CN1150153C - Catalyst for preparing methoxyacetone, preparation method and application thereof - Google Patents
Catalyst for preparing methoxyacetone, preparation method and application thereof Download PDFInfo
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- CN1150153C CN1150153C CNB011312920A CN01131292A CN1150153C CN 1150153 C CN1150153 C CN 1150153C CN B011312920 A CNB011312920 A CN B011312920A CN 01131292 A CN01131292 A CN 01131292A CN 1150153 C CN1150153 C CN 1150153C
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- oxide
- methoxyl group
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- 239000003054 catalyst Substances 0.000 title claims abstract description 37
- CUZLJOLBIRPEFB-UHFFFAOYSA-N 1-methoxypropan-2-one Chemical compound COCC(C)=O CUZLJOLBIRPEFB-UHFFFAOYSA-N 0.000 title claims abstract description 19
- 238000002360 preparation method Methods 0.000 title claims description 9
- 238000006243 chemical reaction Methods 0.000 claims abstract description 25
- 239000002808 molecular sieve Substances 0.000 claims abstract description 13
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 12
- ARXJGSRGQADJSQ-UHFFFAOYSA-N 1-methoxypropan-2-ol Chemical compound COCC(C)O ARXJGSRGQADJSQ-UHFFFAOYSA-N 0.000 claims abstract description 7
- 229910052802 copper Inorganic materials 0.000 claims abstract description 5
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 5
- 229910052709 silver Inorganic materials 0.000 claims abstract description 5
- 229910052804 chromium Inorganic materials 0.000 claims abstract description 4
- 229910052744 lithium Inorganic materials 0.000 claims abstract description 4
- 229910052684 Cerium Inorganic materials 0.000 claims abstract description 3
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 3
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 3
- 230000003647 oxidation Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 229910004298 SiO 2 Inorganic materials 0.000 claims description 4
- 238000000034 method Methods 0.000 claims description 4
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 229910052750 molybdenum Inorganic materials 0.000 claims description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims 1
- 150000003841 chloride salts Chemical class 0.000 claims 1
- 239000003426 co-catalyst Substances 0.000 claims 1
- 238000005470 impregnation Methods 0.000 claims 1
- 150000002823 nitrates Chemical class 0.000 claims 1
- 150000003467 sulfuric acid derivatives Chemical class 0.000 claims 1
- 239000012159 carrier gas Substances 0.000 abstract description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical group O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 abstract description 5
- 229910052751 metal Inorganic materials 0.000 abstract description 3
- 239000002184 metal Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000000741 silica gel Substances 0.000 abstract description 3
- 229910002027 silica gel Inorganic materials 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract description 2
- 150000002739 metals Chemical group 0.000 abstract 2
- 239000000654 additive Substances 0.000 abstract 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 abstract 1
- 230000009466 transformation Effects 0.000 description 11
- 230000003197 catalytic effect Effects 0.000 description 10
- 238000011049 filling Methods 0.000 description 7
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 150000001875 compounds Chemical class 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 5
- 239000004480 active ingredient Substances 0.000 description 5
- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical group CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 description 4
- 150000002576 ketones Chemical class 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- 230000009849 deactivation Effects 0.000 description 3
- 238000007598 dipping method Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- GRVDJDISBSALJP-UHFFFAOYSA-N methyloxidanyl Chemical group [O]C GRVDJDISBSALJP-UHFFFAOYSA-N 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate group Chemical group [N+](=O)([O-])[O-] NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 206010013786 Dry skin Diseases 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229960004643 cupric oxide Drugs 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- -1 methoxy propyl Chemical group 0.000 description 2
- 239000006199 nebulizer Substances 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 229910000480 nickel oxide Inorganic materials 0.000 description 2
- GNRSAWUEBMWBQH-UHFFFAOYSA-N oxonickel Chemical compound [Ni]=O GNRSAWUEBMWBQH-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 229910014459 Ca-Ni Inorganic materials 0.000 description 1
- 229910014473 Ca—Ni Inorganic materials 0.000 description 1
- 229910017518 Cu Zn Inorganic materials 0.000 description 1
- 229910017752 Cu-Zn Inorganic materials 0.000 description 1
- 229910017943 Cu—Zn Inorganic materials 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000002153 concerted effect Effects 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- SWXVUIWOUIDPGS-UHFFFAOYSA-N diacetone alcohol Natural products CC(=O)CC(C)(C)O SWXVUIWOUIDPGS-UHFFFAOYSA-N 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000007210 heterogeneous catalysis Methods 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 238000004949 mass spectrometry Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003333 secondary alcohols Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
一种制备甲氧基丙酮的催化剂，催化剂主体为Cu、Ag或Mo等金属，助剂主要包括Mg、Ni、Cr、K、Li、Ce等金属，载体可为硅胶、三氧化二铝、分子筛等。反应温度一般在250℃-350℃之间，载气压力为1大气压，空速在1.4-4.2ml/g.h之间。1-甲氧基-2-丙醇在催化剂表面上转化率高、选择性好，为甲氧基丙酮从产物中分离创造了条件，催化剂制备方便，寿命长且易再生，能满足工业化生产的要求。A catalyst for preparing methoxyacetone. The main body of the catalyst is metals such as Cu, Ag, or Mo. The additives mainly include metals such as Mg, Ni, Cr, K, Li, and Ce. The carrier can be silica gel, aluminum oxide, and molecular sieves. wait. The reaction temperature is generally between 250°C and 350°C, the carrier gas pressure is 1 atmosphere, and the space velocity is between 1.4-4.2ml/g.h. 1-methoxy-2-propanol has a high conversion rate and good selectivity on the surface of the catalyst, which creates conditions for the separation of methoxyacetone from the product. The catalyst is convenient to prepare, has a long life and is easy to regenerate, and can meet the requirements of industrial production. Require.
Description
Technical field
This patent relates to a kind of 1-of being used for methoxyl group-2-propyl alcohol catalyzed oxidation and prepares the used Catalysts and its preparation method of methoxy propyl reactive ketone.
Background technology
Methoxy acetone is a kind of important chemical product, adopts the method preparation of oxidation 1-methoxyl group-2-propyl alcohol usually.Because the influence of methoxyl group inductive effect, the activity of 1-methoxyl group-2-propyl alcohol is far below other secondary alcohol.The consistence of 1-methoxyl group-2-propyl alcohol and methoxy acetone boiling point also is the where the shoe pinches of synthesizing methoxy acetone simultaneously.
U.S. Pat 3,462,495 disclose a kind of mixture (1-25: 1) pump into reactor after preheating of 1-methoxyl group-2-third alcohol and water.Be filled with the phosphate catalyst of Ca-Ni in the reactor.The transformation efficiency of 1-methoxyl group-2-propyl alcohol is 55% under certain condition.But catalyzer is inactivation very easily, needs regeneration in per 1 hour once.
In addition, document (Heterogeneous Catalysis and Fine Chemicals IV.Dehydrogenation of methoxyisopropanol to methoxyacetone onsupported bimetallic Cu-Zn catalysts, 1997,407.) reported a kind of technology of utilizing above-mentioned prepared in reaction methoxy acetone, be at long 20cm, caliber is filling 5g 8%Cu-10%Zn/Al in the tubular reactor of 10mm
2O
3Catalyzer is done carrier gas with nitrogen, and nebulizer gas pressure is 1 normal atmosphere, and design temperature is 270 degree.In air speed is 7.0h
-1Transformation efficiency about 46.2%, yield 40%.Obviously, the transformation efficiency that how to improve 1-methoxyl group-2-propyl alcohol oxidizing reaction is an industrial urgency problem to be solved.
Summary of the invention
In order to address the above problem, the invention provides a kind of catalyzer that is used to prepare methoxy acetone.Utilize well oxidation 1-methoxyl group-2-propyl alcohol of catalyst system of the present invention, also satisfied simultaneously when separating requirement the methoxy acetone relative content.
Specifically, the invention provides the catalyzer of the oxidative dehydrogenation of a kind of 1-of being used for methoxyl group-2-propyl alcohol, it is characterized in that being represented by formula M N/PZ, wherein: M represents that the activity of such catalysts component is the oxide compound of Cu, Ag or Mo; N represents that promotor is a kind of or two kinds in the oxide compound of Mg, Ni or Cr; P represents that promotor is the oxide compound of Li, K or Ce; Z represents that carrier is a molecular sieve, Al
2O
3Or SiO
2Active ingredient M content is the 5-20% of catalyst weight; Promotor N content is the 0-20% of catalyst weight; Promotor P content is the 0-10% of catalyst weight; All the other are carrier Z.
In above-mentioned catalyzer, preferably M is the oxide compound of Cu, and N is the oxide compound of Ni, and the weight ratio of M: N is 0.5: 1-2.5: 1.
In addition, in above-mentioned catalyzer, preferably P is the oxide compound of K, and the content of P is the 0.5-5% of catalyst weight.
The invention provides the Preparation of catalysts method of the oxidative dehydrogenation of the above-mentioned 1-of being used for methoxyl group-2-propyl alcohol, be to adopt pickling process that active ingredient and cocatalyst component are supported on the carrier, promptly use the solution impregnating carrier Z of the soluble salt of the element that contains active ingredient M and/or cocatalyst component N and P, then after drying, obtain catalyzer in 350-700 ℃ of following roasting.
In above-mentioned preparation method, soluble salt is nitrate, vitriol or the muriate that contains active ingredient M, cocatalyst component N and P.In addition, at first dipping M and/or N component on carrier are flooded the P component after drying again.
The oxidation of 1-methoxyl group provided by the invention-2-propyl alcohol prepares the reaction of methoxy acetone, use the above-mentioned catalyzer of the present invention, reaction conditions is: temperature of reaction is at 250-350 ℃, and air speed is between 1.5-4.3ml/g.h, and flow rate of carrier gas is between 500-2000ml/h.
From the above, because Preparation of Catalyst of the present invention is convenient, the transformation efficiency height of 1-methoxyl group-2-propyl alcohol, the selectivity of methoxy acetone is better, and has the life-span preferably.Active ingredient exists with the state of oxidation in the catalyzer simultaneously, does not need reduction activation, has bigger space-time yield, easily regeneration behind the catalyst deactivation, and active nothing obviously reduces.
Embodiment
Below by example catalyst system is further described.
Example 1 Preparation of catalysts
With carrier Y molecular sieve, beta-molecular sieve, 4A molecular sieve, Al
2O
3Or SiO
2Become 40-60 order particulate state, the nitrate aqueous solution impregnated carrier with containing M and N after 120 ℃ of following dryings, made single component, two-pack or three component catalysts in 5 hours in 550 ℃ of following roastings.Carry out for the dipping of the P component aqueous solution with its nitrate or oxyhydroxide, dipping is after after 120 ℃ of dryings, carry out roasting and obtain catalyzer under 550 ℃.
In following experiment, the catalyzer that catalyst system therefor is all prepared as stated above, the composition of its catalyzer is represented with weight % in each embodiment.In addition, example of the present invention related respond and all in fixed-bed reactor, carry out.The long 20cm of fixed-bed reactor, internal diameter 10mm, thermocouple jack 1mm.General filling 5g catalyzer (about 5-7cm), catalyzer two ends filling inert quartz sand.Carrier gas is an air, and nebulizer gas pressure is 1 normal atmosphere, and flow rate of carrier gas is measured by soap-foam flowmeter.Product receives through condensation.
Example 2
Filling 5g 15%CuO-19.5%NiO/ molecular sieve in reactor, beds two ends filling inert quartz sand.Carrier gas is an air, pressure 1 normal atmosphere.System temperature is set at 300 ℃, and flow rate of carrier gas is adjusted to 1482.5ml/h, air speed 2.4ml/g.h (unit time is by the volume number of unit vol catalyzer).Under this condition 1-methoxyl group-2-propyl alcohol is pumped into reactor after preheating, product is collected in condensation behind catalyst bed reaction.Product is quantitative through the chromatography-mass spectroscopy analysis.The transformation efficiency 74.3% of 1-methoxyl group-2-propyl alcohol.Ketone yield 63.0%.。By product mainly is propionic aldehyde, acetone and methyl alcohol.
Example 3
Filling 5g 15%Ag in reactor
2O-19.5%NiO/r-Al
2O
3, other condition is identical with example 1.The transformation efficiency 73.3% of 1-methoxyl group-2-propyl alcohol, ketone yield 45.7%.
Example 4
Filling 5g 1.5%MgO-15%CuO-19.5%NiO/ silica gel in reactor, other condition is identical with example 1.The transformation efficiency 80% of 1-methoxyl group-2-propyl alcohol, ketone yield 67.5%.Be continuously pumped into 24 hours catalytic activitys with fresh feed pump and do not have bigger variation.Can onlinely regenerate behind the catalyst deactivation, promptly stop charging, continue blowing air after 3-4 hour, it is active that catalyzer can recover fully.
Example 5
Press example 2 described reactions, adopt different catalysts to carry out, it the results are shown in table 1.
As can be seen from Table 1, the catalytic activity of different catalysts main body has very big difference, and is best with the effect of cupric oxide.The charge capacity of catalyzer also has very big influence to the catalytic activity of 1-methoxyl group-2-propyl alcohol simultaneously.By a series of investigation, find that cupric oxide, nickel oxide have very strong concerted catalysis activity, nickel oxide shows the extremely strong catalytic activity that helps.Be with r-Al in the table 1
2O
3Investigated of the influence of catalyzer composition as carrier to catalytic activity.
Table 1 catalyzer is formed the influence to catalytic activity
No. catalyzer is formed (wt%) transformation efficiency (%) yield (%)
1 15％MoO
3 73.1 11.9
2 15％CuO 36.7 24.5
3 19.5％NiO 8.1 4.3
4 15％CuO-6.5％NiO 59.5 47.1
5 15％CuO-19.5％NiO 78.8 62.9
6 15％Ag
2O-19.5％NiO 73.3 45.7
7 15％CuO-19.5％Cr
2O
3?86.0 28.3
Reaction conditions: 300 ℃ of temperature of reaction, air speed 2.4ml/g.h, flow rate of carrier gas 1482ml/h.
Example 6
Press example 2 described reactions, adopt different catalysts to carry out, it the results are shown in table 2.As can be seen from Table 2, the used carrier of the present invention to transformation efficiency to influence difference little, have ubiquity.But the acidity of carrier itself has very big influence to the selectivity of reaction.1-methoxyl group-2-propyl alcohol and methoxy acetone all can carry out acidolysis on the acidic site of carrier, main by product is propionic aldehyde, methyl alcohol and acetone.Better with the effect of molecular sieve, aluminium sesquioxide and silica gel in used carrier, and the result of 4A molecular sieve is the poorest.The existence of metal such as lithium, potassium can weaken the acidity of carrier, thereby can suppress the sour decomposition reaction of 1-methoxyl group-2-propyl alcohol and methoxy acetone, and the methoxy acetone selectivity is improved.
Table 2 different carriers is to the influence of catalytic activity
No. carrier transformation efficiency (%) yield (%)
8 15％CuO-19.5NiO％/r-Al
2O
3 78.8 62.9
9 15％CuO-19.5NiO％/SiO
2 77.5 65.5
10 15%CuO-19.5NiO%/γ molecular sieve 74.3 63.0
11 15%CuO-19.5NiO%/molecular sieve 77.4 48.3
12 15%CuO-19.5NiO%/4A molecular sieve 65.4 27.0
13 15%CuO-19.5NiO%/acidity-Al
2O
3 *82.3 41.6
14 3%K
2O15%CuO-19.5NiO%/acidity-Al
2O
3 *70.0 64.1
Reaction conditions: 300 ℃ of temperature of reaction, air speed 2.4ml/g.h, flow rate of carrier gas 1482ml/h.
*Flow rate of carrier gas 850ml/h, air speed 2.2ml/g.h
Example 7
Pressing example 2 described reactions, is that example is investigated the influence of reaction conditions to catalytic activity with the 15%CuO-19.5%NiO/Y molecular sieve, and it the results are shown in Table 3.Temperature of reaction, air speed and flow rate of carrier gas obviously affect 1-methoxyl group-2-propyl alcohol oxidative dehydrogenation as shown in Table 3.Generally between 250-350 ℃, the air speed scope is 1.4-4.3ml/g.h to temperature of reaction, and flow rate of carrier gas can change between 500-2000ml/h.When temperature of reaction is 300 ℃, air speed is 2.4ml/g.h, and when flow rate of carrier gas was 1482ml/h, 1-methoxyl group-2-propyl alcohol can well be converted into product, and the yield of methoxy acetone is preferably 63%.
Table 3 reaction conditions is to the influence of catalytic activity
No. reaction conditions I reaction conditions II reaction conditions III transformation efficiency (%) yield (%)
15 250℃ 1482.5ml/h 2.4ml/g.h 59.1 25.1
16 300℃ 1482.5ml/h 2.4ml/g.h 74.3 63
17 350℃ 1482.5ml/h 2.4ml/g.h 89.3 49.9
18 300℃ 1482.5ml/h 1.5ml/g.h 80.3 47.8
19 300℃ 1482.5ml/h 2.4ml/g.h 74.3 63
20 300℃ 1482.5ml/h 4.3ml/g.h 71.1 53.5
21 300℃ 566.4ml/h 2.4ml/g.h 69.6 53.7
22 300℃ 806.3ml/h 2.4ml/g.h 72.2 53.8
23 300℃ 1482.5ml/h 2.4ml/g.h 74.3 63
24 300℃ 1831.8ml/h 2.4ml/g.h 67.1 50.4
Can be seen that by above-mentioned sample result the present invention has following outstanding effect: 1. preferably resolve the problem of oxidation of 1-methoxyl group-2-propyl alcohol, catalytic activity is far above the result of known technology; 2. preferably resolve the separation problem of product from system, the transformation efficiency of 1-methoxyl group-2-propyl alcohol is high more, helps the separation of methoxy acetone more; 3. it is cheap to have satisfied industrial production requirement 4. catalyzer raw materials basically, easily synthetic, directly uses oxidation state, does not need reduction activation; 5. have the life-span preferably, but in-situ regeneration behind the catalyst deactivation.
Claims (6)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011312920A CN1150153C (en) | 2001-09-05 | 2001-09-05 | Catalyst for preparing methoxyacetone, preparation method and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011312920A CN1150153C (en) | 2001-09-05 | 2001-09-05 | Catalyst for preparing methoxyacetone, preparation method and application thereof |
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| Publication Number | Publication Date |
|---|---|
| CN1403431A CN1403431A (en) | 2003-03-19 |
| CN1150153C true CN1150153C (en) | 2004-05-19 |
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|---|---|---|---|
| CNB011312920A Expired - Fee Related CN1150153C (en) | 2001-09-05 | 2001-09-05 | Catalyst for preparing methoxyacetone, preparation method and application thereof |
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Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB0327514D0 (en) * | 2003-11-26 | 2003-12-31 | Davy Process Techn Ltd | Catalyst |
| CN104399474A (en) * | 2014-11-20 | 2015-03-11 | 西安近代化学研究所 | Catalyst for synthesizing methoxy acetone through alcohol dehydrogenization, preparation method and application of catalyst |
| CN105384616A (en) * | 2015-10-29 | 2016-03-09 | 山东联创节能新材料股份有限公司 | Synthetic method for methoxyacetone |
| CN107628933B (en) * | 2017-09-28 | 2020-08-14 | 中触媒新材料股份有限公司 | Continuous production process for synthesizing 1-methoxy-2-acetone by directly dehydrogenating 1-methoxy-2-propanol |
| CN107790128A (en) * | 2017-09-28 | 2018-03-13 | 中触媒新材料股份有限公司 | A kind of catalyst in the acetone synthetic reaction of 1 methoxyl group 2 and preparation method thereof |
| CN112844248B (en) * | 2020-12-28 | 2022-07-12 | 山东滨农科技有限公司 | Dehydrogenation interlocking control method for preparation of s-metolachlor raw pesticide |
| CN115106115B (en) * | 2021-03-19 | 2023-11-03 | 中国石油大学(华东) | A kind of method for producing acetone from alkanes |
-
2001
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