CN203678222U - Glyphosate tail gas absorption liquid recycling equipment - Google Patents
Glyphosate tail gas absorption liquid recycling equipment Download PDFInfo
- Publication number
- CN203678222U CN203678222U CN201320859930.3U CN201320859930U CN203678222U CN 203678222 U CN203678222 U CN 203678222U CN 201320859930 U CN201320859930 U CN 201320859930U CN 203678222 U CN203678222 U CN 203678222U
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- CN
- China
- Prior art keywords
- tail gas
- absorption
- absorption liquid
- absorption tower
- heat exchanger
- 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 - Lifetime
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 108
- 239000007788 liquid Substances 0.000 title claims abstract description 59
- 239000005562 Glyphosate Substances 0.000 title claims abstract description 28
- 229940097068 glyphosate Drugs 0.000 title claims abstract description 28
- XDDAORKBJWWYJS-UHFFFAOYSA-N glyphosate Chemical compound OC(=O)CNCP(O)(O)=O XDDAORKBJWWYJS-UHFFFAOYSA-N 0.000 title claims abstract description 23
- 238000004064 recycling Methods 0.000 title claims abstract description 13
- 238000000034 method Methods 0.000 claims abstract description 22
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 claims description 61
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 238000007599 discharging Methods 0.000 claims description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 150
- NKDDWNXOKDWJAK-UHFFFAOYSA-N dimethoxymethane Chemical compound COCOC NKDDWNXOKDWJAK-UHFFFAOYSA-N 0.000 abstract description 58
- 238000003795 desorption Methods 0.000 abstract description 7
- 230000002745 absorbent Effects 0.000 abstract description 4
- 239000002250 absorbent Substances 0.000 abstract description 4
- 238000009833 condensation Methods 0.000 abstract description 2
- 230000005494 condensation Effects 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000005406 washing Methods 0.000 description 15
- 229940050176 methyl chloride Drugs 0.000 description 13
- 239000007864 aqueous solution Substances 0.000 description 10
- 230000007115 recruitment Effects 0.000 description 10
- 230000001276 controlling effect Effects 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 238000010992 reflux Methods 0.000 description 6
- 239000013589 supplement Substances 0.000 description 6
- 238000000605 extraction Methods 0.000 description 5
- -1 glyphosate chloromethanes Chemical class 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 125000004122 cyclic group Chemical class 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 125000000217 alkyl group Chemical group 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000005886 esterification reaction Methods 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to glyphosate tail gas absorption liquid recycling equipment. In the equipment, glyphosate tail gas is introduced into the lower part of an absorption tower by a material conveying tube; the bottom end of the absorption tower is communicated into a charge hole in the bottom end of a heat exchanger by a circulating pump; a discharge hole in the top end of the heat exchanger is communicated into the upper part of a desorption tower; the bottom end of the desorption tower enters the upper part of the absorption tower by the circulating pump. Concentration of methanol and methylal in glyphosate tail gas is concentrated and enriched by an absorption process and a desorption process, and methanol and methylal in the gas are recycled by condensation. After the absorption liquid is desorbed, concentration of methanol and methylal is greatly lowered, so that the absorption liquid enters an absorption tower to be recycled as circulating absorption liquid. The glyphosate tail gas absorption liquid recycling equipment disclosed by the utility model solves a problem that the absorption efficiency of methanol and methylal in the glyphosate tail gas is low, the circulation amount of an absorbent is improved by recycling, the absorption liquid in lower concentration in an absorption process can be kept, and the absorption efficiency is greatly improved.
Description
Technical field
The utility model relates to a kind of glyphosate tail gas absorption liquid recycling device, belongs to chemical production equipment field.
Background technology
Adopt alkyl esterification method to produce glyphosate and can produce a large amount of chloromethanes tail gas, methyl alcohol, the dimethoxym ethane that in the time that chloromethanes tail gas is recycled, need in removing chloromethanes tail gas, carry secretly by condensation, washing.The equilibrium concentration that can reach because of water absorption liquid is lower, need to supplement a large amount of clear water, and low concentration methanol, the cost recovery of the dimethoxym ethane aqueous solution of follow-up generation are higher, and a large amount of waste water producing.In the time that summer temperature is higher, when chloromethanes tail gas condensing can not be up to standard, situation can be more serious.Therefore solve the problem that chloromethanes water absorption liquid recycles and can produce larger economic benefit and environmental benefit.
Traditionally, the general absorption tower chloromethanes tail gas that adopts washs, remove methyl alcohol, dimethoxym ethane in chloromethanes tail gas, absorption liquid concentration is only at 4%-5%, purify 1 ton of methyl alcohol, dimethoxym ethane content at 15% chloromethanes, need to produce 3 tons of waste water, its organic efficiency is low, cost is high, and is attached with corresponding environmental problem.
Summary of the invention
The purpose of this utility model is to provide a kind of glyphosate tail gas absorption liquid recycling device, be specially glyphosate tail gas and pass into bottom, absorption tower through conveying pipeline, bottom, absorption tower passes into heat exchanger bottom charging aperture through circulating pump, heat exchanger top discharging opening passes into desorber top, and desorber bottom enters top, absorption tower through circulating pump;
Described desorber top passes into heat exchanger top charging aperture through vavuum pump, and heat exchanger bottom discharging opening passes into condenser; Pure chloromethanes air compensating system is added in described desorber bottom;
Described desorber passes in the process of absorption tower through circulating pump, adds water charging system.
Adopt above-mentioned process equipment to carry out the technique that glyphosate tail gas absorption liquid recycles, can effectively reduce use amount and the cost recovery of absorption liquid, and solve the environmental issue of bringing because of a large amount of uses of absorption liquid.Concrete technology scheme is as follows:
1. the chloromethanes tail gas of glyphosate production enters absorption tower, absorption liquid enters the chloromethanes tail gas counter current contacting of top, absorption tower and bottom, absorption tower, in absorption tower, supplement clear water simultaneously, clear water magnitude of recruitment should ensure that absorption tower global cycle amount equals absorption liquid produced quantity in absorption tower, and controlling the supplementary flow of clear water is 40m
3/ h, and ensure by chloromethanes tail gas at least the methyl alcohol of 75-80%, dimethoxym ethane be washed down, through washing after methyl chloride gas enter subsequent recovery operation, absorption liquid contains methyl alcohol and dimethoxym ethane and further recycles after once washing;
The described absorption liquid aqueous solution or the pure water lower than 0.2% methyl alcohol and dimethoxym ethane that be mass concentration lower than 0.2% the dimethoxym ethane aqueous solution, mass concentration.
2. the absorption liquid after once washing in step 1 pumps into heat exchanger through circulating pump, absorption liquid is sent into through vavuum pump and is vacuumized the desorber that is decompressed to 5-10KPa after heating up in heat exchanger, and to desorber top uniform flow, with carry out counter current contacting to lower and upper supplementary pure methyl chloride gas, wherein the control of pure chloromethanes magnitude of recruitment is 100-400Kg/h.In absorption liquid, most methyl alcohol, dimethoxym ethane evaporate in gas, in liquid, methyl alcohol, dimethoxym ethane content are reduced to below 0.2%, parsing tail gas methyl alcohol, dimethoxym ethane enter heat exchanger by vavuum pump, absorption liquid is in desorption process, again pumped into absorption tower and absorb methyl alcohol, dimethoxym ethane, in this cyclic process, through vavuum pump, compression there will be intensification to desorber tail gas, utilizes absorption liquid and desorber tail gas to carry out heat exchange, absorption liquid heats up, the cooling of desorber tail gas.
3. in step 2, desorb tail gas enters condenser through heat exchanger, controlling condenser air pressure is that 120KPa and condenser reflux gas temperature are controlled at-5 ~-10 DEG C, in tail gas, methyl alcohol, dimethoxym ethane, moisture are condensed, form methyl alcohol, the dimethoxym ethane aqueous solution of high concentration, enter rectification working process and reclaim, the methyl alcohol not being condensed, the methyl chloride gas of dimethoxym ethane are sent back in glyphosate chloromethanes tail gas again.
The utility model has solved methyl alcohol in glyphosate tail gas, problem that dimethoxym ethane absorption efficiency is low, by recycling the internal circulating load that can improve to greatest extent absorbent, keep absorption liquid in absorption process, to maintain low concentration scope, increase substantially absorption efficiency.In the present invention, absorbent is repeated to utilize, and the absorbent magnitude of recruitment in whole cyclic process is considerably less, has avoided a large amount of generations of waste liquid in conventional process mode.Realize recycling of all heats and material, both reduced cost, realized again environmental protection recovery.
Brief description of the drawings
Fig. 1 is glyphosate tail gas absorption liquid recycling device flow chart, wherein 1. absorption towers, 2. circulating pump, 3. circulating pump, 4. desorber, 5. vavuum pump, 6. heat exchanger, 7. condenser, 8. water charging system, 9. pure chloromethanes air compensating system.
Detailed description of the invention
embodiment 1
Glyphosate tail gas passes into 1 bottom, absorption tower through conveying pipeline, and 1 bottom, absorption tower passes into heat exchanger 6 bottom charging apertures through circulating pump 2, and heat exchanger 6 top discharging openings pass into desorber 4 tops, and desorber 4 bottoms enter 1 top, absorption tower through circulating pump 3.
Described desorber 4 tops pass into heat exchanger 6 top charging apertures through vavuum pump 5, and heat exchanger 6 bottom discharging openings pass into condenser 7.Pure chloromethanes air compensating system 9 is added in described desorber 4 bottoms; Desorber 4 passes in the process of absorption tower through circulating pump 3, adds water charging system 8.
Chloromethanes tail gas is imported in absorption tower 1, and the dimethoxym ethane aqueous solution that mass concentration is 0.1% enters the chloromethanes tail gas counter current contacting of top, absorption tower and bottom, absorption tower, and one time clear water supplements flow-control to 40m
3/ h, vavuum pump 5 moves, stable desorber 4 vacuums of controlling are at 9.5KPa, absorption liquid pumps into desorber 4 through circulating pump 2 and circulates, according to desorber 4 bottom extraction liquid dimethoxym ethane content, progressively increasing in desorber 4 pure chloromethanes and controlling pure chloromethanes flow is 100Kg/h, keeps desorber bottom extraction liquid dimethoxym ethane content below 0.2%.Stripping liquid pumps into absorption tower 1 through circulating pump 3 and circulates, and reduces clear water magnitude of recruitment and makes absorption tower global cycle amount be controlled at 40 m
3/ h.Desorb tail gas enters heat exchanger 6 after compressing by vavuum pump 5, and condenser 7 carries out fractional condensaion, regulates condenser air pressure in 120KPa(absolute pressure), condensing agent flow makes reflux gas temperature be controlled at-10 DEG C.Most methyl alcohol in gas, dimethoxym ethane, moisture are condensed, form mass concentration higher than 85% methyl alcohol, the dimethoxym ethane aqueous solution, entering rectification working process reclaims, the methyl chloride gas that contains minute quantity methyl alcohol, dimethoxym ethane is sent back in glyphosate chloromethanes tail gas again, regulating system stable operation.
The 10% dimethoxym ethane weak solution that chloromethanes washing tail gas is reclaimed is with 40 m
3the flow of/h passes in desorber 4, the pure chloromethanes of continuous supplementation is also controlled and is supplemented flow at 400Kg/h, start vavuum pump 5, control desorber 4 pressure at 5KPa, desorb tail gas enters heat exchanger 6 after by vavuum pump successively, condenser 7, control condenser reflux gas temperature at-5 DEG C, condenser air pressure is in 120KPa(absolute pressure), the separation that is condensed of dimethoxym ethane in gas and a small amount of moisture, form mass concentration higher than 50% dimethoxym ethane pregnant solution, entering rectifying column recycles, the mass concentration that desorber forms is added for carrying out chloromethanes washing and reclaims lower than 0.2% stripping liquid.
The chloromethanes tail gas of glyphosate production enters absorption tower, and pure water enters the chloromethanes tail gas counter current contacting of top, absorption tower and bottom, absorption tower, simultaneously in absorption tower, supplements clear water, and to control the supplementary flow of clear water be 40m
3/ h, clear water magnitude of recruitment should ensure that absorption tower global cycle amount equals absorption liquid produced quantity in absorption tower, and ensure at least 75% methyl alcohol, dimethoxym ethane in chloromethanes tail gas to be washed down, methyl chloride gas after washing enters subsequent recovery operation, and absorption liquid will contain methyl alcohol and dimethoxym ethane and further recycle after once washing.
Absorption liquid in above-mentioned steps after once washing pumps into heat exchanger through circulating pump, after 28 DEG C of the absorption liquid systems of heating up in heat exchanger, send into through vavuum pump and vacuumize the desorber that is decompressed to 8.5KPa, and to desorber top uniform flow, with carry out counter current contacting to lower and upper supplementary pure methyl chloride gas, wherein the control of pure chloromethanes magnitude of recruitment is 320Kg/h.In absorption liquid, most methyl alcohol, dimethoxym ethane evaporate in gas, and in the liquid of control extraction, methyl alcohol, dimethoxym ethane content are reduced to below 0.2%.Desorb tail gas methyl alcohol, dimethoxym ethane enter heat exchanger by vavuum pump, and absorption liquid, in desorption process, is again pumped into absorption tower and absorbs methyl alcohol, dimethoxym ethane.
In above-mentioned steps, desorb tail gas enters condenser through heat exchanger, controlling condenser air pressure is that 120KPa and condenser reflux gas temperature are controlled at-7 DEG C, in tail gas, methyl alcohol, dimethoxym ethane, moisture are condensed, form mass concentration higher than 50% methyl alcohol, the dimethoxym ethane aqueous solution, enter rectification working process and reclaim, the methyl alcohol not being condensed, the methyl chloride gas of dimethoxym ethane are sent back in glyphosate chloromethanes tail gas again.
The chloromethanes tail gas of glyphosate production enters absorption tower, and 0.2 the dimethoxym ethane aqueous solution enters the chloromethanes tail gas counter current contacting of top, absorption tower and bottom, absorption tower, simultaneously in absorption tower, supplements clear water, and to control the supplementary flow of clear water be 40m
3/ h, clear water magnitude of recruitment should ensure that absorption tower global cycle amount equals absorption liquid produced quantity in absorption tower, and ensure at least 78% methyl alcohol, dimethoxym ethane in chloromethanes tail gas to be washed down, methyl chloride gas after washing enters subsequent recovery operation, and absorption liquid will contain methyl alcohol and dimethoxym ethane and further recycle after once washing.
Absorption liquid in above-mentioned steps after once washing pumps into heat exchanger through circulating pump, after 30 DEG C of the absorption liquid systems of heating up in heat exchanger, send into through vavuum pump and vacuumize the desorber that is decompressed to 10.0KPa, and to desorber top uniform flow, with carry out counter current contacting to lower and upper supplementary pure methyl chloride gas, wherein the control of pure chloromethanes magnitude of recruitment is 280Kg/h.In absorption liquid, most methyl alcohol, dimethoxym ethane evaporate in gas, and in the liquid of control extraction, methyl alcohol, dimethoxym ethane content are reduced to below 0.2%.Desorb tail gas methyl alcohol, dimethoxym ethane enter heat exchanger by vavuum pump, and absorption liquid, in desorption process, is again pumped into absorption tower and absorbs methyl alcohol, dimethoxym ethane.
In above-mentioned steps, desorb tail gas enters condenser through heat exchanger, controlling condenser air pressure is that 120KPa and condenser reflux gas temperature are controlled at-10 DEG C, in tail gas, methyl alcohol, dimethoxym ethane, moisture are condensed, form mass concentration higher than 75% methyl alcohol, the dimethoxym ethane aqueous solution, enter rectification working process and reclaim, the methyl alcohol not being condensed, the methyl chloride gas of dimethoxym ethane are sent back in glyphosate chloromethanes tail gas again.
The chloromethanes tail gas of glyphosate production enters absorption tower, mass concentration is the chloromethanes tail gas counter current contacting that the mixed solution of 0.15% methyl alcohol and dimethoxym ethane enters top, absorption tower and bottom, absorption tower, simultaneously in absorption tower, supplement clear water, and to control the supplementary flow of clear water be 40m
3/ h, clear water magnitude of recruitment should ensure that absorption tower global cycle amount equals absorption liquid produced quantity in absorption tower, and ensure at least 80% methyl alcohol, dimethoxym ethane in chloromethanes tail gas to be washed down, methyl chloride gas after washing enters subsequent recovery operation, and absorption liquid will contain methyl alcohol and dimethoxym ethane and further recycle after once washing.
Absorption liquid in above-mentioned steps after once washing pumps into heat exchanger through circulating pump, after 27 DEG C of the absorption liquid systems of heating up in heat exchanger, send into through vavuum pump and vacuumize the desorber that is decompressed to 6.5KPa, and to desorber top uniform flow, with carry out counter current contacting to lower and upper supplementary pure methyl chloride gas, wherein the control of pure chloromethanes magnitude of recruitment is 250Kg/h.In absorption liquid, most methyl alcohol, dimethoxym ethane evaporate in gas, and in the liquid of control extraction, methyl alcohol, dimethoxym ethane content are reduced to below 0.2%.Desorb tail gas methyl alcohol, dimethoxym ethane enter heat exchanger by vavuum pump, and absorption liquid, in desorption process, is again pumped into absorption tower and absorbs methyl alcohol, dimethoxym ethane.
In above-mentioned steps, desorb tail gas enters condenser through heat exchanger, controlling condenser air pressure is that 120KPa and condenser reflux gas temperature are controlled at-5 DEG C, in tail gas, methyl alcohol, dimethoxym ethane, moisture are condensed, form mass concentration higher than 78% methyl alcohol, the dimethoxym ethane aqueous solution, enter rectification working process and reclaim, the methyl alcohol not being condensed, the methyl chloride gas of dimethoxym ethane are sent back in glyphosate chloromethanes tail gas again.
Claims (3)
1. glyphosate tail gas absorption liquid recycling device, it is characterized in that, glyphosate tail gas passes into bottom, absorption tower (1) through conveying pipeline, bottom, absorption tower (1) passes into heat exchanger (6) bottom charging aperture through circulating pump (2), heat exchanger (6) top discharging opening passes into desorber (4) top, and desorber (4) bottom enters top, absorption tower (1) through circulating pump (3).
2. glyphosate tail gas absorption liquid recycling device according to claim 1, it is characterized in that, described desorber (4) top passes into heat exchanger (6) top charging aperture through vavuum pump (5), and heat exchanger (6) bottom discharging opening passes into condenser (7).
3. glyphosate tail gas absorption liquid recycling device according to claim 1, is characterized in that, pure chloromethanes air compensating system (9) is added in described desorber (4) bottom; Desorber (4) passes in the process of absorption tower through circulating pump (3), adds water charging system (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320859930.3U CN203678222U (en) | 2013-12-25 | 2013-12-25 | Glyphosate tail gas absorption liquid recycling equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320859930.3U CN203678222U (en) | 2013-12-25 | 2013-12-25 | Glyphosate tail gas absorption liquid recycling equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203678222U true CN203678222U (en) | 2014-07-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320859930.3U Expired - Lifetime CN203678222U (en) | 2013-12-25 | 2013-12-25 | Glyphosate tail gas absorption liquid recycling equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203678222U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103691257A (en) * | 2013-12-25 | 2014-04-02 | 湖北泰盛化工有限公司 | Recycling process and equipment for glyphosate exhaust gas absorption liquid |
| CN104163832A (en) * | 2014-08-12 | 2014-11-26 | 湖北泰盛化工有限公司 | Glyphosate continuous production device and glyphosate continuous production method |
| CN106823667A (en) * | 2017-01-04 | 2017-06-13 | 安徽国星生物化学有限公司 | Chloride methane waste product handling process in a kind of paraquat production |
-
2013
- 2013-12-25 CN CN201320859930.3U patent/CN203678222U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103691257A (en) * | 2013-12-25 | 2014-04-02 | 湖北泰盛化工有限公司 | Recycling process and equipment for glyphosate exhaust gas absorption liquid |
| CN103691257B (en) * | 2013-12-25 | 2016-02-10 | 湖北泰盛化工有限公司 | Glyphosate tail gas absorption liquid utilization process and equipment thereof |
| CN104163832A (en) * | 2014-08-12 | 2014-11-26 | 湖北泰盛化工有限公司 | Glyphosate continuous production device and glyphosate continuous production method |
| CN106823667A (en) * | 2017-01-04 | 2017-06-13 | 安徽国星生物化学有限公司 | Chloride methane waste product handling process in a kind of paraquat production |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
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| CX01 | Expiry of patent term |
Granted publication date: 20140702 |