CN102432550A - Methods for preparing sulfadoxine and intermediate of sulfadoxine - Google Patents
Methods for preparing sulfadoxine and intermediate of sulfadoxine Download PDFInfo
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Abstract
The invention relates to methods for preparing sulfadoxine and an intermediate of the sulfadoxine. The method for preparing the sulfadoxine sequentially comprises the following steps of: (1), in the presence of sodium ethylate, reacting methyl methoxyacetate with excessive diethyl oxalate to generate 3-methoxyl-2-oxo-ethyl methyl succinate, decarbonylating the 3-methoxyl-2-oxo-ethyl methyl succinate to obtain 2-methoxyl-ethyl methyl malonate; (2) reacting the 2-methoxyl-ethyl methyl malonate with formamide to generate a cyclized compound; (3) reacting the cyclized compound with phosphorus oxychloride to generate chloride; (4) performing condensation reaction; and (5) performing methyl oxidation reaction, wherein the purity of the 2-methoxyl-ethyl methyl malonate which is obtained in the step (1) is controlled to be more than or equal to 95 weight percent. By adoption of the methods, the purity of the 2-methoxyl-ethyl methyl malonate is effectively controlled to be more than 95 weight percent, the quality of the cyclized compound for cyclization reaction in next step can be improved, operation is simplified, and production cost is reduced.
Description
Technical field
The invention belongs to the sulfa drugs preparing technical field, particularly a kind of sulphormethoxine and intermediates preparation thereof.
Background technology
Sulphormethoxine, chemistry 4-(p-amino benzene sulfonyl)-5 by name, the 6-dimethoxypyridin, structural formula is following:
Sulphormethoxine can be used for treating general inflammation clinically, like upper respiratory tract infection tonsillitis, bacillary dysentery enteritis, skin infections etc., also can with other medicine compatibilities, treatment pulmonary tuberculosis, lymphoid tuberculosis; It also has certain curative effect to leprosy (crazy) disease, also can treat malaria, and in addition, sulphormethoxine also can be made the sick prophylactic of rheumatic.When being used for such use, it is long that sulphormethoxine has curative effect, the characteristics that toxicity is low.
Sulphormethoxine has experienced several generations' research and development, domesticly begins development in the eighties, and the situ production in three to five years of its production technique experience is progressively stable.Domestic sulphormethoxine traditional technology was implemented nearly 30 years, went through several generations' improvement, was limited to the condition restriction of scientific effort, comprised the restriction of novel material, new technology etc., and do not have more suitably technology substitutes traditional technology always.Traditional sulphormethoxine makes through following steps:
Step (1):
Step (2):
Step (3):
Step (4):
Step (5):
There is following problem in above-mentioned technology:
1, step (1) Ke Shi reaction is carried out raw material in sodium ethylate/ethanolic soln, and after the decarbonylation, removes low-boiling-point substance through first fractionation and (comprise unreacted raw material; Intermediate A 3 etc.); Fractionation obtains midbody 2-methoxyl group-propanedioic acid methyl ethyl ester then, and the purity lower (generally being lower than 92%) of this method gained 2-methoxyl group-propanedioic acid methyl ethyl ester is unfavorable for follow-up reaction; Particularly in big trial production, influenced the quality and the yield of sulphormethoxine product.
2, step (2) ring-closure reaction gained cyclocomplex is of poor quality: traditional method separates out cyclocomplex under acidic conditions; Gained cyclocomplex (A5) can exist with hydroxylic species and two kinds of forms of hydroxyl sodium salt, because hydroxylic species has certain solubleness in water, makes and must apply mechanically repeatedly the mother liquor of ring-closure reaction in the traditional technology; And make the salt concentration in the mother liquor quite big because of applying mechanically mother liquor; Cause cyclocomplex (nearly 40% salt is wherein arranged) of poor quality, material is clamminess, shortcomings such as difficult oven dry; And the environment of slant acidity is to equipment pipe, and whizzer, drying room all produce corrosive nature, and production site is difficult for cleaning.
3, the preparation of step (3) muriate (A6) must be adopted N; Accelerine is as catalyzer, make catalyzer recovery and apply mechanically the bigger expense of generation, and; The muriate quality is garnet; To next step condensation reaction obviously is disadvantageous, and the color and luster of condensation reaction is red partially, and it is yellow partially directly can to have influence on finished product (quality) color and luster.
4, sodium methylate/methanol solution is adopted in step (5) methoxy reaction; In post-processing stages; Recovery methyl alcohol is difficult for to the greatest extent, and recovery stage is inhomogeneous than causing long heat-up time the interior bottoms material of (product) reaction kettle to be heated, and causes local superheating; Produce decomposing phenomenon, and the color and luster of bullion is not ideal enough.
To sum up, the total recovery of traditional method is the highest only to be reached about 65%, and production cost is higher, and the quality of product is still waiting further improvement.
Summary of the invention
Technical problem to be solved by this invention is the deficiency that overcomes prior art, and a kind of preparation method of improved sulphormethoxine is provided.
The present invention also will provide a kind of improved sulphormethoxine intermediates preparation simultaneously.
For solving the problems of the technologies described above, the present invention adopts following technical scheme:
A kind of preparation method of sulphormethoxine, it comprises the following step of carrying out successively:
(1), methoxy menthyl acetate and excessive oxalic acid diethyl ester are reacted generate 3-methoxyl group-oxosuccinic acid methyl ethyl ester in the presence of sodium ethylate, and make 3-methoxyl group-further decarbonylation of oxosuccinic acid methyl ethyl ester obtain 2-methoxyl group-propanedioic acid methyl ethyl ester;
(2), step (1) gained 2-methoxyl group-propanedioic acid methyl ethyl ester and methane amide are reacted in the presence of sodium methylate and generate cyclocomplex;
(3), make step (2) gained cyclocomplex and phosphorus oxychloride reaction generate 4,6-two chloro-5-methoxy pyrimidines;
(4), make step (3) gained 4,6-two chloro-5-methoxy pyrimidines with SULFAMIDE sodium generation condensation reaction is generated 4-(p-amino benzene sulfonyl)-5-methoxyl group-6-chloropyrimide;
(5), make step (4) gained 4-(p-amino benzene sulfonyl) 5-methoxyl group-6-chloropyrimide generation methoxy reaction generate 4-(p-amino benzene sulfonyl)-5, the 6-dimethoxypyridin,
In the step (1), described sodium ethylate is a solid form, and generates being reflected under the temperature that temperature is lower than 65 ℃ of 3-methoxyl group-oxosuccinic acid methyl ethyl ester and carry out; After decarbonylation finishes; Reclaim low-boiling-point substance through the separation column vacuum fractionation; Said low-boiling-point substance is to be present in the material that all boiling points in the system are lower than 2-methoxyl group-propanedioic acid methyl ethyl ester; Divide remove low-boiling-point substance after, without separation column, directly cool off residual reaction liquid and promptly get purity more than or equal to 2-methoxyl group-propanedioic acid methyl ethyl ester of 95%.
According to further embodiment of the present invention: in the step (1); The implementation process that generates the reaction of 3-methoxyl group-oxosuccinic acid methyl ethyl ester is: in the exsiccant reaction kettle, add methoxy menthyl acetate and excessive oxalic acid diethyl ester; Under agitation condition; Solid sodium ethanol is dropped in the reaction kettle, and the control reacting liquid temperature is no more than 65 ℃, again in 45～65 ℃ of following insulation reaction of temperature more than 0.5 hour.Wherein: the preferred molar ratio of methoxy menthyl acetate and oxalic acid diethyl ester is 1: 1.02～1.18.
According to a preferred aspect of the present invention, after the reaction that generates 3-methoxyl group-oxosuccinic acid methyl ethyl ester finishes, earlier reaction solution is used anhydrous organic solvent diluting; Using inorganic aqueous acid to regulate pH again is 1～2; Leave standstill, layering is after wherein organic solvent layer reclaims organic solvent; Under 175～200 ℃ of temperature, decarbonylation was carried out in the normal pressure insulation in 2～5 hours.More specifically, be cooled to below 30 ℃, join the adjusting of carrying out said pH in the mixed solution of forming by water, mineral acid and trieline that is cooled to below 30 ℃ through reaction solution with dilution.The organic solvent of dilution usefulness is preferably trieline, and reclaims trieline through air distillation.Said mineral acid is preferably hydrochloric acid.The present invention also preferably adds trichloroethylene solvent in the low-boiling-point substance that obtains through fractionation, vacuum fractionation is collected the part of just boiling, and obtains content at the oxalic acid diethyl ester more than 95%.This oxalic acid diethyl ester can be applied mechanically.
The another technical scheme that the present invention takes is: a kind of sulphormethoxine intermediates preparation; Said sulphormethoxine midbody is 2-methoxyl group-propanedioic acid methyl ethyl ester; Said preparation method reacts methoxy menthyl acetate and excessive oxalic acid diethyl ester to generate 3-methoxyl group-oxosuccinic acid methyl ethyl ester in the presence of sodium ethylate; And make 3-methoxyl group-further decarbonylation of oxosuccinic acid methyl ethyl ester obtain 2-methoxyl group-propanedioic acid methyl ethyl ester; Described sodium ethylate is a solid form, and generates being reflected under the temperature that temperature is lower than 65 ℃ of 3-methoxyl group-oxosuccinic acid methyl ethyl ester and carry out; After decarbonylation finishes; Reclaim low-boiling-point substance through the separation column vacuum fractionation; Said low-boiling-point substance is to be present in the material that all boiling points in the system are lower than 2-methoxyl group-propanedioic acid methyl ethyl ester; Divide remove low-boiling-point substance after, without separation column, directly cool off residual reaction liquid and promptly get purity more than or equal to 2-methoxyl group-propanedioic acid methyl ethyl ester of 95%.
According to a preferred aspect of the present invention; The implementation process that generates the reaction of 3-methoxyl group-oxosuccinic acid methyl ethyl ester is: in the exsiccant reaction kettle, add methoxy menthyl acetate and excessive oxalic acid diethyl ester; Under agitation condition; Solid sodium ethanol is dropped in the reaction kettle, and the control reacting liquid temperature is no more than 65 ℃, again in 45～65 ℃ of following insulation reaction of temperature more than 0.5 hour.Further preferred, after the reaction of generation 3-methoxyl group-oxosuccinic acid methyl ethyl ester finishes, reaction solution is used earlier anhydrous organic solvent diluting; It is 1～2 that the back uses inorganic aqueous acid to regulate pH; Leave standstill, layering is after wherein organic solvent layer reclaims organic solvent; Under 170～200 ℃ of temperature, decarbonylation was carried out in the normal pressure insulation in 2～5 hours.Wherein, the organic solvent that said dilution is used is trieline, reclaims trieline through air distillation.
Synthetic route of the present invention is represented as follows with chemical equation:
Owing to take above technical scheme; The present invention compared with prior art has following advantage: the present invention carries out methoxy menthyl acetate and oxalic acid diethyl ester in the presence of solid sodium ethanol; And after decarbonylation; Directly the low-boiling-point substance fractionation is removed, and remaining mother liquor be purity more than 90%-methoxyl group-propanedioic acid methyl ethyl ester.The content of 2-methoxyl group-propanedioic acid methyl ethyl ester that strict controlled step (1) is produced is more than 95%, and total impurities content is lower than 5%, helps improving the quality of the cyclocomplex of next step ring-closure reaction, and then improves the quality of the finished product sulphormethoxine.In addition, though the individual event yield of the present invention's step (1) possibly descend than prior art to some extent, can improve the yield of step (2) ring-closure reaction greatly owing to the raising of step (1) product quality; In general; The inventive method yield improves, and cost reduces, the finished product quality-improving.
Embodiment
Below in conjunction with concrete embodiment the present invention is done further detailed explanation, but the invention is not restricted to following examples.
Embodiment 1 preparation 2-methoxyl group-propanedioic acid methyl ethyl ester (A4)
(1) reaction equation is following:
(2) charge ratio is seen table 1.
Table 1
| Material name | Charging capacity (kg) | Molecular weight | Mol ratio |
| A1 (methoxy menthyl acetate) | 175 | 104 | 1 |
| A2 (oxalic acid diethyl ester) | 280 | 146 | 1.14 |
| Solid sodium ethanol | 130 | 68 | 1.12 |
(3) specific operation process is following:
With reaction kettle dry (normal batch reaction reaction kettle does not need washing), methoxy menthyl acetate is mixed in mixed ester pot with oxalic acid diethyl ester, and be cooled to below 10 ℃; Add reaction kettle, under agitation condition, solid sodium ethanol poured into (the sodium ethylate packing should not tear zero open in the reaction kettle; Should be unit with the sodium ethylate minimum package when feeding intake, gradation be poured into), exothermic heat of reaction; Control reaction temperature surpasses 65 ℃, and insulation made to react completely more than 0.5 hour between 45～65 ℃ of temperature again.
In dilution pot, add 280 liters of trielines (annotate: the trieline of dilution usefulness is suitable anhydrous), below the first precooling to 30 of dilution pot ℃, will react feed liquid and put into the dilution pot, stirring is cooled off.Then feed liquid is pressed into the acidifying storage tank.
Put into 500 liters in water in the acidifying pot, 200 liters of 30% hydrochloric acid, 350 liters of trielines are cooled to below 10 ℃, add reaction solution, and controlled temperature is below 15 ℃, and (acidity must reach in pH=1～2! Peaceful acid is alkali not), static after the acidifying, tell the trieline layer and advance the transfer pot, and be pressed in the layering pot.Water layer is used trieline layer 200,200,200,150 repeatedly, 150,150,350 liters of extractions, and 350 liters of last extracting solution covers are used in down to be criticized.The trieline layer is treated standing demix, and following trieline layer gets into reinforced high-order.Normal pressure reclaims trichloroethylene solvent, and temperature is to 105～110 ℃ in the final control, and reclaim under reduced pressure does not more finally go out to trieline, and the trieline of recovery is recyclable applying mechanically after water washing to pH value 6～7.180 ± 2 ℃ of interior temperature, vacuum tightness-0.04～-0.053MPa, decarbonylation 4 hours, underpressure distillation again, collection vacuum tightness >=-0.095MPa, temperature is Ke Shi thing A4 at 170 ± 10 ℃, finally steams to 180～190 ℃.Obtain at last, Ke Shi thing A4 content >=95% (GC) gets weight range: 220～240kg
Embodiment 2 preparation cyclocomplex-hydroxyl sodium salts (A5)
(1) reaction equation is following:
(2) charge ratio is seen table 2.
Table 2
| Material name | Charging capacity (kg) | Molecular weight | Mol ratio |
| A4 (Ke Shi thing) | 240 | 176 | 1 |
| Methane amide | 186 | 45 | 3.37 |
| Liquid methanol sodium | 830 | 54 | 3.46 |
(3) specific operation process is following:
Earlier that reaction kettle is dry, drop into liquid methanol sodium, stir, be heated to 60～68 ℃; Add methane amide, add step (1) gained A4 then equably, it is 65～70 ℃ that control adds fashionable temperature; Joining day is 1～1.5 hour, and adding finishes, and insulation reaction is more than 0.5 hour.Normal temperature reclaims methyl alcohol, and reclaim under reduced pressure methyl alcohol does not extremely go out then, and then adds entry 1000L; Normal pressure reclaims has water methanol to clarification; Outlet temperature is cooled to below 40 ℃, beginning discharging, centrifuge dehydration; Dry discharging, get into the recirculating air oven drying obtain at last moisture content below 0.5% and cyclocomplex-hydroxyl sodium salt HPLC content more than or equal to cyclocomplex-hydroxyl sodium salt A5 of 92%.Every batch of positive lot number can obtain 200～212kg cyclocomplex-hydroxyl sodium salt.
Embodiment 3 preparation muriates (A6)
(1) reaction equation is following:
(2) charge ratio is seen table 3.
Table 3
| Material name | Charging capacity (kg) | Molecular weight | Mol ratio |
| A5 (cyclocomplex of embodiment 2 preparations) | 240 | 186 | 1 |
| Phosphorus Oxychloride | 825 | 153 | 4.17 |
| Trieline | 900 | 131 | / |
(3) specific operation process is following:
In reactor, (cover tight pot cover), be pressed into the Phosphorus Oxychloride of getting ready in advance.Open and reflux and the hydrogen chloride gas absorption unit, logically be steam heated to 40 ℃, steam off heats up naturally; Beginning slowly adds cyclocomplex-hydroxyl sodium salt (A5); Control adding speed, (adding the string temperature phenomenon that fashionable attention has burst, about ten to 20 minutes); Add remaining cyclocomplex-hydroxyl sodium salt, added in about 0.5～1.5 hour.Suitably need cooling, can open water quench, open the hydrogen chloride absorption device to control interior temperature.After adding the hydroxyl sodium salt, stablize ten minutes after, open heating (steam), rise to 110～120 ℃ (117 ℃) to interior temperature and reflux and insulation.Insulation is more than 0.5 hour, and reaction finishes (hydrogen chloride tail gas seldom).
In reclaiming the Phosphorus Oxychloride pot (dry), the reclaim under reduced pressure Phosphorus Oxychloride is done to material, and the steam off valve is cooled to 90～100 ℃, the trieline 900L in the high position is put into reclaim pot, stirs.In hydrolyzer, add entry 1500kg, start and stir and open and cool off, make hydrolysis temperature be no more than 75 ℃, in the chlorated liquid adding hydrolyzer with the dilution of the trieline in the concentrating pan.After hydrolyzed solution stirred, layering in static 10 minutes was told trieline layer position and is extracted for the first time.When extracting for the second time, add 300 liters of trielines, when extracting for the third time, be pressed into 200 liters of trielines.(annotate: whether need to extract for the 4th time, see chloride in the extracting solution for the third time what come fixed).United extraction liquid in washing pot, with soda ash pH6.5～7 that neutralize, and closes pot cover and stops stirring, and surveys pH6.5～7 with water washing 30 minutes with test paper, and washing is complete, closes water, left standstill 10 minutes, and branch vibration layer, feed liquid is pressed into high-order storage tank; Put into still pot and reclaim trieline, steam off, reclaim under reduced pressure does not flow out to there being trieline again; Blowing, natural air drying obtains content at the muriate more than 98.5% to dry, and wherein dissolvent residual is less than 1%; Muriate A6 fusing point >=52 ℃ gets weight range: 190～210kg.
Embodiment 4 preparation 4-(p-amino benzene sulfonyl)-5-methoxyl group-6-chloropyrimide (A7)
(1) reaction equation:
(2) charge ratio is seen table 4.
Table 4
| Material name | Charging capacity (kg) | Molecular weight | Mol ratio |
| A6 (muriates of embodiment 3 preparations) | 88 | 179 | 1 |
| Sulfanilamide (SN) sodium | 200～210 | 194 | 1.93 |
| N (DMF) | 270 | 73 | / |
| Hydrochloric acid | 60 | 38 | / |
(3) specific operation process is following:
Under the room temperature, the 270kg N is dropped in the exsiccant condensation reaction pot, start stirring, drop into half sulfanilamide (SN) sodium, drop into 72kg 5-methoxyl group-4 again, 6-dichloro pyrimidine (A 6), half the sulfanilamide (SN) sodium with remainder drops in the lump at last.Naturally be warming up to 60 ℃, survey pH value 8～9, survey pH value 8～9 during (available chilled water modulation) controlled temperature to 90 ± 2 ℃ and be incubated 1.5 hours; Insulation finishes, and drives vacuum pump, reclaims D.M.F, control vacuum tightness>=-0.098MPa, outlet temperature is 120～130 ℃ (interior temperature). and yield is (recyclable the applying mechanically of DMF moisture≤3.0% of recovery) about 250Kg; The hot water that adds 500Kg90～100 ℃ then, treat all dissolvings after, be pressed into cooling pan, prepare cooling pan in advance and add water at 300～400L; Then, 6 add 10～15% hydrochloric acid then, and regulating pH is 7.0～7.2, is cooled to 15～20 ℃, spinning sulfanilamide (SN), be washed with water to mother liquor water clear till, dry; Temperature drips 10～15% hydrochloric acid acid out at 70 ± 2 ℃, and acid out endpoint pH 3.8～4.1, sedimentation speed want slow, are controlled at 20～40 minutes, and centrifuge dehydration is then clarified with hot wash to liquid outlet more than 90 ℃, dries discharging; In 110 ± 5 ℃ of dryings 1.5～3 hours, cooling discharging please be tested analysis, content>=90%, and fusing point>=193 ℃, moisture≤0.5%, condenses A7 gets weight range: 120～130kg.
Embodiment 5 preparation sulphormethoxine (A8)
(1) reaction equation:
(2) charge ratio is referring to table 5.
Table 5
| Material name | Charging capacity (kg) | Molecular weight | Mol ratio |
| A7 (condensess of embodiment 4 preparations) | 240 | 324.5 | 1 |
| Methyl alcohol | 960 | 32 | / |
| Solid sodium hydroxide | 103 | 40 | 3.66 |
| Gac | 20 | 12 | / |
| Glacial acetic acid min. 99.5 | 100 | 60 | / |
(3) concrete operations are following:
A methyl alcohol suction high position is put into reaction kettle, open chuck and advance water coolant, open reverse flow valve, drop into solid sodium hydroxide, open stirring, controlled temperature does not surpass 60 ℃; After stablizing 10 minutes, drop into condenses, slowly be warming up to 69～72 ℃, reflux insulation more than 0.5 hour, reaction finishes; Closing volume valve, normal pressure reclaim anhydrous methanol, and reclaim under reduced pressure does not go out methyl alcohol to looking handleless cup again, and closing anhydrous opening of valves has water valve, adds more than the about 100Kg of water, and continuing recovery has more than the water methanol to 80 ℃, and feed liquid is pressed into dissolving pan; With 25～30% hydrochloric acid reacting liquid pH value is transferred to 9.5～10.5, adds water and make the about 2000L of total amount, pour gac 20Kg into, 60 ℃ of insulation decolourings 1 hour; Decolouring is finished, and feed liquid is back to clearly through pressure filter, is delivered to the bullion clarifying kettle; Slowly dripping glacial acetic acid solution more than 60 ℃, to pH value 4.5～6 be terminal point, after stirring repetition measurement pH value is errorless; Water washing is used in centrifuge dehydration, dries discharging and gets Sulphadoxine bullion (tide article) A8; Weight loss on drying≤20%, content>=98% gets weight range: 250～280kg.
The embodiment 6 refining sulphormethoxine finished products that obtain
Table 6
In Decolouring pot, add purified water, calcium hydroxide, heating; Stir adding bullion down, regulate above its of pH value to 9 and dissolve entirely, add gac, temperature is incubated more than 0.5 hour more than 60 ℃; Be back to clearly through pressure filter,, be delivered in the elaboration crystallizing pan of cleaning through being covered with the monolithic pressure filter of two metafiltration cloth one deck filter paper; More than 60 ℃, drip glacial acetic acid solution, to pH value 4.5～6; Repetition measurement pH value is constant, and centrifuge dehydration is with purified water wash crystallization pot, and filter cake washs to liquid outlet with purified water and clarifies; Centrifuge dripping 30 minutes, discharging; The tide article evenly are layered in the drip pan, put into the thermal cycling oven drying, be cooled to 45 ℃ with bottom discharge.Behind the crushing screening (according to customer requirement decision smashing fineness), the finished product week turning barrel of packing into, weighing please be tested analysis, analyzes qualified after, send into the mixing post and mix, every batch produce weight range: 200～210kg; Mixing, wrapping process: after production batch analysis was qualified, several batches of finished products need mix 10 minutes through the mixing of V-type rotary blender at every turn, and were static, put into finished barrel one by one, and weighing after the QC sampling inspection is qualified, is packed (the 25kg/ bucket is formed 500kg/ commerce and criticized) and put in storage.
The above embodiments 1 to 6 have constituted the production technology of sulphormethoxine, and on the whole, it has following characteristics:
1, technology is succinct, and is easy to operate, and the quality of product is improved.
2, the starting material unit consumption has bigger decline, and this is because the technology after improving is very easy to operate, produces highly stable; Raw materials cost drops to about 110,000 from about 150,000, by producing about 400 tons per year, this technology considerable economic benefit.
3, the maintenance of equipment and maintenance are improved greatly, demonstrate fully in cyclization, on the post of chlorination reaction.
4, production environment is improved greatly, owing to stop using N, N-xylidene(s), production plant do not have N fully, the taste of N-xylidene(s).
5, the application of this technology has greatly improved the discharging of the three wastes, has alleviated the pressure of environmental protection treatment.The aftertreatment wastewater flow rate in chlorination post reduces, and through simple process after high concentrations of phosphoric acid solution, be converted into phosphate fertilizer by phosphate fertilizer plant and be generalized to agriculture prodn later on, the annual phosphorus that reduces up to a hundred tons discharges.
More than the present invention has been done detailed description; Its purpose is to let the personage that is familiar with this art can understand content of the present invention and implements; Can not limit protection scope of the present invention with this; All equivalences of doing according to spirit of the present invention change or modify, and all should be encompassed in protection scope of the present invention.
Claims (10)
1. the preparation method of a sulphormethoxine, it comprises the following step of carrying out successively:
(1), methoxy menthyl acetate and excessive oxalic acid diethyl ester are reacted generate 3-methoxyl group-oxosuccinic acid methyl ethyl ester in the presence of sodium ethylate, and make 3-methoxyl group-further decarbonylation of oxosuccinic acid methyl ethyl ester obtain 2-methoxyl group-propanedioic acid methyl ethyl ester;
(2), step (1) gained 2-methoxyl group-propanedioic acid methyl ethyl ester and methane amide are reacted in the presence of sodium methylate and generate cyclocomplex;
(3), make step (2) gained cyclocomplex and phosphorus oxychloride reaction generate 4,6-two chloro-5-methoxy pyrimidines;
(4), make step (3) gained 4,6-two chloro-5-methoxy pyrimidines with SULFAMIDE sodium generation condensation reaction is generated 4-(p-amino benzene sulfonyl)-5-methoxyl group-6-chloropyrimide;
(5), make step (4) gained 4-(p-amino benzene sulfonyl) 5-methoxyl group-6-chloropyrimide generation methoxy reaction generate 4-(p-amino benzene sulfonyl)-5, the 6-dimethoxypyridin,
It is characterized in that: in the step (1), described sodium ethylate is a solid form, and generates being reflected under the temperature that temperature is lower than 65 ℃ of 3-methoxyl group-oxosuccinic acid methyl ethyl ester and carry out; After decarbonylation finishes; Reclaim low-boiling-point substance through the separation column vacuum fractionation; Said low-boiling-point substance is to be present in the material that all boiling points in the system are lower than 2-methoxyl group-propanedioic acid methyl ethyl ester; Divide remove low-boiling-point substance after, without separation column, directly cool off residual reaction liquid and promptly get purity more than or equal to 2-methoxyl group-propanedioic acid methyl ethyl ester of 95%.
2. the preparation method of sulphormethoxine according to claim 1; It is characterized in that: in the step (1); The implementation process that generates the reaction of 3-methoxyl group-oxosuccinic acid methyl ethyl ester is: in the exsiccant reaction kettle, add methoxy menthyl acetate and excessive oxalic acid diethyl ester, under agitation condition, solid sodium ethanol is dropped in the reaction kettle; And the control reacting liquid temperature is no more than 65 ℃, again in 45～65 ℃ of following insulation reaction of temperature more than 0.5 hour.
3. the preparation method of sulphormethoxine according to claim 1 and 2, it is characterized in that: in the step (1), the molar ratio of said methoxy menthyl acetate and oxalic acid diethyl ester is 1: 1.02～1.18.
4. the preparation method of sulphormethoxine according to claim 1 and 2 is characterized in that: in the step (1), after the reaction of generation 3-methoxyl group-oxosuccinic acid methyl ethyl ester finishes; Reaction solution is used earlier anhydrous organic solvent diluting, and it is 1～2 that the back uses inorganic aqueous acid to regulate pH, leaves standstill; Layering; After wherein organic solvent layer reclaimed organic solvent, under 175～200 ℃ of temperature, decarbonylation was carried out in the normal pressure insulation in 2～5 hours.
5. the preparation method of sulphormethoxine according to claim 4; It is characterized in that: the reaction solution through with dilution is cooled to below 30 ℃, joins the adjusting of carrying out said pH in the mixed solution of being made up of water, mineral acid and trieline that is cooled to below 30 ℃.
6. the preparation method of sulphormethoxine according to claim 4, it is characterized in that: the organic solvent that above-mentioned dilution is used is trieline, reclaims trieline through air distillation.
7. sulphormethoxine intermediates preparation; Said sulphormethoxine midbody is 2-methoxyl group-propanedioic acid methyl ethyl ester; Said preparation method reacts methoxy menthyl acetate and excessive oxalic acid diethyl ester to generate 3-methoxyl group-oxosuccinic acid methyl ethyl ester in the presence of sodium ethylate; And make 3-methoxyl group-further decarbonylation of oxosuccinic acid methyl ethyl ester obtain 2-methoxyl group-propanedioic acid methyl ethyl ester; It is characterized in that: described sodium ethylate is a solid form, and generates being reflected under the temperature that temperature is lower than 65 ℃ of 3-methoxyl group-oxosuccinic acid methyl ethyl ester and carry out; After decarbonylation finishes; Reclaim low-boiling-point substance through the separation column vacuum fractionation; Said low-boiling-point substance is to be present in the material that all boiling points in the system are lower than 2-methoxyl group-propanedioic acid methyl ethyl ester; Divide remove low-boiling-point substance after, without separation column, directly cool off residual reaction liquid and promptly get purity more than or equal to 2-methoxyl group-propanedioic acid methyl ethyl ester of 95%.
8. sulphormethoxine intermediates preparation according to claim 7; It is characterized in that: the implementation process that generates the reaction of 3-methoxyl group-oxosuccinic acid methyl ethyl ester is: in the exsiccant reaction kettle, add methoxy menthyl acetate and excessive oxalic acid diethyl ester; Under agitation condition; Solid sodium ethanol is dropped in the reaction kettle, and the control reacting liquid temperature is no more than 65 ℃, again in 45～65 ℃ of following insulation reaction of temperature more than 0.5 hour.
9. according to claim 7 or 8 described sulphormethoxine intermediates preparation, it is characterized in that: after generating the reaction end of 3-methoxyl group-oxosuccinic acid methyl ethyl ester, reaction solution is used earlier anhydrous organic solvent diluting; It is 1～2 that the back uses inorganic aqueous acid to regulate pH; Leave standstill, layering is after wherein organic solvent layer reclaims organic solvent; Under 170～200 ℃ of temperature, decarbonylation was carried out in the normal pressure insulation in 2～5 hours.
10. sulphormethoxine intermediates preparation according to claim 9 is characterized in that: the organic solvent that said dilution is used is trieline, reclaims trieline through air distillation.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103910687A (en) * | 2014-03-10 | 2014-07-09 | 常熟市南湖实业化工有限公司 | Preparation method of 4-(p-anilinesulfonamide)-5-methoxy-6 chloropyrimidine |
| CN105153044A (en) * | 2015-09-15 | 2015-12-16 | 桂林南药股份有限公司 | Method for one-pot synthesis of sulfadoxine by monitoring reaction progress through HPLC |
| CN108658871A (en) * | 2018-06-19 | 2018-10-16 | 张家港威胜生物医药有限公司 | The preparation method of sulfamethoxine intermediate 4,6- dichloro-5-methoxy pyrimidines |
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| RO63342A2 (en) * | 1973-03-07 | 1978-06-15 | Medicamente Intreprinderea De | PROCESS FOR THE PREPARATION OF 4-SULFANILAMIDO-5,6-DIMETHOXYPYRIMIDINE |
| CN1569843A (en) * | 2004-04-29 | 2005-01-26 | 常熟市南湖实业化工厂 | Preparation method for sulfadoxine |
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| RO63342A2 (en) * | 1973-03-07 | 1978-06-15 | Medicamente Intreprinderea De | PROCESS FOR THE PREPARATION OF 4-SULFANILAMIDO-5,6-DIMETHOXYPYRIMIDINE |
| CN1569843A (en) * | 2004-04-29 | 2005-01-26 | 常熟市南湖实业化工厂 | Preparation method for sulfadoxine |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103910687A (en) * | 2014-03-10 | 2014-07-09 | 常熟市南湖实业化工有限公司 | Preparation method of 4-(p-anilinesulfonamide)-5-methoxy-6 chloropyrimidine |
| CN105153044A (en) * | 2015-09-15 | 2015-12-16 | 桂林南药股份有限公司 | Method for one-pot synthesis of sulfadoxine by monitoring reaction progress through HPLC |
| CN108658871A (en) * | 2018-06-19 | 2018-10-16 | 张家港威胜生物医药有限公司 | The preparation method of sulfamethoxine intermediate 4,6- dichloro-5-methoxy pyrimidines |
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