CN104844414B - A kind of producing glyphosate by using glycine solvent reclaimer and technique - Google Patents

A kind of producing glyphosate by using glycine solvent reclaimer and technique Download PDF

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CN104844414B
CN104844414B CN201510258999.4A CN201510258999A CN104844414B CN 104844414 B CN104844414 B CN 104844414B CN 201510258999 A CN201510258999 A CN 201510258999A CN 104844414 B CN104844414 B CN 104844414B
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tower
conveying pipeline
methanol
dehydrating tower
methanol column
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CN104844414A (en
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田义群
徐森军
覃立忠
王瑞宝
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Hubei Taisheng Chemical Co Ltd
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Hubei Taisheng Chemical Co Ltd
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Abstract

The present invention provides a kind of producing glyphosate by using glycine solvent reclaimer and technique, is specifically related to glyphosate solvent recovery continuous prodution, vapor phase method recovery technology.The purpose of invention is to solve the shortcomings such as existing operation interval, labor intensity is big, energy consumption is high, chloromethanes purity is the highest.The present invention makes the content of chloromethanes bring up to reach 99.9% by realizing whole operation continuous prodution, reduces energy consumption, is widely used in glyphosate production field.

Description

A kind of producing glyphosate by using glycine solvent reclaimer and technique
Technical field
The present invention relates to a kind of producing glyphosate by using glycine solvent recovery new equipment and technique thereof, be specifically related to vapor phase method and reclaim Solvent technology.
Background technology
Glyphosate be by Monsanto Chemicals nineteen seventies research and develop a kind of efficiently, low toxicity, wide spectrum go out natural disposition Uptake and translocation herbicide, occupies the first place of world pesticide sales volume the most for years, along with transgenic resistance glyphosate is made in recent years The establishing in large scale of thing such as Semen sojae atricolor, Semen Maydis etc., the demand of glyphosate is continued to increase by the whole world.Current domestic glyphosate main flow produces Technique has two lines: (two-step method, first synthesizes PMIDA, then will be double for glycine method (one-step method) and iminodiacetic acid (salt) acid system The oxidation of sweet phosphine is referred to as glyphosate), external production technology is then mainly the iminodiacetic acid (salt) acid system of Monsanto Chemicals.State Interior glycine synthetic route be first first in synthesis reactor through depolymerization, addition, condensation;Condensation liquid squeeze into again deacidification still be hydrolyzed, Precipitation, deacidification;The mixed gas (chloromethanes, dilute methanol) in hydrolysis precipitation stage enters dilute methanol through three grades of condensations, condensed fluid Storage tank, uncooled tail gas enters chloromethanes recovery system and reclaims.Dilute methanol enters Distallation systm after neutralizing again and reclaims;This technology is grasped Making discontinuous, labor intensive is big, and yield is low, and energy consumption is high.
Summary of the invention
The purpose of invention
The present invention is directed to the existing existing glyphosate process route response time long, operation is discontinuous, and yield is low, and energy consumption is high, should Invention can realize continuous prodution, reduces energy resource consumption, improves glyphosate yield and the quality of chloromethanes.
A kind of producing glyphosate by using glycine solvent reclaimer, glyphosate tail gas conveying pipeline and diluted alkaline storage tank are through conveying pipeline and neutralization Tower connects, and neutralizing tower top is connected with gaseous mixture storage tank through conveying pipeline, and the top of gaseous mixture storage tank is connected with dehydrating tower ventilating fan After be connected with in the middle part of dehydrating tower through conveying pipeline again, dehydrating tower top is connected with dehydrating tower condenser through conveying pipeline, dehydrating tower condenser Being connected with dehydrating tower gas-liquid separator through conveying pipeline, dehydrating tower gas-liquid separator is connected with methanol column ventilating fan through conveying pipeline, de- It is connected with dehydrating tower backflow surge tank again after conveying pipeline converges respectively with bottom dehydrating tower gas-liquid separator bottom water tower condenser, Dehydrating tower backflow surge tank divides two-way after being connected with dehydrating tower reflux pump, and a road is connected with the middle part of methanol column, a road and dehydrating tower Top connects, and forms closed circuit;
In above-mentioned, from dehydrating tower reflux pump conveying pipeline with from dehydrating tower gas-liquid separator through the conveying pipeline one of methanol column ventilating fan With entering in the middle part of methanol column, methanol column top is connected with dimethoxym ethane first-stage condenser, dimethoxym ethane secondary condenser successively through conveying pipeline, Two-way is divided through conveying pipeline in dimethoxym ethane secondary condenser top, and a road is directly connected with chloromethanes recycling can after being connected with gas-liquid separator, One tunnel is connected with methanol column backflow surge tank through conveying pipeline, and methanol column backflow surge tank is connected with methanol column reflux pump through conveying pipeline, Methanol column reflux pump divides two-way through conveying pipeline, and a road is connected with methanol column top through conveying pipeline, forms closed circuit, and a road is through defeated Material pipe is connected with methanol blowdown condenser, and methanol blowdown condenser is connected with dimethoxym ethane finished pot top through conveying pipeline, and dimethoxym ethane becomes Product tank top is connected with dimethoxym ethane finished pot top after conveying pipeline is connected with reflux condenser again, forms closed circuit.
Described neutralizing tower bottom is additionally provided with neutralizing tower heater, with neutralizing tower heater base through conveying manifold bottom neutralizing tower Being connected with neutralizing tower reflux pump after conjunction, neutralizing tower reflux pump divides two-way through conveying pipeline, and a road is connected with neutralizing tower top, and formation follows Loop back path, a road is connected with in the middle part of dehydrating tower.
Two-way is divided through conveying pipeline, bottom a road and the conveying pipeline at neutralizing tower heater top, neutralizing tower bottom described dehydrating tower Conveying pipeline, the conveying pipeline of gaseous mixture storage tank are connected with sewage plant through conveying pipeline after converging, and a road is through conveying pipeline with waste water discharging pump even Connecing, waste water discharging pump divides two-way through conveying pipeline;One tunnel and the conveying pipeline of gaseous mixture storage tank bottom, neutralizing tower heater bottom defeated After material manifold closes, being connected with the conveying pipeline from waste water profit reduction and reserving tower bottom, a road is connected with waste water surge tank, at the bottom of waste water surge tank After the conveying pipeline in portion is connected with profit reduction and reserving tower feed pump, then it is connected with waste water profit reduction and reserving top of tower.
Described gaseous mixture tank bottom is connected with bottom dehydrating tower after conveying pipeline is connected with condenser discharging pump again.
Described waste water profit reduction and reserving top of tower is also connected with gaseous mixture storage tank bottom through conveying pipeline;Waste water surge tank top is additionally provided with useless The backflow conveying pipeline of water pot blowdown condenser.
Described dehydrating tower backflow surge tank top also sets up to be converged with dehydrating tower condenser to dehydrating tower gas-liquid separator conveying pipeline Conveying pipeline.
Being connected with methanol finished product condenser after conveying pipeline is connected with methanol discharging pump bottom described methanol column, methanol finished product is cold again Condenser is connected with methanol finished pot through conveying pipeline, and methanol finished pot top is additionally provided with the backflow conveying pipeline of dimethoxym ethane blowdown condenser.
Described methanol column bottom is also connected with methanol column reboiler, through conveying pipeline and methanol column reboiler through conveying pipeline bottom methanol column It is connected with decontamination station after converging.
A kind of producing glyphosate by using glycine solvent recovery process, specifically includes following steps:
Include chloromethanes, methanol, dimethoxym ethane, the mixture of steam from glyphosate synthesis post with mass concentration are The liquid caustic soda of 25%-30% blasts neutralizing tower together and is neutralized to pH is 7-8, neutralizes materials at bottom of tower neutralized tower heater and is heated to 60-80 DEG C of rear portion squeezes into dehydrating tower, and a part squeezes into neutralizing tower top, forms circulation, and neutralizing tower overhead gas enters mixing Gas surge tank, then blasts dehydrating tower;
Dehydration column overhead gas is condensed, after gas-liquid separator separates, gas enters methanol column, liquid through methanol column ventilating fan Condensed return to dehydrating tower backflow surge tank, dehydrating tower backflow surge tank in liquid through dehydrating tower reflux pump also into methanol column, Enter dehydrating tower without dehydration completely and form circulation;
Mixed liquor at the bottom of dehydrating tower tower enters waste water surge tank;The condensation of dehydration column overhead gas condensed device is slow also into dehydrating tower backflow Rush tank, part backflow, after a part is the most condensed, deliver to methanol column through dehydrating tower reflux pump;
Mixed liquor at the bottom of methanol column tower is condensed, and condensed fluid reclaims and obtains methanol, and the gas that methanol column tower top is not condensed is cold through two-stage Reclaim after solidifying, gas-liquid separation and obtain chloromethanes;It is delivered to dimethoxym ethane return tank the most residual night, through adding for condensation, gas-liquid separation Hot reflux rear portion extraction gas obtains dimethoxym ethane after emptying methanol, and a part delivers to methanol column top, carries out next step and follows Ring, whole during, it is 65 ± 5 DEG C that temperature bottom methanol column controls, and it is 35 ± 2 DEG C that the temperature on methanol column top controls;
The waste liquid of dehydrating tower inner bottom part is delivered to waste water profit reduction and reserving tower through waste water surge tank, and after profit reduction and reserving, mixed gas sends into gaseous mixture storage Tank, neutralizing tower heater delivered to by the mixed liquor after profit reduction and reserving;
The waste water that neutralizing tower heater, neutralizing tower, gaseous mixture storage tank, dehydrating tower, methanol column produce enters waste water station and processes.
By the linking of continuous device, it is that whole production procedure can continual continuous prodution.It is thus possible to existing In the case of, it is achieved dilatation of expanding production, save freezing energy consumption and steam energy consumption.Chloromethanes first passes through Distallation systm and goes out to remove impurity, chlorine The main content of methane can bring up to 99.9%.Continuous prodution automaticity is high, decreases the safety and environmental protection that anthropic factor causes Accident.High-temperature tail gas enters the temperature of dehydrating tower utilization itself, and low-boiling-point substance is gone out from tower top automatically, and high-boiling components falls into and enters at the bottom of tower Sewage Disposal, which decreases the COD of waste water, decreases the waste water pollution to environment.Totally saying, this invention has preferably Economy, environmental protection and social benefit, application prospect is extensive.
Accompanying drawing explanation
Fig. 1 is producing glyphosate by using glycine solvent recovery unit.
Wherein, 1. neutralizing tower, 2. gaseous mixture storage tank, 3. dehydrating tower ventilating fan, 4. dehydrating tower, 5. dehydrating tower condenser, 6. dehydration Tower gas-liquid separator, 7. methanol column ventilating fan, 8. dehydrating tower backflow surge tank, 9. dehydrating tower reflux pump, 10. methanol column, 11. Dimethoxym ethane first-stage condenser, 12. dimethoxym ethane secondary condensers, 13. gas-liquid separators, 14. methanol column reflux accumulator, 15. methanol columns Reflux pump, 16. methanol blowdown condensers, 17. dimethoxym ethane finished pots, 18. condensers, 19. neutralizing tower heaters, 20. neutralizing towers return Stream pump, 21. waste water discharging pumps, 22. waste water profit reduction and reserving towers, 23. waste water surge tanks, 24. profit reduction and reserving tower feed pumps, 25. condenser discharging pumps, 26. waste water tank blowdown condensers, 27. methanol discharging pumps, 28. methanol column reboilers, 29. methanol finished pots, 30. methanol finished product coolings Device, 31. dimethoxym ethane emptying coolers, 32. diluted alkaline storage tanks.
Detailed description of the invention
Embodiment 1
Producing glyphosate by using glycine can produce substantial amounts of chloromethanes and methanol, dimethoxym ethane, water vapour etc. in precipitation, deacidification Mixed gas.Traditional technique is mixed gas to be condensed through three grades of condensations, methanol, dimethoxym ethane, water (dilute methanol) Entering storage tank, the chloromethanes not condensed out (carrying methanol, dimethoxym ethane secretly) enters Chloromethane recovery device.Dilute methanol with Liquid caustic soda neutralizes, and neutralizer is squeezing into distillation system, reclaims methanol dimethoxym ethane.Traditional process energy consumption is high, chloromethanes removal process In every consumption higher, and chloromethanes content is on the low side.By research of technique, invent a kind of vapor phase method recovery process.This technique It is to be directly entered neutralizing tower, dehydrating tower, methanol column recovery methanol, first by the most condensed for the mixed gas in precipitation, deacidification Acetal, waste water at the bottom of dehydrating tower tower enters waste water rectifying column and again extracts methanol, dimethoxym ethane, and it is pre-that waste water at the bottom of high temperature tower enters neutralizing tower Hot device and temperature rise heat exchanger.This technique not only energy consumption is low, heat energy recycling, the content of chloromethanes can bring up to 99.9% with On.First the present invention provides a kind of producing glyphosate by using glycine solvent reclaimer, glyphosate tail gas conveying pipeline and diluted alkaline storage tank 32 are connected with neutralizing tower 1 through conveying pipeline, and neutralizing tower 1 top is connected with gaseous mixture storage tank 2 through conveying pipeline, gaseous mixture storage tank 2 Top is connected in the middle part of dehydrating tower 4 through conveying pipeline after being connected with dehydrating tower ventilating fan 3 again, dehydrating tower 4 top through conveying pipeline with Dehydrating tower condenser 5 connects, and dehydrating tower condenser 5 is connected with dehydrating tower gas-liquid separator 6 through conveying pipeline, and dehydrating tower gas-liquid is divided Be connected with methanol column ventilating fan 7 through conveying pipeline from device 6, bottom dehydrating tower condenser 5 with dehydrating tower gas-liquid separator 6 bottom It is connected with dehydrating tower backflow surge tank 8 again after conveying pipeline converges respectively, dehydrating tower backflow surge tank 8 and dehydrating tower reflux pump 9 Point two-way after connection, a road is connected with the middle part of methanol column 10, and a road is connected with dehydrating tower 4 top, forms closed circuit; In above-mentioned, from dehydrating tower reflux pump 9 conveying pipeline with from defeated through methanol column ventilating fan 7 of dehydrating tower gas-liquid separator 6 Material pipe together enters in the middle part of methanol column 10, methanol column 10 top through conveying pipeline successively with dimethoxym ethane first-stage condenser 11, dimethoxym ethane Secondary condenser 12 connects, and two-way is divided through conveying pipeline in dimethoxym ethane secondary condenser 12 top, and a road is connected with gas-liquid separator 13 Directly being connected with chloromethanes recycling can afterwards, a road is connected with methanol column backflow surge tank 14 through conveying pipeline, methanol column backflow surge tank 14 are connected with methanol column reflux pump 15 through conveying pipeline, and methanol column reflux pump 15 divides two-way through conveying pipeline, and a road is through conveying pipeline and first Alcohol tower 10 top connects, and forms closed circuit, and a road is connected with methanol blowdown condenser 16 through conveying pipeline, methanol emptying condensation Device 16 is connected with dimethoxym ethane finished pot 17 top through conveying pipeline, and dimethoxym ethane finished pot 17 top is through conveying pipeline and reflux condenser It is connected with dimethoxym ethane finished pot 17 top again after 18 connections, forms closed circuit.
Described neutralizing tower 1 bottom is additionally provided with neutralizing tower heater 19, bottom neutralizing tower 1 with neutralizing tower heater 19 bottom Being connected with neutralizing tower reflux pump 20 after conveying pipeline converges, neutralizing tower reflux pump 20 divides two-way through conveying pipeline, a road and neutralizing tower 1 top connects, and forms closed circuit, and a road is connected in the middle part of dehydrating tower 4.
Two-way is divided through conveying pipeline, a road and the conveying pipeline at neutralizing tower heater 19 top, neutralizing tower 1 bottom described dehydrating tower 4 The conveying pipeline of bottom, the conveying pipeline of gaseous mixture storage tank 2 are connected with sewage plant through conveying pipeline after converging, and a road is through conveying pipeline and waste water Discharging pump 21 connects, and waste water discharging pump 21 divides two-way through conveying pipeline;One tunnel and the conveying pipeline of gaseous mixture storage tank 2 bottom, neutralization After the conveying pipeline of tower heater 19 bottom converges, being connected with from the conveying pipeline bottom waste water profit reduction and reserving tower 22, a road is delayed with waste water Rush tank 23 to connect, after the conveying pipeline bottom waste water surge tank 23 is connected with profit reduction and reserving tower feed pump 24, then retain a percentage of the total profits for the enterprise's own use tower 22 with waste water Top connects.
It is connected with bottom dehydrating tower 4 again after conveying pipeline is connected with condenser discharging pump 25 bottom described gaseous mixture storage tank 2.
Described waste water profit reduction and reserving tower 22 top is also connected with gaseous mixture storage tank 2 bottom through conveying pipeline;Waste water surge tank 23 top is also It is provided with the backflow conveying pipeline of waste water tank blowdown condenser 26.
Described dehydrating tower backflow surge tank 8 top also sets up and dehydrating tower condenser 5 to dehydrating tower gas-liquid separator 6 conveying pipeline The conveying pipeline converged.
It is connected with methanol finished product condenser 30 again after conveying pipeline is connected with methanol discharging pump 27 bottom described methanol column 10, first Alcohol finished product condenser 30 is connected with methanol finished pot 29 through conveying pipeline, and it is cold that methanol finished pot 29 top is additionally provided with dimethoxym ethane emptying The backflow conveying pipeline of condenser 31.
Described methanol column 10 bottom is also connected with methanol column reboiler 28, boils with methanol column through conveying pipeline bottom methanol column 10 again Device 28 is connected with decontamination station after conveying pipeline converges.
Mixed gas from glyphosate synthesis post is blasted neutralizing tower by aerator and neutralizes with liquid caustic soda by the present invention, materials at bottom of tower warp Squeezing into dehydrating tower after neutralizing tower heat exchanger heat exchange, overhead gas enters mixing surge tank, then blasts dehydrating tower;Dehydration column overhead Gas enters methanol column through gas-liquid separator separates, gas, and the condensed return tank that returns to of liquid, at the bottom of tower, waste liquid is partly into dirt Water treatment station, is partly into wastewater storage tank;Gas enters methanol column with the liquid of return tank, and the condensed device of overhead gas condenses Entering return tank, part backflow, a part is the most condensed, and condensed fluid enters finished product dimethoxym ethane storage tank, methanol column tower bottom liquid warp Condensation, condensed fluid enters methanol finished product storage tank, and the gas that tower top is not condensed enters chloromethanes recovery system;Giving up of wastewater storage tank Water squeezes into the profit reduction and reserving tower that floods, and overhead gas enters mixing surge tank, and waste water at the bottom of tower enters temperature rise heat exchanger heating, recycles.
Specific as follows:
A kind of producing glyphosate by using glycine solvent recovery process, includes chloromethanes, methanol, first from glyphosate synthesis post Acetal, the mixture of steam blast neutralizing tower 1 together with the liquid caustic soda that mass concentration is 25%-30% to be neutralized to pH be 7-8, in Being heated to 60-80 DEG C of rear portion with tower 1 substrate material neutralized tower 1 heater and squeeze into dehydrating tower 4, a part squeezes into neutralizing tower 1 Top, forms circulation, and neutralizing tower 1 overhead gas enters gaseous mixture surge tank 2, then blasts dehydrating tower 4;
Dehydrating tower 4 overhead gas is condensed, after gas-liquid separator separates, gas enters methanol column 10, liquid through methanol column ventilating fan 7 Body is condensed returns to dehydrating tower backflow surge tank 8, the liquid in dehydrating tower backflow surge tank 8 through dehydrating tower reflux pump 9 also into Methanol column 10, enters dehydrating tower 4 completely and forms circulation without dehydration;
Mixed liquor at the bottom of dehydrating tower 4 tower enters waste water surge tank 23;The condensation of dehydrating tower 4 overhead gas condensed device refluxes also into dehydrating tower Surge tank 8, part backflow, deliver to methanol column 10 through dehydrating tower reflux pump 9 after a part is the most condensed;
Mixed liquor at the bottom of methanol column 10 tower is condensed, and condensed fluid reclaims and obtains methanol, and the gas that methanol column 10 tower top is not condensed is through two-stage Reclaim after condensation, gas-liquid separation and obtain chloromethanes;It is delivered to dimethoxym ethane return tank 14 the most residual night for condensation, gas-liquid separation, Heated backflow rear portion extraction gas obtains dimethoxym ethane after emptying methanol, and a part delivers to methanol column top, carries out next Step circulation, it is 65 ± 5 DEG C that the temperature bottom methanol column 10 controls, and it is 35 ± 2 DEG C that the temperature on methanol column 10 top controls;
The waste liquid of dehydrating tower 4 inner bottom part is delivered to waste water profit reduction and reserving tower 22 through waste water surge tank 23, and after profit reduction and reserving, mixed gas sends into mixing Gas storage tank 2, neutralizing tower heater 19 delivered to by the mixed liquor after profit reduction and reserving;
The waste water that neutralizing tower heater 19, neutralizing tower 1, gaseous mixture storage tank 2, dehydrating tower 3, methanol column 10 produce enters waste water station and enters Row processes.

Claims (9)

1. a producing glyphosate by using glycine solvent reclaimer, it is characterised in that
nullGlyphosate tail gas conveying pipeline is connected with neutralizing tower (1) through conveying pipeline with diluted alkaline storage tank (32),Neutralizing tower (1) top is connected with gaseous mixture storage tank (2) through conveying pipeline,The top of gaseous mixture storage tank (2) is connected with dehydrating tower (4) middle part through conveying pipeline after being connected with dehydrating tower ventilating fan (3) again,Dehydrating tower (4) top is connected with dehydrating tower condenser (5) through conveying pipeline,Dehydrating tower condenser (5) is connected with dehydrating tower gas-liquid separator (6) through conveying pipeline,Dehydrating tower gas-liquid separator (6) is connected with methanol column ventilating fan (7) through conveying pipeline,Dehydrating tower condenser (5) bottom is connected with dehydrating tower backflow surge tank (8) respectively with dehydrating tower gas-liquid separator (6) bottom after conveying pipeline converges again,Dehydrating tower backflow surge tank (8) divides two-way after being connected with dehydrating tower reflux pump (9),One tunnel is connected with the middle part of methanol column (10),One tunnel is connected with dehydrating tower (4) top,Form closed circuit;
nullIn above-mentioned,Conveying pipeline from dehydrating tower reflux pump (9) together enters methanol column (10) middle part with from dehydrating tower gas-liquid separator (6) through the conveying pipeline of methanol column ventilating fan (7),Methanol column (10) top through conveying pipeline successively with dimethoxym ethane first-stage condenser (11)、Dimethoxym ethane secondary condenser (12) connects,Two-way is divided through conveying pipeline in dimethoxym ethane secondary condenser (12) top,One tunnel is directly connected with chloromethanes recycling can after being connected with gas-liquid separator (13),One tunnel is connected with methanol column backflow surge tank (14) through conveying pipeline,Methanol column backflow surge tank (14) is connected with methanol column reflux pump (15) through conveying pipeline,Methanol column reflux pump (15) divides two-way through conveying pipeline,One tunnel is connected with methanol column (10) top through conveying pipeline,Form closed circuit,One tunnel is connected with methanol blowdown condenser (16) through conveying pipeline,Methanol blowdown condenser (16) is connected with dimethoxym ethane finished pot (17) top through conveying pipeline,Dimethoxym ethane finished pot (17) top is connected with dimethoxym ethane finished pot (17) top after conveying pipeline is connected with reflux condenser (18) again,Form closed circuit;
Two-way is divided through conveying pipeline in described dehydrating tower (4) bottom, the conveying pipeline of the conveying pipeline at one tunnel and neutralizing tower heater (19) top, neutralizing tower (1) bottom, the conveying pipeline of gaseous mixture storage tank (2) are connected with sewage plant through conveying pipeline after converging, one tunnel is connected with waste water discharging pump (21) through conveying pipeline, and waste water discharging pump (21) divides two-way through conveying pipeline;After one tunnel is converged with the conveying pipeline of gaseous mixture storage tank (2) bottom, the conveying pipeline of neutralizing tower heater (19) bottom, it is connected with the conveying pipeline from waste water profit reduction and reserving tower (22) bottom, one tunnel is connected with waste water surge tank (23), after the conveying pipeline of waste water surge tank (23) bottom is connected with profit reduction and reserving tower feed pump (24), then it is connected with waste water profit reduction and reserving tower (22) top.
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterized in that, neutralizing tower (1) bottom is additionally provided with neutralizing tower heater (19), neutralizing tower (1) bottom is connected with neutralizing tower reflux pump (20) after conveying pipeline converges with neutralizing tower heater (19) bottom, neutralizing tower reflux pump (20) divides two-way through conveying pipeline, one tunnel is connected with neutralizing tower (1) top, forms closed circuit, and a road is connected with dehydrating tower (4) middle part.
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterised in that gaseous mixture storage tank (2) bottom is connected with dehydrating tower (4) bottom after conveying pipeline is connected with condenser discharging pump (25) again.
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterised in that waste water profit reduction and reserving tower (22) top is also connected with gaseous mixture storage tank (2) bottom through conveying pipeline;Waste water surge tank (23) top is additionally provided with the backflow conveying pipeline of waste water tank blowdown condenser (26).
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterised in that dehydrating tower backflow surge tank (8) top also sets up the conveying pipeline converged with dehydrating tower condenser (5) to dehydrating tower gas-liquid separator (6) conveying pipeline.
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterized in that, methanol column (10) bottom is connected with methanol finished product condenser (30) after conveying pipeline is connected with methanol discharging pump (27) again, methanol finished product condenser (30) is connected with methanol finished pot (29) through conveying pipeline, and methanol finished pot (29) top is additionally provided with the backflow conveying pipeline of dimethoxym ethane blowdown condenser (31).
Producing glyphosate by using glycine solvent reclaimer the most according to claim 1, it is characterized in that, methanol column (10) bottom is also connected with methanol column reboiler (28), and methanol column (10) bottom is connected with decontamination station with methanol column reboiler (28) through conveying pipeline after conveying pipeline converges.
8. a producing glyphosate by using glycine solvent recovery process, it is characterised in that
Blast neutralizing tower (1) together with the liquid caustic soda that mass concentration is 25%-30% to be neutralized to pH be 7-8 from glyphosate synthesis post containing chloromethanes, methanol, dimethoxym ethane, the mixture of steam, neutralizing tower (1) substrate material neutralized tower (1) heater is heated to 60-80 DEG C of rear portion and squeezes into dehydrating tower (4), a part squeezes into neutralizing tower (1) top, form circulation, neutralizing tower (1) overhead gas enters gaseous mixture storage tank (2), then blasts dehydrating tower (4);
Dehydrating tower (4) overhead gas is condensed, after gas-liquid separator separates, gas enters methanol column (10) through methanol column ventilating fan (7), liquid is condensed returns to dehydrating tower backflow surge tank (8), liquid in dehydrating tower backflow surge tank (8) also into methanol column (10) through dehydrating tower reflux pump (9), is not dehydrated and enters dehydrating tower (4) formation circulation completely;
Mixed liquor at the bottom of dehydrating tower (4) tower enters waste water surge tank (23);The condensation of dehydrating tower (4) overhead gas condensed device, also into dehydrating tower backflow surge tank (8), part backflow, delivers to methanol column (10) through dehydrating tower reflux pump (9) after a part is the most condensed;
Mixed liquor at the bottom of methanol column (10) tower is condensed, and condensed fluid reclaims and obtains methanol, and the gas that methanol column (10) tower top is not condensed reclaims after condensed in two stages, gas-liquid separation and obtains chloromethanes;Uncooled, gas-liquid separation residual liquid completely is delivered to methanol column backflow surge tank (14), and heated backflow rear portion extraction gas obtains dimethoxym ethane after emptying methanol, and a part delivers to methanol column (10) top, carries out next step circulation;
The waste liquid of dehydrating tower (4) inner bottom part is delivered to waste water profit reduction and reserving tower (22) through waste water surge tank (23), and after profit reduction and reserving, mixed gas sends into gaseous mixture storage tank (2), and neutralizing tower heater (19) delivered to by the mixed liquor after profit reduction and reserving;
The waste water that neutralizing tower heater (19), neutralizing tower (1), gaseous mixture storage tank (2), dehydrating tower (4), methanol column (10) produce enters waste water station and processes.
Producing glyphosate by using glycine solvent recovery process the most according to claim 8, it is characterised in that the temperature of methanol column (10) bottom controls to be 65 ± 5 DEG C, and it is 35 ± 2 DEG C that the temperature on methanol column (10) top controls.
CN201510258999.4A 2015-05-20 2015-05-20 A kind of producing glyphosate by using glycine solvent reclaimer and technique Active CN104844414B (en)

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