CN104355976B - A kind of method of acetone through one-step method synthesis mesityl oxide - Google Patents
A kind of method of acetone through one-step method synthesis mesityl oxide Download PDFInfo
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- CN104355976B CN104355976B CN201410642509.6A CN201410642509A CN104355976B CN 104355976 B CN104355976 B CN 104355976B CN 201410642509 A CN201410642509 A CN 201410642509A CN 104355976 B CN104355976 B CN 104355976B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
- C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
- C07C45/72—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups
- C07C45/74—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups combined with dehydration
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- C07—ORGANIC CHEMISTRY
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- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/79—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
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Abstract
The present invention is the method for a kind of acetone through one-step method synthesis mesityl oxide, adopt the combination process of fixed-bed reactor and the series connection of molecular sieve adsorbing and dewatering tank, be reaction raw materials with acetone, filling solid catalyst in reactor, acetone carries out condensation reaction and generates mesityl oxide and water; Product enters first molecular sieve adsorbing and dewatering tank; After dehydration, organic oil phase enters second fixed-bed reactor, and acetone condensation reaction occurs further and generates mesityl oxide and water, then through second molecular sieve adsorbing and dewatering tank; Reactor and water knockout series connection hop count are 2 ~ 3 grades; After dehydration, acetone and mesityl oxide oil phase are sent to rectifying separation system, and unreacted acetone recycle returns reactor; Liquid phase at the bottom of tower obtains purity & gt by separation; The mesityl oxide of 99%.Present approach provides the method for bimolecular acetone by condensation One-step production mesityl oxide, break molecular balance and improve transformation efficiency, obtain high-purity mesityl oxide product, reduce energy consumption and products production cost simultaneously.
Description
Technical field
The present invention relates to the method for a kind of acetone through one-step method synthesis mesityl oxide.
Background technology
Mesityl oxide (another name: isomesityl oxide, 4-methyl-3-amylene-2-ketone, MesitylOxide, be called for short MO) be a kind of mid-boiling point strong solvent, main be used as nitrocellulose and various kinds of resin, especially Vinylite and the solvent to spray paint etc.; It or important organic synthesis intermediate, be mainly used in medicine, fine chemicals and agrochemical, is also the raw material producing methyl-isobutyl (first) ketone and methyl isobutyl alcohol simultaneously.
The traditional production method of mesityl oxide is two-step approach:
The first step, acetone (AC) is under basic catalyst exists, and pressurization condensation, change into Pyranton (DAA), catalyzer is calcium hydroxide or hydrated barta.
Condensation of acetone reaction formula:
2CH
3-CO-CH
3→(CH
3)
2COH-CH
2-CO-CH
3。
Second step: Pyranton dehydration generates mesityl oxide.The Pyranton obtained by condensation of acetone, its concentration is 10% ~ 15%, adopt atmospheric distillation, unconverted acetone is steamed from tower top, tower reactor goes out the material containing Pyranton 80%, and then Pyranton in the presence of acidic (nitric acid, boric acid, Phenylsulfonic acid), is heated to 100 ~ 200 DEG C, Pyranton dehydration generates mesityl oxide, and transformation efficiency is 80% ~ 85%.Reaction formula is:
(CH
3)
2COH-CH
2-CO-CH
3→(CH
3)
2C＝CH-CO-CH
3+H
2O。
Industrial in methylisobutanone synthesized from acetone (being called for short MIBK) reaction process at present, use Pd/ resin catalyst, this catalyzer has dehydration, hydrogenation is difunctional, the method that original acetone can be made to synthesize MIBK by three-step reaction changes single stage method into, namely on Pd/ resin catalyst, two molecule condensation of acetone also dehydration generation MO before this; Then MO hydrogenation generation MIBK on a catalyst.Therefore the MO that this technique meeting by-product is a small amount of, in theory, two molecule acetone also a step can complete condensation, dehydration generation MO, change single stage method into by original two-step approach.But because this reaction is a balanced reaction, transformation efficiency is very low, so also nobody adopts this route to produce MO so far.
CN103772175A discloses a kind of combined technical method synthesizing mesityl oxide and sec-butyl alcohol, and adopting fixed-bed reactor, take solid acid as catalyzer, comprise acetone and n-butene in charging simultaneously, at catalyzed reaction bed, acetone carries out condensation reaction, generates mesityl oxide and water; N-butene and water react and generate sec-butyl alcohol; From reactor product out, after cooling, decompression, be sent in high-pressure separator, unreacted n-butene vaporization, through gas-liquid separation, n-butene loops back reactor; Liquid phase obtains respective substance by separation.This inventive method is in fact utilize n-butene and water to react to realize removing of water in condensation of acetone process, carries out to positive reaction direction to utilize reaction.There are two kinds of reactions in the method, under selected reaction conditions, due to the existence of different compound, inevitably some side reactions, therefore target product mesityl oxide selectivity ~ 97% occurs in the reactor.There is a small amount of by product in product, increase if its follow-up separation costs of high purity target product will be obtained.In addition condensation of acetone reaction must take higher pressure condition 3 ~ 10MPa, the transformation efficiency of guarantee acetone, but more side reaction can be caused to occur, and causes facility investment high simultaneously.
Summary of the invention
The present invention is directed to the deficiency that mesityl oxide technology is produced in the dehydration of existing bimolecular condensation of acetone, innovate from process aspect, there is provided a kind of newly by the method for bimolecular acetone by condensation One-step production mesityl oxide, can realize breaking molecular balance and improve transformation efficiency, obtain high-purity mesityl oxide product, thus reduce energy consumption and products production cost.
The method of acetone through one-step method synthesis mesityl oxide of the present invention, comprise the steps: the combination process adopting fixed-bed reactor and the series connection of molecular sieve adsorbing and dewatering tank, take acetone as reaction raw materials, filling solid catalyst in fixed-bed reactor, at catalyzed reaction bed, acetone carries out condensation reaction, generates mesityl oxide and water; From reactor product out, enter a molecular sieve adsorbing and dewatering tank; After dehydration, organic oil phase enters second fixed-bed reactor, and acetone further condensation reaction occurs, and generates mesityl oxide and water; Again through second molecular sieve adsorbing and dewatering tank; A series connection water knockout after each reactor, reactor and water knockout series connection hop count are 2-3 level; After dehydration, acetone and mesityl oxide oil phase are sent to rectifying separation system, and the unreacted acetone recycle of tower top returns reactor; Liquid phase at the bottom of tower obtains the mesityl oxide product of purity >99% by being separated;
Described solid catalyst is γ-Al
2o
3the calcium catalyst of load, wherein CaO content is 2.0 ~ 5.0%, or is γ-Al
2o
3the titanate catalyst of load, wherein BaO content is 2.0 ~ 5.0%, can by the existing method preparation in this area;
Reaction conditions in described fixed-bed reactor is: reaction pressure is 0.8 ~ 1.5MPa, is preferably 1.0MPa ~ 1.2MPa; Temperature of reaction is 100 ~ 150 DEG C, and be preferably 110 DEG C ~ 140 DEG C, during acetone solution, volume space velocity is 0.5h
-1~ 2.0h
-1, be preferably 0.8h
-1~ 1.2h
-1.
In the inventive method, two parallel way blocked operations taked by molecular sieve adsorbing and dewatering tank, after one of them adsorption dewatering tank is saturated, switch to another adsorption dewatering tank processing reaction product.Regeneration after molecular sieve adsorption water saturation, can carry out processed by the existing renovation process in this area.
In the inventive method, owing to there is no water in last water knockout product out, there is not azeotrope, the separation of organic oil phase can adopt ordinary method, as distillating method, mesityl oxide and unreacted acetone separation are opened, the acetone of recovery sends back to reactive system and recycles.
In the inventive method, a water knockout of connecting after a reactor is 1 grade and says, along with the increase of series connection hop count, acetone conversion can be improved.But owing to affecting by molecular balance, along with the increase of series connection hop count, acetone conversion declines, and reaction conversion ratio no longer includes and significantly improves thereupon, hop count of therefore connecting is no more than 3 grades.
Compared with prior art, the advantage of the inventive method is:
1, the inventive method is innovated from process aspect, propose the method for acetone through one-step method synthesis mesityl oxide, the a small amount of water produced that dewaters after making condensation is removed by molecular sieve adsorption, can realize the molecular balance breaking acetone synthesis mesityl oxide, improve its transformation efficiency.
2, adopt method provided by the invention, reaction process process is simple, and selected operational condition relaxes, and side reaction is few, can obtain high purity mesityl oxide product.
3, adopt method provided by the invention, MO synthetic technology upgrades to the Green Chemical Technology without the discharge of spent acid salkali waste, also reduces the production cost of energy consumption and product.
Embodiment
The present invention, by the reaction for condensation of acetone one-step synthesis method mesityl oxide, obtains following understanding through experiment and research:
(1) reaction of acetone through one-step method synthesis MO is a balanced reaction, under low temperature, equilibrium conversion is large, but when temperature of reaction is too low, speed of response is very slow again, carries out in process in reaction, if the water that reaction generates can be shifted out in time, the carrying out of this reaction will be conducive to.
(2) by known to the research of this reaction kinetics: reaction adopts solid catalyst to be γ-Al
2o
3the calcium catalyst of load, or be γ-Al
2o
3the titanate catalyst of load.Two kinds of catalyzer are for having condensation and the bifunctional solid catalyst that dewaters, the acetone of two molecules condensation in the heart in the alkali of catalyzer in reaction process, the acid site of catalyzer comes off the water of a molecule, and generate the MO reaction of a part, the rate-determining steps of reaction is surface reaction step.
(3) condition that acetone through one-step method synthesis MO reaction is suitable is: reaction pressure is 0.8 ~ 1.5MPa, and temperature of reaction is 100 ~ 150 DEG C, and during acetone solution, volume space velocity is 0.5h
-1~ 2.0h
-1.
Based on above research, the technique of acetone through one-step method of the present invention synthesis mesityl oxide is proposed.
Further illustrate the inventive method and effect below in conjunction with embodiment, percentage ratio is wherein the purity >99% of massfraction, reaction raw materials acetone.
Embodiment 1 ~ 2
By pseudo-boehmite (Shandong Aluminum Plant's production), mix with extrusion aid, tackiness agent, through kneading, extrusion after adding water, make cylinder shape.Extrudate is dried at 130 DEG C, then roasting 3 hours at 500 DEG C, namely obtain γ-Al
2o
3carrier.By 500ml γ-Al
2o
3carrier immerses in the calcium nitrate aqueous solution of 500ml7.5%, and flood 4 hours, then 120 DEG C of dryings 4 hours, at 400 DEG C, roasting obtains catalyst B TM-I in 4 hours.Catalyzer physical property is in table 1.
Table 1
| Embodiment | 1 | 2 | 3 | 4 |
| Catalyzer | BTM-I | BTM-I | BTM-II | BTM-III |
| CaO content, % | 2.44 | 2.44 | - | 4.2 |
| Ba content, % | - | - | 3.0 | |
| Pore volume, ml/g | 0.42 | 0.42 | 0.42 | 0.41 |
| Specific surface area, m 2/g | 220 | 220 | 216 | 208 |
| Side pressure strength, N/cm | 158 | 158 | 164 | 172 |
| Profile | Cylindrical | Cylindrical | Trifolium | Trifolium |
| Tap density, g/ml | 0.65 | 0.65 | 0.58 | 0.59 |
The reaction of bimolecular condensation of acetone is all carried out in trickle-bed reactor, and each catalyst reactor loadings is 100ml, and reaction conditions is in table 2.Acetone raw material passes through first reactor catalyst bed, and out product enters molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters second trickle-bed reactor, and selected reaction conditions is identical with first reactor.Reaction product passes through beds, then enters second molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Second adsorption dewatering tank product out enters a rectifying separation tower, and the unreacted acetone recycle of tower top returns first reactor; Product mesityl oxide for the purpose of liquid product at the bottom of tower.Each adsorption dewatering tank product out and rectifying separation tower bottom product are by capillary gas chromatography.Acetone synthesis MO reaction conditions and test-results are in table 2.
Table 2
| Embodiment | 1 | 2 |
| Solid catalyst | BTM-I | BTM-I |
| Feeding manner | Lower charging | Lower charging |
| Temperature of reaction, DEG C | 110 | 120 |
| Reaction pressure, MPa | 1.0 | 1.2 |
| Acetone feed volume space velocity, h -1 | 1.0 | 0.8 |
| Reaction result | ||
| Acetone conversion (first reactor), % | 15.5 | 15.2 |
| Acetone conversion (second reactor), % | 30.2 | 30.8 |
| MO selectivity, % | 99.8 | 99.6 |
Embodiment 3
By pseudo-boehmite (Shandong Aluminum Plant's production), mix with extrusion aid, tackiness agent, through kneading, extrusion after adding water, make cylinder shape.Extrudate is dried at 130 DEG C, then roasting 3 hours at 500 DEG C, namely obtain γ-Al
2o
3carrier.By 500ml γ-Al
2o
3carrier immerses in the barium nitrate aqueous solution of 500ml5.3%, and flood 4 hours, then 120 DEG C of dryings 4 hours, at 400 DEG C, roasting obtains catalyst B TM-II in 4 hours.Catalyzer physical property is in table 1.
The reaction of bimolecular condensation of acetone is all carried out in trickle-bed reactor, and each catalyst reactor loadings is 100ml, and reaction conditions is in table 4.Acetone raw material passes through beds, and product enters molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters second trickle-bed reactor, catalyst filling 100ml, and reactor condition is identical with first reactor.Reaction product passes through beds, then enters second molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Second adsorption dewatering tank product out enters a rectifying separation tower, and the unreacted acetone recycle of tower top returns first reactor; Product mesityl oxide for the purpose of liquid product at the bottom of tower.Each adsorption dewatering tank product out and rectifying separation tower bottom product are by capillary gas chromatography.Acetone synthesis MO reaction conditions and test-results are in table 3.
Embodiment 4
By pseudo-boehmite (Shandong Aluminum Plant's production), mix with extrusion aid, tackiness agent, through kneading, extrusion after adding water, make cylinder shape.Extrudate is dried at 130 DEG C, then roasting 3 hours at 500 DEG C, namely obtain γ-Al
2o
3carrier.By 500ml γ-Al
2o
3carrier immerses in the calcium nitrate aqueous solution of 500ml12.3%, and flood 4 hours, then 120 DEG C of dryings 4 hours, at 400 DEG C, roasting obtains catalyst B TM-III in 4 hours.Catalyzer physical property is in table 1.
The reaction of bimolecular condensation of acetone is all carried out in trickle-bed reactor, and each catalyst reactor loadings is 100ml, and reaction conditions is in table 4.Acetone raw material passes through beds, and product enters molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters second trickle-bed reactor, catalyst filling 100ml, and reactor condition is identical with first reactor.Reaction product passes through beds, then enters second molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Second adsorption dewatering tank product out enters a rectifying separation tower, and the unreacted acetone recycle of tower top returns first reactor; Product mesityl oxide for the purpose of liquid product at the bottom of tower.Each adsorption dewatering tank product out and rectifying separation tower bottom product are by capillary gas chromatography.Acetone synthesis MO reaction conditions and test-results are in table 3.
Table 3
| Embodiment | 3 | 4 |
| Solid catalyst | BTM-II | BTM-III |
| Feeding manner | Lower charging | Lower charging |
| Temperature of reaction, DEG C | 115 | 125 |
| Reaction pressure, MPa | 1.0 | 1.5 |
| Acetone feed volume space velocity, h -1 | 1.2 | 0.8 |
| Reaction result | ||
| Acetone conversion (first reactor), % | 14.6 | 16.1 |
| Acetone conversion (second reactor), % | 29.2 | 30.8 |
| Acetone conversion (the 3rd reactor), % | 39.5 | 40.6 |
| MO selectivity, % | 99.9 | 99.5 |
Embodiment 5
The reaction of bimolecular condensation of acetone is carried out in trickle-bed reactor, and catalyzer is BTM-I, and loaded catalyst 100ml, reaction conditions is in table 3.Acetone raw material passes through first reactor catalyst bed, and product enters molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters second trickle-bed reactor, catalyst filling 100ml, and the reaction conditions that follow-up each reactor is selected is identical with first reactor.Reaction product passes through beds, then enters second molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters the 3rd trickle-bed reactor, catalyst filling 100ml.Reaction product passes through beds, then enters the 3rd molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
3rd adsorption dewatering tank product out enters a rectifying separation tower, and the unreacted acetone recycle of tower top returns first reactor; Product mesityl oxide for the purpose of liquid product at the bottom of tower.Each adsorption dewatering tank product out and rectifying separation tower bottom product are by capillary gas chromatography.Acetone synthesis MO reaction conditions and test-results are in table 4.
Comparative example 1
The reaction of bimolecular condensation of acetone is carried out in trickle-bed reactor, and catalyzer is BTM-I, and loaded catalyst 100ml, reaction conditions is in table 3.Acetone raw material passes through beds, and product enters molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters second trickle-bed reactor, catalyst filling 100ml, and selected reaction conditions is identical with embodiment 5.Reaction product passes through beds, then enters second molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters the 3rd trickle-bed reactor, catalyst filling 100ml, and subsequent reactor volume is all identical with embodiment 5.Reaction product passes through beds, then enters the 3rd molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
Product after dehydration enters the 4th trickle-bed reactor, catalyst filling 100ml.Reaction product passes through beds, then enters the 4th molecular sieve adsorbing and dewatering tank.The molecular sieve selected in adsorption dewatering tank is 4A molecular sieve.
4th adsorption dewatering tank product out enters a rectifying separation tower, and the unreacted acetone recycle of tower top returns first reactor; Product mesityl oxide for the purpose of liquid product at the bottom of tower.Each adsorption dewatering tank product out and rectifying separation tower bottom product are by capillary gas chromatography.Acetone synthesis MO reaction conditions and test-results are in table 4.
Table 4
| Embodiment 5 | Comparative example 1 | |
| Solid catalyst | BTM-I | BTM-I |
| Feeding manner | Lower charging | Lower charging |
| Temperature of reaction, DEG C | 110 | 110 |
| Reaction pressure, MPa | 1.0 | 1.0 |
| Acetone feed volume space velocity, h -1 | 1.0 | 1.0 |
| Reaction result | ||
| Acetone conversion (first reactor), % | 15.5 | 15.6 |
| Acetone conversion (second reactor), % | 30.2 | 30.2 |
| Acetone conversion (the 3rd reactor), % | 40.4 | 40.3 |
| Acetone conversion (the 4th reactor), % | - | 42.1 |
| MO selectivity, % | 99.5 | 99.2 |
From table 2,3 and table 4 in data relatively, due to have employed condensation of acetone one-step synthesis method mesityl oxide and molecular sieve adsorbing and dewatering process combination process, broken the molecular balance of acetone synthesis mesityl oxide, improve acetone conversion; In addition, selected operational condition relaxes, and side reaction is few, and therefore product purity is high, and mesityl oxide selectivity is all more than 99%.From data in table 4 relatively, too much reaction-adsorption dewatering series connection progression, acetone conversion is decreased significantly, in facility investment and energy consumption, do not have economic advantages.
Claims (4)
1. a method for acetone through one-step method synthesis mesityl oxide, it is characterized in that, be reaction raw materials with acetone, filling solid catalyst in fixed-bed reactor, and at catalyzed reaction bed, acetone carries out condensation reaction, generates mesityl oxide and water; From reactor product out, enter a molecular sieve adsorbing and dewatering tank; After dehydration, organic oil phase enters second fixed-bed reactor, and acetone further condensation reaction occurs, and generates mesityl oxide and water; Again through second molecular sieve adsorbing and dewatering tank; A series connection water knockout after each reactor, reactor and water knockout series connection hop count are 2 ~ 3 grades; After dehydration, acetone and mesityl oxide oil phase are sent to rectifying separation system, and the unreacted acetone recycle of tower top returns reactor; Liquid phase at the bottom of tower obtains the mesityl oxide product of purity >99% by being separated;
Wherein, described solid catalyst is γ-Al
2o
3the calcium catalyst of load, wherein CaO content is 2.0 ~ 5.0%, or is γ-Al
2o
3the titanate catalyst of load, wherein BaO content is 2.0 ~ 5.0%;
Reaction conditions in described fixed-bed reactor is: reaction pressure is 0.8 ~ 1.5MPa, and temperature of reaction is 100 ~ 150 DEG C, and during acetone solution, volume space velocity is 0.5h
-1~ 2.0h
-1.
2. in accordance with the method for claim 1, it is characterized in that: two parallel way blocked operations taked by described molecular sieve adsorbing and dewatering tank, after one of them adsorption dewatering tank is saturated, switch to another adsorption dewatering tank processing reaction product.
3. in accordance with the method for claim 1, it is characterized in that: after dehydration, acetone and mesityl oxide separation of oil adopt distillating method to reclaim acetone, are back to reactive system and recycle.
4. in accordance with the method for claim 1, it is characterized in that: the reaction conditions in described fixed-bed reactor is: reaction pressure is 1.0MPa ~ 1.2MPa, temperature of reaction is 110 DEG C ~ 140 DEG C, and during acetone solution, volume space velocity is 0.8h
-1~ 1.2h
-1.
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|---|---|---|---|---|
| CN86104786A (en) * | 1985-07-16 | 1987-02-04 | 武田药品工业株式会社 | The renovation process of zeolite |
| US5583263A (en) * | 1995-08-30 | 1996-12-10 | Shell Oil Company | Process of making ketones |
| CN1787986A (en) * | 2003-05-15 | 2006-06-14 | 三菱化学株式会社 | Process for producing diacetone alcohol |
| CN102786397A (en) * | 2012-07-30 | 2012-11-21 | 中国海洋石油总公司 | Method for continuous production of polyformaldehyde dimethyl ether |
| CN103435461A (en) * | 2013-07-24 | 2013-12-11 | 河北工业大学 | Production technology for isophorone |
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