CN107456988B - A kind of molybdenum nitride hydrogenation deoxidation catalyst and its preparation method and application - Google Patents

A kind of molybdenum nitride hydrogenation deoxidation catalyst and its preparation method and application Download PDF

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CN107456988B
CN107456988B CN201710696453.6A CN201710696453A CN107456988B CN 107456988 B CN107456988 B CN 107456988B CN 201710696453 A CN201710696453 A CN 201710696453A CN 107456988 B CN107456988 B CN 107456988B
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hydrogenation deoxidation
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hydrogen
molybdenum nitride
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CN107456988A (en
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鲁墨弘
魏斌
杜虎
李明时
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Changzhou University
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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
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/24—Nitrogen compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • C10G3/44—Catalytic treatment characterised by the catalyst used
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/50—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids in the presence of hydrogen, hydrogen donors or hydrogen generating compounds
    • 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
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

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  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

The present invention has studied a kind of support type Nitrides Catalysts and preparation method thereof.The catalyst is that active component is supported on carrier by carrier using equi-volume impregnating with mesoporous carbon (MC), and the presoma of catalyst is obtained after drying, obtained presoma is first carbonized the Nitrides Catalysts for nitrogenizing loaded again.The catalyst that this method is prepared reacts activity with higher to guaiacol hydrogenation deoxidation, to benzene selectivity with higher.

Description

A kind of molybdenum nitride hydrogenation deoxidation catalyst and its preparation method and application
Technical field
The invention belongs to catalyst technical field, more particularly to a kind of for being catalyzed guaiacol selective hydrogenation deoxidation Catalyst.
Background technique
The non-renewable and its a large amount of consumption of fossil fuel causes energy resource supply to be becoming tight and the continuous deterioration of ecological environment, Cause the concern of people's environmentally friendly renewable energy research and development.In this context, to important renewable resource The research of lignocellulose-like biomass be paid more and more attention.Lignin is the main composition portion of lignocellulose-like biomass Point, it is the Main By product of lignocellulose biomass by hydrolyzation fermentation ethanol industry and paper industry processed, due to that cannot fill Divide and utilize, becomes environmental contaminants, have seriously polluted the environment.Therefore from environmental protection and the strategy of sustainable development, benefit Alkane fuel is produced with lignin, has both the double meaning of efficent use of resources and Environment control.
Lignin is a kind of natural polymers being made of phenylpropyl alcohol alkyl structure, can be with by directional catalyzing cracking Obtain the product liquid rich in aromatic rings.But wherein contain a large amount of containing oxygen derivative, especially a large amount of guaiacol base junction The phenol derivatives compound of structure.Its temperature is low, viscosity is big, unstable, corrosivity by force cannot directly as fuel oil substitute, because This, carries out efficient catalytic hydrogenation deoxidation process (HDO) to lignin depolymerization product, is the necessary of production high-quality biological oil Approach.
In early days, the hydrogenation deoxidation treatment process of bio oil is this to urge mainly using NiMo, CoMo of vulcanization as catalyst Agent has good hydrogenation deoxidation effect, and the General Promotion of bio oil performance indicator may be implemented.However the active metal of vulcanization Catalyst has unstability, there is the generation of many by-products.And sulfide catalyst can introduce sulfur-containing compound, so that producing Object reduces, and to overcome the deficiency, researcher is by noble metal alternatively object, such as Rh, Pt of load, Pd etc., but noble metal price It is expensive, being widely used for it is limited to a certain extent.
Summary of the invention
For shortcoming and defect of the existing technology, the present invention is prepared for a kind of relatively inexpensive transitional metal nitride molybdenum Catalyst carries out hydrogenation deoxidation research to guaiacol, by using mesoporous carbon as carrier, with for active component, using isometric leaching Stain method, active component is supported on carrier, and the presoma of catalyst is obtained after drying, then by obtained presoma elder generation Carbonization nitrogenizes to obtain Nitrides Catalysts again.Nitrides Catalysts prepared by the present invention are not only cheap, but also have good Hydrogenation deoxidation effect, have very high productive value.
The present invention is to guaiacol compound (being the containing oxygen derivative that can most represent lignin cracking compound characteristic) Progress hydrogenation deoxidation can effectively improve the selectivity to benzene using the molybdenum nitride of synthesis as catalyst for target.
Molybdenum nitride hydrogenation deoxidation catalyst provided by the invention, the catalyst is using mesoporous carbon (MC) as carrier, with nitrogen Change molybdenum as active component, wherein active component accounts for the 5%~50% of catalyst quality in terms of molybdenum trioxide quality.
The present invention also provides a kind of preparation method of Nitrides Catalysts, the preparation method uses incipient impregnation The salting liquid of molybdenum is supported on the carrier of catalyst by method, and by drying, being first carbonized, it is obtained to nitrogenize again.
The equi-volume impregnating prepares Nitrides Catalysts, and specific step is as follows:
A. mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance, then the water absorption rate according to mesoporous carbon (MC) accurately weighs Jie Hole carbon is used as impregnated carrier after drying and roasting；
B. ammonium molybdate is dissolved in pure water, obtains maceration extract；
C. it by the maceration extract that step (b) obtains and the impregnated carrier incipient impregnation that step (a) obtains, impregnates at room temperature 12h obtains the presoma of catalyst after dry；
D. the catalyst precursor that step (c) obtains first is carbonized and nitrogenizes to obtain Nitrides Catalysts again；
Wherein, in catalyst of the present invention, carrier mesoporous carbon (MC), SBA-15, Ce-SBA-15 can use existing commercially available quotient Product, can also be by prior art preparation.
Drying condition described in step (c) are as follows: dry 1~12h at 100~120 DEG C in drying box；
Presoma described in step (d) is first carbonized the multi-stage procedure Elevated Temperature Conditions nitrogenized again are as follows: under the atmosphere of hydrogen Temperature rate rises to 350 DEG C from room temperature for 5~10 DEG C/min, is that 0.5~1 DEG C/min is warming up to 450 from 350 DEG C with heating rate DEG C, it is that 2~10 DEG C/min rises to 650 DEG C~750 DEG C ammonification final temperatures from 450 DEG C with heating rate, converts ammonia for hydrogen at this time Gas keeps 1 in nitridation final temperature~5 hours.
Hydrogenation deoxidation of the Nitrides Catalysts prepared by the present invention for guaiacol reacts, and its step are as follows: more to create The wooden phenol is raw material, under the conditions of existing for the solvent and catalyst, hydrogen is added and carries out catalysis reaction.
Preferably, the reaction condition are as follows: reaction temperature is 300~400 DEG C, and hydrogen reaction pressure is 2~5MPa.
Preferably, the solvent is decane, the mass ratio of guaiacol and decane is 1: 50~1: 100.
Preferably, the liquid hourly space velocity (LHSV) (LHSV) of reaction raw materials is 2~10h-1。
Beneficial effects of the present invention:
1, the catalyst in the present invention is by the way that in hydrogen reduction, Mo reacts Mr. with the C in carrier mesoporous carbon At molybdenum carbide, ammonia then is converted by hydrogen when final temperature, molybdenum carbide is converted into the higher molybdenum nitride of activity, in the system of catalyst Mesoporous carbon is not only used as carrier during standby, but also as reactant, therefore catalyst reaction activity obtained is higher, to guaiacol With good hydrogenation deoxidation effect, to benzene selectivity with higher.
2, the present invention is that 2~10 DEG C/min rises to 650 DEG C~750 DEG C ammonification final temperatures from 450 DEG C with heating rate, this temperature Degree range ensure that molybdenum carbide can effectively be converted into molybdenum nitride, while the molybdenum nitride reaction with higher generated also being made to live Property.
3, the catalyst carrier in the present invention selects mesoporous carbon, and suitable duct is conducive to reduce inside diffusional resistance, mention High reaction rate；Active component molybdenum nitride has the property of class noble metal, and hydrogenation deoxidation activity is high, good to the selectivity of benzene.
Specific embodiment
In order to further illustrate the present invention, following embodiment is enumerated.
Embodiment 1
The preparation of catalyst
Water absorption rate according to mesoporous carbon (MC) (mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance) accurately weighs carrier, roasts through dry It is used as impregnated carrier after burning, 0.27g ammonium molybdate is dissolved in pure water, maceration extract is obtained；By the bodies such as maceration extract and impregnated carrier Product dipping impregnates 12h at room temperature, obtains the presoma of catalyst after dry；The presoma that will be obtained carries out multistage journey Sequence temperature reaction；Temperature rate is that 5 DEG C/min from room temperature rises to 350 DEG C under the atmosphere of hydrogen, with warm rate be 1 DEG C/min from 350 DEG C are warming up to 450 DEG C, are that 5 DEG C/min rises to 700 DEG C of final temperatures from 450 DEG C with heating rate, convert ammonia for hydrogen at this time Gas is kept for 2 hours in final temperature, obtains 10%MoN/MC catalyst.
In fixed bed reactors, 10%MoN/MC catalyst 2ml, the liquid hourly space velocity (LHSV) of reaction raw materials is added
(LHSV)3h-1, being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature Reach 300 DEG C of reactions, reaction product is finally taken out, using gas chromatographic analysis.
Embodiment 2
0.27g ammonium molybdate in embodiment 1 is replaced with 0.54g ammonium molybdate, other steps are the same as embodiment 1.
Embodiment 3
0.27g ammonium molybdate in embodiment 1 is replaced with 0.82g ammonium molybdate, other steps are the same as embodiment 1.
Embodiment 4
0.27g ammonium molybdate in embodiment 1 is replaced with 1.08g ammonium molybdate, other steps are the same as embodiment 1.
Comparative example 1
The preparation of catalyst
Water absorption rate according to SBA-15 accurately weighs carrier, impregnated carrier is used as after drying and roasting, by 0.27g ammonium molybdate It is dissolved in pure water, obtains maceration extract；By maceration extract and impregnated carrier incipient impregnation, 12h is impregnated at room temperature, is after dry Obtain the presoma of catalyst；The presoma that will be obtained carries out multi-stage procedure temperature reaction；The temperature speed under the atmosphere of hydrogen Rate rises to 350 DEG C from room temperature for 5 DEG C/min, is that 1 DEG C/min is warming up to 450 DEG C from 350 DEG C with warm rate, with heating rate for 5 DEG C/min rises to 700 DEG C of final temperatures from 450 DEG C, converts ammonia for hydrogen at this time, it is kept for 2 hours in final temperature, obtains 10%MoN/ SBA-15 catalyst.
In fixed bed reactors, 10%MoN/SBA-15 catalyst 2ml, the liquid hourly space velocity (LHSV) (LHSV) of reaction raw materials is added 3h-1, being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C of reactions, Reaction product is finally taken out, using gas chromatographic analysis.
Comparative example 2
0.27g ammonium molybdate in comparative example 1 is replaced with 0.54g ammonium molybdate, other steps are the same as comparative example 1.
Comparative example 3
0.27g ammonium molybdate in comparative example 1 is replaced with 0.82g ammonium molybdate, other steps are the same as comparative example 1.
Comparative example 4
0.27g ammonium molybdate in comparative example 1 is replaced with 1.08g ammonium molybdate, other steps are the same as comparative example 1.
Comparative example 5
The preparation of catalyst
Water absorption rate according to Ce-SBA-15 accurately weighs carrier, impregnated carrier is used as after drying and roasting, by 0.27g molybdenum Sour ammonium is dissolved in pure water, obtains maceration extract；By maceration extract and impregnated carrier incipient impregnation, 12h is impregnated at room temperature, it is dry The presoma of catalyst is obtained afterwards；The presoma that will be obtained carries out multi-stage procedure temperature reaction；It is warm under the atmosphere of hydrogen Degree rate rises to 350 DEG C from room temperature for 5 DEG C/min, is that 1 DEG C/min is warming up to 450 DEG C from 350 DEG C with warm rate, with heating rate 700 DEG C of final temperatures are risen to from 450 DEG C for 5 DEG C/min, convert ammonia for hydrogen at this time, are kept for 2 hours in final temperature, are obtained 10% MoN/Ce-SBA-15 catalyst.
In fixed bed reactors, 10%MoN/Ce-SBA-15 catalyst 2ml, the liquid hourly space velocity (LHSV) of reaction raw materials is added (LHSV)3h-1, being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C reaction, reaction product is finally taken out, using gas chromatographic analysis.
Comparative example 6
0.27g ammonium molybdate in comparative example 5 is replaced with 0.54g ammonium molybdate, other steps are the same as comparative example 5.
Comparative example 7
0.27g ammonium molybdate in comparative example 5 is replaced with 0.82g ammonium molybdate, other steps are the same as comparative example 5.
Comparative example 8
0.27g ammonium molybdate in comparative example 5 is replaced with 1.08g ammonium molybdate, other steps are the same as comparative example 5.
Comparative example 9
The preparation of catalyst
Water absorption rate according to mesoporous carbon (MC) (mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance) accurately weighs carrier, roasts through dry It is used as impregnated carrier after burning, 0.27g ammonium molybdate is dissolved in pure water, maceration extract is obtained；By the bodies such as maceration extract and impregnated carrier Product dipping impregnates 12h at room temperature, obtains the presoma of catalyst after dry；The presoma that will be obtained carries out multistage journey Sequence temperature reaction；Temperature rate is that 5 DEG C/min from room temperature rises to 350 DEG C under the atmosphere of hydrogen, with warm rate be 1 DEG C/min from 350 DEG C are warming up to 450 DEG C, are that 5 DEG C/min rises to 500 DEG C of final temperatures from 450 DEG C with heating rate, convert ammonia for hydrogen at this time Gas is kept for 2 hours in final temperature, obtains 10%MoN/MC catalyst.
In fixed bed reactors, 10%MoN/MC catalyst 2ml, liquid hourly space velocity (LHSV) (LHSV) 3h of reaction raw materials is added-1, Being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C of reactions, finally Reaction product is taken out, using gas chromatographic analysis.
Comparative example 10
The preparation of catalyst
Water absorption rate according to mesoporous carbon (MC) (mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance) accurately weighs carrier, roasts through dry It is used as impregnated carrier after burning, 0.27g ammonium molybdate is dissolved in pure water, maceration extract is obtained；By the bodies such as maceration extract and impregnated carrier Product dipping impregnates 12h at room temperature, obtains the presoma of catalyst after dry；The presoma that will be obtained carries out multistage journey Sequence temperature reaction；Temperature rate is that 5 DEG C/min from room temperature rises to 350 DEG C under the atmosphere of hydrogen, with warm rate be 1 DEG C/min from 350 DEG C are warming up to 450 DEG C, are that 5 DEG C/min rises to 600 DEG C of final temperatures from 450 DEG C with heating rate, convert ammonia for hydrogen at this time Gas is kept for 2 hours in final temperature, obtains 10%MoN/MC catalyst.
In fixed bed reactors, 10%MoN/MC catalyst 2ml, liquid hourly space velocity (LHSV) (LHSV) 3h of reaction raw materials is added-1, Being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C of reactions, finally Reaction product is taken out, using gas chromatographic analysis.
Comparative example 11
The preparation of catalyst
Water absorption rate according to mesoporous carbon (MC) (mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance) accurately weighs carrier, roasts through dry It is used as impregnated carrier after burning, 0.27g ammonium molybdate is dissolved in pure water, maceration extract is obtained；By the bodies such as maceration extract and impregnated carrier Product dipping impregnates 12h at room temperature, obtains the presoma of catalyst after dry；The presoma that will be obtained carries out multistage journey Sequence temperature reaction；Temperature rate is that 5 DEG C/min from room temperature rises to 350 DEG C under the atmosphere of hydrogen, with warm rate be 1 DEG C/min from 350 DEG C are warming up to 450 DEG C, are that 5 DEG C/min rises to 800 DEG C of final temperatures from 450 DEG C with heating rate, convert ammonia for hydrogen at this time Gas is kept for 2 hours in final temperature, obtains 10%MoN/MC catalyst.
In fixed bed reactors, 10%MoN/MC catalyst 2ml, liquid hourly space velocity (LHSV) (LHSV) 3h of reaction raw materials is added-1, Being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C of reactions, finally Reaction product is taken out, using gas chromatographic analysis.
Comparative example 12
The preparation of catalyst
Water absorption rate according to mesoporous carbon (MC) (mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance) accurately weighs carrier, roasts through dry It is used as impregnated carrier after burning, 0.27g ammonium molybdate is dissolved in pure water, maceration extract is obtained；By the bodies such as maceration extract and impregnated carrier Product dipping impregnates 12h at room temperature, obtains the presoma of catalyst after dry；The presoma that will be obtained carries out multistage journey Sequence temperature reaction；Temperature rate is that 5 DEG C/min from room temperature rises to 350 DEG C under the atmosphere that nitrogen and hydrogen volume are 1:3, with temperature Rate is warming up to 450 DEG C from 350 DEG C for 1 DEG C/min, is that 5 DEG C/min rises to 700 DEG C of final temperatures from 450 DEG C with heating rate, at this time Ammonia is converted by hydrogen, is kept for 2 hours in final temperature, obtains 10%MoN/MC catalyst.
In fixed bed reactors, 10%MoN/MC catalyst 2ml, liquid hourly space velocity (LHSV) (LHSV) 3h of reaction raw materials is added-1, Being filled with hydrogen makes the reaction pressure of reaction system reach 2.0MPa, and heating reaction furnace makes reaction temperature reach 300 DEG C of reactions, finally Reaction product is taken out, using gas chromatographic analysis.
Catalyst made from 1 embodiment and comparative example of table compares the performance of guaiacol hydrogenation deoxidation
Table 1 illustrates that the support type Nitrides Catalysts of this method preparation react with higher to guaiacol hydrogenation deoxidation Activity and to benzene selectivity with higher.
It should be understood that for those of ordinary skills, it can be modified or changed according to the above description, And all these modifications and variations should all belong to the protection domain of appended claims of the present invention.

Claims (5)

1. a kind of preparation method of molybdenum nitride hydrogenation deoxidation catalyst, it is characterised in that: specific step is as follows for the preparation method:
A. mesoporous carbon is handled with 2M concentrated hydrochloric acid in advance, then accurately weighs mesoporous carbon according to the water absorption rate of mesoporous carbon, passed through Impregnated carrier is used as after drying and roasting；
B. ammonium molybdate is dissolved in pure water, obtains maceration extract；
C. by the maceration extract that step (b) obtains and the impregnated carrier incipient impregnation that step (a) obtains, 12h is impregnated at room temperature, The presoma of catalyst is obtained after drying；
D. the presoma of catalyst step (c) obtained is first carbonized and nitrogenizes to obtain Nitrides Catalysts again；
The presoma is first carbonized the condition nitrogenized again are as follows: temperature rate is 5 ~ 10 DEG C/min from room temperature liter under the atmosphere of hydrogen To 350 DEG C, it is that 0.5 ~ 1 DEG C/min is warming up to 450 DEG C from 350 DEG C with heating rate, is 2 ~ 10 DEG C/min from 450 with heating rate DEG C 650 DEG C ~ 750 DEG C final temperatures are risen to, hydrogen is converted into ammonia at this time, kept for 1 ~ 5 hour in final temperature；
The catalyst is using mesoporous carbon as carrier, using molybdenum nitride as active component, wherein active component is with molybdenum trioxide matter Meter accounts for the 5 ~ 50% of catalyst gross mass.
2. the preparation method of molybdenum nitride hydrogenation deoxidation catalyst as described in claim 1, it is characterised in that: institute in step (c) The drying condition stated are as follows: dry 1 ~ 12h at 100 ~ 120 DEG C in drying box.
3. a kind of application of the molybdenum nitride hydrogenation deoxidation catalyst of method preparation as described in claim 1, it is characterised in that: described Catalyst is used to be catalyzed the hydrogenation deoxidation reaction of guaiacol, and method is as follows: using guaiacol as raw material, in solvent and plus hydrogen Under the conditions of dehydrogenation catalyst is existing, hydrogen is added and carries out hydrogenation deoxidation reaction.
4. the application of molybdenum nitride hydrogenation deoxidation catalyst as claimed in claim 3, it is characterised in that: the hydrogenation deoxidation reaction Condition are as follows: reaction temperature is 300 ~ 400 DEG C, and Hydrogen Vapor Pressure is 1 ~ 4 MPa.
5. the application of molybdenum nitride hydrogenation deoxidation catalyst as claimed in claim 3, it is characterised in that: the solvent is positive ten The mass ratio of alkane, guaiacol and decane is 1: 50 ~ 1: 100.
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