CN1169817C - Preparation method of high-purity acephate raw powder (2) - Google Patents
Preparation method of high-purity acephate raw powder (2) Download PDFInfo
- Publication number
- CN1169817C CN1169817C CNB021139369A CN02113936A CN1169817C CN 1169817 C CN1169817 C CN 1169817C CN B021139369 A CNB021139369 A CN B021139369A CN 02113936 A CN02113936 A CN 02113936A CN 1169817 C CN1169817 C CN 1169817C
- Authority
- CN
- China
- Prior art keywords
- preparation
- former powder
- acephate
- purity
- purity acetyl
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- YASYVMFAVPKPKE-UHFFFAOYSA-N acephate Chemical compound COP(=O)(SC)NC(C)=O YASYVMFAVPKPKE-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 239000000843 powder Substances 0.000 title claims abstract description 33
- 238000002360 preparation method Methods 0.000 title claims abstract description 23
- 239000013078 crystal Substances 0.000 claims abstract description 40
- 238000002425 crystallisation Methods 0.000 claims abstract description 24
- 230000008025 crystallization Effects 0.000 claims abstract description 24
- 239000010779 crude oil Substances 0.000 claims abstract description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000001556 precipitation Methods 0.000 claims abstract description 11
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 9
- 239000003960 organic solvent Substances 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 239000002904 solvent Substances 0.000 claims abstract description 9
- 238000007670 refining Methods 0.000 claims abstract description 7
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 5
- 238000001953 recrystallisation Methods 0.000 claims abstract description 5
- 239000002994 raw material Substances 0.000 claims abstract description 3
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 claims description 30
- -1 acetyl acephatemet Chemical compound 0.000 claims description 23
- 239000012452 mother liquor Substances 0.000 claims description 15
- 239000003921 oil Substances 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 9
- OIFBSDVPJOWBCH-UHFFFAOYSA-N Diethyl carbonate Chemical class CCOC(=O)OCC OIFBSDVPJOWBCH-UHFFFAOYSA-N 0.000 claims description 8
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 claims description 8
- JZMJDSHXVKJFKW-UHFFFAOYSA-M methyl sulfate(1-) Chemical compound COS([O-])(=O)=O JZMJDSHXVKJFKW-UHFFFAOYSA-M 0.000 claims description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 6
- 150000007933 aliphatic carboxylic acids Chemical class 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 6
- RXKJFZQQPQGTFL-UHFFFAOYSA-N dihydroxyacetone Chemical compound OCC(=O)CO RXKJFZQQPQGTFL-UHFFFAOYSA-N 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 230000035484 reaction time Effects 0.000 claims description 6
- USFZMSVCRYTOJT-UHFFFAOYSA-N Ammonium acetate Chemical compound N.CC(O)=O USFZMSVCRYTOJT-UHFFFAOYSA-N 0.000 claims description 4
- 239000005695 Ammonium acetate Substances 0.000 claims description 4
- 230000010933 acylation Effects 0.000 claims description 4
- 238000005917 acylation reaction Methods 0.000 claims description 4
- 229940043376 ammonium acetate Drugs 0.000 claims description 4
- 235000019257 ammonium acetate Nutrition 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 claims description 4
- 150000002191 fatty alcohols Chemical class 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 2
- 125000000217 alkyl group Chemical group 0.000 claims description 2
- 239000003456 ion exchange resin Substances 0.000 claims description 2
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 2
- 150000002576 ketones Chemical class 0.000 claims description 2
- 239000007790 solid phase Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 10
- 239000002699 waste material Substances 0.000 abstract description 3
- UBRYVVDAYNKOOR-UHFFFAOYSA-N methoxy(methylsulfanyl)phosphinic acid Chemical compound COP(O)(=O)SC UBRYVVDAYNKOOR-UHFFFAOYSA-N 0.000 abstract 2
- 230000021736 acetylation Effects 0.000 abstract 1
- 238000006640 acetylation reaction Methods 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- NHNUFAASKXPOQA-UHFFFAOYSA-N (3-acetamido-2-hydroxyphenyl)arsonic acid Chemical compound C(C)(=O)NC=1C(=C(C=CC1)[As](O)(=O)O)O NHNUFAASKXPOQA-UHFFFAOYSA-N 0.000 description 1
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 229960001196 thiotepa Drugs 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Abstract
本发明公开了一种高纯度乙酰甲胺磷原粉的制备方法，以O，O-二甲基硫代磷酰胺或O，S-二甲基硫代磷酰胺为原料，将O，O-二甲基硫代磷酰胺经异构化和乙酰化或由O，S-二甲基硫代磷酰胺经乙酰化，制得乙酰甲胺磷原油后经加入溶剂后通入氨气或液氨进行中和、固液分离、脱溶，经一次结晶分离和二次结晶分离得乙酰甲胺磷粗晶体、在乙酰甲胺磷粗晶体中加入有机溶剂进行重结晶精制获得高纯度乙酰甲胺磷原粉。采用本发明制备的乙酰甲胺磷原粉得率高，纯度高，由于萃取液可回收利用，因此成本低，无废液排放，减少对环境的污染。The invention discloses a preparation method of high-purity acephate raw powder. O, O-dimethylphosphorothioate or O, S-dimethylphosphorothioate is used as raw material, and O, O- Dimethylphosphorothioate is subjected to isomerization and acetylation or O, S-dimethylphosphorothioate is acetylated to obtain acephate crude oil, and after adding solvent, add ammonia gas or liquid ammonia Neutralization, solid-liquid separation, precipitation, first crystallization separation and secondary crystallization separation to obtain acephate crude crystals, adding an organic solvent to the acephate crude crystals for recrystallization and refining to obtain high-purity acephate Original powder. The raw acephate powder prepared by the method has high yield and high purity, and because the extract can be recycled, the cost is low, and no waste liquid is discharged, thereby reducing environmental pollution.
Description
Technical field
The present invention relates to a kind of method of producing the former powder of high-purity acetyl acephatemet.
Background technology
Acephate, formal name used at school O, S-dimethyl-N-ethanoyl thio-phosphamide claims N-acetylaminohydroxyphenylarsonic acid O again, S-dimethyl phosphoric acid ester, molecular structure is
Pure product are white crystal, and fusing point 92-93 ℃ is a kind of agricultural chemicals of high-efficiency low-toxicity.
By O; the O-dimethyl thiophosphoryl amide is through isomerization and acetylize (or O; S-dimethyl thiophosphoryl amide crude oil is through acetylize) the general content of acephate crude oil that obtains is 30-70% (mass percent), must could obtain the former powder of desirable high-purity acetyl acephatemet through separating to purify.
Japanese Patent JP-B48-34583 has reported the former powder separating and extracting method of a kind of acephate: at first use chloroform extraction acephate crude oil, wash with salt solution then, carry out condensing crystal again.Japanese Patent JP-A64-75494 reported method is: at first use in the alkaline aqueous solution and acephate crude oil, extract with ethylene dichloride or chloroform then, concentrating and recrystallization.United States Patent (USP) 5,616,769 have reported a kind of two-phase (water and organic phase) recrystallization method (acephate crystalline process for purification).Chinese patent 1238340 reported method are at first acephate crude oil to be carried out crystallization, and after the isolation of crystalline, neutralizing or washing processes such as crystalline mother solution, extraction, the crystallization of extraction phase precipitation, coarse crystal be refining gets the former powder of high-purity acetyl acephatemet.Chinese patent 1277201 reported method then are that acephate crude oil is carried out crystallization, after the isolation of crystalline, and the impurity in the extractive crystallization mother liquor, the process such as refining of secondary crystal, coarse crystal gets the former powder of high-purity acetyl acephatemet.Except that Chinese patent 1238340 and 1277201, all there is the problem of the former powder yield of acephate (corresponding mother liquor yield is big) in above-mentioned these methods.In addition, except that Chinese patent 1277201, all need processing to contain organophosphorus and other organic waste water in a large number, and the consumption of organic extractant is generally all bigger.
Summary of the invention
The object of the present invention is to provide a kind of yield height, the purity height, cost is low, the preparation method of the former powder of acephate that discharging of waste liquid is few.
The objective of the invention is to realize in the following way: the preparation method of the former powder of a kind of high-purity acetyl acephatemet; with O; O-dimethyl thiophosphoryl amide or O; the S-dimethyl thiophosphoryl amide is a raw material; with O; the O-dimethyl thiophosphoryl amide is through isomerization and acetylize or by O; the S-dimethyl thiophosphoryl amide is through acetylize; make acephate crude oil after feed ammonia after adding solvent or liquefied ammonia neutralizes; solid-liquid separation; precipitation, through primary crystallization separate separate with secondary crystal the acephate coarse crystal; in the acephate coarse crystal, add organic solvent and carry out the former powder of recrystallizing and refining acquisition high-purity acetyl acephatemet.
At first at O, add methyl-sulfate in the O-dimethyl thiophosphoryl amide and carry out isomerization reaction, O, O-dimethyl thiophosphoryl amide and methyl-sulfate mass ratio are 0.02-0.1: 1,30-90 ℃ of isomerization reaction temperature, reaction times is 2-10 hour, generate O, the S-dimethyl thiophosphoryl amide is then at O, the S-dimethyl thiophosphoryl amide directly adds aceticanhydride and carries out acetylization reaction, generates acephate crude oil; Aceticanhydride and O, S-dimethyl thiophosphoryl amide quality proportioning is 0.5-1.0: 1,30-90 ℃ of acetylization reaction temperature, reaction times 2-10 hour.
By O; S-dimethyl thiophosphoryl amide crude oil and aceticanhydride carry out acetylization reaction and generate acephate crude oil in the presence of acylation catalyst, aceticanhydride and O, and S-dimethyl thiophosphoryl amide crude quality is than being 0.5-1.0: 1; 30-90 ℃ of acetylization reaction temperature, reaction times 2-10 hour.
Acylation catalyst is the vitriol oil or methyl-sulfate or strong-acid ion exchange resin or solid super-strong acid.
The solvent that adds can be halogenated aliphatic hydrocarbon, carbonic ether, aliphatic carboxylic acid esters,, fatty alcohol, aliphatic ketone or the mixture that contains two or more these material preparations.
The halogenated aliphatic hydrocarbon is C
1-C
8The halogenated aliphatic hydrocarbon.
Carbonic ether is to contain C
1-C
4The carbonic ether of alkyl.
The aliphatic carboxylic acid esters, is C
2-C
12Carboxylic acid C
2-C
8Ester.
Aliphatic ketone is C
1-C
8Aliphatic ketone.
The concentration that contains ammonia gas is 10-100%, and the temperature of neutralization reaction is less than 25-60 ℃.
After the liquid-solid separation, solid phase is handled recovery ammonium acetate or acetic acid wherein, and liquid phase is carried out precipitation and crystallization.
Liquid phase after the solid-liquid separation to be carried out the vacuum precipitation, carry out primary crystallization behind the recovery part solvent, temperature is-10-55 ℃, the time is 0.5-30 hour; Separate the coarse crystal that the primary crystallization material obtains, the configurable after treatment missible oil of mother liquor; Carry out secondary crystal then, Tc is-30-10 ℃, the time is 0.5-30 hour; The coarse crystal that the separated secondary crystallized stock obtains, and mother liquor disposes missible oil after treatment.
The acephate coarse crystal that primary crystallization and secondary crystal obtained joined carry out recrystallizing and refining in the organic solvent, being used for the purified organic solvent is halogenated aliphatic hydrocarbon, carbonic ether, aliphatic carboxylic acid esters,, fatty alcohol, aliphatic ketone or the mixture that contains two or more these materials preparations; Recrystallization temperature is-15-10 ℃, and the time is 0.5-30 hour; Separate the back crystal and promptly get the former powder of high-purity acetyl acephatemet after super-dry, mother liquor can recycle or is prepared missible oil after treatment.
Adopt the former powder yield of the acephate height of the present invention's preparation, the purity height, because the recyclable utilization of extraction liquid, so cost is low, no discharging of waste liquid reduces the pollution to environment.
The present invention will be further described below in conjunction with embodiment:
Embodiment 1
At 920kg content 94% O, add the 55.2kg methyl-sulfate in the O-dimethyl thiophosphoryl amide crude oil and carry out isomerization, add the aceticanhydride that 682.6kg concentration is 98% (quality) then, reacted 3 hours down, get the acephate crude oil of content 56.4% at 55 ℃.In this crude oil, add the 3107kg solvent, under normal pressure, be neutralized to pH value 6.5-7.0 then, filter the ammonium acetate crystal that neutralization produces, get 4330kg content and be 21.6% liquid with ammonia.This liquid puts into the crystallization kettle that band stirs and is cooled to behind the vacuum precipitation-5-0 ℃ carries out primary crystallization, separate 742.6kg coarse crystal and 978.4kg mother liquor.With this mother liquor precipitation, put into the crystallization kettle that band stirs to be cooled to-20--10 ℃ carries out secondary crystal, separate to such an extent that 310.3kg coarse crystal and 282.8kg content are 28.1% secondary mother liquid.The acephate coarse crystal that primary crystallization and secondary crystal obtained is dissolved in the 1180kg organic solvent, in 0.5-30 hour, be cooled to terminal temperature-15-10 ℃ gradually, through separate, dry 821.5kg content is 98.2% the former powder of acephate crystal.Refinement mother liquor can recycle or dispose after treatment missible oil.
Embodiment 2:
At 880kg content is 75% O, adds 616kg content in the S-dimethyl thiophosphoryl amide crude oil and be 98% aceticanhydride and 8.8kg content and be 98% sulfuric acid, 55 ℃ of reactions 3 hours down, 1504.8kg content be the acephate crude oil of 55-57%.In this crude oil, add the 3107kg solvent, be neutralized to pH value 6.5-7.0 with ammonia then, filter the ammonium acetate crystal that neutralization produces, get 3959.8kg content and be 21.2% liquid.Put into the crystallization kettle that band stirs behind the vacuum precipitation to be cooled to-5-0 ℃ carries out primary crystallization, separate 657.5kg coarse crystal and 853.6kg mother liquor, with this mother liquor precipitation, put into the crystallization kettle that band stirs to be cooled to-20-10 ℃ carries out secondary crystal, separate the secondary crystal mother liquor of 281.6kg coarse crystal and 245.2kg content 30.5%.The acephate coarse crystal that primary crystallization and secondary crystal obtained is dissolved in the 1056.5kg organic solvent, was cooled to terminal temperature-15-10 ℃ gradually at 0.5-30 hour, through separate, dry 736.7kg content is 98.0% the former powder of acephate crystal.Refinement mother liquor can recycle or dispose after treatment missible oil.
Claims (13)
1; the preparation method of the former powder of a kind of high-purity acetyl acephatemet; with O; O-dimethyl thiophosphoryl amide or O; the S-dimethyl thiophosphoryl amide is a raw material; it is characterized in that: with O; the O-dimethyl thiophosphoryl amide is through isomerization and acetylize or by O; the S-dimethyl thiophosphoryl amide is through acetylize; after making acephate crude oil; feeding ammonia or liquefied ammonia neutralize after adding solvent; solid-liquid separation; precipitation, through primary crystallization separate separate with secondary crystal the acephate coarse crystal; in the acephate coarse crystal, add organic solvent and carry out the former powder of recrystallizing and refining acquisition high-purity acetyl acephatemet.
2, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 1, it is characterized in that: at first at O, add methyl-sulfate in the O-dimethyl thiophosphoryl amide and carry out isomerization reaction, O, O-dimethyl thiophosphoryl amide and methyl-sulfate mass ratio are 0.02-0.1: 1,30-90 ℃ of isomerization reaction temperature, reaction times is 2-10 hour, generate O, the S-dimethyl thiophosphoryl amide, at O, the S-dimethyl thiophosphoryl amide directly adds aceticanhydride and carries out acetylization reaction then, generates acephate crude oil; Aceticanhydride and O, S-dimethyl thiophosphoryl amide quality proportioning is 0.5-1.0: 1,30-90 ℃ of acetylization reaction temperature, reaction times 2-10 hour.
3, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 1; it is characterized in that: by O; S-dimethyl thiophosphoryl amide crude oil and aceticanhydride carry out acetylization reaction and generate acephate crude oil in the presence of acylation catalyst; aceticanhydride and O; S-dimethyl thiophosphoryl amide crude quality is than being 0.5-1.0: 1; 30-90 ℃ of acetylization reaction temperature, reaction times 2-10 hour.
4, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 3 is characterized in that: acylation catalyst is the vitriol oil or methyl-sulfate or strong-acid ion exchange resin or solid super-strong acid.
5, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 5 is characterized in that: the solvent of adding can be halogenated aliphatic hydrocarbon, carbonic ether, aliphatic carboxylic acid esters,, fatty alcohol, aliphatic ketone or the mixture that contains two or more these material preparations.
6, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 6, it is characterized in that: the halogenated aliphatic hydrocarbon is C
1-C
8The halogenated aliphatic hydrocarbon.
7, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 6, it is characterized in that: carbonic ether is to contain C
1-C
4The carbonic ether of alkyl.
8, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 6, it is characterized in that: the aliphatic carboxylic acid esters, is C
2-C
12Carboxylic acid C
2-C
8Ester.
9, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 6, it is characterized in that: aliphatic ketone is C
1-C
8Aliphatic ketone.
10, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 5, it is characterized in that: the concentration that contains ammonia gas is 10-100%, and the temperature of neutralization reaction is less than 25-60 ℃.
11, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 1 is characterized in that: after the liquid-solid separation, solid phase is handled recovery ammonium acetate or acetic acid wherein, and liquid phase is carried out precipitation and crystallization.
12, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 1 is characterized in that: the liquid phase after the solid-liquid separation carried out the vacuum precipitation, carries out primary crystallization behind the recovery part solvent, and temperature is-10-55 ℃, the time is 0.5-30 hour; Separate the coarse crystal that the primary crystallization material obtains, the configurable after treatment missible oil of mother liquor; Carry out secondary crystal then, Tc is-30-10 ℃, the time is 0.5-30 hour; The coarse crystal that the separated secondary crystallized stock obtains, and mother liquor disposes missible oil after treatment.
13, the preparation method of the former powder of high-purity acetyl acephatemet according to claim 1, it is characterized in that: the acephate coarse crystal that primary crystallization and secondary crystal obtained is joined carry out recrystallizing and refining in the organic solvent, being used for the purified organic solvent is halogenated aliphatic hydrocarbon, carbonic ether, aliphatic carboxylic acid esters,, fatty alcohol, aliphatic ketone or the mixture that contains two or more these material preparations; Recrystallization temperature is-15-10 ℃, and the time is 0.5-30 hour; Separate the back crystal and promptly get the former powder of high-purity acetyl acephatemet after super-dry, mother liquor can recycle or is prepared missible oil after treatment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021139369A CN1169817C (en) | 2002-01-28 | 2002-01-28 | Preparation method of high-purity acephate raw powder (2) |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB021139369A CN1169817C (en) | 2002-01-28 | 2002-01-28 | Preparation method of high-purity acephate raw powder (2) |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1362415A CN1362415A (en) | 2002-08-07 |
| CN1169817C true CN1169817C (en) | 2004-10-06 |
Family
ID=4742881
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB021139369A Expired - Fee Related CN1169817C (en) | 2002-01-28 | 2002-01-28 | Preparation method of high-purity acephate raw powder (2) |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1169817C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1931864B (en) * | 2005-09-18 | 2010-05-05 | 李坚 | Preparation of high content methamidophos and acetyl methamidophos product |
| CN101289462B (en) * | 2007-04-20 | 2010-12-01 | 济南大学 | Method for preparing acephate from ketene |
| CN101255174B (en) * | 2007-12-25 | 2010-07-21 | 山东华阳科技股份有限公司 | Novel process for synthesis of acephate |
| US20230339989A1 (en) * | 2020-01-31 | 2023-10-26 | Upl Ltd | A continuous flow process for preparation of acephate and its intermediates |
| CN112592368A (en) * | 2020-12-10 | 2021-04-02 | 安道麦股份有限公司 | Method for synthesizing acephate |
| CN112979698A (en) * | 2021-02-24 | 2021-06-18 | 湖南沅江赤蜂农化有限公司 | Synthesis method of acephate |
| BR112023017031A2 (en) * | 2021-02-25 | 2023-09-26 | Upl Ltd | Process for producing acephate |
-
2002
- 2002-01-28 CN CNB021139369A patent/CN1169817C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1362415A (en) | 2002-08-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0613878B1 (en) | Citric acid extraction | |
| CN109134287B (en) | Purification method of byproduct sodium chloride in betaine or betaine hydrochloride production | |
| CN1169817C (en) | Preparation method of high-purity acephate raw powder (2) | |
| CN109180436A (en) | A kind of synthetic method of phloroglucin | |
| EP2945949A1 (en) | Method for preparing a pyripyropene compound | |
| US20240327445A1 (en) | Method for purifying sucralose-6-acetate | |
| CN1176929C (en) | Preparation method of high-purity acephate powder | |
| CN1215769C (en) | Prepn of soluble acephate powder | |
| CN101289462B (en) | Method for preparing acephate from ketene | |
| KR100371241B1 (en) | Method for Purifying O, S-Dimethyl N-acetylphosphoramidothioate | |
| CN118406081A (en) | A method for purifying diphenyl phosphate from mixed phenyl phosphate | |
| CN1133638C (en) | Method for extracting high-purity acephate raw powder from acephate crude oil (2) | |
| CN101074241A (en) | Method for preparing acephate | |
| CN117000166A (en) | Multistage tubular guanidinoacetic acid production system and production method | |
| CN113024398B (en) | Preparation method of capsaicin and capsaicin prepared by using same | |
| CN1073114C (en) | Process (1) for extracting high-purity raw powder of acephate from raw oil of acephate | |
| JP3291987B2 (en) | Purification method of O, S-dimethyl-N-acetylphosphoramidothioate | |
| CN115322239B (en) | Method for recovering diketone from mandipropamid carbon loss ester mother liquor | |
| CN101492400A (en) | Method for preparing high-purity acamprosate calcium | |
| US6316657B1 (en) | Process for purification or recovery of sweetener | |
| CN115772136B (en) | A preparation method of parecoxib sodium and its intermediates | |
| JP3831476B2 (en) | Purification method of xylose | |
| CN114736118B (en) | Method for separating 3-methoxy-4-hydroxy mandelic acid and preparing high-purity product thereof | |
| CN112694397B (en) | Method for purifying 2, 6-naphthalenedicarboxylic acid | |
| CN117843481A (en) | Method for recycling byproducts in beta-hydroxyalkylamide crystallization mother liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |