CN203999455U - A kind of glyphosate continuous production device - Google Patents
A kind of glyphosate continuous production device Download PDFInfo
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- CN203999455U CN203999455U CN201420452658.1U CN201420452658U CN203999455U CN 203999455 U CN203999455 U CN 203999455U CN 201420452658 U CN201420452658 U CN 201420452658U CN 203999455 U CN203999455 U CN 203999455U
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Abstract
The utility model provides a kind of glyphosate continuous production device, being specially synthesis reactor is connected with the mixing tank on condensation tower top through carrier pipe, condensation tower is connected hybrid reactor bottom again and is connected with multistage compensating groove top after carrier pipe is connected with magnetic drive pump again with mixing tank after being connected with recycle pump, multistage compensating groove bottom is connected with multistage depickling still top through carrier pipe, soda-wash tower top via line pipeline is connected with methylal tower bottom, methylal tower top end via line pipeline is connected with condenser, condenser lower end is connected with gas-liquid separator top, gas-liquid separator bottom is connected with methylal storage tank, methanol column top is connected with condenser through carrier pipe, condenser bottom is connected with gas-liquid separator top, gas-liquid separator bottom is connected with methyl alcohol storage tank.The utility model is produced and the content of methyl chloride is brought up to reach 99.9% by realizing whole operation serialization, and glyphosate yield improves 0.5%, reduces energy consumption, is widely used in glyphosate production field.
Description
Technical field
The device that the utility model provides a kind of glyphosate serialization to produce, belongs to chemical industry equipment field.
Background technology
Glyphosate is at the go out interior suction conductivity weedicide of natural disposition of a kind of efficient, low toxicity, the wide spectrum of nineteen seventies research and development by About Monsanto Chemicals, occupy the first place of world pesticide sales volume for years, along with transgenosis glyphosate resistant crops is as the establishing in large scale of soybean, corn etc. in recent years, the whole world continues to increase the demand of glyphosate.Current domestic glyphosate main flow production technique has two lines: glycine method (single stage method) and iminodiacetic acid (salt) acid system (two-step approach, first synthetic pmida98, again pmida98 oxidation is called to glyphosate), external production technique is mainly the iminodiacetic acid (salt) acid system of About Monsanto Chemicals.Amino acetic acid in China synthetic route be first first in synthesis reactor through depolymerization, addition, condensation; Condensated liquid squeezes into that depickling still is hydrolyzed again, precipitation, depickling; The mixed gas (methyl chloride, dilute methanol) in hydrolysis precipitation stage is through three grades of condensations, and phlegma enters dilute methanol storage tank, then after neutralization, enters Distallation systm recovery; Uncooled tail gas enters methyl chloride recovery system and reclaims.This technological operation is discontinuous, and labor intensive is large, and yield is low, and energy consumption is high.
Summary of the invention
The device that provides a kind of glyphosate serialization to produce is provided the purpose of this utility model, specific as follows:
A kind of glyphosate continuous production device, synthesis reactor bottom is connected with the mixing tank on condensation tower top through carrier pipe, condensation tower is connected with mixing tank front end after carrier pipe is connected with recycle pump again, mixing tank upper end is provided with high-order hydrochloric acid tank, mixing tank end is connected with recycle pump through carrier pipe, recycle pump via line pipeline is connected with hybrid reactor top, hybrid reactor bottom is connected with multistage compensating groove top after carrier pipe is connected with magnetic drive pump again, multistage compensating groove bottom is connected with multistage depickling still top through carrier pipe, (top is connected with soda-wash tower bottom multistage depickling still after another cable tubing converges, soda-wash tower top via line pipeline is connected with methylal tower bottom, methylal tower top end via line pipeline is connected with condenser, condenser lower end is connected with gas-liquid separator top, gas-liquid separator bottom is connected with methylal storage tank, gas-liquid separator top is connected with methanol column bottom, methanol column top is connected with condenser through carrier pipe, condenser bottom is connected with gas-liquid separator top, gas-liquid separator bottom is connected with methyl alcohol storage tank.
On described synthesis reactor, be provided with two carrier pipes and hopper.On the mixing tank on condensation tower top, be provided with carrier pipe.
Described multistage compensating groove composes in parallel at least 3 compensating grooves, and described multistage depickling still composes in parallel at least 3 depickling stills, and each compensating groove bottom is connected with each depickling still top respectively.
Soda-wash tower bottom via line pipeline is connected with liquid caustic soda tank, and methylal tower bottom via line pipeline is connected with reboiler.Methanol column bottom is provided with steam carrier pipe.
Synthetic tower to carrier pipe, condensation kettle to carrier pipe, mixing tank to the carrier pipe of hybrid reactor of mixing tank of condensation kettle is insulating pipe.
Adopt said apparatus to carry out serialization and produce the method for glyphosate, specifically methyl alcohol and quadrol are entered to synthesis reactor through carrier pipe respectively, contact with paraformaldehyde with the Padil of inputting in hopper carry out depolymerization, addition reaction obtains reaction solution;
Reaction solution is inputed to the mixing tank on condensation kettle top through insulation feeding pipe, and mixing with the dimethyl ester of inputting in the mixing tank on condensation kettle top, input again and in condensation kettle, carry out condensation reaction, the condensated liquid obtaining;
After condensated liquid is together entered to mixing tank after the mixed in hydrochloric acid of utilidor and high-order hydrochloric acid tank mixing, this mixed solution is squeezed into the mixing kettle reaction that is hydrolyzed, obtain hydrolyzed solution;
This hydrolyzed solution is squeezed into compensating groove by magnetic drive pump, after compensating groove is all pressed, hydrolyzed solution is squeezed into depickling still precipitation, obtain glyphosate and depickling tail gas, by the glyphosate blowing, crystallization, dry, the packaging that reach after processing requirement, next batch hydrolyzed solution directly drops into depickling still, make it uninterrupted, continuous operations is produced, and the still of depickling simultaneously does not need temperature-fall period, energy efficient;
Depickling tail gas (80-90 DEG C) is directly entered to soda-wash tower and removes sour gas without condensation, tail gas after removing sour gas is from input methylal bottom, soda-wash tower top, tail gas enters the condensation of condensed in two stages device in methylal tower after cut, condensed tail gas is delivered to gas-liquid separator, phlegma after gas-liquid separator separates enters methylal storage tank, tail gas enters methanol column, tail gas enters the condensation of condensed in two stages device in methanol column after cut, condensed tail gas is delivered to methyl chloride recovery system, and phlegma enters methyl alcohol storage tank.
Temperature control in described soda-wash tower is more than 65 DEG C; At the bottom of methylal tower tower, controlling temperature is 70-80 DEG C, and methylal column overhead control temperature is to 30-40 DEG C; The control of methanol column column bottom temperature is 100-105 DEG C, and the control of methanol column tower top temperature is 60-65 DEG C.
By the linking of continuous device, be that whole Production Flow Chart can be produced in continual serialization.Thereby can, in existing situation, realize the dilatation of expanding production, save freezing energy consumption and steam energy consumption.This technology can make the yield of glyphosate improve 0.5%, and methyl chloride first goes out to remove impurity through Distallation systm, and the main content of methyl chloride can bring up to 99.9%.Serialization production automation degree is high, has reduced the safety and environmental protection accident that human factor causes.High-temperature tail gas enters the temperature low-boiling-point substance of dehydration tower utilization itself and automatically can send out from tower top and go out, and high boiling material enters sewage works at the bottom of falling into tower, has reduced like this COD of waste water, has reduced the pollution of waste water to environment.Totally say, this invention has good economy, environmental protection and social benefit, and application prospect is extensive.
Brief description of the drawings
Fig. 1 is the structural representation of glyphosate continuous production device, wherein, and 1. synthesis reactor, 2. condensation tower, 3. mixing tank, 4. mixing tank, 5. hybrid reactor, 6. magnetic drive pump, 7-1,2,3 compensating grooves, 8-1,2,3 depickling stills, 9. soda-wash tower, 10. methylal tower, 11-1,2 condensers, 12. methylal storage tanks, 13. methanol columns, 14-1,2. gas-liquid separator, 15. methyl alcohol storage tanks, 16. liquid caustic soda tanks, 17. reboilers, 18. hydrochloric acid tanks.
Embodiment
embodiment 1
A kind of glyphosate continuous production device, synthesis reactor 1 bottom is connected with the mixing tank on condensation tower 2 tops through carrier pipe, condensation tower 2 is connected with mixing tank 4 front ends after carrier pipe is connected with recycle pump again, mixing tank 4 upper ends are provided with high-order hydrochloric acid 18 storage tanks, mixing tank 4 ends are connected with recycle pump through carrier pipe, recycle pump via line pipeline is connected with hybrid reactor 5 tops, hybrid reactor 5 bottoms after carrier pipe is connected with magnetic drive pump 6 again with multistage compensating groove 7-1, 2, 3 tops connect, multistage compensating groove 7-1, 2, 3 bottoms are through carrier pipe and multistage depickling still 8-1, 2, 3 tops connect, multistage depickling still 8-1, 2, 3 tops are connected with soda-wash tower 9 bottoms after another cable tubing converges, soda-wash tower 9 top via line pipelines are connected with methylal tower 10 bottoms, methylal tower 10 top via line pipelines are connected with condenser 11-1, condenser 11-1 lower end is connected with gas-liquid separator 14-1 top, gas-liquid separator 14-1 bottom is connected with methylal storage tank 12, 14-1 top is connected with 13 bottoms, methanol column 13 tops are connected with condenser 11-2 through carrier pipe, condenser 11-2 bottom is connected with gas-liquid separator 14-2 top, gas-liquid separator 14-2 bottom is connected with 15.
On described synthesis reactor 1, be provided with two carrier pipes and hopper.On the mixing tank 3 on described condensation tower 2 tops, be provided with carrier pipe.
Described multistage compensating groove 7-1,2,3 at least 3 compensating grooves compose in parallel, described multistage depickling still 8-1,2,3 at least 3 depickling stills compose in parallel, and each compensating groove bottom is connected with each depickling still top respectively.
Soda-wash tower 9 bottom via line pipelines are connected with liquid caustic soda tank 16, and methylal tower 10 bottom via line pipelines are connected with reboiler 17.
Described methanol column 13 bottoms are provided with steam carrier pipe.
Synthetic tower 1 to carrier pipe, condensation kettle 2 to carrier pipe, mixing tank 4 to the carrier pipe of hybrid reactor 5 of mixing tank 4 of condensation kettle 2 is insulating pipe.
embodiment 2
Glyphosate serialization produce a method, methyl alcohol and quadrol enter synthesis reactor through carrier pipe respectively, contact with paraformaldehyde with the Padil of inputting in hopper carry out depolymerization, addition reaction obtains reaction solution;
Reaction solution is inputed to the mixing tank on condensation kettle top through insulation feeding pipe, and mixing with the dimethyl ester of inputting in the mixing tank on condensation kettle top, input again and in condensation kettle, carry out condensation reaction, the condensated liquid obtaining;
After condensated liquid is together entered to mixing tank after the mixed in hydrochloric acid of utilidor and high-order hydrochloric acid tank mixing, this mixed solution is squeezed into the mixing kettle reaction that is hydrolyzed, obtain hydrolyzed solution;
This hydrolyzed solution is squeezed into compensating groove by magnetic drive pump, after compensating groove is all pressed, hydrolyzed solution is squeezed into depickling still precipitation, obtain glyphosate and depickling tail gas, by the glyphosate blowing, crystallization, dry, the packaging that reach after processing requirement;
Depickling tail gas is entered to soda-wash tower and removes sour gas, tail gas after removing sour gas is from input methylal bottom, soda-wash tower top, tail gas enters the condensation of condensed in two stages device in methylal tower after cut, condensed tail gas is delivered to gas-liquid separator, phlegma after gas-liquid separator separates enters methylal storage tank, tail gas enters methanol column, tail gas enters the condensation of condensed in two stages device in methanol column after cut, condensed tail gas is delivered to methyl chloride recovery system, and phlegma enters methyl alcohol storage tank.
Temperature control in described soda-wash tower is more than 65 DEG C; At the bottom of methylal tower tower, controlling temperature is 70-80 DEG C, and methylal column overhead control temperature is to 30-40 DEG C; The control of methanol column column bottom temperature is 100-105 DEG C, and the control of methanol column tower top temperature is 60-65 DEG C.
Claims (7)
1. a glyphosate continuous production device, it is characterized in that: synthesis reactor (1) bottom is connected with the mixing tank on condensation tower (2) top through carrier pipe, condensation tower (2) is connected with mixing tank (4) front end after carrier pipe is connected with recycle pump again, mixing tank (4) upper end is provided with high-order hydrochloric acid (18) storage tank, mixing tank (4) end is connected with recycle pump through carrier pipe, recycle pump via line pipeline is connected with hybrid reactor (5) top, hybrid reactor (5) bottom after carrier pipe is connected with magnetic drive pump (6) again with multistage compensating groove (7-1, 2, 3) top connects, multistage compensating groove (7-1, 2, 3) bottom is through carrier pipe and multistage depickling still (8-1, 2, 3) top connects, multistage depickling still (8-1, 2, 3) top is connected with soda-wash tower (9) bottom after another cable tubing converges, soda-wash tower (9) top via line pipeline is connected with methylal tower (10) bottom, methylal tower (10) top via line pipeline is connected with condenser (11-1), condenser (11-1) lower end is connected with gas-liquid separator (14-1) top, gas-liquid separator (14-1) bottom is connected with methylal storage tank (12), gas-liquid separator (14-1) top is connected with methanol column (13) bottom, methanol column (13) top is connected with condenser (11-2) through carrier pipe, condenser (11-2) bottom is connected with gas-liquid separator (14-2) top, gas-liquid separator (14-2) bottom is connected with methyl alcohol storage tank (15).
2. glyphosate continuous production device according to claim 1, is characterized in that: on synthesis reactor (1), be provided with two carrier pipes and hopper.
3. glyphosate continuous production device according to claim 1, is characterized in that: on the mixing tank (3) on condensation tower (2) top, be provided with carrier pipe.
4. glyphosate continuous production device according to claim 1, it is characterized in that: described multistage compensating groove (7-1,2,3) at least 3 compensating grooves compose in parallel, described multistage depickling still (8-1,2,3), at least 3 depickling stills compose in parallel, each compensating groove bottom is connected with each depickling still top respectively.
5. glyphosate continuous production device according to claim 1, is characterized in that: soda-wash tower (9) bottom via line pipeline is connected with liquid caustic soda tank (16), and methylal tower (10) bottom via line pipeline is connected with reboiler (17).
6. glyphosate continuous production device according to claim 1, is characterized in that: methanol column (13) bottom is provided with steam carrier pipe.
7. glyphosate continuous production device according to claim 1, is characterized in that: synthetic tower (1) to carrier pipe, condensation kettle (2) to carrier pipe, mixing tank (4) to the carrier pipe of hybrid reactor (5) of mixing tank (4) of condensation kettle (2) is insulating pipe.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201420452658.1U CN203999455U (en) | 2014-08-12 | 2014-08-12 | A kind of glyphosate continuous production device |
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| CN201420452658.1U CN203999455U (en) | 2014-08-12 | 2014-08-12 | A kind of glyphosate continuous production device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110922426A (en) * | 2019-11-22 | 2020-03-27 | 湖北泰盛化工有限公司 | Alkyl ester method glyphosate continuous production system and process |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110922426A (en) * | 2019-11-22 | 2020-03-27 | 湖北泰盛化工有限公司 | Alkyl ester method glyphosate continuous production system and process |
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