CN103007565A - Method and device for triple-effect separation of methylbenzene and polyethylene - Google Patents
Method and device for triple-effect separation of methylbenzene and polyethylene Download PDFInfo
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- CN103007565A CN103007565A CN201310010361XA CN201310010361A CN103007565A CN 103007565 A CN103007565 A CN 103007565A CN 201310010361X A CN201310010361X A CN 201310010361XA CN 201310010361 A CN201310010361 A CN 201310010361A CN 103007565 A CN103007565 A CN 103007565A
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Abstract
The invention relates to a method for the triple-effect separation of methylbenzene and polyethylene and a device used for the method. The method comprises the following step: separating a polyethylene-containing methylbenzene waste liquid sequentially through primary reduced-pressure distillation, primary normal-pressure distillation and primary positive-pressure distillation, wherein methylbenzene steam serves as a heat source which is used repeatedly. The device comprises a waste liquid preheater, a negative-pressure evaporator, a methylbenzene condenser, a decanter, a tail gas condenser, a normal-pressure evaporator, a positive-pressure evaporator, a positive-pressure methylbenzene intermediate tank, a methylbenzene residue storage tank and a residue evaporation tank. The device provided by the invention is an energy-saving and emission-reducing device. According to the method provided by the invention, based on the distillation range difference of one liquid under different pressures, the material is concentrated by using secondary steam, thereby greatly saving the production cost.
Description
Technical field
The present invention relates to a kind of triple effect separation of methylbenzene and poly method, and the used device of the method.
Technical background
Microfiber synthetic leather manufacturing works, in the manufacture process of nonwoven be with toluene as solvent, the polyethylene in the dissolving wash-out base cloth.As eluting solvent, production line production capacity is directly proportional with the toluene consumption within the specific limits, is synchronous operated as enterprise's production line with the retracting device of toluene and toluene.
Toluene waste liquid in the microfiber synthetic leather production process derives to be extracted groove out and finds out groove in the production line, the polyethylene concentration in the waste liquid is about about 2%.In the production process with water seal as the seal approach of advancing cloth, so also with part water, because toluene is insoluble in water, water separates with toluene in the process of depositing in waste tank in the waste liquid of toluene, water is discharged in the treatment tank, therefore moisture is less in the recovery system.
Be the single-action treatment technology of Japan in super fine toluene recovery technique in the past, its energy consumption is higher, and makes still-process easily produce bumping because of containing moisture, impact recovery toluene quality.Along with the production-scale expansion of enterprise, the consumption of toluene increases thereupon, so the yield of toluene restricting the production capacity of microfiber synthetic leather, and the recovery technique of economic benefits and social benefits also no longer satisfies the demand that enlarges of producing.
Summary of the invention
The purpose of this invention is to provide a kind of energy consumption low, shorten the residue treatment time and avoid triple effect separation of methylbenzene and the poly method of boiling explosion phenomenon.
Another object of the present invention provides the employed device of the method.
The technical solution used in the present invention:
A kind of triple effect separation of methylbenzene and poly method, it is to separate through one-level decompression distillation, one-level air-distillation, the distillation of one-level malleation successively containing poly toluene waste liquid, toluene vapor reuses as thermal source; Specifically comprise the steps: to contain poly toluene waste liquid and at first enter vacuum evaporator carry out the decompression distillation concentrate after preheating, toluene vapor separates through the laggard decanter of condenser condenses; Enter again the atmospheric evaporation device through the toluene waste liquid of decompression distillation and carry out the air-distillation concentrate, atmospheric evaporation device top toluene vapor separates through the laggard decanter of heat exchange condensation, toluene waste liquid after the normal pressure distillation advances the malleation evaporimeter and continues the distillation concentrate, the top toluene vapor after the heat exchange of normal pressure evaporimeter flash distillation to vacuum evaporator, the laggard decanter of condensation separates, and malleation evaporimeter waste liquid advances the residue evaporation boiler and continues the concentrate evaporation.
In the described malleation evaporimeter with low pressure steam as a thermal source, the atmospheric evaporation device is take the toluene vapor of malleation evaporimeter as thermal source, the toluene vapor that vacuum evaporator steams in the atmospheric evaporation device is as thermal source.
Toluene vapor flash distillation behind pans in described malleation evaporimeter top is carried out Btu utilization again to vacuum evaporator.
Described residue evaporation boiler adopts the negative pressure intermittent operation.
A kind of device of implementing said method comprises waste liquid preheater, vacuum evaporator, toluene condenser, decanter, tail gas condenser, atmospheric evaporation device, malleation evaporimeter, malleation toluene pans, toluene residue storage tank and residue evaporation boiler;
Described waste liquid preheater is connected with the top of vacuum evaporator, and the entrance of toluene condenser connects the toluene vapor outlet on vacuum evaporator top, and the outlet of toluene condenser connects decanter, and the gas vent of decanter connects tail gas condenser; The bottom of vacuum evaporator is connected through the bottom of pump with the atmospheric evaporation device; The toluene vapor outlet on atmospheric evaporation device top connects the top of vacuum evaporator; The bottom of atmospheric evaporation device is connected with the malleation evaporimeter through pump; The toluene vapor outlet on malleation evaporimeter top connects the upper inlet of atmospheric evaporation device, and the toluene condensate outlet of atmospheric evaporation device 2 bottoms is connected with the top of vacuum evaporator 1 through malleation toluene pans; The toluene outlet on malleation evaporimeter top connects toluene residue storage tank, and the outlet at bottom of toluene residue storage tank connects the residue evaporation boiler.
Be provided with heat(ing) coil in the described residue evaporation boiler.
The present invention reclaims the separation basis in original single-action has increased the one-level vacuum evaporator, one-level malleation evaporimeter.In the vacuum evaporator top fed, because toluene and water azeotropic, and azeotropic point reduces, and have immediately partial material flash distillation gasification, thereby the proportion because of water is larger when having avoided atmospheric evaporation with the waste liquid after the preheating, and the low boiling explosion phenomenon that produces of boiling point; The negative pressure discharging is to the atmospheric evaporation device, and the toluene vapor of atmospheric evaporation device is used for the heating source of vacuum evaporator; The normal pressure discharging is to the malleation evaporimeter, and the toluene vapor of malleation evaporimeter at first is used for the heating source of atmospheric evaporation device, again after the flash distillation of malleation toluene pans as the thermal source of vacuum evaporator; After the malleation evaporation, the polyethylene toluene solution that concentration is higher is delivered to the residue evaporation boiler and is continued the concentrate evaporation, because concentration increases, poly mobile the reduction, its heat transfer is very slow, and simple jacket type evaporimeter heating effect is undesirable, increases heat(ing) coil in the residue evaporation boiler, make in the pot and conduct heat evenly, reduced concentration time.
Description of drawings
Fig. 1 is the process principle figure of the inventive method.
In Fig. 1: 1 vacuum evaporator, 2 atmospheric evaporation devices, 3 malleation toluene evaporates devices, 4 toluene condensers, 5 decanters, 6 tail gas condensers, 7 toluene residue storage tanks, 8 residue evaporation boilers, 8-1 heat(ing) coil, 9 malleation toluene pans, 10 waste liquid preheaters.
The specific embodiment
As shown in Figure 1, the device of the present embodiment comprises waste liquid preheater 10, vacuum evaporator 1, toluene condenser 4, decanter 5, tail gas condenser 6, atmospheric evaporation device 2, malleation toluene evaporates device 3, malleation toluene pans 9, toluene residue storage tank 7 and residue evaporation boiler 8;
Described waste liquid preheater 10 is connected with the top of vacuum evaporator 1, and the entrance of toluene condenser 4 connects the toluene vapor outlet on vacuum evaporator 1 top, and the outlet of toluene condenser 4 connects decanter 5, and the gas vent of decanter 5 connects tail gas condenser 6; The bottom of vacuum evaporator 1 is connected through the bottom of pump with atmospheric evaporation device 2; The toluene vapor outlet on atmospheric evaporation device 2 tops connects the top of vacuum evaporator 1; The bottom of atmospheric evaporation device 2 is connected with malleation evaporimeter 3 through pump; The toluene vapor outlet on malleation evaporimeter 3 tops connects the upper inlet of atmospheric evaporation device 2, and the toluene condensate outlet of atmospheric evaporation device 2 bottoms is connected with the top of vacuum evaporator 1 through malleation toluene pans 9; The toluene outlet on malleation evaporimeter 3 tops connects toluene residue storage tank 7, and the outlet at bottom of toluene residue storage tank 7 connects residue evaporation boiler 8.Be provided with heat(ing) coil 8-1 in the described residue evaporation boiler 8.
The device of use the present embodiment carries out the triple effect separation of methylbenzene and poly process is as follows:
Contain poly toluene waste liquid tentatively concentrated through the laggard vacuum evaporator 1 of waste liquid preheater 10 preheatings, the negative pressure toluene vapor is through the laggard decanter 5 standing separation water of toluene condenser 4 condensations, toluene; Vacuum evaporator 1 discharging steams toluene through pump to atmospheric evaporation device 2 further concentrates, and the toluene vapor of atmospheric evaporation device 2 is as the thermal source of vacuum evaporator 1, through the laggard decanter 5 of heat exchange condensation; 2 dischargings of atmospheric evaporation device continue concentrate through pump to malleation evaporimeter 3 and steam toluene, the toluene vapor of malleation evaporimeter 3 is at first as the thermal source of atmospheric evaporation device 2, through the laggard malleation toluene of heat exchange condensation pans 9, malleation toluene pans 9 through the non-return valve flash distillations after again as the thermal source of vacuum evaporator 1, through the polyethylene toluene solution overflow of malleation evaporimeter 3 concentrates to toluene residue storage tank 7, to guarantee the continued operation of evaporization process, discharge polyethylene after being delivered to 8 engler distillations of residue evaporation boiler by toluene residue storage tank 7, increase heat(ing) coil in the cylindrical shell of residue evaporation boiler 8, make in the pot and conduct heat evenly, reduced concentration time.Technique of the present invention is malleation, normal pressure, the distillation of negative pressure triple effect, because the vapor partial pressure of toluene is higher, increases tail gas condenser 6 the uncooled toluene vapor condensation of decanter 5 isolated parts is reclaimed, and water is discharged through pump.
Triple effect separation of methylbenzene of the present invention and poly device are a kind of energy-saving emission-reducing apparatus, and this device utilizes the boiling range difference of same liquid under the different pressures, utilize indirect steam concentrate material, thereby greatly save production cost.
The consumption of this covering device primary steam is compared with traditional toluene evaporates device steam consumption, and unit toluene vapor consumption lowers 55%.According to investigations, traditional toluene evaporates device steam consumption is 0.17 ton of steam/ton crude cresylic acid, and using this process unit to lower is 0.08 ton of steam/ton crude cresylic acid.
By 300 days, counted 24 hours every days with the production line producing days:
Per hour the crude cresylic acid treating capacity is 30 cubic metres, 0.09 ton of every cubic metre of steam saving, steam in 180 yuan/per ton:
Can save every day: 0.09*30*24*180=11664 unit,
Can save every year: ten thousand yuan of 11664*300=349.92.
Claims (6)
1. a triple effect separation of methylbenzene and poly method is characterized in that: contain poly toluene waste liquid and separate through one-level decompression distillation, one-level air-distillation, the distillation of one-level malleation successively, toluene vapor reuses as thermal source; Detailed process is: contain poly toluene waste liquid and at first enter vacuum evaporator carry out the decompression distillation concentrate after preheating, toluene vapor separates through the laggard decanter of condenser condenses; Enter again the atmospheric evaporation device through the toluene waste liquid of decompression distillation and carry out the air-distillation concentrate, atmospheric evaporation device top toluene vapor separates through the laggard decanter of heat exchange condensation, toluene waste liquid after the normal pressure distillation advances the malleation evaporimeter and continues the distillation concentrate, the top toluene vapor after the heat exchange of normal pressure evaporimeter flash distillation to vacuum evaporator, the laggard decanter of condensation separates, and malleation evaporimeter waste liquid advances the residue evaporation boiler and continues the concentrate evaporation.
2. method according to claim 1, it is characterized in that in the described malleation evaporimeter with low pressure steam as a thermal source, the atmospheric evaporation device is take the toluene vapor of malleation evaporimeter as thermal source, and the toluene vapor that vacuum evaporator steams in the atmospheric evaporation device is as thermal source.
3. method according to claim 1 is characterized in that toluene vapor flash distillation behind pans in described malleation evaporimeter top carries out Btu utilization again to vacuum evaporator.
4. method according to claim 1 is characterized in that described residue evaporation boiler adopts the negative pressure intermittent operation.
5. a device of implementing each described method of claim 1-4 is characterized in that comprising waste liquid preheater (10), vacuum evaporator (1), toluene condenser (4), decanter (5), tail gas condenser (6), atmospheric evaporation device (2), malleation evaporimeter (3), malleation toluene pans (9), toluene residue storage tank (7) and residue evaporation boiler (8);
Described waste liquid preheater (10) is connected with the top of vacuum evaporator (1), the entrance of toluene condenser (4) connects the toluene vapor outlet on vacuum evaporator (1) top, the outlet of toluene condenser (4) connects decanter (5), and the gas vent of decanter (5) connects tail gas condenser (6); The bottom of vacuum evaporator (1) is connected through the bottom of pump with atmospheric evaporation device (2); The toluene vapor outlet on atmospheric evaporation device (2) top connects the top of vacuum evaporator (1); The bottom of atmospheric evaporation device (2) is connected with malleation evaporimeter (3) bottom through pump; The toluene vapor outlet on malleation evaporimeter (3) top connects the upper inlet of atmospheric evaporation device (2), and the toluene condensate outlet of atmospheric evaporation device (2) bottom is connected through the top of malleation toluene pans (9) with vacuum evaporator (1); The toluene outlet on malleation evaporimeter (3) top connects toluene residue storage tank (7), and the outlet at bottom of toluene residue storage tank (7) connects residue evaporation boiler (8).
6. device according to claim 5 is characterized in that being provided with in the described residue evaporation boiler (8) heat(ing) coil (8-1).
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| CN201310010361.XA CN103007565B (en) | 2013-01-11 | 2013-01-11 | Method and device for triple-effect separation of methylbenzene and polyethylene |
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| CN201310010361.XA CN103007565B (en) | 2013-01-11 | 2013-01-11 | Method and device for triple-effect separation of methylbenzene and polyethylene |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104557421A (en) * | 2013-10-16 | 2015-04-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recovery technology |
| CN110746258A (en) * | 2019-10-31 | 2020-02-04 | 上海聚友化工有限公司 | Method for separating toluene and polyethylene |
| CN113277538A (en) * | 2021-06-18 | 2021-08-20 | 沈阳铝镁设计研究院有限公司 | Method for reducing consumption of new steam in alumina production |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
| CN102211992A (en) * | 2011-04-18 | 2011-10-12 | 湖南百利工程科技有限公司 | Process for reclaiming dibasic acid from adipic acid production waste solution |
| CN102824751A (en) * | 2012-08-31 | 2012-12-19 | 烟台东洁环保机械工程有限公司 | Distillation separation and recovery method for toluene-polyethylene mixed solution and used equipment |
-
2013
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
| CN102211992A (en) * | 2011-04-18 | 2011-10-12 | 湖南百利工程科技有限公司 | Process for reclaiming dibasic acid from adipic acid production waste solution |
| CN102824751A (en) * | 2012-08-31 | 2012-12-19 | 烟台东洁环保机械工程有限公司 | Distillation separation and recovery method for toluene-polyethylene mixed solution and used equipment |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104557421A (en) * | 2013-10-16 | 2015-04-29 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple-effect toluene recovery technology |
| CN104557421B (en) * | 2013-10-16 | 2016-05-18 | 禾欣可乐丽超纤皮(嘉兴)有限公司 | Triple effect toluene recovery technology |
| CN110746258A (en) * | 2019-10-31 | 2020-02-04 | 上海聚友化工有限公司 | Method for separating toluene and polyethylene |
| CN113277538A (en) * | 2021-06-18 | 2021-08-20 | 沈阳铝镁设计研究院有限公司 | Method for reducing consumption of new steam in alumina production |
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