CN102989487A - After-treatment method for molybdenum vanadium tellurium niobium catalyst - Google Patents
After-treatment method for molybdenum vanadium tellurium niobium catalyst Download PDFInfo
- Publication number
- CN102989487A CN102989487A CN2012105521398A CN201210552139A CN102989487A CN 102989487 A CN102989487 A CN 102989487A CN 2012105521398 A CN2012105521398 A CN 2012105521398A CN 201210552139 A CN201210552139 A CN 201210552139A CN 102989487 A CN102989487 A CN 102989487A
- Authority
- CN
- China
- Prior art keywords
- acrylic acid
- catalyst
- propane
- percent
- molybdenum
- 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.)
- Pending
Links
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses an after-treatment method for a molybdenum vanadium tellurium niobium catalyst. The after-treatment method for the baked molybdenum vanadium tellurium niobium catalyst comprises the following steps of: oxidizing the catalyst for a while in a hydrogen peroxide solution with certain concentration, wherein the volume percent concentration of the hydrogen peroxide is 0.5-30 percent, and the treatment time is 0.1-5 hours. The catalyst prepared by a roasting container is used for a reaction for preparing acrylic acid through selective oxidation of propane, and under the optimal treatment conditions, the propane conversion rate and the acrylic acid selectivity are respectively 36.1 percent and 74.6 percent and the acrylic acid yield is 26.9 percent. Compared with a catalyst before being treated with the hydrogen peroxide solution, the catalyst has the advantages that the acrylic acid selectivity is improved by 21.3 percent and the effect is obvious.
Description
Technical field
The invention belongs to organic chemical industry's acrylic acid preparing technical field, be specifically related to a kind of post-processing approach of molybdenum-vanadium-tellurium-niobium catalytic agent.
Background technology
Acrylic acid (Acrylic Acid, be called for short AA) and ester class series of products thereof are very important Organic Chemicals, and they are widely used in the industries such as coating, chemical fibre, weaving, light industry, and oil exploitation, oil dope etc.At present also continually developing new application.
A plurality of developing stage have been experienced in acrylic acid production.1843, JoseplRedtenbach got acrylic acid by acrolein oxidation under the condition that silver oxide exists.Offo Rohm in 1901 has found that the polymer of acrylicacidandesters has important industrial use, and so far acrylicacidandesters has been subject to people and has paid close attention to widely nineteen twenty-seven Rohm﹠amp; Hass company is that raw material makes cyanoethanol with chlorethanol and Cymag, obtains methyl acrylate through dehydration, hydrolysis and methanol esterification again, thereby has begun suitability for industrialized production.Developed successively afterwards the process route of other acrylicacidandesters, at present industrial take the propylene two-step oxidizing process as main.But the propylene cost is higher, approximately is 1.5～2 times of propane prices, and along with the day by day exhaustion of petroleum resources and a large amount of development and use of natural gas resource, the propane direct oxidation of employing relative low price prepares acrylic acid and has very tempting application prospect.Because n butane oxidation production of maleic anhydride process route is obtained immense success, so people also expect to replace direct oxidation of propylene to prepare the important organic chemicals such as acrylic acid by propane.Propane is a main component of casing-head gas, natural gas, refinery gas, and the source is abundant, and the relative propylene of price is cheap, simultaneously because process route weak point, Energy Intensity Reduction etc. all will bring huge economic benefit, and environmental friendliness more.
In sum, because enrich in cheap, the source of propane, as preparing acrylic acid, the raw material oxidation step has significant economic benefit and practical significance take propane.
By propane oxidation step acrylic acid processed some basic research reports have been arranged, the catalyst of employing mainly comprises vanadium phosphorus oxygen (V-P-O), heteropoly acid and the three class systems such as salt (HPCs) and composite metal oxide (MMO) thereof.As the vanadium phosphorus oxygen system catalyst that is used for the butane oxidation production of maleic anhydride of suitability for industrialized production, it is unsatisfactory to be used for the acrylic acid effect of selective oxidation of propane system, once through yield often is no more than 13%, although and heteropoly acid and salt catalyst thereof have the controlled advantage of structure, but because its structure is stable not, be higher than under 400 ℃ the operating temperature easily because of the structure inactivation that caves in, except the relatively poor shortcoming of heat endurance, it is also undesirable that it is used for the acrylic acid effect of propane oxidation step system, and the highest acrylic acid yield only is 13%.Since nineteen ninety, obtained widely research take the catalyst based mixed metal oxide catalyst system as representative of MoV, in selective oxidation of propane acrylic acid reaction processed, also obtained very good catalytic effect, such as the Japan Patent (patent No.: h10-57813), Mitsubishi Kasai company is at the Mo-V-Te-Nb-O catalyst, and acrylic acid yield also has a few studies person (EP Patent 962 in addition up to 52.3%, 253, A2 (1999); Catal.Today117 (2006) 259; J.Am.Chem.Soc.124 (2002) 5608) report the acrylic acid once through yield can be higher than 42%, but many research groups of US and European all do not repeat out the result of study of Mitsubishi Kasai company, and this is because the multi-step of many components of its complexity, preparation process and for the sensitiveness of preparation parameter to a great extent.
Comprising paper and the document published, seldom relate to about the subsequent treatment of molybdenum-vanadium-tellurium-niobium catalytic agent, often all is to be directly used in reaction through after the roasting.Our invention shows that the further subsequent treatment of the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting also is very important.This is because in the roasting process of molybdenum-vanadium-tellurium-niobium catalytic agent, can generate some certain is reacted unwanted crystalline phase to a great extent; In addition, the tellurium in the catalyst is easy to distillation and evaporates in roasting process, deposit thereby cause catalyst surface to have many telluriums, finally certainly will have influence on the performance of catalyst.The objective of the invention is to find a kind of method for subsequent processing, can eliminate some unwanted crystalline phase, the tellurium dissolving that simultaneously catalyst surface is covered, thus make the Nomenclature Composition and Structure of Complexes of catalyst composition and structure and expection keep relative consistent.Significantly improved acrylic acid selective through the catalyst after processing.
Summary of the invention
The post-processing approach that the purpose of this invention is to provide a kind of molybdenum-vanadium-tellurium-niobium catalytic agent,
The invention provides a kind of post-processing approach of molybdenum-vanadium-tellurium-niobium catalytic agent, the subsequent treatment of the molybdenum-vanadium-tellurium-niobium catalytic agent of finger after roasting, being about to it places the hydrogen peroxide solution of certain concentration to carry out the oxidation processes certain hour, the concentration of volume percent of hydrogen peroxide is 0.5% ~ 30%, and the processing time is 0.1 hour ~ 5 hours.
The post-processing approach of molybdenum-vanadium-tellurium-niobium catalytic agent provided by the invention, the concentration of volume percent of described hydrogen peroxide solution are 0.5% ~ 30%, and preferred concentration of volume percent concentration is 1% ~ 3%.
The post-processing approach of molybdenum-vanadium-tellurium-niobium catalytic agent provided by the invention, described oxidation treatment time are 1 hour ~ 2 hours.
Through the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, for the ease of using, we can be with the presoma of described catalyst after the two-part high-temperature roasting, after products therefrom fully being ground and processing through follow-up hydrogen peroxide, drying molding, granulating again, obtaining at last particle diameter is 20 ~ 30 purpose catalyst granules.
The invention has the advantages that: selectively significantly increase acrylic acid through the catalyst after processing.
The specific embodiment
The following examples will be further described the present invention, but not thereby limiting the invention.
In selective oxidation of propane acrylic acid reaction processed, product is divided into gas, liquid two-phase.Gas-phase product comprises CO, CO
2, C
2H
4And C
2H
6, liquid product comprises purpose product acrylic acid (AA), a small amount of by-product acetic acid and acetone.
Conversion ratio calculates with following formula with selective and productive rate:
Conversion ratio (%)=(∑ Mi * ni)/3 * (amount of substance of propane in the charging) * 100%
Selectively (%)=(Mi * ni)/(∑ Mi * ni) * 100%
Productive rate (%)=conversion ratio * selective * 100
(Mi: the amount of substance of certain product i; Ni: institute's carbon atom quantity in certain product i molecule)
Embodiment 1
According to embodiment 1 among the patent ZL200410100456.1, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent presoma, be placed in the calcination vessel, be raised to take 3 ℃/minute heating rates from room temperature 300 ℃ and be incubated 2 hours after (atmosphere is air), then take same heating rate rise to 600 ℃ continue insulation after 2 hours (atmosphere is as nitrogen) naturally lower the temperature, products therefrom is the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, fully grind and be placed on the 0.5%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 0.1 hour, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.Get 1g and be used for the selective oxidation of propane reaction, reaction condition is: 350 ℃ of reaction temperatures, react total volume space velocity 3000h
-1, propane/air/water steam (volume ratio) is 1/6/3.Reaction result is: conversion of propane 20.5%, acrylic acid is selective 70.5%, acrylic acid yield 14.5%.Reaction result is listed in the table 1.
0.5% ~ 30%, the processing time is 0.1 hour ~ 5 hours.
Embodiment 2
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 1%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 0.5 hour, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 23.1%, acrylic acid is selective 73.2%, acrylic acid yield 16.9%.Reaction result is listed in the table 1.
Embodiment 3
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on abundant grinding and is placed on the 2%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 1 hour, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 25.1%, acrylic acid is selective 74.2%, acrylic acid yield 18.6%.Reaction result is listed in the table 1.
Embodiment 4
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 3%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 1 hour, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 27.5%, acrylic acid is selective 74.3%, acrylic acid yield 20.4%.Reaction result is listed in the table 1.
Embodiment 5
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 3%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 32.1%, acrylic acid is selective 74.5%, acrylic acid yield 23.9%.Reaction result is listed in the table 1.
Embodiment 6
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 3%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 3 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 36.1%, acrylic acid is selective 74.6%, acrylic acid yield 26.9%.Reaction result is listed in the table 1.
Embodiment 7
Embodiment 1 is described in according to the present invention, obtain molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 3%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 4 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 25.1%, acrylic acid is selective 73.6%, acrylic acid yield 18.5%.Reaction result is listed in the table 1.
Embodiment 8
Embodiment 1 is described in according to the present invention, obtain by the molybdenum-vanadium-tellurium-niobium catalytic agent after killing, it is fully ground is placed on the 3%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 5 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 22.1%, acrylic acid is selective 70.6%, acrylic acid yield 15.6%.Reaction result is listed in the table 1.
Embodiment 9
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 4%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 25.5%, acrylic acid is selective 73.5%, acrylic acid yield 18.4%.Reaction result is listed in the table 1.
Embodiment 10
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 7%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 23.1%, acrylic acid is selective 72.5%, acrylic acid yield 16.7%.Reaction result is listed in the table 1.
Embodiment 11
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 12%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 20.1%, acrylic acid is selective 71.4%, acrylic acid yield 14.4%.Reaction result is listed in the table 1.
Embodiment 12
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 20%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 16.1%, acrylic acid is selective 69.9%, acrylic acid yield 11.3%.Reaction result is listed in the table 1.
Embodiment 13
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 25%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 14.1%, acrylic acid is selective 67.8%, acrylic acid yield 9.6%.Reaction result is listed in the table 1.
Embodiment 14
Embodiment 1 is described in according to the present invention, obtain the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, it is fully ground is placed on the 25%(percent by volume) hydrogen peroxide solution in, under room temperature, stirred 2 hours, then again fully grind and molding, granulating after the oven dry in 80 ℃ baking oven, it is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst that final sizing becomes particle diameter.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 10.1%, acrylic acid is selective 65.3%, acrylic acid yield 6.6%.Reaction result is listed in the table 1.
Comparative example 1
Embodiment 1 is described in according to the present invention, obtains the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting, and it is fully ground the aftershaping granulation, and being sieved into particle diameter is that 20 ~ 30 purpose catalyst granules are used for evaluating catalyst.According to reaction condition similarly to Example 1, the gained reaction result is: conversion of propane 30.1%, acrylic acid is selective 61.5%, acrylic acid yield 18.5%.Reaction result is listed in the table 2.
Comparative example 2
M.Baca etc. are " Propane oxidation on Mo VTeNbO mixed oxidecatalysts:study of thephase composition of active and selective catalysts " at title of article, in Top.Catal.23 (2003) 39 1 literary compositions to Mo
1V
0.33Te
0.22Nb
0.11O
xCatalyst has carried out oxidation of propane acrylic acid research processed.Catalyst is by the dry slurries that consist of Mo/V/Te/Nb=1/0.33/0.22/0.11 under 150 ° of C, and then (first paragraph, sintering temperature are 300 ° of C, and atmosphere is air, roasting time 2h to pass through two-segment calcining; Second segment, sintering temperature are 600 ° of C, and atmosphere is nitrogen, roasting time 2h) and get.Reactor feed gas is than V (C
3H
8)/V (O
2)/V (H
2O)/V (N
2)/V (He)=6/10/43/36/5, reaction velocity are 2500h
-1, reaction temperature is 380 ℃.
Experimental result: conversion of propane and acrylic acid selectively are respectively 34.9% and 53%, acrylic acid yield 18.5%.
Comparative example 3
P.Botella etc. are " Selective oxidation of propane to acrylic acidon MoVNbTe mixed oxides catalysts prepared by hydrothermalsynthesis " at title of article, Mo-V-Nb-Te-O catalyst to the hydro-thermal method preparation in Catal.Lett.74 (2001) 149 1 literary compositions has carried out oxidation of propane acrylic acid research processed, and catalyst passes through at N
2In 600 ℃ of roasting 120min one-part form roastings and get reactor feed gas ratio V (C
3H
8)/V (O
2)/V (H
2O)/and V (He)=4/8/30/58, reaction velocity 409g
Cat.h.mol
-1, 380 ℃ of reaction temperatures.Experimental result: conversion of propane and acrylic acid selectively are respectively 31.1% and 56.5%, acrylic acid yield 17.6%.
Comparative example 4
Lin Luo etc. is " Comparison of Reaction Pathways for thePartial Oxidation of Propane over Vanadyl Ion-Exchanged Zeolite Beta andMo at title of article
1V
0.3Te
0.23Nb
0.12O
x", in J.Catal.200 (2001) 222 1 literary compositions to Mo
1V
0.3Te
0.23Nb
0.12O
xCatalyst has carried out oxidation of propane acrylic acid research processed.Catalyst precursor obtains by slurry method, then passes through at N
2In 600 ℃ of roasting 120min roasting obtain Mo
1V
0.3Te
0.23Nb
0.12O
xCatalyst.Catalyst amount is 0.70g, and reactor feed gas is than V (C
3H
8)/V (O
2)/V (H
2O)/and V (He)=4/2/4/5, the gas overall flow rate is 15mL/min,, 350 ℃ of reaction temperatures.Experimental result: conversion of propane and acrylic acid selectively are respectively 27.2% and 64.7%, acrylic acid yield 17.6%.
Comparative example 5
In the patents such as Ushikubo " EP0608838A2 " to Mo
1V
0.3Te
0.23Nb
0.12O
xCatalyst has carried out oxidation of propane acrylic acid research processed.Catalyst precursor obtains by slurry method, then passes through behind the molding, granulating at N
2In 600 ℃ of roasting 120min roasting obtain Mo
1V
0.3Te
0.23Nb
0.12O
xCatalyst.Catalyst amount is 0.37g, and reactor feed gas is than V (C
3H
8)/V (air)=1/15, reaction velocity are 1734h
-1, reaction temperature is 400 ℃.Experimental result: conversion of propane and acrylic acid selectively are respectively 75.3% and 42.4%, acrylic acid yield 32%.
Comparative example 6
M.Baca etc. are " Synergetic effect between phasesinMoVTe (Sb) NbO catalysts used forthe oxidation of propane into acrylic acid " at title of article, in J.Catal.233 (2005) 234 1 literary compositions to Mo
1V
0.33Te
0.22Nb
0.11O
xCatalyst has carried out oxidation of propane acrylic acid research processed.Catalyst is by consisting of the slurries of Mo/V/Te/Nb=1/0.33/0.22/0.11 150 ° of ℃ of lower dryings, and then (first paragraph, sintering temperature are 300 ° of C, and atmosphere is air, roasting time 2h through two-segment calcining; Second segment, sintering temperature are 600 ° of C, and atmosphere is nitrogen, roasting time 2h) and get.Reactor feed gas is than V (C
3H
8)/V (O
2)/V (H
2O)/V (N
2)/V (Ne)=1.5/3/13.5/10.5/1.5, gas overall flow rate are 30mL/min, and reaction temperature is 380 ℃.Experimental result: conversion of propane and acrylic acid selectively are respectively 33% and 55%, acrylic acid yield 18.2%.
Comparative example 7
In the Japan Patent " h10-57813 " to Mo
1V
0.3Te
0.23Nb
0.12O
xCatalyst has carried out oxidation of propane acrylic acid research processed.Can know that in embodiment 4 reaction temperature is 380 ℃ and is that conversion of propane and acrylic acid selectively reach respectively 84.2% and 62.5%, the acrylic acid yield is 52.5%.
Reaction result among table 1 embodiment
Reaction result in table 2 comparative example
Claims (4)
1. the post-processing approach of a molybdenum-vanadium-tellurium-niobium catalytic agent is characterized in that: the molybdenum-vanadium-tellurium-niobium catalytic agent after the roasting was placed the hydrogen peroxide solution oxidation processes 0.1 hour ~ 5 hours.
2. according to the post-processing approach of the described molybdenum-vanadium-tellurium-niobium catalytic agent of claim 1, it is characterized in that: the concentration of volume percent of described hydrogen peroxide solution is 0.5% ~ 30%.
3. according to the post-processing approach of the described molybdenum-vanadium-tellurium-niobium catalytic agent of claim 2, it is characterized in that: the concentration of volume percent of described hydrogen peroxide solution is 1% ~ 3%.
4. according to the post-processing approach of the described molybdenum-vanadium-tellurium-niobium catalytic agent of claim 1, it is characterized in that: described oxidation treatment time is 1 hour ~ 2 hours.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105521398A CN102989487A (en) | 2012-12-17 | 2012-12-17 | After-treatment method for molybdenum vanadium tellurium niobium catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012105521398A CN102989487A (en) | 2012-12-17 | 2012-12-17 | After-treatment method for molybdenum vanadium tellurium niobium catalyst |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102989487A true CN102989487A (en) | 2013-03-27 |
Family
ID=47918893
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012105521398A Pending CN102989487A (en) | 2012-12-17 | 2012-12-17 | After-treatment method for molybdenum vanadium tellurium niobium catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102989487A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104248949A (en) * | 2013-06-27 | 2014-12-31 | 中国科学院大连化学物理研究所 | Molybdenum-vanadium composite oxide material and preparation method thereof |
| CN109562361A (en) * | 2016-07-22 | 2019-04-02 | 国际壳牌研究有限公司 | For alkanes oxidative dehydrogenation and/or olefin oxidation based on molybdenum-vanadium-niobium-ceria catalyst |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012209A1 (en) * | 1998-08-28 | 2000-03-09 | Asahi Kasei Kabushiki Kaisha | Method for producing oxide catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutane |
| CN1491745A (en) * | 2002-10-01 | 2004-04-28 | ��������ķ������ | Mo-V-M-Nb-X oxide catalyst for selective hydrocarbon oxidation synthesied by water heat |
| CN1795987A (en) * | 2004-12-23 | 2006-07-05 | 中国科学院大连化学物理研究所 | Catalyst of Mo, V, Te, Nb in use for reaction of producing crylic acid by selective oxidation of propane |
| CN101722017A (en) * | 2008-10-22 | 2010-06-09 | 中国科学院大连化学物理研究所 | Molybdenum-vanadium-tellurium-niobium catalytic agent for preparing acrylic acid by propane oxidation and preparation method thereof |
-
2012
- 2012-12-17 CN CN2012105521398A patent/CN102989487A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012209A1 (en) * | 1998-08-28 | 2000-03-09 | Asahi Kasei Kabushiki Kaisha | Method for producing oxide catalyst for use in producing acrylonitrile or methacrylonitrile from propane or isobutane |
| CN1491745A (en) * | 2002-10-01 | 2004-04-28 | ��������ķ������ | Mo-V-M-Nb-X oxide catalyst for selective hydrocarbon oxidation synthesied by water heat |
| CN1795987A (en) * | 2004-12-23 | 2006-07-05 | 中国科学院大连化学物理研究所 | Catalyst of Mo, V, Te, Nb in use for reaction of producing crylic acid by selective oxidation of propane |
| CN101722017A (en) * | 2008-10-22 | 2010-06-09 | 中国科学院大连化学物理研究所 | Molybdenum-vanadium-tellurium-niobium catalytic agent for preparing acrylic acid by propane oxidation and preparation method thereof |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104248949A (en) * | 2013-06-27 | 2014-12-31 | 中国科学院大连化学物理研究所 | Molybdenum-vanadium composite oxide material and preparation method thereof |
| CN109562361A (en) * | 2016-07-22 | 2019-04-02 | 国际壳牌研究有限公司 | For alkanes oxidative dehydrogenation and/or olefin oxidation based on molybdenum-vanadium-niobium-ceria catalyst |
| CN109562361B (en) * | 2016-07-22 | 2022-07-15 | 国际壳牌研究有限公司 | Catalyst based on molybdenum-vanadium-niobium-ceria for the oxidative dehydrogenation of alkanes and/or the oxidation of alkenes |
| US11707731B2 (en) | 2016-07-22 | 2023-07-25 | Shell Usa, Inc. | Molybdenum-vanadium-niobium-ceria-based catalyst for oxidative dehydrogenation of alkanes and/or alkene oxidation |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101722017A (en) | Molybdenum-vanadium-tellurium-niobium catalytic agent for preparing acrylic acid by propane oxidation and preparation method thereof | |
| Yang et al. | Effect of calcination temperature on the catalytic activity of VPO for aldol condensation of acetic acid and formalin | |
| JP6417009B2 (en) | Catalyst for glycerol dehydration reaction, method for producing the same, and method for producing acrolein | |
| JP5920750B2 (en) | Gold catalyst for ethanol oxidation and method for producing acetaldehyde and acetic acid using the same | |
| CN103894179A (en) | Molybdenum-vanadium based composite oxide catalyst and preparation and application thereof | |
| CN105080575A (en) | Molybdenum vanadium tellurium niobium oxygen catalyst for preparing ethene from ethane and preparation method and application | |
| CN104203401A (en) | Process for making ethylene and acetic acid | |
| Albuquerque et al. | Lactic acid production from aqueous-phase selective oxidation of hydroxyacetone | |
| CN103848719B (en) | Method for preparing 1,5-pentanediol via selective hydrogenolysis of tetrahydrofurfuryl alcohol | |
| CN109395755A (en) | A kind of Heat Conduction Material doping vanadium-phosphor oxide catalyst and preparation and the application in normal butane selective catalytic oxidation synthesis cis-butenedioic anhydride | |
| CN104837799A (en) | Catalytic conversion of bio-mass derivable aliphatic alcohols to valuable alkenes or oxygenates | |
| CN103071514B (en) | A kind of preparation method preparing acrylic acid catalyst for propylene one step catalytic oxidation | |
| CN104437584A (en) | Application of nitrogen-doped porous carbon used as catalyst in dehydrogenation of low-carbon alkane through oxidation by carbon dioxide | |
| Lan et al. | CeO 2 promoting allyl alcohol synthesis from glycerol direct conversion over MoFe/CeO 2 oxide catalysts: morphology and particle sizes dependent | |
| CN102989487A (en) | After-treatment method for molybdenum vanadium tellurium niobium catalyst | |
| CN102786499A (en) | Method for preparing cyclohexene oxide | |
| CN102476057A (en) | Preparation method of MoVTeNbO catalyst for reaction of preparing acrylic acid by propane oxidation | |
| CN106552657A (en) | A kind of platinum based catalyst of SiC carriers confinement and preparation method thereof | |
| CN108503529A (en) | Propane prepares acrylic acid | |
| CN108855158B (en) | Preparation method and application of cobalt-ruthenium bimetallic heterogeneous catalyst | |
| CN104437456A (en) | Catalyst for preparing isobutene by isobutane dehydrogenation and preparation method and application of catalyst | |
| CN103301879B (en) | Preparation method and application of supported molecular sieve based catalyst | |
| CN112569945B (en) | Metal-loaded dolomite catalyst for preparing ethanol by glycerol dehydration and preparation thereof | |
| CN105582964B (en) | A kind of O composite metallic oxide catalyst and its preparation method and application | |
| CN113877613A (en) | CO (carbon monoxide)2Hydrogenated biomass charcoal-based transition metal catalyst and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130327 |