CN103012161A - Cleaning and dehydrating method of toluenediamine - Google Patents
Cleaning and dehydrating method of toluenediamine Download PDFInfo
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- CN103012161A CN103012161A CN2013100153905A CN201310015390A CN103012161A CN 103012161 A CN103012161 A CN 103012161A CN 2013100153905 A CN2013100153905 A CN 2013100153905A CN 201310015390 A CN201310015390 A CN 201310015390A CN 103012161 A CN103012161 A CN 103012161A
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- VOZKAJLKRJDJLL-UHFFFAOYSA-N 2,4-diaminotoluene Chemical compound CC1=CC=C(N)C=C1N VOZKAJLKRJDJLL-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000004140 cleaning Methods 0.000 title claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000002351 wastewater Substances 0.000 claims abstract description 19
- 239000007791 liquid phase Substances 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract description 9
- 239000007792 gaseous phase Substances 0.000 claims abstract description 7
- 230000018044 dehydration Effects 0.000 claims description 73
- 238000006297 dehydration reaction Methods 0.000 claims description 73
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 48
- 229910052757 nitrogen Inorganic materials 0.000 claims description 24
- 238000000605 extraction Methods 0.000 claims description 15
- 239000007789 gas Substances 0.000 claims description 13
- 238000009835 boiling Methods 0.000 claims description 12
- 230000008676 import Effects 0.000 claims description 10
- 241000282326 Felis catus Species 0.000 claims description 8
- 239000000470 constituent Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
- 239000006227 byproduct Substances 0.000 claims description 4
- 230000009286 beneficial effect Effects 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000011521 glass Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 230000002093 peripheral effect Effects 0.000 claims description 3
- 230000005501 phase interface Effects 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 239000000126 substance Substances 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 238000005292 vacuum distillation Methods 0.000 abstract 1
- 239000011541 reaction mixture Substances 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- DYSXLQBUUOPLBB-UHFFFAOYSA-N 2,3-dinitrotoluene Chemical compound CC1=CC=CC([N+]([O-])=O)=C1[N+]([O-])=O DYSXLQBUUOPLBB-UHFFFAOYSA-N 0.000 description 2
- DVKJHBMWWAPEIU-UHFFFAOYSA-N toluene 2,4-diisocyanate Chemical compound CC1=CC=C(N=C=O)C=C1N=C=O DVKJHBMWWAPEIU-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention belongs to the technical field of chemical rectifying, separating and dehydrating, and relates to a cleaning and dehydrating method of toluenediamine. The cleaning and dehydrating method comprises the following steps: dehydrating in a double-tower dehydrating device, so that crude TDA (Toluenediamine) enters the lower part of a dehydrating tower, tower-top gaseous phase of the dehydrating tower enters a tower-top condenser for condensing; continuously collecting liquid-phase process water at the middle lateral line part of the dehydrating tower, wherein the liquid-phase process water enters a wastewater storage tank after being cooled by a wastewater cooler to carry out wastewater biochemical treatment; entering the tower-bottom materials of the dehydrating tower into a tower-bottom re-boiler through a tower-bottom circulating pump; entering the tower-bottom materials of the dehydrating tower into the tower top of a stripping tower; and entering tower-bottom liquid phase of the stripping tower into a follow-up vacuum distillation system. The cleaning and dehydrating method is reliable in process principle, simple in device structure, convenient for assembling operation, good in dehydrating effect, high in dehydrating rate and good in environment-friendliness, and resources and raw materials are saved.
Description
Technical field:
The invention belongs to chemical industry rectifying separation dehydration technique field, relate to a kind of cleaning dewatering that from the reaction mixture of tolylene diamine, distills the novel process, particularly a kind of tolylene diamine that remove water.
Background technology:
Tolylene diamine (TDA) is the main raw material of producing tolylene diisocyanate (TDI), and the latter has the extensive uses such as synthesis of polyurethane flexible foam, elastomerics and coating because of its excellent performance; At present, TDA adopts the dinitrotoluene (DNT) hydrogenation to obtain usually, in the reaction mixture except containing purpose product TDA, the by products such as the water that also containing responds generates and ortho position tolylene diamine, and high-boiling-point impurity tar and lower-boiling impurity Tolylamine and hexamethylene compounds; Reaction mixture usually removes water, ortho position tolylene diamine, tar and obtains the finished product TDA through a series of rectifying, and therefore the water in the TDA mixture being removed is the essential step of TDA rectifying.In the art methods that from reaction mixture water is removed away, wherein a large amount of hydrominings removes with atmospheric distillation, because the atmospheric boiling point of TDA is about 284 ℃, so the normal pressure process only can be with reduced water content to 3000-7000ppm.China Patent No. is that 200810018118.1 document removes with under the condition of negative pressure for a small amount of hydromining, Chinese patent ZL200580002158.1 directly carries out rectification under vacuum to the thick TDA that contains minor amount of water, the former removes minor amount of water by a newly-increased cover vacuum unit specially, the latter is rectifying TDA under vacuum condition, the existence of minor amount of water must increase the load of vacuum apparatus, also can cause in addition the water-content among the product TDA to exceed standard; Chinese patent CN101848885A adopts two-stage vacuum double tower dewatering process, be applicable to separating of TDA product and water, but do not consider to contain in the mixture way that removes of low boiling component situation, although the TDA water content can be reduced to and be lower than 200ppm even lower, but COD content is usually at 3000mg/L even higher in the waste discharge, and this must increase difficulty and the expense of subsequent wastewater treatment.
Summary of the invention:
The object of the invention is to overcome the shortcoming that prior art exists, seek to design a kind of tolylene diamine cleaning dewatering of novel process, TDA in the reaction mixture is dewatered, make at the bottom of the tower among the TDA water-content below 200ppm, to reduce the vacuum-load of follow-up distillation system; Simultaneously dehydration column overhead waste water is processed, to reduce amount of components having low boiling points wherein, reached the requirement of follow-up biochemical treatment.
To achieve these goals, double tower dewatering unit and technique thereof that the present invention adopts atmospheric distillation tower and nitrogen stripping tower to constitute are dewatered to TDA, select first and install the double tower dewatering unit, and in device, dewater, import enters the dehydration tower bottom through TDA to make thick TDA mixture, the top gaseous phase of dehydration tower enters overhead condenser and carries out condensation, the liquid phase that condensation is got off enters return tank, low boiling component is destroyed system with the tail gas that non-condensable gas enters peripheral hardware, install additional on the return tank and be shaped with common gage glass, adopt at ordinary times total reflux to be beneficial to the enrichment of low boiling component, to being enriched to when finding that liquid level is in respect of phase interface, being interrupted the above liquid phase in extraction interface and collecting as byproduct; Side line partial continuous extraction liquid phase process water in the dehydration tower, through enter wastewater storage tank after the gaseous effluent cooler cooling and carry out after the wastewater biochemical in a step process; The materials at bottom of tower of dehydration tower recycle pump at the bottom of tower enters tower bottom reboiler, and a part is returned in the dehydration tower and vaporized, another part as tower at the bottom of discharging enter the cat head of stripping tower; The column bottom temperature of dehydration tower is 190-220 ℃, and preferred 200-210 ℃, water-content is 4000-10000ppm at the bottom of the tower of dehydration tower, preferred 5000-8000ppm; The trim the top of column temperature of dehydration tower is 40-80 ℃, preferred 50-70 ℃; The plate number of the dehydration column plate that is shaped with of being arranged above and below in the dehydration tower is the 8-25 piece, preferred 12-20 piece; Side line extraction position is at top-down 3-8 piece plate place, preferred 4-6 piece plate place; The materials at bottom of tower of dehydration tower enters the cat head of stripping tower, pass into the nitrogen that temperature after heating is higher than 100 ℃ by nitrogen pot at the bottom of the tower of stripping tower, carry out nitrogen stripping in stripping tower, the top gaseous phase of stripping tower enters at the bottom of the tower of dehydration tower, and liquid phase enters follow-up rectification under vacuum system at the bottom of the tower of stripping tower; Nitrogen flow and feed water mass ratio are 2-6.
The agent structure of the double tower dewatering unit that the present invention relates to comprises that recycle pump at the bottom of dehydration tower, overhead condenser, return tank, the tower, tower bottom reboiler, stripping tower, gaseous effluent cooler, tail gas destroy system, light constituent storage tank, wastewater storage tank, nitrogen pot, rectification under vacuum system, TDA import, dehydration column plate and stripping column plate; Place, the bottom of dehydration tower is communicated with recycle pump at the bottom of the tower and tower bottom reboiler by pipeline respectively and consists of circulation loop, is connected to pipeline on the connecting tube of recycle pump and tower bottom reboiler at the bottom of the tower and is communicated with the top of stripping tower; Be communicated with the top of stripping tower by pipeline on the bottom sides of dehydration tower, top, bottom one side of dehydration tower is shaped with the TDA import, enters dehydration tower for thick TDA; Evenly distributing in the inner chamber of dehydration tower is arranged above and below is shaped with respectively 8-25 piece dehydration column plate; Be shaped with pipeline communication formula gaseous effluent cooler and wastewater storage tank on the middle part upper side of dehydration tower; Be communicated with overhead condenser and return tank by pipeline respectively on the top of dehydration tower and the top-side and consist of loop structure, overhead condenser and tail gas destroy system connectivity, and return tank is communicated with the light constituent storage tank; The bottom of the stripping tower of conventional structure and rectification under vacuum system connectivity are communicated with nitrogen pot on the bottom sides.
The present invention compared with prior art adopts the double tower dewatering process, and front tower conventional rectification removes large water gaging, rear tower adopts nitrogen stripping to remove minor amount of water, and the gas phase that will carry minor amount of water returns front tower, after guaranteeing at the bottom of the Tata water-content among the TDA lower, reduce the load of follow-up vacuum; The existence of nitrogen more is conducive to removing of front column overhead low boiling component, and having guaranteed has lower light constituent impurity in the side line waste water in the tower, has reduced COD content in the waste water; Because from side line extraction process water, allow low-boiling-point substance in cat head enrichment and extraction, realized that water and low-boiling-point substance continue to separate with theoretical stage between cat head by side line, guaranteed lower COD in the side line extraction process water, reclaimed low-boiling point material; Its technological principle is reliable, and device structure is simple, and assembly operation is convenient, and dehydrating effect is good, and dehydration rate is high, saving resource and raw material, environmental friendliness.
Description of drawings:
Fig. 1 is double tower dewatering unit structural principle synoptic diagram of the present invention.
Embodiment:
Also be described further by reference to the accompanying drawings below by embodiment.
Double tower dewatering unit and technique thereof that present embodiment adopts atmospheric distillation tower and nitrogen stripping tower to constitute are dewatered to TDA, select first and install the double tower dewatering unit, and in device, dewater, make thick TDA mixture enter dehydration tower 1 bottom through TDA import 13, the top gaseous phase of dehydration tower 1 enters overhead condenser 2 and carries out condensation, the liquid phase that condensation is got off enters return tank 3, low boiling component is destroyed system 8 with the tail gas that non-condensable gas enters peripheral hardware, install additional on the return tank 3 and be shaped with common gage glass, adopt at ordinary times total reflux to be beneficial to the enrichment of low boiling component, to being enriched to when finding that liquid level is in respect of phase interface, be interrupted the above liquid phase in extraction interface and also in light constituent storage tank 9, collect as byproduct; Side line partial continuous extraction liquid phase process water in the dehydration tower 1, through enter wastewater storage tank 10 after gaseous effluent cooler 7 cooling and carry out after the wastewater biochemical in a step process; The materials at bottom of tower of dehydration tower 1 recycle pump 4 at the bottom of tower enters tower bottom reboiler 5, and a part is returned in the dehydration tower 1 and vaporized, another part as tower at the bottom of discharging enter the cat head of stripping tower 6; The column bottom temperature of dehydration tower 1 is 190-220 ℃, and preferred 200-210 ℃, water-content is 4000-10000ppm at the bottom of the tower of dehydration tower 1, preferred 5000-8000ppm; The trim the top of column temperature of dehydration tower 1 is 40-80 ℃, preferred 50-70 ℃; The plate number of the dehydration column plate 14 that is shaped with of being arranged above and below in the dehydration tower 1 is the 8-25 piece, preferred 12-20 piece; Side line extraction position is at top-down 3-8 piece plate place, preferred 4-6 piece plate place; The materials at bottom of tower of dehydration tower 1 enters the cat head of stripping tower 6, pass into the nitrogen that temperature after heating is higher than 100 ℃ by nitrogen pot 11 at the bottom of the tower of stripping tower 6, in stripping tower 6, carry out nitrogen stripping, the top gaseous phase of stripping tower 6 enters at the bottom of the tower of dehydration tower 1, and liquid phase enters follow-up rectification under vacuum system 12 at the bottom of the tower of stripping tower 6; Nitrogen flow and feed water mass ratio are 2-6.
The agent structure of the double tower dewatering unit that present embodiment relates to comprises that recycle pump 4 at the bottom of dehydration tower 1, overhead condenser 2, return tank 3, the tower, tower bottom reboiler 5, stripping tower 6, gaseous effluent cooler 7, tail gas destroy system 8, light constituent storage tank 9, wastewater storage tank 10, nitrogen pot 11, rectification under vacuum system 12, TDA import 13, dehydration column plate 14 and stripping column plate 15; Place, the bottom of dehydration tower 1 is communicated with recycle pump at the bottom of the tower 4 and tower bottom reboiler 5 by pipeline respectively and consists of circulation loop, is connected to pipeline on the connecting tube of recycle pump 4 and tower bottom reboiler 5 at the bottom of the tower and is communicated with the top of stripping tower 6; Be communicated with by the top of pipeline with stripping tower 6 on the bottom sides of dehydration tower 1, top, bottom one side of dehydration tower 1 is shaped with TDA import 13, enters dehydration tower 1 for thick TDA; Evenly distributing in the inner chamber of dehydration tower 1 is arranged above and below is shaped with respectively 8-25 piece dehydration column plate 14; Be shaped with pipeline communication formula gaseous effluent cooler 7 and wastewater storage tank 10 on the middle part upper side of dehydration tower 1; Be communicated with overhead condenser 2 and return tank 3 by pipeline respectively on the top of dehydration tower 1 and the top-side and consist of loop structure, overhead condenser 2 destroys system 8 with tail gas and is communicated with, and return tank 3 is communicated with light constituent storage tank 9; The bottom of the stripping tower of conventional structure is communicated with rectification under vacuum system 12, is communicated with nitrogen pot 11 on the bottom sides.
Embodiment;
It is 1000kg/h that present embodiment is selected thick TDA mixture flow rate, and the overhead condensation temperature of dehydration tower 1 is 50 ℃, and column bottom temperature is 190 ℃, and the flow that passes into 150 ℃ in the stripping tower 6 is the nitrogen of 8kg/h; The diameter of dehydration tower 1 is 400mm, the quantity of dehydration column plate 14 be the position of 20, TDA import 13 at the 17th column plate place, side line extraction position is the 4th; The diameter of stripping tower 6 is 250mm, and the quantity of stripping column plate 15 is 10; After the operation of double tower dewatering unit continous-stable, the outlet water-content of dehydration tower 1 is between 4000-4500ppm, water-content is stabilized in 110-180ppm among the TDA behind stripping, the COD value of side line extracted waste water is at 600-900mg/L, after the operate continuously 24 hours, return tank extraction low-boiling-point organic compound 10.5kg; The described side line extraction of present embodiment position is the position of water collection point.
Claims (2)
1. the cleaning dewatering of a tolylene diamine, it is characterized in that the double tower dewatering unit and the technique thereof that adopt atmospheric distillation tower and nitrogen stripping tower to constitute dewaters to TDA, select first and install the double tower dewatering unit, and in device, dewater, import enters the dehydration tower bottom through TDA to make thick TDA mixture, the top gaseous phase of dehydration tower enters overhead condenser and carries out condensation, the liquid phase that condensation is got off enters return tank, low boiling component is destroyed system with the tail gas that non-condensable gas enters peripheral hardware, install additional on the return tank and be shaped with common gage glass, adopt at ordinary times total reflux to be beneficial to the enrichment of low boiling component, to being enriched to when finding that liquid level is in respect of phase interface, being interrupted the above liquid phase in extraction interface and collecting as byproduct; Side line partial continuous extraction liquid phase process water in the dehydration tower, through enter wastewater storage tank after the gaseous effluent cooler cooling and carry out after the wastewater biochemical in a step process; The materials at bottom of tower of dehydration tower recycle pump at the bottom of tower enters tower bottom reboiler, and a part is returned in the dehydration tower and vaporized, another part as tower at the bottom of discharging enter the cat head of stripping tower; The column bottom temperature of dehydration tower is 190-220 ℃, and water-content is 4000-10000ppm at the bottom of the tower of dehydration tower; The trim the top of column temperature of dehydration tower is 40-80 ℃; The plate number of the dehydration column plate that is shaped with of being arranged above and below in the dehydration tower is the 8-25 piece; Side line extraction position is at top-down 3-8 piece plate place; The materials at bottom of tower of dehydration tower enters the cat head of stripping tower, pass into the nitrogen that temperature after heating is higher than 100 ℃ by nitrogen pot at the bottom of the tower of stripping tower, carry out nitrogen stripping in stripping tower, the top gaseous phase of stripping tower enters at the bottom of the tower of dehydration tower, and liquid phase enters follow-up rectification under vacuum system at the bottom of the tower of stripping tower; Nitrogen flow and feed water mass ratio are 2-6.
2. the cleaning dewatering of tolylene diamine according to claim 1, the agent structure that it is characterized in that the double tower dewatering unit that relates to comprise that recycle pump at the bottom of dehydration tower, overhead condenser, return tank, the tower, tower bottom reboiler, stripping tower, gaseous effluent cooler, tail gas destroy system, light constituent storage tank, wastewater storage tank, nitrogen pot, rectification under vacuum system, TDA import, dehydration column plate and stripping column plate; Place, the bottom of dehydration tower is communicated with recycle pump at the bottom of the tower and tower bottom reboiler by pipeline respectively and consists of circulation loop, is connected to pipeline on the connecting tube of recycle pump and tower bottom reboiler at the bottom of the tower and is communicated with the top of stripping tower; Be communicated with the top of stripping tower by pipeline on the bottom sides of dehydration tower, top, bottom one side of dehydration tower is shaped with the TDA import, enters dehydration tower for thick TDA; Evenly distributing in the inner chamber of dehydration tower is arranged above and below is shaped with respectively 8-25 piece dehydration column plate; Be shaped with pipeline communication formula gaseous effluent cooler and wastewater storage tank on the middle part upper side of dehydration tower; Be communicated with overhead condenser and return tank by pipeline respectively on the top of dehydration tower and the top-side and consist of loop structure, overhead condenser and tail gas destroy system connectivity, and return tank is communicated with the light constituent storage tank; The bottom of the stripping tower of conventional structure and rectification under vacuum system connectivity are communicated with nitrogen pot on the bottom sides.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100153905A CN103012161A (en) | 2013-01-16 | 2013-01-16 | Cleaning and dehydrating method of toluenediamine |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013100153905A CN103012161A (en) | 2013-01-16 | 2013-01-16 | Cleaning and dehydrating method of toluenediamine |
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| CN103012161A true CN103012161A (en) | 2013-04-03 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439872A (en) * | 2015-12-28 | 2016-03-30 | 甘肃银光聚银化工有限公司 | Method for removing moisture in toluenediamine (TDA) |
| CN110124346A (en) * | 2019-05-18 | 2019-08-16 | 济宁市金泰利华化工科技有限公司 | A kind of reactive distillation column with quick temperature-reducing function |
| CN110452125A (en) * | 2019-09-03 | 2019-11-15 | 天津科技大学 | A kind of toluenediamine dewatering and device based on mechanical steam recompression MVR |
| CN113461527A (en) * | 2020-03-30 | 2021-10-01 | 中石油吉林化工工程有限公司 | Method for dehydrating side-stream withdrawn material flow of methyl methacrylate device primary distillation tower |
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|---|---|---|---|---|
| US4720326A (en) * | 1986-03-08 | 1988-01-19 | Bayer Aktiengesellschaft | Process for working-up aqueous amine solutions |
| US20050263385A1 (en) * | 2004-06-01 | 2005-12-01 | Bayer Materialscience Ag | Process for the distillative separation of aqueous amine solutions |
| WO2009069584A1 (en) * | 2007-11-27 | 2009-06-04 | Mitsui Chemicals Polyurethanes, Inc. | Method of dehydrating tolylenediamine and dehydrator |
| CN101712621A (en) * | 2009-09-02 | 2010-05-26 | 甘肃银达化工有限公司 | Method for continuously preparing toluenediamine |
-
2013
- 2013-01-16 CN CN2013100153905A patent/CN103012161A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4720326A (en) * | 1986-03-08 | 1988-01-19 | Bayer Aktiengesellschaft | Process for working-up aqueous amine solutions |
| US20050263385A1 (en) * | 2004-06-01 | 2005-12-01 | Bayer Materialscience Ag | Process for the distillative separation of aqueous amine solutions |
| WO2009069584A1 (en) * | 2007-11-27 | 2009-06-04 | Mitsui Chemicals Polyurethanes, Inc. | Method of dehydrating tolylenediamine and dehydrator |
| CN101712621A (en) * | 2009-09-02 | 2010-05-26 | 甘肃银达化工有限公司 | Method for continuously preparing toluenediamine |
Non-Patent Citations (1)
| Title |
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| 李玉刚等: "甲苯二胺脱水过程的节能分析", 《节能技术》, vol. 22, no. 1, 31 January 2004 (2004-01-31), pages 13 - 14 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105439872A (en) * | 2015-12-28 | 2016-03-30 | 甘肃银光聚银化工有限公司 | Method for removing moisture in toluenediamine (TDA) |
| CN110124346A (en) * | 2019-05-18 | 2019-08-16 | 济宁市金泰利华化工科技有限公司 | A kind of reactive distillation column with quick temperature-reducing function |
| CN110452125A (en) * | 2019-09-03 | 2019-11-15 | 天津科技大学 | A kind of toluenediamine dewatering and device based on mechanical steam recompression MVR |
| CN113461527A (en) * | 2020-03-30 | 2021-10-01 | 中石油吉林化工工程有限公司 | Method for dehydrating side-stream withdrawn material flow of methyl methacrylate device primary distillation tower |
| CN113461527B (en) * | 2020-03-30 | 2023-10-17 | 中石油吉林化工工程有限公司 | Method for dehydrating side-stream of primary distillation tower of methyl methacrylate device |
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Application publication date: 20130403 |