CN102503978A - Process of adding acids prior to hydrolysis in glyphosate production - Google Patents
Process of adding acids prior to hydrolysis in glyphosate production Download PDFInfo
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- CN102503978A CN102503978A CN2011103201155A CN201110320115A CN102503978A CN 102503978 A CN102503978 A CN 102503978A CN 2011103201155 A CN2011103201155 A CN 2011103201155A CN 201110320115 A CN201110320115 A CN 201110320115A CN 102503978 A CN102503978 A CN 102503978A
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- hydrolysis
- glyphosate
- acid adding
- water cooler
- adding process
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- 239000005562 Glyphosate Substances 0.000 title claims abstract description 40
- XDDAORKBJWWYJS-UHFFFAOYSA-N glyphosate Chemical compound OC(=O)CNCP(O)(O)=O XDDAORKBJWWYJS-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 229940097068 glyphosate Drugs 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 39
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 30
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 30
- 239000002253 acid Substances 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 150000007513 acids Chemical class 0.000 title abstract 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 238000006482 condensation reaction Methods 0.000 claims abstract description 15
- 238000002156 mixing Methods 0.000 claims description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 20
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 claims description 19
- 230000001413 cellular effect Effects 0.000 claims description 17
- 150000003839 salts Chemical class 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 15
- 239000010439 graphite Substances 0.000 claims description 15
- 229910002804 graphite Inorganic materials 0.000 claims description 15
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 claims description 14
- 239000012267 brine Substances 0.000 claims description 14
- 235000013905 glycine and its sodium salt Nutrition 0.000 claims description 14
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims description 12
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 12
- 238000012856 packing Methods 0.000 claims description 12
- 230000003301 hydrolyzing effect Effects 0.000 claims description 9
- 239000011521 glass Substances 0.000 claims description 8
- 239000000945 filler Substances 0.000 claims description 7
- 230000000694 effects Effects 0.000 abstract description 3
- 230000002411 adverse Effects 0.000 abstract 1
- 239000012295 chemical reaction liquid Substances 0.000 abstract 1
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 description 9
- 238000007086 side reaction Methods 0.000 description 5
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 230000002363 herbicidal effect Effects 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- -1 phosphonomethyl Chemical group 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000004471 Glycine Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- GEVWHIDSUOMVRI-UHFFFAOYSA-N anisatin Chemical compound CC1(O)C(OC(=O)C2O)CC22C(C)CC(O)C2(O)C21COC2=O GEVWHIDSUOMVRI-UHFFFAOYSA-N 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000004009 herbicide Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- DWNBOPVKNPVNQG-LURJTMIESA-N (2s)-4-hydroxy-2-(propylamino)butanoic acid Chemical compound CCCN[C@H](C(O)=O)CCO DWNBOPVKNPVNQG-LURJTMIESA-N 0.000 description 1
- QIVBCDIJIAJPQS-VIFPVBQESA-N L-tryptophane Chemical compound C1=CC=C2C(C[C@H](N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-VIFPVBQESA-N 0.000 description 1
- 206010067482 No adverse event Diseases 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 229930040373 Paraformaldehyde Natural products 0.000 description 1
- QIVBCDIJIAJPQS-UHFFFAOYSA-N Tryptophan Natural products C1=CC=C2C(CC(N)C(O)=O)=CNC2=C1 QIVBCDIJIAJPQS-UHFFFAOYSA-N 0.000 description 1
- 239000006035 Tryptophane Substances 0.000 description 1
- 125000001539 acetonyl group Chemical group [H]C([H])([H])C(=O)C([H])([H])* 0.000 description 1
- 238000007259 addition reaction Methods 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 230000001684 chronic effect Effects 0.000 description 1
- 238000012691 depolymerization reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- BDUPRNVPXOHWIL-UHFFFAOYSA-N dimethyl sulfite Chemical compound COS(=O)OC BDUPRNVPXOHWIL-UHFFFAOYSA-N 0.000 description 1
- 150000002085 enols Chemical class 0.000 description 1
- 239000007770 graphite material Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 229920002866 paraformaldehyde Polymers 0.000 description 1
- COLNVLDHVKWLRT-UHFFFAOYSA-N phenylalanine Natural products OC(=O)C(N)CC1=CC=CC=C1 COLNVLDHVKWLRT-UHFFFAOYSA-N 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 229960004799 tryptophan Drugs 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Physical Or Chemical Processes And Apparatus (AREA)
- Agricultural Chemicals And Associated Chemicals (AREA)
Abstract
The invention provides a process of adding acids prior to hydrolysis in glyphosate production. According to the invention, firstly hydrochloric acid is mixed with the condensation reaction liquid before hydrolysis to carry away most heat, and then hydrolysis is carried out. The process effectively reduces adverse effects of reaction heat, increases the yield of glyphosate and makes post-treatment easy.
Description
Technical field
The present invention relates to a kind of production technique of Glyphosate 62 IPA Salt, more particularly, the present invention relates to the acid adding process of hydrolysis in a kind of glyphosate production.
Background technology
Glyphosate 62 IPA Salt (glyphosate), formal name used at school N-((phosphonomethyl)) glycocoll, N-((phosphonomethyl)) Padil is a kind of organophosphorus herbicide.The herbicidal properties of Glyphosate 62 IPA Salt is to be found by U.S. D.D. Baird etc. in 1971, by Monsanto Company's Development and Production, has become the important kind of world's weedicide to the eighties in last century.Glyphosate 62 IPA Salt is the chronic wide spectrum steriland herbicide of inner sucting conduction type; The main interior enol acetonyl shikimin phosphate synthase of object that suppresses; Thereby suppress the conversion of shikimin, make proteinic synthetic being interfered cause plant dead to phenylalanine(Phe), cruel propylhomoserin and tryptophane.Glyphosate 62 IPA Salt is transmitted to each position of plant after absorbing through cauline leaf, can prevent and kill off the plant of sections more than 40 such as unifacial leaf and dicotyledonous, annual and perennial, draft and shrub.Combine with metals ions such as iron, aluminium very soon after Glyphosate 62 IPA Salt buries and lose activity, seed and the soil microorganisms that hides in the soil had no adverse effects.
The industrialized preparing process of Glyphosate 62 IPA Salt mainly contains two kinds at present: IDA method and glycine method.The glycine method key step is synthetic, hydrolysis, crystallization and solid-liquid separation.Be specially methyl alcohol, Paraformaldehyde 96 and triethylamine and carry out depolymerization reaction; Add glycocoll after reaction is accomplished and carry out addition reaction; Add dimethyl sulfite after the reaction again and carry out condensation reaction and obtain the synthetic liquid of condensation reaction, obtain Glyphosate 62 IPA Salt and acid mother liquor through hydrolysis, crystallization and solid-liquid separation at last, acid mother liquor adds the liquid caustic soda neutralization; After reclaiming triethylamine, remaining is alkaline mother liquor.Contain a small amount of Glyphosate 62 IPA Salt in the alkali liquor, about 1-2% has higher recovery value.
Will carry out the acid adding process step before the condensated liquid hydrolysis, traditional to add acid be in still, to add earlier to go up the step condensation reaction solution and add hydrochloric acid again, or add hydrochloric acid earlier and add and go on foot condensation reaction solution.Which kind of mode all can be because of increasing the generation of controlling difficulty and side reaction with concentrated heat release in hydrochloric acid and the triethylamine.
Summary of the invention
The present invention is intended to solve the problem of acid adding process concentrated heat release increasing control difficulty and side reaction in the prior art, and the acid adding process before the hydrolysis in a kind of glyphosate production is provided, and can effectively reduce the generation of reaction heat and side reaction.
In order to realize the foregoing invention purpose, concrete technical scheme of the present invention is following:
Acid adding process in a kind of glyphosate production before the hydrolysis is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is equal to or less than the hydrolysis process temperature;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
The glycocoll in the steps A of the present invention and the mol ratio of hydrogenchloride are 1:2.8～3.5.
Mixing tank in the steps A of the present invention is the mixing tank of ripple packing mode.
The filler of the mixing tank of above-mentioned ripple packing mode is pottery or acrylic plastering.
The sheating material of the mixing tank of above-mentioned ripple packing mode is graphite or acrylic plastering.
Water cooler among the step B of the present invention can be piece cellular type graphite cooler or piece cellular type glass cools device.
Water cooler of the present invention is to adopt chilled brine circulation cooling.
Water cooler material liquid outlet among the step B of the present invention is provided with TP, according to outlet feed temperature control neutralizer flow.
Hydrolysis process temperature among the step B of the present invention is 45 ℃.
The useful technique effect that the present invention brings:
1, through earlier condensation reaction solution and hydrochloric acid being reacted, cooling gets in the refrigerative pipeline again, produces neutralization reaction, has removed reaction heat in time, makes reaction become gentle, and side reaction reduces;
2, side reaction is inhibited, and under the identical situation of other technology of Glyphosate 62 IPA Salt synthetic, the yield of Glyphosate 62 IPA Salt has improved 1.2% (respectively doing three times MV), simultaneously aftertreatment is become easily, and the washing water yield reduces by 250 kilograms, has reduced production cost greatly.
3, effectively shift reaction is hot for the mixing tank of the graphite material of ripple packing mode and piece cellular type graphite cooler or piece cellular type glass cools device, reduces the severe of reaction, has improved the security of producing.
Description of drawings
Fig. 1 of Figure of description is a process flow diagram of the present invention.
Fig. 2 of Figure of description is the structural representation of the preceding feeding device of hydrolysis in the glyphosate production of the present invention's employing.
Reference numeral: 1 is that condensation reaction still, 2 is that hydrochloric acid scale tank, 3 is that flow director, 4 is that mixing tank, 5 is that water cooler, 6 is that TP, 7 is that hydrolytic reaction pot, 8 is that chilled brine import, 9 is that chilled brine exports.
Embodiment
Embodiment 1
Acid adding process in a kind of glyphosate production before the hydrolysis is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is 30 ℃;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
The glycocoll in the steps A of the present invention and the mol ratio of hydrogenchloride are 1:2.8.
Mixing tank in the steps A of the present invention is the mixing tank of ripple packing mode.
The filler of above-mentioned mixing tank is pottery or acrylic plastering.
The sheating material of above-mentioned mixing tank is graphite or acrylic plastering.
Water cooler among the step B of the present invention can be piece cellular type graphite cooler or piece cellular type glass cools device.
Water cooler of the present invention is to adopt chilled brine circulation cooling, and the temperature of chilled brine is-15 ℃.
Water cooler material liquid outlet among the step B of the present invention is provided with TP, according to outlet feed temperature control neutralizer flow.
Embodiment 2
Acid adding process in a kind of glyphosate production before the hydrolysis is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is 45 ℃;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
The glycocoll in the steps A of the present invention and the mol ratio of hydrogenchloride are 1:3.5.
Mixing tank in the steps A of the present invention is the mixing tank of ripple packing mode.
The filler of above-mentioned mixing tank is pottery or acrylic plastering.
The sheating material of above-mentioned mixing tank is graphite or acrylic plastering.
Water cooler among the step B of the present invention can be piece cellular type graphite cooler or piece cellular type glass cools device.
Water cooler of the present invention is to adopt chilled brine circulation cooling, and the temperature of chilled brine is-35 ℃.
Water cooler material liquid outlet among the step B of the present invention is provided with TP, according to outlet feed temperature control neutralizer flow.
Acid adding process in a kind of glyphosate production before the hydrolysis is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is 35 ℃;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
The glycocoll in the steps A of the present invention and the mol ratio of hydrogenchloride are 1:3.15.
Mixing tank in the steps A of the present invention is the mixing tank of ripple packing mode.
The filler of above-mentioned mixing tank is pottery or acrylic plastering.
The sheating material of above-mentioned mixing tank is graphite or acrylic plastering.
Water cooler among the step B of the present invention can be piece cellular type graphite cooler or piece cellular type glass cools device.
Water cooler of the present invention is to adopt chilled brine circulation cooling, and the temperature of chilled brine is-15 ℃.
Water cooler material liquid outlet among the step B of the present invention is provided with TP, according to outlet feed temperature control neutralizer flow.
Embodiment 4
Acid adding process in a kind of glyphosate production before the hydrolysis is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is 40 ℃;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
The glycocoll in the steps A of the present invention and the mol ratio of hydrogenchloride are 1:3.45.
Mixing tank in the steps A of the present invention is the mixing tank of ripple packing mode.
The filler of above-mentioned mixing tank is pottery or acrylic plastering.
The sheating material of above-mentioned mixing tank is graphite or acrylic plastering.
Water cooler among the step B of the present invention can be piece cellular type graphite cooler or piece cellular type piece cellular type glass cools device.
Water cooler of the present invention is to adopt chilled brine circulation cooling, and the temperature of chilled brine is-35 ℃.
Water cooler material liquid outlet among the step B of the present invention is provided with TP, according to outlet feed temperature control neutralizer flow.
Embodiment 5
In conjunction with Fig. 2: the feeding device in a kind of glyphosate production before the hydrolysis; Comprise condensation reaction still 1, hydrolytic reaction pot 7 and hydrochloric acid scale tank 2; It is characterized in that: through an end of the same mixing tank 4 of pipe connection, described pipeline is provided with flow director 3 respectively for condensation reaction still 1 and hydrochloric acid scale tank 2; The other end of described mixing tank 4 is connected with water cooler 5, and described water cooler 5 is connected with hydrolytic reaction pot 7 again.
Described mixing tank 4 is the mixing tank of ripple packing mode.
The filler of described mixing tank 4 is pottery or acrylic plastering.
The sheating material of described mixing tank 4 is graphite or acrylic plastering.
Described water cooler 5 is piece cellular type graphite cooler or piece cellular type glass cools device.
Described water cooler 5 lower ends are provided with chilled brine import 8, and the upper end is provided with chilled brine outlet 9.
Described water cooler 5 material liquid outlet places are provided with TP 6.
Claims (9)
1. the acid adding process before the hydrolysis in the glyphosate production is characterized in that: comprise following process step:
A, with synthetic liquid of condensation reaction and mol ratio calculating separately the flow of hydrochloric acid according to glycocoll and hydrogenchloride, mix in the input mixer respectively by two pipelines;
B, the neutralizer that after mixing, obtains get into water cooler immediately, in reaction, take the reaction heat exchange out of reaction system, guarantee that water cooler material liquid outlet temperature is equal to or less than the hydrolysis process temperature;
C, mix the neutralizer obtain and laggardly go into hydrolytic reaction pot and be hydrolyzed and make Glyphosate 62 IPA Salt through cooling off.
2. the acid adding process in a kind of glyphosate production according to claim 1 before the hydrolysis, it is characterized in that: the mol ratio at glycocoll described in the steps A and hydrogenchloride is 1:2.8～3.5.
3. the acid adding process in a kind of glyphosate production according to claim 1 before the hydrolysis is characterized in that: be the mixing tank of ripple packing mode at the mixing tank described in the steps A.
4. the acid adding process in a kind of glyphosate production according to claim 3 before the hydrolysis is characterized in that: the filler of the mixing tank of described ripple packing mode is pottery or acrylic plastering.
5. the acid adding process in a kind of glyphosate production according to claim 3 before the hydrolysis, it is characterized in that: the sheating material of the mixing tank of described ripple packing mode is graphite or acrylic plastering.
6. the acid adding process in a kind of glyphosate production according to claim 1 before the hydrolysis, it is characterized in that: at the water cooler described in the step B is piece cellular type graphite cooler or piece cellular type glass cools device.
7. according to the acid adding process before the hydrolysis in claim 1 or the 6 described a kind of glyphosate production, it is characterized in that: water cooler of the present invention is to adopt chilled brine circulation cooling.
8. the acid adding process in a kind of glyphosate production according to claim 1 before the hydrolysis, it is characterized in that: the water cooler material liquid outlet described in the step B is provided with TP.
9. the acid adding process in a kind of glyphosate production according to claim 1 before the hydrolysis, it is characterized in that: in the hydrolysis process temperature described in the step B is 45 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110320115.5A CN102503978B (en) | 2011-10-20 | 2011-10-20 | Process of adding acids prior to hydrolysis in glyphosate production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110320115.5A CN102503978B (en) | 2011-10-20 | 2011-10-20 | Process of adding acids prior to hydrolysis in glyphosate production |
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| Publication Number | Publication Date |
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| CN102503978A true CN102503978A (en) | 2012-06-20 |
| CN102503978B CN102503978B (en) | 2015-03-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739625A (en) * | 2014-01-23 | 2014-04-23 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis process for preparing glyphosate by glycine method |
| CN103788127A (en) * | 2014-01-23 | 2014-05-14 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis system for preparing glyphosate by glycine method |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993455A (en) * | 2010-12-13 | 2011-03-30 | 四川省乐山市福华通达农药科技有限公司 | Glyphosate synthesis process |
-
2011
- 2011-10-20 CN CN201110320115.5A patent/CN102503978B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993455A (en) * | 2010-12-13 | 2011-03-30 | 四川省乐山市福华通达农药科技有限公司 | Glyphosate synthesis process |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103739625A (en) * | 2014-01-23 | 2014-04-23 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis process for preparing glyphosate by glycine method |
| CN103788127A (en) * | 2014-01-23 | 2014-05-14 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis system for preparing glyphosate by glycine method |
| CN103739625B (en) * | 2014-01-23 | 2017-01-11 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis process for preparing glyphosate by glycine method |
| CN103788127B (en) * | 2014-01-23 | 2017-01-11 | 四川省乐山市福华通达农药科技有限公司 | Continuous hydrolysis system for preparing glyphosate by glycine method |
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Denomination of invention: Process of adding acids prior to hydrolysis in glyphosate production Effective date of registration: 20200617 Granted publication date: 20150318 Pledgee: Chengdu Branch of China CITIC Bank Co.,Ltd. Pledgor: Sichuan Leshan Fuhua Tongda Pesticide Technology Co.,Ltd. Registration number: Y2020510000069 |
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Date of cancellation: 20201125 Granted publication date: 20150318 Pledgee: Chengdu Branch of China CITIC Bank Co.,Ltd. Pledgor: Sichuan Leshan Fuhua Tongda Pesticide Technology Co.,Ltd. Registration number: Y2020510000069 |
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Denomination of invention: A process of adding acid before hydrolysis in glyphosate production Effective date of registration: 20201203 Granted publication date: 20150318 Pledgee: Chengdu Branch of China CITIC Bank Co.,Ltd. Pledgor: Sichuan Leshan Fuhua Tongda Pesticide Technology Co.,Ltd. Registration number: Y2020510000109 |
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Address after: 614803 Jinsu Town, Wutongqiao District, Leshan City, Sichuan Province Patentee after: Fuhua Tongda Chemical Co.,Ltd. Address before: Wutongqiao Qiao Gou Zhen 614800 Sichuan city of Leshan Province Patentee before: Sichuan Leshan Fuhua Tongda Pesticide Technology Co.,Ltd. |
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Date of cancellation: 20230425 Granted publication date: 20150318 Pledgee: Chengdu Branch of China CITIC Bank Co.,Ltd. Pledgor: Sichuan Leshan Fuhua Tongda Pesticide Technology Co.,Ltd. Registration number: Y2020510000109 |