example 8
(1) - (6) same as in example 2.
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ TiO was added2-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 99.5%, and the yield of the cyclohexanol is 92.3%.
Example 9
(1) - (6) same as in example 3;
the core-shell catalyst was used as follows:
in a fixed bed tubeIn a reactor, 0.2g of Co @ Al was charged2O3-SiO2(1:2) catalyst, the reaction temperature is 220 ℃, the reaction pressure is 2MPa, the reaction time is 2h, and hydrogen is addedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 96.3%, and the yield of the cyclohexanol is 88.9%.
Comparative example 1
(1) - (4) same as in example 1;
(5) no Na addition2SiO3·9H2O，Ce(CH3COO)3The mass was 5.16g, (NH)4)2CO3The weight was 3g, as in example 1;
(6) co @ CeO was prepared as in example 12A core-shell catalyst.
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ CeO was added2Catalyst, reaction temperature is 220 ℃, reaction pressure is 2MPa, reaction time is 2h, and hydrogen is usedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 97.8%, and the yield of the cyclohexanol is 90.9%.
Comparative example 2
(1) - (4) same as in example 1;
(5) no addition of Ce (CH)3COO)3，Na2SiO3·9H2The mass of O is 13.25g, Na2CO3Mass 6.5g, the rest being as in example 1;
(6) co @ SiO prepared as in example 32A core-shell catalyst.
The core-shell catalyst was used as follows:
in a fixed bed tubular reactor, 0.2g of Co @ SiO was added2Catalyst, reaction temperature is 220 ℃, reaction pressure is 2MPa, reaction time is 2h, and hydrogen is usedVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1Collecting the generated mixed product of cyclohexanol and the like, wherein the guaiacol isThe conversion of (a) was 93.7% and the yield of cyclohexanol was 85.6%.
Comparative example 3
(1) 1.724g Ce (CH)3COO)3、8.83g Na2SiO3·9H2O was dissolved in 50mL of deionized water to obtain 6.5g (NH)4)2CO3Dissolving in 50ml deionized water to prepare a solution;
(2) under the condition of stirring at 60 ℃, dropwise adding the two into 100mL of deionized water at the same time, and stirring for 0.5 h;
(3) taking out the product obtained in the step (2) and filtering and washing to be neutral;
(4) dispersing the precipitate obtained in the step (3) into 100mL of n-butanol, stirring and evaporating at 50 ℃, placing in an oven for drying at 100 ℃ overnight to prepare CeO2-SiO2(1:2) a carrier;
(2) weighing 1.53g Co (NO)3)2·6H2O, preparing an equal volume of solution to be impregnated into CeO2-SiO2In a carrier, and then dried at 100 ℃;
(3) the catalyst is roasted for 3 hours at 400 ℃, and then reduced for 3 hours in hydrogen flow to prepare 10 percent Co/CeO2-SiO2(1:2) a catalyst.
The application of the catalyst is as follows:
in a fixed bed tubular reactor, 0.2g of Co/CeO was added2-SiO2(1:2) catalyst, reaction temperature is 220 ℃, reaction pressure is 2MPa, reaction time is 2.5h, hydrogenVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1And collecting the generated mixed products of cyclohexanol and the like, wherein the conversion rate of the guaiacol is 99.3%, and the yield of the cyclohexanol is 93.6%. After 480h, the guaiacol conversion was 85.5%.
Table 1 shows cyclohexanol yield data over 220 ℃ catalyst.
Claims (8)
1. The preparation method of the core-shell catalyst is characterized by comprising the following steps:
(1) preparing two parts of hexadecyl trimethyl ammonium bromide aqueous solution with the same volume; one part of the hydrazine hydrate contains a cobalt source precursor and a sodium hydroxide solution which are measured;
(2) mixing two parts of the hexadecyl trimethyl ammonium bromide solution prepared in the step (1), and mechanically stirring for 1-2 hours at 80 ℃;
(3) taking out the product obtained in the step (2), alternately washing the product for 2-3 times by using ethanol and deionized water, and carrying out vacuum drying overnight at 50 ℃ to obtain Co nanoparticles;
(4) dispersing the Co nano particles obtained in the step (3) in a mixed solution of deionized water and ethanol to obtain a suspension;
(5) preparing a metal carrier precursor and a silicon source precursor into a mixed solution, and under the condition of mechanical stirring at the temperature of 60-80 ℃, adding the mixed solution and an alkali solution into the suspension liquid obtained in the step (4) in a parallel flow manner, and keeping the mixed solution for 0.5 h;
(6) taking out the precipitate obtained in the step (5), filtering, washing to neutrality, placing in n-butanol, stirring at 50 ℃, evaporating to dryness, placing in an oven at 100 ℃ for 12h, and reducing the catalyst in hydrogen flow before use to obtain Co @ MxOy-SiO2A core-shell catalyst.
2. The method of claim 1, wherein the cobalt source precursor in step (1) is Co (NO)3)2·6H2O, the concentration of the sodium hydroxide solution is 1mol/L, and the concentration of the hexadecyl trimethyl ammonium bromide in the solution is 0.1 mol/L.
3. The method for preparing the core-shell catalyst according to claim 1, wherein the metal carrier precursor in step (5) is a nitrate, acetate or chloride of metal M, wherein M is Ce, Ti, Al; the precursor of the silicon source is Na2SiO3·9H2O。
4. According to claim 1The preparation method of the core-shell catalyst is characterized in that the alkali solution in the step (5) is (NH)4)2CO3Solution, Na2CO3One of the solutions.
5. The preparation method of the core-shell catalyst according to claim 1, wherein the reduction temperature in the step (6) is 400-450 ℃, and the reduction time is 3-4 h; in preparation of Co @ MxOy-SiO2In the core-shell type catalyst, the mass fraction of Co is 10%, MxOy:SiO2The mass ratio of (A) to (B) is 1: 2-3.
6. Use of a core-shell catalyst prepared according to any one of claims 1 to 5 for the preparation of cyclohexanol by hydrodeoxygenation of guaiacol.
7. The use of a core-shell catalyst according to claim 6, wherein the catalyst is introduced into a fixed bed tubular reactor, the guaiacol feedstock and hydrogen gas are introduced, and the product is collected.
8. The use of the core-shell catalyst of claim 7 wherein the catalyst is used in an amount of 0.2 to 0.4g hydrogenVolume ofRaw materialsVolume of800L/L and space velocity of 0.7h-1The reaction temperature is 160-220 ℃, the reaction pressure is 2MPa, and the reaction time is 2-4 h.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010961675.8A CN111992213B (en) | 2020-09-14 | 2020-09-14 | Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010961675.8A CN111992213B (en) | 2020-09-14 | 2020-09-14 | Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111992213A true CN111992213A (en) | 2020-11-27 |
| CN111992213B CN111992213B (en) | 2023-04-11 |
Family
ID=73469293
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010961675.8A Active CN111992213B (en) | 2020-09-14 | 2020-09-14 | Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111992213B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114870853A (en) * | 2022-06-23 | 2022-08-09 | 广东石油化工学院 | Core-shell catalyst for preparing cyclohexanol by catalyzing selective hydrogenation and deoxidation of guaiacol |
| CN115779980A (en) * | 2022-12-08 | 2023-03-14 | 常州大学 | Ni/CeO 2 Application of-Rh catalyst in reaction for preparing cyclohexanol by selective hydrogenation of guaiacol |
| CN115888719A (en) * | 2022-10-31 | 2023-04-04 | 华南理工大学 | Magnesium oxide modified aluminum oxide loaded bimetallic nickel-cobalt catalyst and preparation method and application thereof |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109529857A (en) * | 2018-12-10 | 2019-03-29 | 江苏大学 | Ni@SiO2@CeO2The preparation method of nucleocapsid catalyst and its application in methane carbon dioxide reformation |
-
2020
- 2020-09-14 CN CN202010961675.8A patent/CN111992213B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109529857A (en) * | 2018-12-10 | 2019-03-29 | 江苏大学 | Ni@SiO2@CeO2The preparation method of nucleocapsid catalyst and its application in methane carbon dioxide reformation |
Non-Patent Citations (2)
| Title |
|---|
| 孔韡等: "复合氧化物负载的Ni基催化剂上愈创木酚加氢脱氧性能", 《高等学校化学学报》 * |
| 肖凤等: "纳米Ni/SiO2核壳结构粒子的制备和表征", 《青岛科技大学学报(自然科学版)》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114870853A (en) * | 2022-06-23 | 2022-08-09 | 广东石油化工学院 | Core-shell catalyst for preparing cyclohexanol by catalyzing selective hydrogenation and deoxidation of guaiacol |
| CN114870853B (en) * | 2022-06-23 | 2023-09-26 | 广东石油化工学院 | Core-shell catalyst for preparing cyclohexanol by catalyzing guaiacol to be subjected to selective hydrodeoxygenation |
| CN115888719A (en) * | 2022-10-31 | 2023-04-04 | 华南理工大学 | Magnesium oxide modified aluminum oxide loaded bimetallic nickel-cobalt catalyst and preparation method and application thereof |
| CN115779980A (en) * | 2022-12-08 | 2023-03-14 | 常州大学 | Ni/CeO 2 Application of-Rh catalyst in reaction for preparing cyclohexanol by selective hydrogenation of guaiacol |
| CN115779980B (en) * | 2022-12-08 | 2024-02-13 | 常州大学 | Ni/CeO 2 Application of Rh catalyst in selective hydrogenation of guaiacol to preparation of cyclohexanol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111992213B (en) | 2023-04-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111992213B (en) | Preparation method of core-shell catalyst for preparing cyclohexanol by catalytic hydrogenation and deoxidation of guaiacol | |
| CN111167440B (en) | Catalyst for ammonia borane hydrolysis hydrogen evolution and preparation method thereof | |
| CN114829004B (en) | Method for preparing Ni-X-based oxide catalyst and application of Ni-X-based oxide catalyst in transfer hydrogenation | |
| CN110280250B (en) | Preparation method and application of zeolite imidazole framework material derived metal oxide | |
| CN110368933B (en) | Ruthenium-based ammonia synthesis catalyst with Ce-Ti composite oxide as carrier and preparation method thereof | |
| CN112624917B (en) | Method for producing crotonic acid by catalytic oxidation method | |
| CN112755996A (en) | Catalyst for synthesizing methanol by carbon dioxide hydrogenation, preparation method and application | |
| CN113101964B (en) | Mesoporous cerium oxide photocatalyst and preparation method and application thereof | |
| CN114522688A (en) | Porous carbon loaded bimetallic catalyst and preparation and application thereof | |
| CN107899583A (en) | It is a kind of to prepare catalyst of ethanol and preparation method thereof for methyl methanol syngas | |
| CN114804997B (en) | Preparation method of cyclohexylbenzene and corresponding metal catalyst | |
| WO2020010646A1 (en) | Nano titanium dioxide composite particle and preparation method thereof | |
| CN115837275A (en) | Perovskite type high-entropy oxide and preparation method and application thereof | |
| CN114950439A (en) | Efficient water photolysis hydrogen production MOF TiO 2 -NiO material and preparation method and application thereof | |
| CN112441922B (en) | Method for preparing oxalate through CO oxidative coupling, catalyst and preparation method thereof | |
| CN113083325A (en) | Catalyst Ru for ammonia borane hydrolysis hydrogen production1-xCox/P25 and preparation method thereof | |
| CN111974409A (en) | Flaky porous manganese-doped nickel oxide catalyst, preparation method and application thereof | |
| CN111420657A (en) | Ru-based catalyst for synthesizing 3-pentanone through ethylene conversion and preparation method and application thereof | |
| CN112517021B (en) | Cobalt-doped modified tin dioxide catalyst, preparation method and application thereof | |
| CN107224980B (en) | Preparation method of carbon dioxide methanation catalyst without reduction activation | |
| CN107486210A (en) | A kind of catalyst for acetic acid one-step method ethanol and preparation method thereof | |
| CN115582124B (en) | Copper-based catalyst and preparation method and application thereof | |
| CN112264008B (en) | Pd/TiO 2 - {100} composite catalyst and preparation method and application thereof | |
| CN110479259B (en) | Supported Ru-based catalyst with molybdenum oxide-zinc oxide-zirconium oxide composite oxide as carrier | |
| CN114192142B (en) | Catalyst for dinonyl phenol hydrogenation and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |