CN104478752A - DMAC refining system for spandex spinning production process - Google Patents
DMAC refining system for spandex spinning production process Download PDFInfo
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- CN104478752A CN104478752A CN201410682735.7A CN201410682735A CN104478752A CN 104478752 A CN104478752 A CN 104478752A CN 201410682735 A CN201410682735 A CN 201410682735A CN 104478752 A CN104478752 A CN 104478752A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention relates to a DMAC refining system for a spandex spinning production process. The DMAC refining system comprises a dehydrating system and a deacidifying system which are connected in series, wherein the dehydrating system comprises a dehydrating tower, a dehydrating tower reboiler, a dehydrating tower condenser, a dehydrating tower reflux tank, a dehydrating tower reflux pump and a dehydrating tower discharging pump; the deacidifying system comprises a deacidifying tower, a deacidifying tower reboiler, a deacidifying tower condenser, a deacidifying tower reflux tank, a deacidifying tower reflux pump and a deacidifying tower discharging pump; a middle tower plate is arranged between a tower kettle and a kettle top of the dehydrating tower; a liquid collected in the middle tower plate returns to the inside of the dehydrating tower after being reheated to be vaporized by a dehydrating tower intermediate reboiler; a branch pipeline located at the tower top of the deacidifying tower is connected with a gaseous pipe opening in the upper side of the deacidifying tower intermediate reboiler; and part of gaseous DMAC at the tower top of the deacidifying tower is used as a heating source of the dehydrating tower intermediate reboiler. By adopting the arrangement, the low-pressure steam consumption of the dehydrating tower reboiler is greatly reduced, the energy consumption is reduced, energy is saved, the environment is protected, and the production cost of an enterprise is reduced.
Description
Technical field
The present invention relates to DMAC purification and recover system in a kind of spandex fiber process.
Background technology
In the dry-spinning production process of spandex, need to use solvent DMAC(N, N-N,N-DIMETHYLACETAMIDE).Solvent DMAC adds in the course of the polymerization process, for the dispersion of polymkeric substance, is separated in spinning process.Solvent DMAC after separated and collected needs, through treating process (rectification under vacuum), after the Impurity removals such as the water in solvent DMAC, amine, acetic acid, to get back in polymerization process and recycle.
The purification and recover system of existing solvent DMAC is made up of two Tower Systems, and first tower is dehydration tower, mainly by Light ends removings such as the water in solvent DMAC and amines.Second tower is extracting tower, mainly by heavy component removings such as the acetic acid in solvent DMAC and acetic acid compounds, and the solvent DMAC that on finally in the second tower, side take-off is qualified.Concrete technical process is described below:
As shown in Figure 1, solvent DMAC containing impurity is admitted to the middle part of dehydration tower 11, dehydration tower 11 tower top working pressure is 13kPa (A), tower top temperature 50 DEG C, bottom temperature 109 DEG C, tower reactor adopts reboiler 12, it is made to vaporize by low-pressure steam as heat source tower bottoms, tower top adopts condenser 13, with recirculated cooling water as low-temperature receiver, overhead gas is cooled to liquid (major ingredient is water and amine) and enters return tank 14, the phlegma of collection pressurizes in rear portion reflux tower through reflux pump 15, a part of discharge system.
With transferpump 16, the solvent DMAC of dehydration tower tower reactor through removing water is sent into the middle part of extracting tower 21, extracting tower tower top working pressure is 6kPa (A), tower top temperature 83 DEG C, bottom temperature 99 DEG C, tower reactor adopts reboiler 22, it is made to vaporize by low-pressure steam as heat source tower bottoms, tower top adopts condenser 23, with recirculated cooling water as low-temperature receiver, overhead gas is cooled to liquid (major ingredient is solvent DMAC) and enters return tank 24, the phlegma collected pressurizes in rear portion reflux tower through reflux pump 25, a part of discharge system.Solvent DMAC finished product from tower top side take-off, for polymerization process.
Be provided with dehydration reboiler and depickling reboiler in above-mentioned solvent DMAC purification and recover system, and all adopt low-pressure steam as thermal source, heat energy consumption is larger.Special in dehydration tower, tower reactor and the tower top temperature difference are comparatively large, and in lapse of temperature gradient from tower reactor to tower top, gas is along with the continuous change of composition in uphill process, and boiling point also can reduce, and under partial gas phase can be condensed into liquid stream, increase system energy consumption.
Summary of the invention
Technical problem to be solved by this invention provides a kind of spandex fiber production process DMAC refining system for above-mentioned prior art, under the prerequisite ensureing DMAC refining quality and output, can save in dehydration tower and reheat low-pressure steam consumption, reduce enterprise's production cost.
The present invention's adopted technical scheme that solves the problem is: a kind of spandex fiber production process DMAC refining system, comprise the dewatering system and deacidification system that are connected in series, wherein dewatering system comprises: dehydration tower, dehydration column reboiler, dehydration tower condenser, dehydration tower return tank, dehydration tower reflux pump and dehydrating tower kettle discharging pump, extracting tower system comprises: extracting tower, extracting tower reboiler, extracting tower condenser, extracting tower return tank, extracting tower reflux pump and depickling tower reactor discharging pump, middle column plate is provided with between the tower reactor of described dehydration tower and tower top, described middle column plate bottom liquid phases draws the bottom mouth of pipe of the tube side of the external dehydration tower intermediate reboiler of the mouth of pipe, the upper orifice of dehydration tower intermediate reboiler tube side connects with the gas phase mouth of pipe above middle column plate, extracting tower tower top pipeline is connected with the upside gas phase mouth of pipe of dehydration tower intermediate reboiler, on the downside of dehydration tower intermediate reboiler shell side, the liquid phase mouth of pipe receives extracting tower return tank, solvent DMAC containing impurity sends in the middle part of dehydration tower, dehydration column reboiler is by the liquid heat vaporization in dehydration tower tower reactor, dehydration tower intermediate reboiler sends back in dehydration tower after reheating vaporization to the liquid being collected in middle column plate, the gas rising to dehydration column overhead is cooled to liquid by dehydration tower condenser and sends into dehydration tower return tank, liquid pressing rear portion in dehydration tower return tank is back to a part of discharge system in dehydration tower by dehydration tower reflux pump, solvent DMAC through removing water in dehydration tower tower reactor sends in the middle part of extracting tower by dehydrating tower kettle discharging pump, extracting tower reboiler is by the liquid heat vaporization in extracting tower tower reactor, the gas part rising to extracting tower tower top is cooled to liquid by extracting tower condenser and sends into extracting tower return tank, part access dehydration tower intermediate reboiler is as heat source, again extracting tower return tank is sent into again after being cooled to liquid, liquid pressing rear portion in extracting tower return tank is back in extracting tower and arranges collection outside a part by extracting tower reflux pump, obtain solvent DMAC finished product.
Preferred technique is, the liquid heat in dehydration tower tower reactor is vaporized into the gas of 109 ± 1 DEG C by dehydration column reboiler, and after separating filler in dehydration tower is separated, the temperature of dehydration column overhead gas is 50 ± 1 DEG C, and dehydration column overhead working pressure is 13kPa; Liquid heat in extracting tower tower reactor is vaporized into the gas of 99 ± 1 DEG C by extracting tower reboiler, and after separating filler in extracting tower is separated, the temperature of extracting tower overhead gas is 83 ± 1 DEG C, and extracting tower tower top working pressure is 6kPa.
Preferred setting is, in dehydration tower, tower reactor is lapse of temperature gradient to tower top, described middle column plate is arranged on 70 DEG C of positions, enters in dehydration tower after the dehydrated tower intermediate reboiler of 70 DEG C of liquid be collected on this middle column plate reheats the gas being vaporized into 70 DEG C again.
Preferably, dehydration column reboiler and/or extracting tower reboiler are using low-pressure steam as heat source.
The present invention sets up one block of middle column plate between the tower reactor and tower top of dehydration tower, for collecting the liquid flowed down in tower, and reheat by external dehydration tower intermediate reboiler the gas being vaporized into uniform temp and send in dehydration tower, dehydration tower intermediate reboiler adopts the gas (gas phase DMAC) of extracting tower tower top as heat source, make full use of the latent heat of liquefaction of the gas phase DMAC at extracting tower top, dehydration column reboiler low-pressure steam consumption can be reduced, be conducive to saving additional thermal energy consumption, environmental protection and energy saving, reduce production cost.
Adopt the gas phase DMAC of 83 DEG C to carry out heat vaporized as thermal source to the liquid of 70 DEG C in dehydration tower in the present invention, can guarantee that vaporization is reliable, improve heat exchange efficiency.
Compared with prior art, the invention has the advantages that: by setting up middle column plate between the tower reactor and tower top of dehydration tower, send back in tower after the liquid being collected in this middle column plate reheats vaporization by dehydration tower intermediate reboiler, and adopt the gas phase DMAC of extracting tower tower top as the heat source of dehydration tower intermediate reboiler, save the additional thermal energy consumption of dehydration column reboiler, energy-conserving and environment-protective, reduce production cost.
Accompanying drawing explanation
Fig. 1 is existing spandex fiber production process DMAC refining system schematic flow sheet;
Fig. 2 is solvent DMAC refining system schematic flow sheet in the embodiment of the present invention.
Embodiment
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in Figure 2, spandex fiber production process DMAC refining system in the present embodiment, comprise: the dewatering system be connected in series and deacidification system, wherein dewatering system comprises: dehydration tower 11, dehydration column reboiler 12, dehydration tower condenser 13, dehydration tower return tank 14, dehydration tower reflux pump 15 and dehydrating tower kettle discharging pump 16, extracting tower system comprises: extracting tower 21, extracting tower reboiler 22, extracting tower condenser 23, extracting tower return tank 24, extracting tower reflux pump 25 and depickling tower reactor discharging pump 26, dehydration tower 11 tower top working pressure is 13kPa (A), tower top temperature 50 DEG C, bottom temperature 109 DEG C, extracting tower 21 tower top working pressure is 6kPa (A), tower top temperature 83 DEG C, bottom temperature 99 DEG C, it is a lapse of temperature gradient from dehydration tower 11 tower reactor to tower top, between the tower reactor and tower top of dehydration tower 11,70 DEG C of places arrange middle column plate 18, middle column plate 18 bottom liquid phases draws the bottom mouth of pipe of the tube side of the external dehydration tower intermediate reboiler 17 of the mouth of pipe, the upper orifice of dehydration tower intermediate reboiler 17 tube side connects with the gas phase mouth of pipe above middle column plate 18, extracting tower 21 tower top pipeline is connected with the upside gas phase mouth of pipe of dehydration tower intermediate reboiler 17, on the downside of dehydration tower intermediate reboiler 17 shell side, the liquid phase mouth of pipe receives extracting tower return tank 24, the liquid being collected in middle column plate 18 is drawn access dehydration tower intermediate reboiler 17, column plate 18 top in the middle of accessing again after the gas of heat vaporized one-tenth 70 DEG C.
The work flow of above-mentioned DMAC refining system is, solvent DMAC containing impurity sends in the middle part of dehydration tower 11, dehydration column reboiler 12 is that the liquid heat in dehydration tower 11 tower reactor is vaporized into rising 109 DEG C of gases by thermal source with low-pressure steam, the 70 DEG C of liquid being collected in middle column plate 18 place are reheated the gas being vaporized into 70 DEG C by dehydration tower intermediate reboiler 17, access in dehydration tower 11 again, after separating filler in dehydration tower 11 is separated, the gas (being mainly water and the amine of 50 DEG C) rising to dehydration tower 11 tower top is cooled to liquid by dehydration tower condenser 13 and sends into dehydration tower return tank 14, liquid pressing rear portion in dehydration tower return tank 14 is back to a part of discharge system in dehydration tower 11 by dehydration tower reflux pump 15, solvent DMAC through removing water in dehydration tower 11 tower reactor sends in the middle part of extracting tower 21 by dehydrating tower kettle discharging pump 16, liquid heat in extracting tower 21 tower reactor is vaporized into the gas of 99 DEG C by extracting tower reboiler 22, after separating filler in extracting tower 21 is separated, rise to the gas (being mainly the gas phase DMAC of 83 DEG C) of extracting tower 21 tower top, a part is cooled to liquid by extracting tower condenser 23 and sends into extracting tower return tank 24, the hot side of part access dehydration tower intermediate reboiler 17 is as heat source, again extracting tower return tank 24 is sent into again after being cooled to the liquid of 83 DEG C, liquid pressing rear portion in extracting tower return tank 24 is back in extracting tower 21 and arranges collection outside a part by extracting tower reflux pump 25, obtain solvent DMAC finished product, residual liquid in extracting tower 21 tower reactor discharges system by depickling tower reactor discharging pump 26.
In the present embodiment, dehydration column reboiler 12 and extracting tower reboiler 22 are all using low-pressure steam as heat source.Dehydration tower condenser 13 and extracting tower condenser 23 are all using 32 DEG C of water coolants as cooling medium.
Economic measuring and calculating:
The polyurethane fiber dry spinning factory producing 20000 tons per year needs supporting DMAC refining plant to be 5 tons/hour, calculates energy-saving effect with 5 tons/little timer.
The temperature of extracting tower 21 top gaseous phase DMAC is 83 DEG C, flow 8540kg/h, the latent heat of vaporization be 526.23kJ/kg, gas phase DMAC be cooled to synthermal under liquid phase DMAC, the heat that can discharge is 8540kg/h × 526.23kJ/kg=4.494 × 106 kJ/h.
An extracting tower 21 top gaseous phase part as the thermal source of dehydration tower intermediate reboiler 17, can be reduced the low-pressure steam consumption of dehydration column reboiler 12 by the present invention.Calculate according to technical process, 60% of extracting tower 21 top gaseous phase DAMC flow can be supplied to dehydration tower intermediate reboiler 17 as heating medium, the low-pressure steam vaporization heat of 0.3MPa (G) is 2133.4kJ/kg, so the amount that the caloric value being supplied to dehydration tower intermediate reboiler 17 is equivalent to low-pressure steam is 4.494 × 10
5kJ/h ÷ 2133.4kJ/kg × 60%=1264kg/h.Former Technology dehydration column reboiler 12 needs the low-pressure steam amount consumed to be 2165kg/h, and after adopting the art of this patent, the low-pressure steam amount that can save is 1.264t/h, and steam unit price is by 180 yuan/ton, and the energy expenditure of saving is:
1.264 t/h × 180 yuan/ton × 24h × 350 day=1,910,000 yuan/year.
In technique scheme, middle column plate 18 is set between dehydration tower 11 tower reactor and tower top, dehydration tower intermediate reboiler 17 is sent back in dehydration tower 11 after reheating vaporization to the liquid be collected on this column plate, and using the heat source of extracting tower 21 tower top part gas phase as dehydration tower intermediate reboiler 17, the low-pressure steam consumption of dehydration column reboiler 12 can be reduced, environmental protection and energy saving, reduce enterprise's production cost.
Claims (4)
1. a spandex fiber production process DMAC refining system, comprise the dewatering system and deacidification system that are connected in series, wherein dewatering system comprises: dehydration tower (11), dehydration column reboiler (12), dehydration tower condenser (13), dehydration tower return tank (14), dehydration tower reflux pump (15) and dehydrating tower kettle discharging pump (16), extracting tower system comprises: extracting tower (21), extracting tower reboiler (22), extracting tower condenser (23), extracting tower return tank (24), extracting tower reflux pump (25) and depickling tower reactor discharging pump (26), it is characterized in that: between the tower reactor of described dehydration tower and tower top, be provided with middle column plate (18), described middle column plate (18) bottom liquid phases draws the bottom mouth of pipe of the tube side of the external dehydration tower intermediate reboiler (17) of the mouth of pipe, the upper orifice of dehydration tower intermediate reboiler (17) tube side connects with middle column plate (18) the top gas phase mouth of pipe, extracting tower (21) tower top pipeline is connected with the upside gas phase mouth of pipe of dehydration tower intermediate reboiler (17), on the downside of dehydration tower intermediate reboiler (17) shell side, the liquid phase mouth of pipe receives extracting tower return tank (24), solvent DMAC containing impurity sends into from dehydration tower (11) middle part, dehydration column reboiler (12) is by the liquid heat vaporization in dehydration tower (11) tower reactor, dehydration tower intermediate reboiler (17) sends back in dehydration tower after reheating vaporization to the liquid being collected in middle column plate (18), the gas rising to dehydration tower (11) tower top is cooled to liquid by dehydration tower condenser (13) and sends into dehydration tower return tank (14), liquid pressing rear portion in dehydration tower return tank (14) is back to a part of discharge system in dehydration tower (11) by dehydration tower reflux pump (15), solvent DMAC through removing water in dehydration tower (11) tower reactor sends into extracting tower (21) middle part by dehydrating tower kettle discharging pump (16), extracting tower reboiler (22) is by the liquid heat vaporization in extracting tower (21) tower reactor, the gas part rising to extracting tower (21) tower top is cooled to liquid by extracting tower condenser (23) and sends into extracting tower return tank (24), part access dehydration tower intermediate reboiler (17) is as heat source, again extracting tower return tank (24) is sent into after being cooled to liquid again, liquid pressing rear portion in extracting tower return tank (24) is back in extracting tower (21) and arranges collection outside a part by extracting tower reflux pump (25), obtain solvent DMAC finished product.
2. spandex fiber production process DMAC refining system according to claim 1, it is characterized in that: the liquid heat in dehydration tower (11) tower reactor is vaporized into the gas of 109 ± 1 DEG C by dehydration column reboiler (12), after separating filler in dehydration tower (11) is separated, the temperature of dehydration tower (11) overhead gas is 50 ± 1 DEG C, and dehydration tower (11) tower top working pressure is 13kPa; Liquid heat in extracting tower (21) tower reactor is vaporized into the gas of 99 ± 1 DEG C by extracting tower reboiler (22), after separating filler in extracting tower (21) is separated, the temperature of extracting tower (21) overhead gas is 83 ± 1 DEG C, and extracting tower (21) tower top working pressure is 6kPa.
3. spandex fiber production process DMAC refining system according to claim 2, it is characterized in that: dehydration tower (11) interior tower reactor is lapse of temperature gradient to tower top, described middle column plate (18) is arranged on 70 DEG C of positions, enters in dehydration tower (11) after the dehydrated tower intermediate reboiler (17) of 70 DEG C of liquid be collected on this middle column plate (18) reheats the gas being vaporized into 70 DEG C again.
4. spandex fiber production process DMAC refining system according to claim 1, is characterized in that: dehydration column reboiler (12) and/or extracting tower reboiler (22) are using low-pressure steam as heat source.
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| CN201410682735.7A CN104478752B (en) | 2014-11-25 | 2014-11-25 | A kind of spandex fiber production process DMAC refining system |
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| CN201410682735.7A CN104478752B (en) | 2014-11-25 | 2014-11-25 | A kind of spandex fiber production process DMAC refining system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111233690A (en) * | 2020-03-27 | 2020-06-05 | 天津精分科技发展有限公司 | DMAc thermal coupling refining and recycling system and method |
| CN114516816A (en) * | 2022-02-24 | 2022-05-20 | 深圳瑞华泰薄膜科技股份有限公司 | Method and device for recovering DMAC (dimethyl acetamide) and isoquinoline from solution |
| CN114917608A (en) * | 2022-06-30 | 2022-08-19 | 中国天辰工程有限公司 | Low-energy-consumption propylene oligomer separation system and separation method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201161987Y (en) * | 2008-02-01 | 2008-12-10 | 江阴中绿化纤工艺技术有限公司 | Dimethylacetylamide solvent recovery device |
| CN203916121U (en) * | 2014-06-20 | 2014-11-05 | 浙江开普特氨纶有限公司 | DMAC reclaims physical property index optimization system |
-
2014
- 2014-11-25 CN CN201410682735.7A patent/CN104478752B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201161987Y (en) * | 2008-02-01 | 2008-12-10 | 江阴中绿化纤工艺技术有限公司 | Dimethylacetylamide solvent recovery device |
| CN203916121U (en) * | 2014-06-20 | 2014-11-05 | 浙江开普特氨纶有限公司 | DMAC reclaims physical property index optimization system |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111233690A (en) * | 2020-03-27 | 2020-06-05 | 天津精分科技发展有限公司 | DMAc thermal coupling refining and recycling system and method |
| CN114516816A (en) * | 2022-02-24 | 2022-05-20 | 深圳瑞华泰薄膜科技股份有限公司 | Method and device for recovering DMAC (dimethyl acetamide) and isoquinoline from solution |
| CN114516816B (en) * | 2022-02-24 | 2023-12-01 | 深圳瑞华泰薄膜科技股份有限公司 | Method and device for recycling DMAC and isoquinoline from solution |
| CN114917608A (en) * | 2022-06-30 | 2022-08-19 | 中国天辰工程有限公司 | Low-energy-consumption propylene oligomer separation system and separation method |
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| CN104478752B (en) | 2016-03-09 |
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