CN87102469A - The novel method of industrial production salicylaldhyde - Google Patents

Abstract

A kind of processing method that is used for the industrial production salicylaldhyde.Be on the basis of the operational path that makes salicylaldhyde from ortho-cresol through esterification, chlorination, hydrolysis three process, adopted the material proportion that helps suitability for industrialized production most.In hydrolyzing process, used effective diffusant, make muriate can be evenly and fully be beneficial to reaction and carry out fully, and by product has formed loose and tiny grainy sludge, not only helped the carrying out that reacts but also helped the removing of residue with the water effect.Each step of this law reaction does not use solvent, intermediate not to need to carry out intermediate treatment.

Description

The novel method of industrial production salicylaldhyde

The present invention is a kind of processing method of industrial production salicylaldhyde.Characteristics are on the basis of the operational path that makes salicylic aldehyde from ortho-cresol through esterification, chlorination, hydrolysis three process, adopted the material proportion that helps suitability for industrialized production most, and in hydrolyzing process, used diffusant, sodium methylene bis-naphthalene sulfonate (NNO) particularly, make in the hydrolysis muriate can be evenly and fully and the water effect, reaction be carried out fully.Owing to added diffusant, by product forms loose and tiny grainy sludge, both helped the carrying out that react, helping residue again removes, change in the hydrolytic process the high poly-by product caking of resin and condensed upon and be difficult on the reactor wall remove, and in caking, comprised the phenomenon that a large amount of not materials of complete hydrolysis make it not continue to react.

Preparation or industrial production salicylaldhyde generally can be summed up as two big classes in the past: a class is to make salicylaldhyde from phenol through benzene phenol-chloroform method or phenol-chlorination carbon high pressure synthesis method, though these method technologies are simple, but it is lower to exist yield, raw material consumption is big, phenolic wastewater is difficult for handling, and processing requirement adopts shortcomings such as high-tension apparatus.The boric acid ester route is newer, but complex process, and need to use palladium/carbon catalytic oxidant, (industrial economy is worth not high) costs an arm and a leg.In addition, the somebody studied phenol, and the formaldehyde one-step synthesis shows through the trial production of full scale plant: its long reaction time, and yield yields poorly, and effect is also undesirable; Another kind of is to be the synthetic method of raw material from ortho-cresol.Adopt this method raw material easily to reach, cheap.Through esterification, chlorination and hydrolysis reaction make product from ortho-cresol.Formed different routes because the formed esterification protecting group of esterification step is different, mainly contained three kinds and see Table one

Bo Litongfa is owing to make raw material with phosgene, and it is limited to originate, and the accumulating difficulty is produced danger greatly, and no matter phosphoric acid ester method and acetic ester method are from yield, raw materials cost, or the reaction conditions aspect considers that people think that the former is more superior.

The present invention just is being based on the phosphoric acid ester route, and above-mentioned various shortcoming makes improvements in order to overcome.

Above-mentioned task is the material proportion that helps suitability for industrialized production most by having adopted, and the method for use diffusant is finished in hydrolyzing process.

This law is produced salicylaldhyde, in esterification step, adopted and be furnished with stirring, the reactor of widely different flow condenser and gas-liquid separator, with ortho-cresol and phosphorus oxychloride in 1: 0.502～0.54 best 1: 0.502～0.52(mole number) ratio once drop in the still; In ortho-cresol: magnesium oxide=1(mole): the 0.1(gram)～the 0.2(gram) 1(mole preferably): the ratio 0.1(gram) drops into appropriate amount of catalysts (magnesium oxide).In 4～8 hours, make reactive system be warming up to 150 ℃～180 ℃ preferably 170 ℃～180 ℃.At first in 1 hour, make system be warming up to 80 ℃, be warming up to 130 ℃ in 4 hours, be warming up to again about 170 ℃ in 2 hours.Be incubated 1～3 hour, to reacting completely.Strict proportioning raw materials and to the control of heat-up rate has guaranteed that each components contents remains in the optimal scope (two ester contents＞65%) in the esterification products.

Chloride process adopts stirring-type blistering reaction still to mix with enhancement of heat transfer and promotion gas-liquid two-phase, takes negative-pressure operation, is convenient to hydrogenchloride and discharges in time and prevent that gas reactor from overflowing.The esterification material is once dropped into chlorination tank, allow chlorine enter reactor when being warming up to 150 ℃ from stirring arm below continuous bubbling, regulate flow so that gas, liquid distributes and to be in the logical chlorine dose of optimum regime generally at 50～150 gram/kilogram esters hour, preferably be controlled in the scope of 65～90 gram/kilogram esters hour, still is pressed and is remained on 960mmH ₂About O, temperature remains in 190 ℃～200 ℃ the scope.By the proportion of assaying reaction thing, chlorinity is controlled reaction end (D ²⁰ ₄1.50～1.52 D preferably ²⁰ ₄1.505～1.51, chlorinity (weight) 30～40% preferably 36～40%).The strict control chlorination degree of depth also prevents that impurity from bringing reactor into, is beneficial to be controlled at bottom line with paying reaction.

Hydrolyzing process adopts and has agitator, condenser, the jacketed type reactor of aldehyde water separator, chloride material is equipped with an amount of water and diffusant input reactor, material proportion is generally, muriate: water: NNO diffusant=1: 3: 0.05～10/100 part weight muriate, preferably 1: 3: 0.5～2.5/100 part weight muriate.Be warming up to 103 ℃～110 ℃ with steam by the chuck heating system, the adjacent hydroxyl formaldehyde that hydrolysis is come out distills with the form of aldehyde-water azeotrope immediately.After layering, water is widely different again to be flow in the still.Afterreaction finished in about 5～8 hours.Owing to adopted the proportioning of rational muriate and water, not only reduced the consumption of water, and also very favourable to hydrolysis reaction, particularly added diffusant, the dispersing property of muriate in water improved, hydrolysis is more abundant; Hydrolytic residue is loose, and particle is thin and even, is convenient to remove.

Adopt this law to produce salicylaldhyde product purity is brought up to more than 95%, yield is brought up to about 60%.

Embodiment is as follows:

210 kilograms of (1.3 moles) phosphorus oxychloride of 275.5 kilograms of (2.5 moles) ortho-cresols and 0.25 kilogram of magnesium oxide are dropped into 500L and are furnished with the stirring anchor, in the reactor of condenser and cyclonic separator.In greater than 1 hour material is warming up to 80 ℃, was warming up to 130 ℃ with 100 ℃ in 4 hours, be warming up to 170 ℃ again in 2.5 hours, be incubated 2 hours then, getting proportion is D ²⁰ ₄1.25 chloride content is 10% esterification products.

With esterification products input-500L and be furnished with stirring arm, in the reactor of Chlorination tube and cyclonic separator.System is warming up to begins logical chlorine more than 150 ℃.Logical chlorine speed is 36 kilograms/hour.Still is pressed and is kept 960mmH ₂About O, temperature remains in 190 ℃～200 ℃ the scope, and after about 15～16 hours, the assaying reaction material ratio weighs 1.51, and during chloride content 39%, chlorination reaction is promptly accused and finished.

Chlorizate and 1630 kg of water and 2.7 kilograms of NNO diffusants are dropped into-are furnished with the stirring anchor, in the hydrolytic reaction pot of the jacketed type of condenser and aldehyde water separator, when system is warming up to 105 ℃, distillation begins to carry out, the aldehyde water mixed liquid is after the condensation layering, and water is widely different to be flow in the still, after about 8 hours, hydrolysis reaction is complete, content is 198.25 kilograms of salicylaldhydes more than 95%.

Adopt each step reaction of this law not use any solvent, improved utilization rate of equipment and installations, removed desolventizing equipment from, saved energy, simplified operation. Reaction intermediate need not separate, and purifies or intermediate treatment, makes each procedure connection of flow process compacter. Particularly hydrolyzing process has successfully adopted activating agent, has improved the dispersiveness of material in water, has strengthened hydrolysis and has improved the proterties of hydrolytic residue, is easy to remove. Adopt this technology owing to react completely, make the only 0.172PPm of the phenol amount that contains in the waste water.

Claims (5)

1, a kind of by the ortho-cresol esterification, chlorination, the processing method of hydrolysis suitability for industrialized production salicylaldhyde is characterized in that: the esterification step material proportion is ortho-cresol: phosphorus oxychloride: magnesium oxide=1 (mole): 0.502 (mole)～0.54 (mole)～: 0.1 (gram)～0.2 (gram); The logical chlorine dose of chloride process is controlled at 50～150 gram/kilogram esters hour; Hydrolyzing process has used diffusant, sodium methylene bis-naphthalene sulfonate (NNO) preferably, and its consumption is 0.05～10/100 of a muriate weight.

2, in accordance with the method for claim 1, it is characterized in that: the esterification step material proportion is preferably, ortho-cresol: phosphorus oxychloride: magnesium oxide=1(mole): the 0.502(mole)～and the 0.52(mole): the 0.1(gram).

According to claim 1 or 2 described methods, it is characterized in that 3, the logical chlorine dose of chloride process preferably is controlled at 65～90 gram/kilogram esters hour.

According to claim 1 or 2 described methods, it is characterized in that 4, the usage quantity as the sodium methylene bis-naphthalene sulfonate (NNO) of diffusant in the hydrolyzing process is preferably 0.5～2.5/100 of muriate weight.

5, in accordance with the method for claim 3, it is characterized in that the usage quantity as the sodium methylene bis-naphthalene sulfonate (NNO) of diffusant in the hydrolyzing process is preferably 0.5～2.5/100 of muriate weight.