CN101176847A - Complex vitriolate dehydration catalyst as well as method for preparing propenoic acid and methyl ester using the same - Google Patents
Complex vitriolate dehydration catalyst as well as method for preparing propenoic acid and methyl ester using the same Download PDFInfo
- Publication number
- CN101176847A CN101176847A CNA2007101571861A CN200710157186A CN101176847A CN 101176847 A CN101176847 A CN 101176847A CN A2007101571861 A CNA2007101571861 A CN A2007101571861A CN 200710157186 A CN200710157186 A CN 200710157186A CN 101176847 A CN101176847 A CN 101176847A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- dehydration catalyst
- acrylic acid
- dehydration
- complex vitriolate
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention relates to a compound sulfate-based dehydration catalyst and a method of preparing acrylic acid and methyl acrylate with the catalyst. The compound sulfate-based dehydration catalyst comprising calcium sulfate as main catalyst and copper sulfate plus phosphate as promoter is made through crushing of wet mixed solid with the above components, then screening separation and calcinations. The method of preparing acrylic and methyl acrylate with the catalyst adopts fixed-bed reactor, utilizing biomass-based lactic-acid and derivative of the lactic-acid as raw materials, purging gas of nitrogen or carbon dioxide at the speed of 10 ml/min to 100ml/min, the temperature of the reactor rose to 250 to 500 degree C, obtaining acrylic and methyl acrylate reaction of gas-phase dehydration. The invention has the advantages that: the preparation cost of the compound sulfate-based dehydration catalyst is low, the reaction condition is easy to control, the preparation technology is simple preparing the acrylic and the methyl acrylate with the catalyst, the invention reduces the reliance on the fossils of raw materials and production cost, has broad prospect for industrial application.
Description
Technical field
The present invention relates to complex vitriolate dehydration catalyst and prepare the method for acrylic acid and methyl esters thereof with this catalyst conversion of biomass base lactic acid and methyl lactate.
Background technology
Acrylic acid and ester class thereof are important chemical material, are widely used in numerous industries such as coating, weaving, plastic processing, adhesive, daily chemical products.Acrylic acid in the world in recent years production and application increase rapidly, and the output of whole world acrylic acid and ester class thereof is above 3,000,000 tons/year at present.In the end of the year 2006, Chinese acrylic acid (ester) demand reaches 840,000 tons, accounts for 23% of world's aggregate consumption, has stepped into world's acrylic acid (ester) consumption big country.Present industrial preparation acrylic acid all adopts the propylene two-step oxidizing process, and promptly in the presence of O composite metallic oxide catalyst, propylene changes into methacrylaldehyde through air oxygen, and further Catalytic Oxygen changes into acrylic acid.The method technology is simple, but raw material propylene is from the naphtha pyrolysis product, and along with ethene, propylene shortage and crude oil and Gas Prices sharp rise, the acrylic acid production cost increases day by day.
From the renewable resource angle, with biomass ferment is lactic acid, again lactic acid or derivatives thereof gas-phase dehydration is made the acrylic acid or derivatives thereof, is one of competitive approach, its research and development has been subjected to scientific circles and industrial quarters is paid close attention to (United States Patent (USP) 4729978,4786756) widely.Prepare in the acrylate reactions at the gas-phase dehydration lactic acid derivative, the sulfate of alkali metal and alkaline-earth metal and phosphate are proved to be comparatively appropriate catalyst (United States Patent (USP) 2859240), and metallic copper is as a kind of material of effective inhibition acroleic acid polymerization, and its sulfate is not seen open report as yet to the effect of lactic acid and the reaction of methyl lactate gas-phase dehydration.
Summary of the invention
The purpose of this invention is to provide the complex vitriolate dehydration catalyst that helps reducing production costs and prepare the method for acrylic acid and methyl esters thereof with it.
Complex vitriolate dehydration catalyst of the present invention comprises major catalyst calcium sulfate and co-catalyst copper sulphate and phosphate, by the following method preparation:
(1) according to mass ratio 150: (5.9～70.6): successively take by weighing anhydrous CaSO at 2.5: 1.2
4, anhydrous CuSO
4, NaH
2PO
4And KH
2PO
4, and with anhydrous CuSO
4, NaH
2PO
4And KH
2PO
4Be dissolved in 100～300 gram distilled water and be made into mixed solution;
(2) mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, wore out at least 1 hour under the room temperature, drying is cool to room temperature after at least 2 hours;
(3) with the bulk catalyst fragmentation, the screening that obtain, calcined 2～5 hours down for 300～500 ℃ at Muffle furnace, obtain complex vitriolate dehydration catalyst.
Complex vitriolate dehydration catalyst of the present invention is used to prepare the method for acrylic acid and methyl esters thereof, and step is as follows:
The a certain amount of complex vitriolate dehydration catalyst of in fixed bed reactors, packing into, under nitrogen or carbon dioxide purging, temperature of reactor is risen to 250～500 ℃, the flow of nitrogen or carbon dioxide is 10～100ml/min, the stable back of temperature of reactor continues logical nitrogen or carbon dioxide, and with syringe pump biomass-based lactic acid or methyl lactate are squeezed into and to be carried out the gas-phase dehydration reaction in the fixed bed reactors, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, get final product.
Among the present invention, said biomass-based lactic acid can be the tunning of starch, corn or molasses, and methyl lactate can be the product of fermentation lactic acid after esterification.
Among the present invention, for the concentration of biomass-based lactic acid or methyl lactate and the no specific (special) requirements of liquid reactions air speed (LSHV) of gas-phase dehydration reaction, generally selecting lactic acid concn is 5～85wt%, and methyl lactate concentration is 10～100wt%.The liquid reactions air speed of gas-phase dehydration reaction is 0.1～0.75h
-1In order to improve the acrylate productive rate, preferred lactic acid concn is 20～40wt%, and methyl lactate concentration is 40～60wt%, and the preferred liquid reaction velocity is 0.23～0.28h
-1
Beneficial effect of the present invention is: complex vitriolate dehydration catalyst preparation cost of the present invention is low, and reaction condition is easy to control.With this Preparation of Catalyst acrylic acid and methyl acrylate, preparation technology is simple, and biomass-based lactic acid is made by renewable resources such as starch, corn, molasses, can reduce the dependence to fossil feedstock, reduces production costs.Thereby has an excellent industrial application foreground.
The specific embodiment
Further specify the present invention below by embodiment.
Embodiment 1
The anhydrous CaSO of weighing 150 grams
4, 5.9 the gram anhydrous CuSO
4, 2.5 the gram NaH
2PO
4With 1.2 gram KH
2PO
4, then with anhydrous CuSO after the weighing
4, NaH
2PO
4And KH
2PO
4Be dissolved in the 100 gram distilled water and be made into mixed solution.Mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, under the room temperature aging 1 hour, in 80 ℃ of baking ovens, leave standstill 2 hours then after cool to room temperature.With bulk catalyst fragmentation, the screening that obtains, calcining is 2 hours in 400 ℃ of Muffle furnaces, obtains complex vitriolate dehydration catalyst.
Get the above-mentioned catalyst of the 30 grams fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 40ml/min
2Purge down temperature of reactor is risen to 400 ℃, stable back is squeezed into concentration with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors for the 100wt% methyl lactate, and the liquid reactions air speed is 0.2h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 2
The anhydrous CaSO of weighing 150 grams
4, 70.6 the gram anhydrous CuSO
4, 2.5 the gram NaH
2PO
4With 1.2 gram KH
2PO
4, then with anhydrous CuSO after the weighing
4, NaH
2PO
4And KH
2PO
4Be dissolved in the 200 gram distilled water and be made into mixed solution.Mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, under the room temperature aging 1 hour, in 100 ℃ of baking ovens, leave standstill 2 hours then after cool to room temperature.With bulk catalyst fragmentation, the screening that obtains, calcining is 4 hours in 400 ℃ of Muffle furnaces, obtains complex vitriolate dehydration catalyst.
Get the above-mentioned catalyst of the 30 grams fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 20ml/min
2Purge down temperature of reactor is risen to 400 ℃, stable back is squeezed into concentration with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors for the 100wt% methyl lactate, and the liquid reactions air speed is 0.28h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 3
The anhydrous CaSO of weighing 150 grams
4, 8.8 the gram anhydrous CuSO
4, 2.5 the gram NaH
2PO
4With 1.2 gram KH
2PO
4, then with anhydrous CuSO after the weighing
4, NaH
2PO
4And KH
2PO
4Be dissolved in the 200 gram distilled water and be made into mixed solution.Mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, under the room temperature aging 3 hours, in 100 ℃ of baking ovens, leave standstill 4 hours then after cool to room temperature.With bulk catalyst fragmentation, the screening that obtains, calcining is 4 hours in 400 ℃ of Muffle furnaces, obtains complex vitriolate dehydration catalyst.
Get the above-mentioned catalyst of the 30 grams fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 20ml/min
2Purge down temperature of reactor is risen to 400 ℃, stable back is squeezed into concentration with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors for the 60wt% methyl lactate, and the liquid reactions air speed is 0.28h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 4
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 3, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 20ml/min
2Purge down temperature of reactor is risen to 350 ℃, stable back is squeezed into the 10wt% methyl lactate with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.3h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 5
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 3, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 20ml/min
2Purge down temperature of reactor is risen to 500 ℃, stable back is squeezed into the 60wt% methyl lactate with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.28h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 6
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 3, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 100ml/min
2Purge down temperature of reactor is risen to 250 ℃, stable back is squeezed into the 60wt% methyl lactate with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.28h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid and methyl acrylate, evaluating catalyst the results are shown in Table 1.
Embodiment 7
The anhydrous CaSO of weighing 150 grams
4, 8.8 the gram anhydrous CuSO
4, 2.5 the gram NaH
2PO
4With 1.2 gram KH
2PO
4,
Then with anhydrous CuSO after the weighing
4, NaH
2PO
4And KH
2PO
4Be dissolved in 200 ml distilled waters and be made into mixed solution.Mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, under the room temperature aging 4 hours, in 80 ℃ of baking ovens, leave standstill 4 hours then after cool to room temperature.With bulk catalyst fragmentation, the screening that obtains, calcining is 2 hours in 430 ℃ of Muffle furnaces, obtains complex vitriolate dehydration catalyst.Get the above-mentioned catalyst of the 15 grams fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the CO of 20ml/min
2Purge down temperature of reactor is risen to 330 ℃, stable back is squeezed into 25wt% lactic acid with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.17h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid, evaluating catalyst the results are shown in Table 2.
Embodiment 8
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 3, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the N of 40ml/min
2Purge down temperature of reactor is risen to 350 ℃, stable back, stable back is squeezed into 25wt% lactic acid with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.19h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid, evaluating catalyst the results are shown in Table 2.
Embodiment 9
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 6, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the CO of 20ml/min
2Purge down temperature of reactor is risen to 330 ℃, stable back, stable back is squeezed into 25wt% lactic acid with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.2h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid, evaluating catalyst the results are shown in Table 2.
Embodiment 10
Take by weighing catalyst 30 grams according to the described methods preparation of embodiment 6, the fixed bed reactors stage casing of packing into, fill with bead at two ends, under the normal pressure at the CO of 40ml/min
2Purge down temperature of reactor is risen to 350 ℃, stable back, stable back is squeezed into 25wt% lactic acid with syringe pump and is carried out the gas-phase dehydration reaction in the fixed bed reactors, and the liquid reactions air speed is 0.34h
-1, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, obtain acrylic acid, evaluating catalyst the results are shown in Table 2.
Table 1
| Embodiment | Temperature (℃) | Conversion ratio (%) | Selectivity (%) | Molar yield (%) | ||
| Methyl lactate | Acrylic acid | Methyl acrylate | Acrylic acid | Methyl acrylate | ||
| 1 | 400 | 62.5 | 13.5 | 30.5 | 8.4 | 19.1 |
| 2 | 400 | 70.6 | 11.5 | 10.7 | 8.1 | 7.6 |
| 3 | 400 | 75.9 | 54.3 | 26.4 | 41.2 | 20.1 |
| 4 | 350 | 95.2 | 8.0 | 4.6 | 7.6 | 4.4 |
| 5 | 500 | 98.6 | 3.1 | 3.5 | 3.0 | 3.4 |
| 6 | 250 | 36.1 | 5.1 | 1.5 | 1.6 | 0.5 |
Table 2
| Embodiment | Temperature (℃) | Lactic acid conversion ratio (%) | Acrylic acid selectivity (%) | Acrylic acid molar yield (%) |
| 7 | 330 | 98.6 | 64.8 | 63.9 |
| 8 | 350 | 100 | 26.2 | 26.2 |
| 9 | 330 | 96.5 | 47.6 | 45.9 |
| 10 | 350 | 95.8 | 31.7 | 30.4 |
Claims (5)
1. complex vitriolate dehydration catalyst is characterized in that this catalyst comprises major catalyst calcium sulfate and co-catalyst copper sulphate and phosphate, by the following method preparation:
(1) according to mass ratio 150: (5.9～70.6): successively take by weighing anhydrous CaSO at 2.5: 1.2
4, anhydrous CuSO
4, NaH
2PO
4And KH
2PO
4, and with anhydrous CuSO
4, NaH
2PO
4And KH
2PO
4Be dissolved in 100～300 gram distilled water and be made into mixed solution;
(2) mixed solution is joined anhydrous CaSO
4In, mix the formation blocks of solid rapidly, wore out at least 1 hour under the room temperature, drying is cool to room temperature after at least 2 hours;
(3) with the bulk catalyst fragmentation, the screening that obtain, calcined 2～5 hours down for 300～500 ℃ at Muffle furnace, obtain complex vitriolate dehydration catalyst.
2. the described complex vitriolate dehydration catalyst of claim 1 is used to prepare the method for acrylic acid and methyl esters thereof, it is characterized in that step is as follows:
The a certain amount of complex vitriolate dehydration catalyst of in fixed bed reactors, packing into, under nitrogen or carbon dioxide purging, temperature of reactor is risen to 250～500 ℃, the flow of nitrogen or carbon dioxide is 10～100ml/min, the stable back of temperature of reactor continues logical nitrogen or carbon dioxide, and with syringe pump biomass-based lactic acid or methyl lactate are squeezed into and to be carried out the gas-phase dehydration reaction in the fixed bed reactors, the gaseous product that leaves catalyst layer imported in the cold-trap cool off, get final product.
3. complex vitriolate dehydration catalyst according to claim 2 is used to prepare the method for acrylic acid and methyl esters thereof, it is characterized in that said biomass-based lactic acid is the tunning of starch, corn or molasses, methyl lactate is the product of fermentation lactic acid after esterification.
4. be used to prepare the method for acrylic acid and methyl esters thereof according to the described complex vitriolate dehydration catalyst of claim 2, it is characterized in that said lactic acid concn is 5～85wt%, methyl lactate concentration is 10～100wt%.
5. be used to prepare the method for acrylic acid and methyl esters thereof according to the described complex vitriolate dehydration catalyst of claim 2, it is characterized in that the liquid reactions air speed of said gas-phase dehydration reaction is 0.1～0.75h
-1
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101571861A CN100484627C (en) | 2007-11-27 | 2007-11-27 | Complex sulphate dehydration catalyst as well as method for preparing propenoic acid and methyl acrylic ester using the same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2007101571861A CN100484627C (en) | 2007-11-27 | 2007-11-27 | Complex sulphate dehydration catalyst as well as method for preparing propenoic acid and methyl acrylic ester using the same |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101176847A true CN101176847A (en) | 2008-05-14 |
| CN100484627C CN100484627C (en) | 2009-05-06 |
Family
ID=39403361
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2007101571861A Expired - Fee Related CN100484627C (en) | 2007-11-27 | 2007-11-27 | Complex sulphate dehydration catalyst as well as method for preparing propenoic acid and methyl acrylic ester using the same |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100484627C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014528941A (en) * | 2012-04-11 | 2014-10-30 | ザ プロクター アンド ギャンブルカンパニー | Method for producing acrylic acid or derivative thereof |
| CN105688946A (en) * | 2016-03-02 | 2016-06-22 | 济南大学 | Solid acid catalyst and preparation method and application thereof |
-
2007
- 2007-11-27 CN CNB2007101571861A patent/CN100484627C/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014528941A (en) * | 2012-04-11 | 2014-10-30 | ザ プロクター アンド ギャンブルカンパニー | Method for producing acrylic acid or derivative thereof |
| CN104220412A (en) * | 2012-04-11 | 2014-12-17 | 宝洁公司 | Catalysts for the production of acrylic acid or its derivatives |
| JP2015516292A (en) * | 2012-04-11 | 2015-06-11 | ザ プロクター アンド ギャンブルカンパニー | Catalyst for production of acrylic acid or its derivatives |
| RU2586329C2 (en) * | 2012-04-11 | 2016-06-10 | Дзе Проктер Энд Гэмбл Компани | Catalysts for producing acrylic acid or derivatives thereof |
| RU2591192C2 (en) * | 2012-04-11 | 2016-07-10 | Дзе Проктер Энд Гэмбл Компани | Catalysts for conversion of hydroxypropionic acid or derivatives thereof into acrylic acid or derivatives thereof |
| RU2598380C2 (en) * | 2012-04-11 | 2016-09-27 | Дзе Проктер Энд Гэмбл Компани | Catalytic conversion of lactic acid into acrylic acid |
| CN104220412B (en) * | 2012-04-11 | 2018-04-24 | 宝洁公司 | It is used to prepare the catalyst of acrylic acid or derivatives thereof |
| CN105688946A (en) * | 2016-03-02 | 2016-06-22 | 济南大学 | Solid acid catalyst and preparation method and application thereof |
| CN105688946B (en) * | 2016-03-02 | 2018-05-04 | 济南大学 | A kind of solid acid catalyst and its preparation method and application |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100484627C (en) | 2009-05-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103896765B (en) | Preparation and the application thereof of the loaded nano Ag catalyst of the synthetic methyl formate of a kind of gas-phase photocatalysis partial oxidation methyl alcohol | |
| CN101602010A (en) | Molecular sieve catalyst, preparation method and the application in crylic acid preparation by lactic acid dehydration thereof | |
| CN103752305A (en) | Catalyst, preparation method thereof, and method for production of methyl acrylate and co-production of methyl methacrylate by using catalyst | |
| CN101941887A (en) | Method for indirectly synthesizing ethanol by using carbon monoxide and hydrogen | |
| CN101066771A (en) | Microwave radiation process for producing potassium sulfate | |
| CN104177247A (en) | Method for preparation of formic acid by catalytic oxidation of biomass | |
| CN100484627C (en) | Complex sulphate dehydration catalyst as well as method for preparing propenoic acid and methyl acrylic ester using the same | |
| CN105363438A (en) | Catalyst for synthesizing glycolic acid ester and preparation method and application of catalyst | |
| CN102503817A (en) | Photo-thermo concerted catalysis technology and application thereof on carbon monoxide catalytic coupling | |
| CN110483268A (en) | A kind of method that heteropoly acid catalysis microcrystalline cellulose prepares levulic acid | |
| Zhang et al. | Strong metal-support interaction between AuPd nanoparticles and oxygen-rich defect ZrO2 for enhanced catalytic 5-hydroxymethylfurfural oxidation | |
| CN100372827C (en) | Production of isooctaacid by composite catalytic method | |
| CN104190401A (en) | Molybdenum-based composite metal oxide catalyst for synthesizing propenyl alcohol by glycerol and preparation method of molybdenum-based composite metal oxide catalyst | |
| CN107286006B (en) | Method for preparing vanillone and acetosyringone by catalytic alcoholysis of lignin | |
| CN104945238A (en) | Isocaprylic acid production process | |
| CN103193636B (en) | A kind of method of synthesizing 2,3-butanediol ester | |
| KR101643859B1 (en) | Heterogeneous Catalyst for Production of 3-hydroxypropionic acid From Allyl Alcohol, and A Method for Preparation of 3-hydroxypropionic acid From Allyl Alcohol Using Thereof | |
| CN102580753A (en) | Catalyst for synthesizing methanol by taking multi-carbon sources in metallurgical fume as raw materials and preparation method of catalyst | |
| CN104311404A (en) | Method for producing cinnamyl aldehyde | |
| CN101186576A (en) | Method for preparing acrylic ester | |
| CN107445832B (en) | Method for oxidizing glycolate into glyoxylate | |
| CN111170845B (en) | Method for producing lactic acid by catalytic conversion of glucose and application thereof | |
| CN101417232B (en) | Catalyst for preparing acrylic acid and butyl ester using lactic acid method and preparation method thereof | |
| CN106582744B (en) | Preparation method of catalyst for improving yield of maleic anhydride prepared by n-butane oxidation | |
| CN101049571B (en) | Complex type molecular sieve catalyst, preparation method, and application in preparing crylic acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090506 Termination date: 20131127 |