CN103524317B - The synthetic method of pseudo ionone - Google Patents
The synthetic method of pseudo ionone Download PDFInfo
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- CN103524317B CN103524317B CN201310433879.4A CN201310433879A CN103524317B CN 103524317 B CN103524317 B CN 103524317B CN 201310433879 A CN201310433879 A CN 201310433879A CN 103524317 B CN103524317 B CN 103524317B
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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
Abstract
The invention discloses a kind of synthetic method of pseudo ionone, comprising: 230 ~ 300 DEG C, under the condition of 5 ~ 25MPa, acetone and citral generation condensation reaction, be isolated to described pseudo ionone after reacting completely.This synthetic method does not introduce basic catalyst, be more conducive to the purification of product, there is product purity high (>=98.5%), yield high (reaching 93.8%), by product little (1.0% ~ 8%), processing step is simple, and the amounts of acetone of reacting used greatly reduces, and has the advantages such as energy-saving and environment friendly.
Description
Technical field
The present invention relates to the synthetic method of chemical intermediate, be specifically related to a kind of synthetic method of pseudo ionone.
Background technology
In recent years, supercritical fluid technology is widely used in chemical industry, it is found that the chemical reaction carried out in supercutical fluid is keeping or improving optionally simultaneously, can also improve speed of reaction, change reaction mechanism.Pseudo ionone is the important intermediate of essence and flavoring agent, vitamin A, E and the β-carotenes such as synthesis jononeionone, have detailed describing in US Patent No. 5453546 and German patent DE 19619557, in essence and flavoring agent, medicine, foodstuff additive and synthetic chemistry, purposes is also very extensive.The synthesis route of pseudo ionone mainly contains two: the first synthesis route is also the most frequently used commercial routes is under alkaline catalysts exists, carry out Aldol condensation with citral and acetone to generate pseudo ionone.Select sodium hydroxide catalyst, the product of 75% yield can be obtained.Along with the development of phase transfer catalytic technology, after being optimized sodium hydroxide catalyst, yield is the highest can reach 82%.The alkaline catalysts developed afterwards is as Ba (OH)
2saturated aqueous solution, Na
2o
2, sodium silk; Alcoholic solution sodium ethylate/ethanol, sodium hydroxide/ethyl alcohol, potassium hydroxide/methyl alcohol; KF/Al
2o
3, lithium hydroxide etc., yield can bring up to about 86%.Its shortcoming: basic catalyst is harsh to the requirement of conversion unit under high-temperature and high-pressure conditions, there is potential safety hazard, should not be applied in large production.The second synthetic route is then directly react to obtain etheric acid dehydrolinalool ester with dehydrolinalool and methyl aceto acetate, ketene dimer or pseudoallyl ether, then resets through claisen, thus obtained pseudo ionone.The excess raw material that this route relates to and product separation problem, side reaction is many, and yield is lower, and economic benefit is not remarkable.
Domestic and international Patents invention reports the synthetic method of multiple pseudo ionone, such as: patent US7141698 mentions and makees catalyzer with sodium hydroxide, citral inlet amount 386kg/h, 3800kg/h95% acetone (5%) sodium hydroxide compound, react in 112 DEG C of 160L reactors, acetic acid to be added in aftertreatment neutralize, cause great difficulty to the recycling of acetone, final citral transformation efficiency 93%.In High Temperature High Pressure, and in anhydrous response system, sodium hydroxide is very harsh to equipment requirements, easily " caustic embrittlement " phenomenon occurs, causes great potential safety hazard; Acetone consumption is more than 10 times (mass ratioes) of citral, reclaims energy consumption quite large; Aftertreatment is abnormal loaded down with trivial details, must first use in acetic acid and alkalescence, then be separated the acetate of generation, then go out product through rectifying separation.
Patent US4874900 reports the synthetic method of another pseudo ionone, preparation method and US7141698 similar, catalysts use lithium hydroxide, to the equally easy generation " caustic embrittlement " of conversion unit, yield is relatively also low, does not have economic benefit.
The synthetic method of the pseudo ionone of patent DE-A3319430 report, use mixed metal catalyst, temperature of reaction 280 DEG C, this synthetic method is quite difficult for post-reaction treatment, and productive rate is very low.
The synthetic method of the pseudo ionone of patent PL147748 report, adopts acetone and citral under the katalysis of alkali ion resin, and 56 DEG C are reacted 5 hours, and can obtain the finished product, but yield is quite low, without economic benefit, feasibility is explored.
Summary of the invention
The invention provides a kind of synthetic method of pseudo ionone, this synthetic method avoids the use of solvent and basic catalyst, greatly reduces the discharge of pollutent, and the yield of reaction is high.
A synthetic method for pseudo ionone, comprising: 230 ~ 300 DEG C, under the condition of 5 ~ 25MPa, acetone and citral generation condensation reaction, be isolated to described pseudo ionone after reacting completely.
In the present invention, overcritical acetone (critical temperature is 235.1 DEG C, and emergent pressure is 4.7MPa), both as reaction solvent, participates in and the reaction of citral under on-catalytic condition as reactant again, finally obtains highly purified pseudo ionone.Under overcritical acetone condition, the intermiscibility of acetone and citral increases greatly, decreases resistance to mass transfer, and speed of reaction improves greatly; The charging capacity of acetone can also be reduced in a large number; Do not introduce other solvent and catalyzer, can the discharge of decreasing pollution thing, almost accomplish zero release, meet green chemical industry theory.Reaction formula is as follows:
In this reaction, acetone namely as solvent also as reactant, the acetone under super critical condition is catalyzer equally, and the keto-enol change of acetone adds the acidity of its α-hydrogen, is shown below:
Under low pressure, acetone just has the acidity stronger than water, and when this means that temperature is greater than critical temperature, larger change can occur the acidity of acetone.Be very beneficial for the reaction of acetone and citral.But when being greater than certain temperature, can form more by product, yield declines on the contrary.As preferably, the temperature of described condensation reaction is 250 ~ 270 DEG C.
Reaction pressure also has larger impact to reaction yield, and the super critical condition maintaining solvent also needs certain pressure.Improve reaction pressure, although there is the generation of a small amount of by product, also improve the transformation efficiency of citral simultaneously, as preferably, the pressure of described condensation reaction is 18 ~ 21MPa, and transformation efficiency is up to 100%, and yield can reach 93.8%.
In the present invention, the consumption of acetone is excessive, as long as ensure that acetone is excessive, little on reaction impact, and as preferably, the quality of described acetone is 1.0 ~ 2.0 times of described citral.
In the present invention, the device of the employing of described synthetic method comprises:
High-pressure reactor;
The citral feeding pipe be connected with the entrance of high-pressure reactor respectively and acetone feed pipeline;
And the vaporizer to be connected with the outlet of high-pressure reactor and the product collecting device be connected with evaporator outlet;
Described citral feeding pipe comprises the citral fresh feed pump, citral force (forcing) pump and the citral flow control pump that are communicated with successively;
Described acetone feed pipeline comprises the acetone feed pump, acetone force (forcing) pump and the acetone flow control pump that are communicated with successively.
Described acetone enters high-pressure reactor continuously across acetone feed pump, acetone force (forcing) pump and acetone flow control pump successively, described citral enters described high-pressure reactor continuously across citral fresh feed pump, citral force (forcing) pump and citral flow control pump successively, described acetone and described citral carry out described condensation reaction in described high-pressure reactor, the reaction solution obtained enters vaporizer and is separated, and obtains described pseudo ionone.Now, after having reacted, the reaction solution of direct High Temperature High Pressure passes in vaporizer, and excessive acetone is isolated in flash distillation, greatly saves and reclaims acetone energy, simplify postprocessing working procedures.
As preferably, the feeding rate of described citral is 90 ~ 110g/min.
Under overcritical acetone condition, the intermiscibility of acetone and citral increases greatly, decrease resistance to mass transfer, speed of reaction improves greatly, as preferably, described acetone and the citral residence time in described high-pressure reactor is 0.5 ~ 20 minute, now best to reaction, the formation that the long residence time can increase by product, reduces yield.
As most preferably, the pressure of described condensation reaction is 21MPa, and temperature is 270 DEG C, and the residence time of described citral in described high-pressure reactor is 10 minutes, and now, the yield of reaction is up to 93.8%.
Compared with the existing technology, beneficial effect of the present invention is embodied in:
(1) adopt super critical condition to react, avoid the use of basic catalyst and solvent, reduce the corrosion to equipment, simultaneously more friendly to environment;
(2) adopt super critical condition to react, improve the yield of product, reduce cost.
Accompanying drawing explanation
The setting drawing of Fig. 1 synthetic method for pseudo ionone of the present invention, in figure, 1: acetone feed pump (acetone delivery pump); 2: citral fresh feed pump (citral delivery pump); 3, acetone force (forcing) pump (acetone supercharge pump); 4, acetone flow control pump (acetoneflow control pump); 5, citral force (forcing) pump (citral supercharge pump); 6, citral flow control pump (citral flow control pump); 7, high-pressure reactor (high-pressurereactor); 8, vaporizer (flash tank).
Embodiment
From setting drawing as shown in Figure 1, the setting drawing for the synthetic method of pseudo ionone comprises: high-pressure reactor 7, the citral feeding pipe that is connected with the entrance of high-pressure reactor 7 are respectively with acetone feed pipeline and the vaporizer 8 be connected with the outlet of high-pressure reactor and export with vaporizer 8 product collecting device (omitting in figure) be connected.
Described citral feeding pipe comprises the citral fresh feed pump 2, citral force (forcing) pump 5 and the citral flow control pump 6 that are communicated with successively; Described acetone feed pipeline comprises the acetone feed pump 1, acetone force (forcing) pump 3 and the acetone flow control pump 4 that are communicated with successively.
Use said apparatus, optimum reaction condition acetone: citral=0.5 ~ 2.0(mass ratio), the best is 1.0 ~ 2.0 times (mass ratioes), by acetone and citral after pressurizeing, be metered in high-pressure reactor, pressure-controlling is at 5 ~ 25MPa, and the best is 18 ~ 21MPa again; Reaction under high pressure actuator temperature controls at 230 DEG C ~ 300 DEG C, the best is 250 DEG C ~ 270 DEG C, in high-pressure reactor, the residence time is 0.5 ~ 20 minute, most optimal retention time is 5 ~ 15 minutes, after having reacted, reaction mass enters vaporizer, isolates raw material, obtain the product of higher concentration, obtain the pseudo ionone of more than 98.5% through simple rectifying.
Below in conjunction with specific embodiment, the present invention will be further described:
Embodiment 1
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 230 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 230 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 75.6%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 2770.24g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 73.1%.
Embodiment 2
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 240 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 240 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 97.2%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3505.44g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.5%.
Embodiment 3
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 250 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 250 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 98.1%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3516.8g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.8%.
Embodiment 4
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 260 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 260 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 98.5%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3535.76g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 93.3%.
Embodiment 5
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3554.70g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 93.8%.
Embodiment 6
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 280 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 280 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3467.54g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 91.5%.
Embodiment 7
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 290 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 290 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3418.27g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 90.2%.
Embodiment 8
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 300 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 300 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3346.27g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 88.3%.
Embodiment 9
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 5MPa, to enter pressure be in the reactor of 5MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 93.4%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3452.38g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 91.1%.
Embodiment 10
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 10MPa, to enter pressure be in the reactor of 10MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 95.1%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3486.49g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.0%.
Embodiment 11
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 15MPa, to enter pressure be in the reactor of 15MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 96.3%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3497.86g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.3%.
Embodiment 12
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 18MPa, to enter pressure be in the reactor of 18MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 99.2%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3520.59g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.9%.
Embodiment 13
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 25MPa, to enter pressure be in the reactor of 25MPa, temperature 270 DEG C, and controlling the residence time is 10 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3513.01g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.7%.
Embodiment 14
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 270 DEG C, and controlling the residence time is 0.5 minute.Online GC analyzes, and obtaining citral transformation efficiency is 91.5%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3429.64g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 90.5%.
Embodiment 15
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 270 DEG C, and controlling the residence time is 2.5 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 94.7%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3475.12g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 91.7%.
Embodiment 16
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, being pressurized to 21MPa, to enter pressure be in the reactor of 21MPa, temperature 270 DEG C, and controlling the residence time is 5 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 98.9%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3509.23g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 92.6%.
Embodiment 17
By the device described in Fig. 1, acetone feed amount is 100g/min, and citral inlet amount is 100g/min, respectively through pre-heating temperature elevation to 270 DEG C, be pressurized to 21MPa, entering pressure is in the reactor of 21MPa, temperature 270 DEG C, control the residence time be 20 minutes.Online GC analyzes, and obtaining citral transformation efficiency is 100%, and reaction solution, through the acetone of vaporizer excessive separation and product pseudo ionone, intercepts load half an hour.Treatedly obtain high purity product 3482.70g, analyze through GC, retention time and standard substance completely the same, GC purity is more than 94%, and yield is 91.9%.
According to the result of embodiment 1 ~ 17, obtain table 1, table 2 and table 3 respectively, investigate the impact on reaction result of reaction pressure, temperature of reaction and reaction times.
Table 1 temperature of reaction is on the impact of reaction result
a
| Embodiment | Temperature (DEG C) | Transformation efficiency (%) | Yield (%) | By product (%) |
| 1 | 230 | 75.6 | 73.1 | 2.5 |
| 2 | 240 | 97.2 | 92.5 | 4.7 |
| 3 | 250 | 98.1 | 92.8 | 5.3 |
| 4 | 260 | 98.5 | 93.3 | 5.2 |
| 5 | 270 | 100 | 93.8 | 5.6 |
| 6 | 280 | 100 | 91.5 | 6.9 |
| 7 | 290 | 100 | 90.2 | 7.3 |
| 8 | 300 | 100 | 88.3 | 8.5 |
aresidence time of material is about 10min, pressure 21MPa.
Table 2 reaction pressure is on the impact of reaction result
b
| Embodiment | Pressure (MPa) | Transformation efficiency (%) | Yield (%) | By product (%) |
| 9 | 5 | 93.4 | 91.1 | 2.3 |
| 10 | 10 | 95.1 | 92.0 | 3.1 |
| 11 | 15 | 96.3 | 92.3 | 4.0 |
| 12 | 18 | 99.2 | 92.9 | 6.3 |
| 5 | 21 | 100 | 93.8 | 5.6 |
| 14 | 25 | 100 | 92.7 | 7.1 |
bresidence time of material is about 10min, and temperature of reaction is 270 DEG C.
Table 3 reaction pressure is on the impact of reaction result
c
ctemperature of reaction is 270 DEG C, and reaction pressure is 21 MPa.
Claims (7)
1. a synthetic method for pseudo ionone, is characterized in that, comprising: 250 ~ 270 DEG C, under the condition of 5 ~ 25MPa, acetone and citral generation condensation reaction, be isolated to described pseudo ionone after reacting completely;
The equation of condensation reaction is as follows:
2. the synthetic method of pseudo ionone according to claim 1, is characterized in that, the pressure of described condensation reaction is 18 ~ 21MPa.
3. the synthetic method of pseudo ionone according to claim 1, is characterized in that, the quality of described acetone is 1.0 ~ 2.0 times of described citral.
4. the synthetic method of the pseudo ionone according to any one of claims 1 to 3, it is characterized in that, described acetone is successively continuously across acetone feed pump, acetone force (forcing) pump and acetone flow control pump enter high-pressure reactor, described citral is successively continuously across citral fresh feed pump, citral force (forcing) pump and citral flow control pump enter described high-pressure reactor, described acetone and described citral carry out described condensation reaction in described high-pressure reactor, the reaction solution obtained enters vaporizer and is separated, obtain described pseudo ionone.
5. the synthetic method of pseudo ionone according to claim 4, is characterized in that, the feeding rate of described citral is 90 ~ 110g/min.
6. the synthetic method of pseudo ionone according to claim 5, is characterized in that, described acetone and the citral residence time in described high-pressure reactor is 0.5 ~ 20 minute.
7. the synthetic method of pseudo ionone according to claim 4, is characterized in that, the pressure of described condensation reaction is 21MPa, and temperature is 270 DEG C, and the residence time of described citral in described high-pressure reactor is 10 minutes.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4874900A (en) * | 1987-06-16 | 1989-10-17 | Union Camp Corporation | Preparation of pseudoionones |
| CN102584552A (en) * | 2011-12-29 | 2012-07-18 | 浙江新和成股份有限公司 | Method for preparing benzalacetone under supercritical condition |
| CN103044223A (en) * | 2012-12-28 | 2013-04-17 | 安徽丰原发酵技术工程研究有限公司 | Method for continuously preparing pseudo ionone of vitamin A intermediate |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4874900A (en) * | 1987-06-16 | 1989-10-17 | Union Camp Corporation | Preparation of pseudoionones |
| CN102584552A (en) * | 2011-12-29 | 2012-07-18 | 浙江新和成股份有限公司 | Method for preparing benzalacetone under supercritical condition |
| CN103044223A (en) * | 2012-12-28 | 2013-04-17 | 安徽丰原发酵技术工程研究有限公司 | Method for continuously preparing pseudo ionone of vitamin A intermediate |
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